JPS6365368B2 - - Google Patents
Info
- Publication number
- JPS6365368B2 JPS6365368B2 JP53143535A JP14353578A JPS6365368B2 JP S6365368 B2 JPS6365368 B2 JP S6365368B2 JP 53143535 A JP53143535 A JP 53143535A JP 14353578 A JP14353578 A JP 14353578A JP S6365368 B2 JPS6365368 B2 JP S6365368B2
- Authority
- JP
- Japan
- Prior art keywords
- exhaust gas
- temperature
- bypass
- sox
- gas
- 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
- 238000006477 desulfuration reaction Methods 0.000 claims description 28
- 230000023556 desulfurization Effects 0.000 claims description 28
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 238000002485 combustion reaction Methods 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 5
- 239000012716 precipitator Substances 0.000 claims 1
- 238000011144 upstream manufacturing Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 72
- 229910052815 sulfur oxide Inorganic materials 0.000 description 25
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 24
- 239000011734 sodium Substances 0.000 description 13
- 239000003795 chemical substances by application Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 239000003245 coal Substances 0.000 description 8
- 235000011121 sodium hydroxide Nutrition 0.000 description 8
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 239000012717 electrostatic precipitator Substances 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000000567 combustion gas Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 235000010265 sodium sulphite Nutrition 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】
＜産業上の利用分野＞
この発明は半湿式排煙脱硫装置の構造に関す
る。DETAILED DESCRIPTION OF THE INVENTION <Industrial Application Field> The present invention relates to the structure of a semi-wet flue gas desulfurization apparatus.
＜従来の技術及びその問題点＞
ボイラ等の蒸気発生装置や燃焼装置の排ガス中
には必然的に硫黄酸化物（以下SOxと称す。）が
含まれ公害防止上これを除去する必要がある。そ
の手段としてアルカリ剤、例えばNaOH，
Na2CO3，Ca（OH）2，NH3フライアツシユ、
CaO，CaCO3等の溶液を噴霧にして排ガス中に
供給しSO2，SO3等のSOxと反応させ除去するこ
とが知られている。湿式の噴霧による場合は、ア
ルカリ剤とSOxの反応生成物がスラリ状のものと
して排出されるのでその処理量とその処理手段の
上において種々の困難が生ずるものである。<Prior art and its problems> Sulfur oxides (hereinafter referred to as SOx) are inevitably contained in the exhaust gas from steam generators and combustion devices such as boilers, and it is necessary to remove them to prevent pollution. As a means of doing so, alkaline agents such as NaOH,
Na 2 CO 3 , Ca(OH) 2 , NH 3 fly ash,
It is known that a solution such as CaO or CaCO 3 is supplied into the exhaust gas as a spray and reacted with SOx such as SO 2 or SO 3 to be removed. In the case of wet spraying, the reaction product of the alkaline agent and SOx is discharged in the form of a slurry, which causes various difficulties in terms of the throughput and the processing means.
発明者等はさきに排ガス流路に脱硫反応塔を設
け、アルカリ液（NaOH又はNa2CO3）を極微粒
液滴（エヤロゾル）状態として供給し、しかも排
ガスの保有する熱により水分を蒸発させSOxとの
反応物を固体微粒子として回収し、その粉状物の
除去を電気集塵機等で充分に行ない、しかも回収
物の容積を小さく、袋詰め処理可能にすることを
提案した。 The inventors first installed a desulfurization reaction tower in the exhaust gas flow path, supplied an alkaline liquid (NaOH or Na 2 CO 3 ) in the form of ultrafine droplets (aerosol), and evaporated water using the heat held in the exhaust gas. We proposed that the reactants with SOx be collected as solid particles, that the powdery material be sufficiently removed using an electrostatic precipitator, etc., and that the volume of the collected material be small enough to be packaged in bags.
