JPS5852685B2 - Desulfurization method for flue gas with large fluctuations in SO↓2 concentration - Google Patents
Desulfurization method for flue gas with large fluctuations in SO↓2 concentrationInfo
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- JPS5852685B2 JPS5852685B2 JP55041003A JP4100380A JPS5852685B2 JP S5852685 B2 JPS5852685 B2 JP S5852685B2 JP 55041003 A JP55041003 A JP 55041003A JP 4100380 A JP4100380 A JP 4100380A JP S5852685 B2 JPS5852685 B2 JP S5852685B2
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Description
【発明の詳細な説明】
本発明は塩基性硫酸アルミニウム溶液をＳＯ２吸収液と
する排煙脱硫法に関し、特に、同一出願人に係る特願昭
４７−３６０８９号明細書（特開昭４８−１０３０９４
号公報）および特公昭５３−１５８３５号公報に記載し
た塩基性硫酸アルミニウム水溶液の循環により石膏を得
る排煙脱硫法の改良に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a flue gas desulfurization method using a basic aluminum sulfate solution as an SO2 absorption liquid, and in particular, the present invention relates to a flue gas desulfurization method using a basic aluminum sulfate solution as an SO2 absorption liquid, and in particular, to
This invention relates to an improvement in the flue gas desulfurization method for obtaining gypsum by circulating a basic aluminum sulfate aqueous solution described in Japanese Patent Publication No. 53-15835.
特開昭４８−１０３０９４号公報記載の排煙脱硫法は、
塩基性硫酸アルミニウム溶液のＳＯ２吸収能を利用しな
がら石膏を回収するもので、ＳＯ２吸収能が高く完全ク
ローズドシステムであり、長期安定模様が可能である等
の優れた長所を有し、消石灰吸収方式等に比べて数数の
利点を有している。The flue gas desulfurization method described in JP-A-48-103094 is as follows:
This method recovers gypsum while utilizing the SO2 absorption capacity of basic aluminum sulfate solution.It has excellent advantages such as high SO2 absorption capacity, completely closed system, and long-term stable pattern. It has several advantages compared to other methods.
このプロセスは、大きく分類すると、次の吸収工程、酸
化工程および中和工程からなる。Broadly speaking, this process consists of the following absorption step, oxidation step, and neutralization step.
（１）吸収工程
吸収塔でＳＯ２含有排ガスと塩基性硫酸アル□ニウム溶
液とを気液接触させ、気相中のＳＯ２を（１）式の反応
によって液相中に吸収させる。(1) Absorption step SO2-containing exhaust gas and basic aluminum sulfate solution are brought into gas-liquid contact in an absorption tower, and SO2 in the gas phase is absorbed into the liquid phase by the reaction of formula (1).
（２）酸化工程
吸収工程で塩基性硫酸アルミニウム溶液に吸収させたＳ
Ｏ２は、亜硫酸イオンとなって液中に存在する。(2) S absorbed in basic aluminum sulfate solution in oxidation process absorption process
O2 exists in the liquid as sulfite ions.
この液中に圧縮空気を微細気泡として吸込み、この亜硫
酸イオンを硫酸イオンにする。Compressed air is sucked into this liquid as fine bubbles to convert the sulfite ions into sulfate ions.
この酸化（式２）を酸化塔で行ない、酸化後の液は吸収
塔に繰返し、一部は中和工程に送液する。This oxidation (Formula 2) is performed in an oxidation tower, and the oxidized liquid is repeatedly sent to the absorption tower, and a portion is sent to the neutralization step.
（３）中和工程
吸収工程と酸化工程を循環している塩基性硫酸アルミニ
ウム溶液は次第に硫酸イオンが増加し、下式で定義する
塩基度が低下する。(3) Neutralization step In the basic aluminum sulfate solution circulating through the absorption step and oxidation step, sulfate ions gradually increase, and the basicity defined by the following formula decreases.
このため、その一部をＳＯ２負荷の変動に応じて抜き出
して中和槽に送り、炭酸カルシウムと反応させて所定の
塩基度まで中和し、硫酸イオンは石膏として循環液から
除外する（式３）。For this reason, a part of the SO2 is extracted according to fluctuations in the SO2 load and sent to the neutralization tank, where it is reacted with calcium carbonate and neutralized to a predetermined basicity, and the sulfate ions are removed from the circulating fluid as gypsum (Equation 3 ).
