JPS6327601B2 - - Google Patents
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- Publication number
- JPS6327601B2 JPS6327601B2 JP56038352A JP3835281A JPS6327601B2 JP S6327601 B2 JPS6327601 B2 JP S6327601B2 JP 56038352 A JP56038352 A JP 56038352A JP 3835281 A JP3835281 A JP 3835281A JP S6327601 B2 JPS6327601 B2 JP S6327601B2
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- JP
- Japan
- Prior art keywords
- temperature
- gas
- exhaust gas
- economizer
- combustion exhaust
- Prior art date
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Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、パルプ蒸解廃液（以下、黒液とい
う）を燃焼させて蒸解薬品および蒸気を回収する
ソーダ回収ボイラにおいて、効率を向上させるこ
とができる熱交換方法に関するものである。[Detailed Description of the Invention] [Field of Industrial Application] The present invention improves efficiency in a soda recovery boiler that burns pulp cooking waste liquor (hereinafter referred to as black liquor) to recover cooking chemicals and steam. This relates to a heat exchange method that can be used.
紙パルプ産業におけるソーダ回収ボイラとして
は、現在我国において、スカンジナビア方式回収
ボイラと呼ばれるものが主流を占めている。この
方式は第１図に示すように、燃焼用黒液を真空蒸
発缶１で固形分60〜70重量％の燃焼可能な濃度ま
で濃縮した後、直接ボイラ火炉２内で燃焼させ
て、蒸解薬品をスメルトとしてスメルト排出口３
から回収するとともに、燃焼排ガスを火炉水冷壁
４、過熱器５、ボイラ本体６の伝熱面と順次熱交
換させて蒸気を発生させた後、さらに節炭器７に
導入して熱回収し、電気集じん装置８にてダスト
を除去した後、煙突１０より大気に放散するよう
にしたものである。１１は誘引フアンである。こ
の燃焼排ガスは水分を20〜30％含み、また亜硫酸
ガスが存在するため酸露点が100〜120℃であり、
さらにダスト（大部分は芒硝）が多量に含まれて
いる。一方、節炭器７へのボイラ給水は、３Kg／
cm2Ｇ前後の低圧蒸気を使用し脱気器１２にて120
〜125℃に温度調節されて給水される。１３はボ
イラ給水管、１４は低圧蒸気管、１５は給水ポン
プ、１６は低圧蒸気管に設けられた脱気器圧力制
御弁である。節炭器入口の給水温度を120〜125℃
にするのは、給水温度をこの温度以下にすると節
炭器伝熱面の表面が燃焼排ガスの酸露点以下とな
り伝熱面が腐食するからである。
Currently, the so-called Scandinavian type recovery boiler is the mainstream soda recovery boiler used in the pulp and paper industry in Japan. In this method, as shown in Figure 1, black liquor for combustion is concentrated in a vacuum evaporator 1 to a combustible concentration of 60 to 70% by weight solids, and then directly combusted in a boiler furnace 2 to produce cooking chemicals. Smelt outlet 3 as smelt
At the same time, the combustion exhaust gas is sequentially heat-exchanged with the furnace water cooling wall 4, the superheater 5, and the heat transfer surface of the boiler body 6 to generate steam, and then further introduced into the economizer 7 for heat recovery, After the dust is removed by an electrostatic precipitator 8, it is dissipated into the atmosphere from a chimney 10. 11 is an attraction fan. This combustion exhaust gas contains 20 to 30% water and has an acid dew point of 100 to 120℃ due to the presence of sulfur dioxide gas.
Furthermore, it contains a large amount of dust (mostly mirabilite). On the other hand, the boiler water supply to the economizer 7 is 3Kg/
120 in deaerator 12 using low pressure steam around cm 2 G.
Water is supplied at a temperature of ~125℃. 13 is a boiler water supply pipe, 14 is a low pressure steam pipe, 15 is a water supply pump, and 16 is a deaerator pressure control valve provided in the low pressure steam pipe. Adjust the water supply temperature at the inlet of the economizer to 120-125℃
This is because if the feed water temperature is lower than this temperature, the surface of the heat transfer surface of the economizer will be below the acid dew point of the combustion exhaust gas, and the heat transfer surface will corrode.