従来のボイラにおいては重油が燃料として主に
使用されており、従つてSOxの発生絶対量は燃料
量換言すれば負荷に比例することとなる。従つて
この除去も負荷の変動に応じ脱硫剤としての
NaOH（苛性ソーダ）の供給量をかえ、かつ排ガ
スの温度も脱硫反応器入口でほぼ定常となるよう
に調整すれば良かつた。即ちほぼ定常の負荷（即
ちほぼ定常のSOx排出状態）となつている時間が
長いにものでこまかい調整はそれほど必要としな
いものであつた。しかし近時エネルギー源として
石炭を燃料とする微粉炭燃焼が再び盛んとなる機
運である。このような微粉炭燃焼について各種産
地の石炭を予め混合し微粉炭とする手段等が構ぜ
られているが、それでも従来の負荷変動に加え炭
質の変動がありこれに伴ない発生するSOxも相当
変動するものである。 In conventional boilers, heavy oil is mainly used as fuel, and therefore the absolute amount of SOx generated is proportional to the amount of fuel, in other words, the load. Therefore, this removal also depends on the fluctuation of the load as a desulfurizing agent.
It would have been better to change the supply amount of NaOH (caustic soda) and adjust the temperature of the exhaust gas so that it was almost constant at the inlet of the desulfurization reactor. In other words, since the time when the load is almost constant (that is, the SOx emission state is almost constant) is long, detailed adjustment is not necessary. However, recently there is an opportunity for pulverized coal combustion, which uses coal as fuel, to become popular again as an energy source. For this kind of pulverized coal combustion, methods have been devised to mix coal from various production areas in advance to make pulverized coal, but still, in addition to the conventional load fluctuations, there are also fluctuations in coal quality, and the resulting amount of SOx generated is considerable. It is subject to change.
このような条件に対応する装置については、ま
ず脱硫反応について考察する必要がある。脱硫反
応塔におけるSOxとNaOHとの反応は
SO2＋2NaOH→Na2SO3＋H2O
を主とするもので、NaOHの微粒水滴がSO2と
反応し上記の亜硫酸ソーダ（Na2SO3）含有水滴
となるものである。この亜硫酸ソーダを含む微粉
水滴が排ガスの熱で水分を蒸発させるときは粉状
のNa2SO3となる。 Regarding equipment compatible with such conditions, it is first necessary to consider the desulfurization reaction. The reaction between SOx and NaOH in the desulfurization reaction tower is mainly SO 2 + 2NaOH → Na 2 SO 3 + H 2 O, in which fine water droplets of NaOH react with SO 2 and generate the above sodium sulfite (Na 2 SO 3 )-containing It becomes water droplets. When the fine water droplets containing sodium sulfite evaporate water with the heat of the exhaust gas, they become powdered Na 2 SO 3 .
従つて粉状のNa2SO3を回収するには少なくと
もこの粉状体を回収する集塵器入口の排ガス温度
をその露点以上とする必要がある。好ましくはこ
の温度は90℃以上にする必要がある。 Therefore, in order to recover powdered Na 2 SO 3 , it is necessary to make the temperature of the exhaust gas at least at the inlet of the dust collector that collects this powder above its dew point. Preferably this temperature should be above 90°C.
＜手段の概要＞
この発明は脱硫塔入口の排ガス温度を、フロン
トバーナにより加熱した排ガス又は排ガス硫路外
に位置する高温燃焼ガス発生装置より高温排ガス
を脱硫塔入口に供給し、またはエヤヒータのバイ
パスダクトを使用し排ガスを所望の温度にしSOx
除去を効果的にし粉状のNa2SO3を回収できる半
湿式排煙脱硫装置の構造を提案するものである。<Summary of Means> The present invention reduces the temperature of the exhaust gas at the inlet of the desulfurization tower by supplying exhaust gas heated by a front burner, high-temperature exhaust gas from a high-temperature combustion gas generator located outside the exhaust gas sulfur path, or by bypassing the air heater. Uses a duct to control the exhaust gas to the desired temperature for SOx
This paper proposes the structure of a semi-wet flue gas desulfurization system that can effectively remove and recover powdered Na 2 SO 3 .