生成した石膏は沈殿槽で濃縮させ、スラリー状のものを
遠心分離機で済過脱水する。The generated gypsum is concentrated in a settling tank, and the slurry is dehydrated in a centrifuge.
ろ液および洗浄水は全量工程水として再利用する。All of the filtrate and washing water will be reused as process water.
本発明の目的は、この方法を例えば銅製錬排ガス処理硫
酸工場の排ガス等の如く排ガス量が太きくしかもそのＳ
Ｏ２濃度が例えば転炉の操業状況により急激に変化する
ような排ガス系に有利に適用できるように改良すること
である。The object of the present invention is to apply this method to a process where the amount of exhaust gas is large and its S
The object of the present invention is to improve the method so that it can be advantageously applied to an exhaust gas system in which the O2 concentration changes rapidly depending on the operating conditions of a converter, for example.
この目的において本発明は、排ガス中のＳＯ２負荷の変
動に無関係に最大ＳＯ２負荷に合わせて吸収工程と酸化
工程を循環する循環液を一定量づつ連続的に抜き出して
中和工程に供給し、中和工程でのアルカリ剤添加量を中
和工程出口液の塩基度により制御する排煙脱硫法を提供
する。For this purpose, the present invention continuously extracts a fixed amount of the circulating fluid that circulates between the absorption process and the oxidation process in accordance with the maximum SO2 load, regardless of fluctuations in the SO2 load in the exhaust gas, and supplies it to the neutralization process. Provided is a flue gas desulfurization method in which the amount of alkaline agent added in the neutralization step is controlled by the basicity of the exit liquid from the neutralization step.
以下に本発明法の詳細を操業実施例に従って具体的に説
明する。The details of the method of the present invention will be specifically explained below according to operational examples.
第１図は、Ｋ製錬所転炉排ガス硫酸工場の排ガスに本発
明を適用した設備フローシートである。FIG. 1 is an equipment flow sheet in which the present invention is applied to the exhaust gas from the converter furnace of the K smelter and the exhaust gas from the sulfuric acid factory.
第１図において、１はＡＩ吸収塔、２はＡ２吸収塔、３
はＡ１ポンプタンク、４はＡ２ポンプタンク、５は酸化
塔、６は中和塔、７はシックナー、８は遠心分離機、９
はろ液タンク、ＢＭは塩基度計を示している。In Figure 1, 1 is an AI absorption tower, 2 is an A2 absorption tower, and 3 is an AI absorption tower.
is A1 pump tank, 4 is A2 pump tank, 5 is oxidation tower, 6 is neutralization tower, 7 is thickener, 8 is centrifugal separator, 9
indicates the filtrate tank, and BM indicates the basicity meter.
この排煙脱硫設備の処理能力は、１２５０００ Ｎｄ／
Ｈｒであり、硫酸製造設備が２系列に構成されている事
から排煙脱硫吸収塔も２系列となっている。The processing capacity of this flue gas desulfurization equipment is 125,000 Nd/
Hr, and since the sulfuric acid production equipment is configured in two lines, the flue gas desulfurization absorption tower is also in two lines.
酸化、中和系は、運転管理および保守の面からｌ系列と
なっている。The oxidation and neutralization systems are in the L series from the standpoint of operation management and maintenance.
硫酸工場の吸収塔（図示せず）を出たガスは、排煙脱硫
吸収塔１，２（以下、吸収塔と呼ぶ）に入りＳＯ２を除
去後排出される。Gas leaving the absorption tower (not shown) of the sulfuric acid factory enters flue gas desulfurization absorption towers 1 and 2 (hereinafter referred to as absorption towers) and is discharged after removing SO2.
吸収塔１，２を出た循環液は、ポンプタンク３に入り、
循環ポンプで酸化塔５に送られる。The circulating liquid that has left the absorption towers 1 and 2 enters the pump tank 3,
It is sent to the oxidation tower 5 by a circulation pump.
酸化塔５では循環液中の亜硫酸アルミニウムを空気酸化
し、オーバーフローした液はポンプタン、り４に入り、
循環ポンプで再び吸収塔２，１にスプレーされる。In the oxidation tower 5, the aluminum sulfite in the circulating fluid is oxidized with air, and the overflowing fluid enters the pump sump tank 4.
The circulation pump sprays the absorption towers 2 and 1 again.