ところで伝熱面の腐食防止効果を上げるには、
給水温度を120〜125℃よりも上げることが望まし
い。しかし給水温度を120〜125℃より上げると、
節炭器出口の燃焼排ガス温度を下げるためには燃
焼排ガスとの熱交換に際して伝熱面積が非常に大
きくなり、経済的に燃焼排ガス温度を下げること
ができなくなる。このため一般的には、節炭器７
入口の給水温度は120〜125℃、節炭器７出口の燃
焼排ガス温度は170〜175℃程度が限界とされてい
る。
By the way, in order to increase the corrosion prevention effect on heat transfer surfaces,
It is desirable to raise the feed water temperature above 120-125°C. However, when the water supply temperature is raised above 120-125℃,
In order to lower the temperature of the combustion exhaust gas at the outlet of the economizer, the heat transfer area becomes extremely large during heat exchange with the combustion exhaust gas, making it impossible to lower the combustion exhaust gas temperature economically. For this reason, in general, economizers 7
The temperature limit for the water supply at the inlet is 120 to 125°C, and the temperature of the combustion exhaust gas at the outlet of the economizer 7 is 170 to 175°C.
一方、燃焼用空気は、黒液の燃焼性向上のため
150〜160℃程度の温度に上げる必要がある。燃焼
用空気温度を上げるため、節炭器下流側にガス式
空気予熱器を設けることが考えられる。しかし、
前述のように燃焼排ガス中には、多量の水分およ
び亜硫酸ガスが含まれているので、伝熱面が酸露
点以下となつて腐食し連続運転ができなくなると
いう不都合点がある。 On the other hand, combustion air is used to improve the combustibility of black liquor.
It is necessary to raise the temperature to about 150-160℃. In order to increase the combustion air temperature, it is conceivable to provide a gas-type air preheater downstream of the economizer. but,
As mentioned above, the combustion exhaust gas contains a large amount of moisture and sulfur dioxide gas, so there is a disadvantage that the heat transfer surface becomes below the acid dew point and corrodes, making continuous operation impossible.
そのため、現状においては蒸気式空気予熱器を
設けて、空気温度を前述の温度まで上げている。
蒸気式空気予熱器は３Kg／cm2Ｇ前後の低圧蒸気を
使用した１次加熱器１７と、12Kg／cm2Ｇの中圧蒸
気を使用した２次加熱器１８とから成り立つてい
る。 Therefore, at present, a steam-type air preheater is provided to raise the air temperature to the above-mentioned temperature.
The steam air preheater consists of a primary heater 17 using low pressure steam of about 3 kg/cm 2 G and a secondary heater 18 using medium pressure steam of 12 kg/cm 2 G.
蒸気式空気予熱器を２段に分けるのは、全て低
圧蒸気を使用すると伝熱面が膨大となり経済的で
なく、また全て中圧蒸気を使用するとプラント全
体の熱効率を悪くし経済的でなくなるからであ
る。 The reason why the steam-type air preheater is divided into two stages is that if all low-pressure steam is used, the heat transfer surface becomes enormous and it is not economical, and if all medium-pressure steam is used, the thermal efficiency of the entire plant deteriorates and it becomes uneconomical. It is.
したがつて、現状の設備においては、燃焼排ガ
スの持つ熱量を有効に回収することができず、ま
た２次加熱器に中圧蒸気を使用しているので、プ
ラント全体の熱効率を悪くするという不都合点を
有している。 Therefore, with the current equipment, it is not possible to effectively recover the amount of heat contained in the combustion exhaust gas, and medium-pressure steam is used for the secondary heater, which has the disadvantage of decreasing the thermal efficiency of the entire plant. It has points.