＜発明の目的＞
要するにこの発明は、脱硫塔内を流れる排ガス
に苛性ソーダ液を噴霧して亜硫酸ソーダの水滴と
し、これを排ガス温度を高めて粉状にし集じん装
置で効率よく回収するため、好適に、排ガス温度
を高める排ガス加熱手段を設け、又は温度の高い
排ガスをバイパスして適温の排ガスを脱硫塔に供
給し粉状Na2SO3の回収効果を高めた装置を提案
することを目的とする。<Purpose of the invention> In short, this invention is suitable for spraying caustic soda liquid onto the exhaust gas flowing in the desulfurization tower to form water droplets of sodium sulfite, raising the temperature of the exhaust gas, turning it into powder, and efficiently collecting it with a dust collector. The purpose of this study is to propose a device that improves the recovery effect of powdered Na 2 SO 3 by providing an exhaust gas heating means to raise the exhaust gas temperature, or by bypassing the high temperature exhaust gas and supplying the exhaust gas at an appropriate temperature to the desulfurization tower. do.
＜実施例＞
第１図はこの発明の一実施例にかかる装置の構
造を示すものである。<Embodiment> FIG. 1 shows the structure of an apparatus according to an embodiment of the present invention.
微粉炭用一次二次燃焼用空気はボイラ１の微粉
炭燃焼装置２に供給される。高温燃焼ガスは火炉
３より再熱器４、二次過熱器５、一次過熱器６、
エコノマイザー７を通り管路８よりエヤヒータ９
へ送られる。ついで送風機１０，脱硫反応塔１
１，電気集塵機１２を経由して煙突１３より排出
される。このような装置において、エコノマイザ
ー７とエヤヒータ９との間のダクト１４には排ガ
ス流量計１５，排ガス温度計１６，SOx含有量を
計測するSOx計１７が設けられ、それぞれの数値
の信号は制御箱１８に送られる。 Air for primary and secondary combustion for pulverized coal is supplied to a pulverized coal combustion device 2 of a boiler 1 . High-temperature combustion gas is sent from the furnace 3 to a reheater 4, a secondary superheater 5, a primary superheater 6,
Air heater 9 passes through economizer 7 and from conduit 8
sent to. Next, a blower 10 and a desulfurization reaction tower 1
1. It is discharged from the chimney 13 via the electrostatic precipitator 12. In such a device, a duct 14 between the economizer 7 and the air heater 9 is provided with an exhaust gas flow meter 15, an exhaust gas thermometer 16, and an SOx meter 17 for measuring SOx content, and the respective numerical signals are controlled. Sent to box 18.
脱硫反応塔１１の出口、即ち電気集塵機１２の
排ガス入口ダクト１９にはガス温度計２０が設け
られ、その温度信号は制御箱（排ガス加熱量制御
手段及び排ガスのバイパス流量制御手段を作動さ
せる作動手段）１８に送られる。脱硫反応塔１１
の入口にはフロントバーナ（排ガス加熱手段）２
１が設けられ、このフロントバーナ２１に供給す
る燃料量は制御弁（加熱量制御手段）２２で制御
される。 A gas thermometer 20 is installed at the outlet of the desulfurization reaction tower 11, that is, at the exhaust gas inlet duct 19 of the electrostatic precipitator 12, and the temperature signal is sent to the control box (operating means for operating the exhaust gas heating amount control means and the exhaust gas bypass flow rate control means). ) sent to 18. Desulfurization reaction tower 11
Front burner (exhaust gas heating means) 2 is installed at the inlet of
1 is provided, and the amount of fuel supplied to this front burner 21 is controlled by a control valve (heating amount control means) 22.
またこのフロントバーナは第２図に示すごとく
別に設けた燃焼室（排ガス加熱手段）３６内に設
け、これに燃焼空気３７を供給し高温ガスを発生
させ、通路３８を経由し脱硫反応塔１１の入口に
供給し排ガス温度を上昇させることができる。こ
れは排ガスはボイラ１で既に燃焼したガスであり
含有O2も少ないことによりフロントバーナ（加
熱量制御手段）２１ａを排ガス通路内で燃焼させ
ることが困難を伴うことによるものである。 As shown in FIG. 2, this front burner is installed in a separately provided combustion chamber (exhaust gas heating means) 36, and combustion air 37 is supplied to this to generate high-temperature gas. It can be supplied to the inlet to raise the exhaust gas temperature. This is because the exhaust gas is gas that has already been burned in the boiler 1 and contains little O 2 , so it is difficult to cause the front burner (heating amount control means) 21a to burn the exhaust gas in the exhaust gas passage.