循環液の一部は連続的に酸化塔５かも中和設備６に一定
量抜き出し、炭酸カルシウムパルプで所定の塩基度まで
中和する。A certain amount of the circulating liquid is continuously extracted from the oxidizing tower 5 or into the neutralization equipment 6, and neutralized with calcium carbonate pulp to a predetermined basicity.
中和設備６より液はオーバーフローし、シックナー７に
入る。The liquid overflows from the neutralization equipment 6 and enters the thickener 7.
ここで石膏は１０〜１５％程度のスラリーとなってシッ
クナーアンダーフローとして抜き出され、一部は中和設
備６へ種晶として、残りは遠心分離機８に送られる。Here, the gypsum becomes a slurry of about 10 to 15% and is extracted as a thickener underflow, a part of which is sent to the neutralization equipment 6 as a seed crystal, and the rest to the centrifuge 8.
遠心分離機８で分離された石膏は、付着水１０〜１３優
で系外に排出される。The gypsum separated by the centrifugal separator 8 is discharged from the system with 10 to 13 yen of adhering water.
一方シックナーオーバーフローは再び吸収、酸化工程の
循環液として使用される。On the other hand, the thickener overflow is used again as a circulating fluid for the absorption and oxidation processes.
Ａ１吸収塔１は、直径２．９ｍ、高さ１２．０７７７．
０大きさであり、内部は三段となっており上段はデ□ス
タ一部として使用し、それぞれの段にはＳ型テラレット
が充填されている。A1 absorption tower 1 has a diameter of 2.9 m and a height of 12.0777 m.
0 size, and has three stages inside, the upper stage is used as part of the data storage, and each stage is filled with S-type terraret.
Ａ２吸収塔は、巾４．１４ｍ、長さ６．５ｍ、高さ１２
．９ｍの木製の内部耐酸ライニング構造となっており、
ＡＩ吸収塔１と同様内部は三段になっている。The A2 absorption tower has a width of 4.14 m, a length of 6.5 m, and a height of 12 m.
．． It has a 9m wooden internal acid-resistant lining structure,
Like the AI absorption tower 1, the interior has three stages.
従来の塩基性硫酸アルミニウムー石膏法における排煙脱
硫設備での吸収塔への循環液の装入は、トレイ方式が普
通であるが本発明法では気液接触率を大きくする為にス
プレ一方式とした。In the conventional basic aluminum sulfate-gypsum method, the circulating liquid is normally charged to the absorption tower in flue gas desulfurization equipment using a tray method, but in the present method, a spray method is used to increase the gas-liquid contact ratio. And so.
この方式にした事と排ガス中の酸素濃度が８〜１０係と
高い事により、吸収塔内での自己酸化率が９５％以上と
なり、吸収塔入口ガス中のＳＯ２が３０００泗以下では
酸化塔を経由しなくても操業にはさしつかえない。Due to this method and the high oxygen concentration in the exhaust gas of 8 to 10%, the self-oxidation rate in the absorption tower is over 95%, and when the SO2 in the absorption tower inlet gas is less than 3000 cm, the oxidation tower is closed. Even if you do not go through it, there will be no problem in operation.
酸化塔５は直径３．６ｍ、高さ１０．６ｍの大きさであ
り、吸収液の滞留時間は１３分となっている。The oxidation tower 5 has a diameter of 3.6 m and a height of 10.6 m, and the residence time of the absorption liquid is 13 minutes.
空気圧縮機は吐出圧カフ贅、風量１６．４ ｍ３７ ｍ
ｉｎのものが３基ありｌ基常用、２基予備となっている
。The air compressor has a discharge pressure cuff and an air volume of 16.4 m37 m
There are three in-type units, one for regular use and two for spare.
中和設備６は、第１中和槽、第２中和槽共直径５．０？
７Ｚ、高さ５．０？７Ｚ、内容積９０ｍ３である。The neutralization equipment 6 has a first neutralization tank and a second neutralization tank both having a diameter of 5.0?
7Z, height 5.0~7Z, internal volume 90m3.
液の滞留時間を増す為に攪拌機の回転方向が、第１と第
２が逆にしており、その滞留時間は約１時間である。In order to increase the residence time of the liquid, the rotation directions of the first and second stirrers are reversed, and the residence time is about 1 hour.
炭酸カルシウムは、−２００ｍｅＳｈＯものを使用して
いる。The calcium carbonate used is -200meShO.