本発明は上記の諸点に鑑みなされたもので、節
炭器へ導入するボイラ給水温度を、低圧蒸気で可
能な限りの温度、すなわち140〜150℃に上昇さ
せ、節炭器の下流側の煙道にガス式空気予熱器を
設け排ガスの熱回収を図るとともに、２次加熱器
１８を廃し、中圧蒸気の消費量を減少させて、プ
ラント全体の熱効率を図る熱交換方法の提供を目
的とするものである。 The present invention was made in view of the above points, and it increases the temperature of the boiler feed water introduced into the economizer to the maximum temperature possible with low-pressure steam, that is, 140 to 150°C. The purpose of this project is to provide a heat exchange method that improves the thermal efficiency of the entire plant by installing a gas-type air preheater in the road to recover heat from exhaust gas, eliminating the secondary heater 18, and reducing the consumption of medium-pressure steam. It is something to do.
本発明のソーダ回収ボイラにおける熱交換方法
は、第２図および第３図を参照して説明すれば、
濃縮されたパルプ廃液を燃焼させて蒸解薬品を回
収するとともに、燃焼排ガスを火炉水冷壁４、過
熱器５、ボイラ本体６と順次熱交換させて蒸気を
発生させた後、さらに節炭器７に導入して熱回収
し、この節炭器７に、燃焼排ガス中の亜硫酸ガス
の酸露点よりはるかに高い140〜150℃の温度に３
Kg／cm2Ｇ前後の低圧蒸気により子熱したボイラ給
水を導入するとともに、前記節炭器７の下流側の
煙道にガス式空気予熱器２２を設け、このガス式
空気予熱器に３Kg／cm2Ｇ前後の低圧蒸気により、
ガス式空気予熱器内の温度が燃焼排ガス中の亜硫
酸ガスの酸露点以上になるように予熱した燃焼用
空気を導入することを特徴としている。
The heat exchange method in the soda recovery boiler of the present invention will be explained with reference to FIGS. 2 and 3.
The concentrated pulp waste liquid is combusted to recover cooking chemicals, and the combustion exhaust gas is sequentially heat-exchanged with the furnace water-cooled wall 4, superheater 5, and boiler body 6 to generate steam, and then sent to the energy saver 7. This energy saving device 7 is heated to a temperature of 140 to 150°C, which is much higher than the acid dew point of sulfur dioxide gas in the combustion exhaust gas.
In addition to introducing boiler feed water sub-heated by low-pressure steam of around Kg/cm 2 G, a gas air preheater 22 is installed in the flue on the downstream side of the economizer 7, and this gas air preheater has a heating capacity of 3 kg/cm 2 G. With low pressure steam around cm 2 G,
The combustion air is preheated so that the temperature inside the gas air preheater is higher than the acid dew point of sulfur dioxide gas in the combustion exhaust gas.
節炭器７に導入するボイラ給水温度が14℃未満
の場合は、第１図に示す従来例に近くなり、プラ
ント効率の向上を大幅に図ることができない。一
方、節炭器７に導入するボイラ給水は、脱気器１
２において３Kg／cm2前後の低圧蒸気にて予熱され
るので、脱気器１２の出口のボイラ給水温度は
150℃が上限である。 If the temperature of the boiler feed water introduced into the economizer 7 is less than 14° C., the temperature will be close to that of the conventional example shown in FIG. 1, and it will not be possible to significantly improve plant efficiency. On the other hand, the boiler feed water introduced into the economizer 7 is supplied to the deaerator 1.
2, the boiler feed water temperature at the outlet of the deaerator 12 is preheated with low pressure steam of around 3 kg/ cm2 .
The upper limit is 150℃.