アルカリ剤たるNaOHはタンク２３からポン
プ２４，制御弁２５を経由してアルカリ剤噴霧供
給装置２６に送られる。一方圧縮空気又は圧縮ガ
スは貯槽２７より制御弁２９を経由しアルカリ剤
供給管路２８に送られ噴霧用媒体として使用され
る。送風機１０の入口及び脱硫反応塔１１の入口
にはそれぞれ温度計３０ａ及び３０ｂが設けら
れ、その温度信号は制御箱に送られる。一例にお
いて、エコノマイザー７の出口排ガス温度は350
℃あり、フロントバーナ２１前においては排ガス
温度は140℃でありその温度も120〜145℃と負荷
に応じ変動するものである。またSOx値も500〜
1000ppmと変動する。しかし何れの場合において
も電気集塵機（以下EPと称す。）前ではガス温度
計２０の指示値が90℃以上になるようにして排ガ
ス温度が露点より下ることのないようにする必要
がある。そのためには脱硫反応塔１１の入口ガス
温度をほぼ160〜250℃にする必要があり、このた
めフロントバーナ２１で排ガスを加熱昇温させる
必要がある。EP入口ガス温度を90℃以上にする
ことは一方においてアルカリ液に含有される水分
の蒸発熱を排ガスから充分に与え、脱硫反応塔１
１内で水分を蒸発させNa2SO3を粉状の固体微粒
子にする必要があることによる。これがまたEP
の除塵効率を高めることともなる。この発明にお
いてはガス温度計２０の温度信号を制御箱１８に
送り制御箱１８の記憶する前記他の信号とEP後
流の排ガス中のSOx値を計測するSOx計３１から
の数値が規制値以下であるようにする信号と指令
も加味されフロントバーナ２１の供給燃料の制御
弁２１，並びにアルカリ剤噴霧供給装置２６から
のアルカリ剤供給量を制御する制御弁２５，２９
が制御されるものである。即ちガス温度計２０の
温度信号により制御弁２２，２５，２９が制御さ
れ好適なNa2SO3の粉状微粒固体がEP１２で得ら
れるものである。この捕集された粉状微粒固体は
EP１２に接続する輸送装置３２で袋詰装置（図
示せず）に送られる。 NaOH, which is an alkali agent, is sent from a tank 23 to an alkali agent spray supply device 26 via a pump 24 and a control valve 25. On the other hand, compressed air or compressed gas is sent from the storage tank 27 via the control valve 29 to the alkali agent supply pipe 28 and used as a spraying medium. Thermometers 30a and 30b are provided at the inlet of the blower 10 and the inlet of the desulfurization reaction tower 11, respectively, and their temperature signals are sent to a control box. In one example, the outlet exhaust gas temperature of economizer 7 is 350
The exhaust gas temperature is 140°C in front of the front burner 21, and the temperature also varies from 120 to 145°C depending on the load. Also, the SOx value is 500~
Fluctuations at 1000ppm. However, in either case, it is necessary to ensure that the reading on the gas thermometer 20 in front of the electrostatic precipitator (hereinafter referred to as EP) is 90° C. or higher so that the exhaust gas temperature does not fall below the dew point. For this purpose, the inlet gas temperature of the desulfurization reaction tower 11 needs to be approximately 160 to 250°C, and therefore it is necessary to heat the exhaust gas with the front burner 21 to raise the temperature. On the other hand, setting the EP inlet gas temperature to 90°C or higher provides sufficient heat of evaporation of water contained in the alkaline liquid from the exhaust gas,
This is because it is necessary to evaporate water within the chamber 1 and turn Na 2 SO 3 into powdered solid particles. This is another EP
This will also improve the dust removal efficiency. In this invention, the temperature signal from the gas thermometer 20 is sent to the control box 18, and the other signals stored in the control box 18 and the value from the SOx meter 31 that measures the SOx value in the exhaust gas downstream of the EP are below the regulation value. The control valves 25 and 29 control the control valve 21 for the fuel supplied to the front burner 21 and the amount of alkaline agent supplied from the alkali agent spray supply device 26.
is controlled. That is, the control valves 22, 25, and 29 are controlled by the temperature signal from the gas thermometer 20, and a suitable powdery fine solid of Na 2 SO 3 is obtained in EP12. This collected powdery fine solid is
A transportation device 32 connected to the EP 12 sends it to a bagging device (not shown).
また脱硫反応塔１１の入口ガス温度の制御のた
めエヤーヒーター９にバイパスダクト３３を設
け、その入口にダンパー３４，またエヤーヒータ
ー入口にダンパー３５を設ける。ボイラ１の負荷
条件に応じてバイパス流量制御手段たるダンパー
３５及びダンパー３４を調整し、排ガスの一部を
エヤーヒーター９をバイパスさせ脱硫反応塔１１
の入口ガス温度を確保することができる。ダンパ
ー３４，３５は全開全閉にするとは限らずガス温
度計２０及び３０ａの信号により適当な開度に調
整制御することができる。 Further, in order to control the gas temperature at the inlet of the desulfurization reaction tower 11, a bypass duct 33 is provided in the air heater 9, a damper 34 is provided at the inlet of the bypass duct 33, and a damper 35 is provided at the inlet of the air heater. The damper 35 and the damper 34, which are bypass flow rate control means, are adjusted according to the load conditions of the boiler 1, and a part of the exhaust gas is bypassed through the air heater 9, and the desulfurization reaction tower 11 is made to bypass the air heater 9.
The inlet gas temperature can be ensured. The dampers 34 and 35 are not necessarily fully open or fully closed, but can be adjusted to an appropriate opening degree based on the signals from the gas thermometers 20 and 30a.
しかしこのようなバイパスダクト手段のみでは
脱硫反応塔の排ガス温度を規定値にすることは炭
質の変動もあり限度があり、その場合には脱硫塔
入口にフロントバーナを設けることまたは排ガス
系路外の高温燃焼ガス装置からその高温排ガスを
脱硫塔入口に供給し、SOxを固体粒子化し集塵装
置での捕集の効果を高めるものである。 However, it is difficult to maintain the exhaust gas temperature of the desulfurization reaction tower at a specified value using only such bypass duct means due to variations in carbon quality. The high-temperature exhaust gas is supplied from the high-temperature combustion gas device to the inlet of the desulfurization tower, turning SOx into solid particles and increasing the effectiveness of the dust collector.
脱硫反応塔１１に供給される排ガス中に含まれ
るSOxの絶対値は排ガス量とSOxppmにより定ま
り、排ガスの保有する熱量はガス温度と排ガス量
により定まるものである。一方噴霧されたアルカ
リ液滴の蒸発に必要とする熱量はアルカリ剤の噴
霧量とその濃度により定まるその水分の量と温度
で定まる。煙突１３より排出するガス中のSOx値
は一定値以下に規制されるものである。従つてこ
れらの数値を制御箱にデータとして入れる必要が
あり、またこれらの数値により制御弁２２，２
８，２９又はダンパー３４，３５が制御される。
しかし粉状微粒固体としてNa2SO3を回収するに
は敏感に変動するガス温度計２０の信号により制
御弁、又はバイパス弁を制御し、EP入口のガス
温度を露点以上に保持する必要がある。 The absolute value of SOx contained in the exhaust gas supplied to the desulfurization reaction tower 11 is determined by the amount of exhaust gas and SOxppm, and the amount of heat held by the exhaust gas is determined by the gas temperature and amount of exhaust gas. On the other hand, the amount of heat required to evaporate the atomized alkali droplets is determined by the amount of water and temperature determined by the amount of alkali agent sprayed and its concentration. The SOx value in the gas discharged from the chimney 13 is regulated to be below a certain value. Therefore, it is necessary to input these values into the control box as data, and these values are used to control the control valves 22, 2.