以下、本発明の実施例を図面に基づいて説明す
る。第２図は本発明のソーダ回収ボイラにおける
熱交換方法の一実施例を示している。第２図に示
すように、電気集じん装置８の後にチユーブラ
式、回転再生式などのガス式空気予熱器２２を設
置し、かつ蒸気式空気予熱器の２次加熱器を設置
せずに、３Kg／cm2Ｇ前後の低圧蒸気で90〜100℃
前後まで予熱された空気をガス式空気予熱器２２
に導入する。このようにして中圧蒸気の消費量を
減少させるとともに、燃焼排ガスの熱回収を容易
にし、煙突１０入口の燃焼排ガスの温度を140〜
150℃まで下げてボイラ効果を向上させる。この
場合、ガス式空気予熱器２２のメタル温度は燃焼
排ガスの露点以上になるように、低圧蒸気を使用
する１次加熱器１７で空気温度を上げており、か
つ電気集じん装置８でダストを除去しているの
で、腐食およびダスト閉塞の心配はない。さらに
節炭器７入口のボイラ給水温度を、脱気器１２に
おいて低圧蒸気で可能な限り140〜150℃に上昇さ
せ、ボイラにおける高圧蒸気の蒸発量を増大させ
てプラント効率を向上させる。すなわち、燃焼排
ガスは火炉水冷壁４、過熱器５、ボイラ本体６の
小管群を経て、節炭器７にて従来通りの好適な伝
熱面積にてボイラ給水と熱交換する。一例として
給水温度が140℃の場合、節炭器７出口排ガス温
度は約190℃となる。さらに燃焼排ガスは電気集
じん装置８を経た後、ガス式空気予熱器２２に導
入されて90〜100℃に予熱された空気と熱交換し
排ガス温度が140〜150℃程度になるまで熱回収さ
れた後、煙突１０から大気に放散される。この場
合、ガス式空気予熱器２２に導入される燃焼排ガ
ス温度が190〜200℃前後と従来に比べて高いの
で、伝熱面が燃焼排ガスの酸露点以下になること
はなく、したがつて伝熱面の腐食およびダスト閉
塞のおそれはない。燃焼用空気は蒸気式空気予熱
器（低圧蒸気を使用した１次加熱器１７）によつ
て90〜100℃に加熱された後、煙道に設置された
ガス式空気予熱器２２によつて150〜160℃に加熱
されたボイラ火炉２へ送られる。一方、ボイラ給
水は低圧蒸気を使用した脱気器１２で上げ得る温
度、すなわち140〜150℃まで温度を上昇させ、節
炭器７に送られさらに加熱されてボイラ本体６に
供給される。
Embodiments of the present invention will be described below based on the drawings. FIG. 2 shows an embodiment of the heat exchange method in the soda recovery boiler of the present invention. As shown in FIG. 2, a gas-type air preheater 22 such as a tubular type or a rotary regeneration type is installed after the electrostatic precipitator 8, and a secondary heater of the steam-type air preheater is not installed. 90-100℃ with low pressure steam around 3Kg/ cm2G
The air that has been preheated from front to back is passed through the gas air preheater 22.
to be introduced. In this way, the consumption of medium pressure steam is reduced, and the heat recovery of the flue gas is facilitated, and the temperature of the flue gas at the inlet of the chimney 10 is lowered from 140 to 140°C.
Boiler efficiency is improved by lowering the temperature to 150℃. In this case, the air temperature is raised by the primary heater 17 using low-pressure steam so that the metal temperature of the gas air preheater 22 is higher than the dew point of the combustion exhaust gas, and the dust is removed by the electrostatic precipitator 8. Since it has been removed, there is no need to worry about corrosion or dust clogging. Furthermore, the temperature of the boiler feed water at the inlet of the economizer 7 is raised to 140 to 150°C as much as possible using low pressure steam in the deaerator 12, thereby increasing the amount of evaporation of high pressure steam in the boiler and improving plant efficiency. That is, the combustion exhaust gas passes through the furnace water-cooled wall 4, the superheater 5, and the small tube group of the boiler body 6, and exchanges heat with the boiler feed water in the economizer 7 using a conventional suitable heat transfer area. As an example, when the water supply temperature is 140°C, the exhaust gas temperature at the outlet of the economizer 7 is approximately 190°C. Furthermore, after the combustion exhaust gas passes through the electrostatic precipitator 8, it is introduced into the gas air preheater 22, where it exchanges heat with air preheated to 90 to 100 degrees Celsius, and heat is recovered until the exhaust gas temperature reaches about 140 to 150 degrees Celsius. After that, it is released into the atmosphere from the chimney 10. In this case, the temperature of the combustion exhaust gas introduced into the gas air preheater 22 is around 190 to 200°C, which is higher than before, so the heat transfer surface does not fall below the acid dew point of the combustion exhaust gas, and therefore the temperature of the combustion exhaust gas is high. There is no risk of hot surface corrosion and dust blockage. Combustion air is heated to 90-100°C by a steam-type air preheater (primary heater 17 using low-pressure steam), and then heated to 150°C by a gas-type air preheater 22 installed in the flue. It is sent to boiler furnace 2 heated to ~160°C. On the other hand, the boiler feed water is raised to a temperature that can be raised by the deaerator 12 using low-pressure steam, that is, 140 to 150° C., and sent to the economizer 7 where it is further heated and supplied to the boiler body 6.