8, 29 or dampers 34, 35 are controlled.
However, in order to recover Na 2 SO 3 as a powdery fine solid, it is necessary to control the control valve or bypass valve using the signal from the gas thermometer 20, which fluctuates sensitively, to maintain the gas temperature at the EP inlet above the dew point. .
＜発明の効果＞
この発明を実施することにより以下の効果が得
られた。<Effects of the Invention> The following effects were obtained by implementing this invention.
一実施例においては、排ガス量は25000Nm3／
ｈ
入口SO2濃度は1000ppm、脱硫率は90％
出口ガス温度は100℃、圧力損失は100mmAqで
あつた。 In one embodiment, the amount of exhaust gas is 25000Nm 3 /
h The inlet SO 2 concentration was 1000 ppm, the desulfurization rate was 90%, the outlet gas temperature was 100°C, and the pressure loss was 100 mmAq.
他の実施例においては、
排ガス量は100000Nm3／ｈ、入口SO2濃度は
1000ppm、脱硫率は85％ 出口温度は100℃ 圧
力損失は100mmAqであつた。 In another example, the exhaust gas amount is 100000Nm 3 /h, and the inlet SO 2 concentration is
1000ppm, desulfurization rate was 85%, outlet temperature was 100°C, and pressure loss was 100mmAq.
また運転条件（燃焼用空気のエヤーヒータ通過
による温度上昇）が許容されるときは一例として
の350℃の排ガスの量の約30％をエヤーヒータを
バイパスして流すときはエヤーヒータを通過した
排ガスとその後流で混合し脱硫塔入口で所望の
200℃近傍の排ガスが得られる。 In addition, if the operating conditions (temperature increase due to combustion air passing through the air heater) are permissible, for example, if approximately 30% of the amount of exhaust gas at 350°C is allowed to flow by bypassing the air heater, the exhaust gas that has passed through the air heater and its subsequent flow The desired amount is mixed at the desulfurization tower inlet.
Exhaust gas at around 200℃ can be obtained.
SOx値変動は±30％程度生じていたがSOx除去
は容易に制御され、出口排ガス中のSOx値は制限
規制値を満足するものであつた。また出口ばいじ
ん濃度は0.05ｇ／Ｎm3以下であつた。 Although the SOx value fluctuation occurred by about ±30%, SOx removal was easily controlled and the SOx value in the outlet exhaust gas satisfied the regulatory limit value. In addition, the soot and dust concentration at the outlet was less than 0.05g/ Nm3 .
この発明を実施することによりボイラに負荷変
動があり、しかも排ガス中のSOx値の変動のある
場合においてアルカリ剤、及び加熱エネルギーの
使用量を最も効果的に節約することができ粉状の
Na2SO3を回収し、しかも排ガス中のSOx値は制
制値以下にすることができ、しかも制御容易であ
る等種々の効果を奏することができるものである
ことが確められた。またボイラの排ガスの温度条
件によつては外部に特別の熱源を設ける必要なく
バイパスダクトの設置等の手段によりSOxを
Na2SO3の粉末として回収することが容易にでき
るものである。 By implementing this invention, when there are load fluctuations in the boiler and fluctuations in the SOx value in the exhaust gas, the amount of alkaline agent and heating energy used can be saved most effectively.
It has been confirmed that Na 2 SO 3 can be recovered, and the SOx value in the exhaust gas can be lowered to below the control value, and that it is easy to control and has various effects. Depending on the temperature conditions of the boiler exhaust gas, SOx can be removed by installing bypass ducts or other means without the need for a special external heat source.
It can be easily recovered as Na 2 SO 3 powder.