つぎに本発明の他の実施例を第３図に基づいて
説明する。本例はガス式空気予熱器２２を節炭器
７と電気集じん装置８との間の煙道に設けたもの
である。この場合は、ガス式空気予熱器２２に導
入される燃焼排ガス中には多量のダストが含まれ
るので、伝熱面にダスト堆積が発生する可能性が
ある。堆積したダストはスートブロワ、ハンマリ
ング装置などを用いて定期的に除去する。他の構
成および作用は第２図の場合と同様である。 Next, another embodiment of the present invention will be described based on FIG. In this example, a gas air preheater 22 is provided in the flue between the economizer 7 and the electrostatic precipitator 8. In this case, since the combustion exhaust gas introduced into the gas air preheater 22 contains a large amount of dust, there is a possibility that dust will accumulate on the heat transfer surface. Accumulated dust is removed periodically using a soot blower, hammering device, etc. Other configurations and operations are similar to those in FIG. 2.
なお第２図および第３図に示す節炭器へ導入す
るボイラ給水温度以外の温度は一例として示した
もので、これらに限定されるものではない。 Note that the temperatures other than the boiler feed water temperature introduced into the economizer shown in FIGS. 2 and 3 are shown as examples, and are not limited to these.
以上説明したように、本発明は、紙パルプ産業
におけるスカンジナビア方式のソーダ回収ボイラ
において、節炭器へ導入するボイラ給水温度を、
低圧蒸気で可能な限りの温度、すなわち140〜150
℃に上昇させ、節炭器下流側の煙道に従来設置で
きなかつたガス式空気予熱器を設けて燃焼排ガス
の熱回収をはかるとともに、ガス式空気予熱器を
設けたことによつて中圧蒸気を使用した２次空気
過熱器を省略して中圧蒸気の消費量を減少させ、
プラント効率の向上を図ることができるという効
果を有している。
As explained above, the present invention enables the boiler feed water temperature introduced to the economizer to be adjusted in a Scandinavian soda recovery boiler in the pulp and paper industry.
Temperatures as low as possible with low pressure steam, i.e. 140-150
℃, and installed a gas-type air preheater in the flue downstream of the energy saver, which could not previously be installed, to recover heat from the combustion exhaust gas. Omitting the secondary air superheater using steam reduces the consumption of medium pressure steam,
This has the effect of improving plant efficiency.
第１図は従来のソーダ回収ボイラのフローシー
ト、第２図は本発明の方法を実施するソーダ回収
ボイラの一例を示すフローシート、第３図は本発
明における他の例を示すフローシートである。
１……真空蒸発缶、２……ボイラ火炉、３……
スメルト排出口、４……水冷壁、５……過熱器、
６……ボイラ本体、７……節炭器、８……電気集
じん装置、１０……煙突、１１……誘引フアン、
１２……脱気器、１３……ボイラ給水管、１４…
…低圧蒸気管、１５……給水ポンプ、１６……脱
気器圧力制御弁、１７……１次加熱器、１８……
２次加熱器、２０……押込みフアン、２１……中
圧蒸気管、２２……ガス式空気予熱器。
Fig. 1 is a flow sheet of a conventional soda recovery boiler, Fig. 2 is a flow sheet showing an example of a soda recovery boiler implementing the method of the present invention, and Fig. 3 is a flow sheet showing another example of the present invention. . 1...Vacuum evaporator, 2...Boiler furnace, 3...
Smelt outlet, 4...Water cooling wall, 5...Superheater,
6... Boiler main body, 7... Energy saver, 8... Electrostatic precipitator, 10... Chimney, 11... Induction fan,
12... Deaerator, 13... Boiler water supply pipe, 14...
...Low pressure steam pipe, 15...Water pump, 16...Deaerator pressure control valve, 17...Primary heater, 18...
Secondary heater, 20... Force fan, 21... Medium pressure steam pipe, 22... Gas type air preheater.
Claims (1)
を回収するとともに、燃焼排ガスを火炉水冷壁、
過熱器、ボイラ本体と順次熱交換させて蒸気を発
生させた後、さらに節炭器に導入して熱回収し、
この節炭器に、燃焼排ガス中の亜硫酸ガスの酸露
点よりはるかに高い140〜150℃の温度に３Kg／cm2
Ｇ前後の低圧蒸気により予熱したボイラ給水を導
入するとともに、前記節炭器の下流側の煙道にガ
ス式空気予熱器を設け、このガス式空気予熱器に
３Kg／cm2Ｇ前後の低圧蒸気により、ガス式空気予
熱器内の温度が燃焼排ガス中の亜硫酸ガスの酸露
点以上になるように予熱した燃焼用空気を導入す
ることを特徴とするソーダ回収ボイラにおける熱
交換方法。1 The concentrated pulp waste liquid is combusted to recover cooking chemicals, and the combustion exhaust gas is transferred to the water-cooled wall of the furnace.
After generating steam by sequentially exchanging heat with the superheater and the boiler body, it is further introduced into the economizer to recover the heat.
This economizer uses 3Kg/cm 2 at a temperature of 140 to 150℃, which is much higher than the acid dew point of sulfur dioxide gas in the combustion exhaust gas.
In addition to introducing boiler feed water that has been preheated by low-pressure steam of about 3 kg/cm 2 G, a gas air preheater is installed in the flue on the downstream side of the economizer, and low-pressure steam of about 3 kg/cm 2 G is introduced into the gas air preheater. A heat exchange method in a soda recovery boiler, characterized by introducing combustion air preheated so that the temperature in the gas air preheater is higher than the acid dew point of sulfur dioxide gas in the combustion exhaust gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3835281A JPS57153102A (en) | 1981-03-16 | 1981-03-16 | Heat exchange for black liquor recovery boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3835281A JPS57153102A (en) | 1981-03-16 | 1981-03-16 | Heat exchange for black liquor recovery boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57153102A JPS57153102A (en) | 1982-09-21 |
| JPS6327601B2 true JPS6327601B2 (en) | 1988-06-03 |
Family
ID=12522881
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3835281A Granted JPS57153102A (en) | 1981-03-16 | 1981-03-16 | Heat exchange for black liquor recovery boiler |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS57153102A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4342156C1 (en) * | 1993-12-10 | 1995-04-20 | Balcke Duerr Ag | Arrangement for improving the efficiency of a power station (generating station) or the like |
| JP4497028B2 (en) * | 2005-06-09 | 2010-07-07 | 王子製紙株式会社 | Treatment method of sulfuric acid pitch |
| US8490581B2 (en) * | 2006-06-15 | 2013-07-23 | Exxonmobil Research And Engineering Company | Advanced fired heater unit for use in refinery and petro-chemical applications |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5316101A (en) * | 1976-07-30 | 1978-02-14 | Mitsubishi Heavy Ind Ltd | Boiler plant by using blast furnace gas |
| JPS6012521B2 (en) * | 1976-12-24 | 1985-04-02 | ザ・ラルフ・エム・パ−ソンズ・カンパニ− | Method for removing harmful gases from combustion waste gas in power generation equipment |
-
1981
- 1981-03-16 JP JP3835281A patent/JPS57153102A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57153102A (en) | 1982-09-21 |
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