第１図はこの発明の実施にかかる装置の配置と
配管系統を示す図面、第２図はフロントバーナの
燃焼室を設けた脱硫反応塔入口の部分図である。
１…ボイラ、７…エコノマイザー、９…エヤヒ
ーター、１０…送風機、１１…脱硫反応塔、１２
…電気集塵機（EP）、１３…煙突、１５…ガス流
量計、１６…排ガス温度計、１７…SOx計、１８
…制御箱、１９…排ガス入口ダクト、２０…ガス
温度計、２１…フロントバーナ、２２，２５，２
９…制御弁、２６…アルカリ剤噴霧供給装置、３
３…バイパスダクト、３４，３５…ダンパー、３
６…燃焼室。
FIG. 1 is a drawing showing the arrangement and piping system of an apparatus according to the present invention, and FIG. 2 is a partial view of the inlet of a desulfurization reaction tower provided with a combustion chamber of a front burner. 1...Boiler, 7...Economizer, 9...Air heater, 10...Blower, 11...Desulfurization reaction tower, 12
...Electrostatic precipitator (EP), 13...Chimney, 15...Gas flow meter, 16...Exhaust gas temperature meter, 17...SOx meter, 18
...Control box, 19...Exhaust gas inlet duct, 20...Gas thermometer, 21...Front burner, 22, 25, 2
9... Control valve, 26... Alkaline agent spray supply device, 3
3... Bypass duct, 34, 35... Damper, 3
6... Combustion chamber.
Claims (1)
側より順にエヤヒータ、脱硫反応塔、集じん装置
を設け、かつ前記エヤヒータをバイパスするバイ
パスダクトを設け、該バイパスダクトを流れる排
ガス流量を制御するバイパス流量制御手段を設
け、前記エヤヒータと脱硫反応塔を接続する接続
ダクトに排ガス加熱量制御手段を有する排ガス加
熱手段を設け、前記脱硫反応塔にアルカリ剤噴霧
供給装置を設け、前記バイパスダクトの出口を前
記接続ダクトに開口させ、前記集じん器入口温度
を所望温度に保持するように前記排ガス加熱量制
御手段及び排ガスのバイパス流量制御手段を作動
させる作動手段よりなることを特徴とする半湿式
排ガス脱硫装置。1. An air heater, a desulfurization reaction tower, and a dust collector are provided in order from the upstream side of a combustion exhaust gas channel having a blower, and a bypass duct is provided to bypass the air heater, and a bypass flow rate is provided to control the flow rate of the exhaust gas flowing through the bypass duct. A control means is provided, an exhaust gas heating means having an exhaust gas heating amount control means is provided in a connecting duct connecting the air heater and the desulfurization reaction tower, an alkali spray supply device is provided in the desulfurization reaction tower, and the outlet of the bypass duct is connected to the A semi-humid exhaust gas desulfurization device, characterized in that it is made up of an operating means that is opened in the connecting duct and operates the exhaust gas heating amount control means and the exhaust gas bypass flow rate control means so as to maintain the precipitator inlet temperature at a desired temperature. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14353578A JPS5570323A (en) | 1978-11-22 | 1978-11-22 | Operation of semiwet system exhaust smoke desulfurizing apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14353578A JPS5570323A (en) | 1978-11-22 | 1978-11-22 | Operation of semiwet system exhaust smoke desulfurizing apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5570323A JPS5570323A (en) | 1980-05-27 |
| JPS6365368B2 true JPS6365368B2 (en) | 1988-12-15 |
Family
ID=15340999
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14353578A Granted JPS5570323A (en) | 1978-11-22 | 1978-11-22 | Operation of semiwet system exhaust smoke desulfurizing apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5570323A (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4924342A (en) * | 1972-05-08 | 1974-03-04 | ||
| JPS5213785A (en) * | 1975-07-22 | 1977-02-02 | Matsushita Electric Ind Co Ltd | Temperature compensation typesemiconductor elenent |
-
1978
- 1978-11-22 JP JP14353578A patent/JPS5570323A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4924342A (en) * | 1972-05-08 | 1974-03-04 | ||
| JPS5213785A (en) * | 1975-07-22 | 1977-02-02 | Matsushita Electric Ind Co Ltd | Temperature compensation typesemiconductor elenent |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5570323A (en) | 1980-05-27 |
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