従来の塩基性硫酸アルミニウム石膏法における排煙脱硫
設備でのコントロール方式は、酸化塔から中和槽への循
環液の抜き出し量を循環液の塩基度によりコントロール
していたが、つまり、ＳＯ２負荷の変動によりその抜き
出し量ヲコントロールしていたが、本発明では、急激な
ＳＯ７負荷変動に追従させる為と、コントロール操作を
簡略化する為に、酸化塔から中和槽への抜き出し量をＳ
Ｏ２負荷が最大の点に合わせて一定とした。In the conventional control system for flue gas desulfurization equipment using the basic aluminum sulfate gypsum method, the amount of circulating fluid withdrawn from the oxidation tower to the neutralization tank was controlled by the basicity of the circulating fluid. Previously, the amount of SO7 extracted was controlled by fluctuations, but in the present invention, in order to follow sudden SO7 load fluctuations and to simplify control operations, the amount of SO7 extracted from the oxidation tower to the neutralization tank is controlled by S.
The O2 load was set constant at the maximum point.
例えば、同一出願人に係る特公昭５３１５８３５号公報
に示されているように、従来の塩基性アルミニウムー石
膏法による脱硫法では。For example, in the conventional desulfurization method using the basic aluminum-gypsum method, as shown in Japanese Patent Publication No. 5315835 filed by the same applicant.
酸化系塩基度は５φ以下にならないように、酸化塔から
の液の抜き出し量がコントロールされ、中和系塩基度は
３０％を越えないように、ＣａＣＯ３の添加量がコント
ロールされていた。The amount of liquid withdrawn from the oxidation tower was controlled so that the oxidation basicity did not fall below 5φ, and the amount of CaCO3 added was controlled so that the neutralization basicity did not exceed 30%.
しかし、この従来法によると、急激なＳＯ２負荷の変動
に追従することができない。However, according to this conventional method, it is not possible to follow sudden changes in the SO2 load.
なぜなら、急激にＳＯ２負荷が増加 た場合でも保有液
量の関係から酸化系塩基度が即時に下降するわけではな
く、従って酸化塔抜き出し量もＳＯ２負荷に追従するこ
とができない。This is because even if the SO2 load suddenly increases, the basicity of the oxidizing system does not immediately decrease due to the amount of retained liquid, and therefore the amount extracted from the oxidation tower cannot follow the SO2 load.
さらに、酸化塔抜き出し量を増加させたとしても、その
抜き出し液は中和槽６、シックナー７を経由して流れる
ので、即時に酸化系への液量を増加させることは困難で
あり、酸化系塩基度も即時に上昇しない。Furthermore, even if the amount of liquid extracted from the oxidation tower is increased, the liquid extracted from the oxidation tower flows through the neutralization tank 6 and the thickener 7, so it is difficult to immediately increase the amount of liquid to the oxidation system. Basicity also does not increase immediately.
それゆえ、特公昭５３１５８３５号公報に示されたコン
トロール方式では、ＳＯ２負荷が急激に高くなり酸化系
塩基度が下降してもそれを即時適切な塩基度に戻すこと
ができず、結局、急激なＳＯ２負荷変動に追従ができな
かった。Therefore, with the control method shown in Japanese Patent Publication No. 5315835, even if the SO2 load suddenly increases and the oxidation system basicity decreases, it is not possible to immediately return it to the appropriate basicity, and in the end, the sudden increase in It was not possible to follow SO2 load fluctuations.
本発明はこれらの点を改善し、酸化塔抜き出し量を最大
ＳＯ２負荷に設定した。The present invention has improved these points and set the oxidation tower withdrawal amount to the maximum SO2 load.
この方式によると、酸化塔抜き出し量は常に最大ＳＯ２
負荷に合わせて一定量としているので、ＳＯ２負荷が急
激に増加しても、それ以前にすでに酸化系塩基度は最大
ＳＯ２負荷に対応できるものとなっている。According to this method, the amount of SO2 extracted from the oxidation tower is always the maximum.
Since the amount is kept constant according to the load, even if the SO2 load increases rapidly, the oxidation basicity is already at a level that can correspond to the maximum SO2 load.
これにより、急激なＳＯ２負荷変動に対して追従するこ
とが可能となった。This makes it possible to follow sudden SO2 load fluctuations.
つまり、急激なＳＯ２負荷変動に対応するには、特公昭
５３−１５８３５号公報に示された中和系塩基度により
ＣａＣＯ３の添加量をコントロールする方式だけでは無
理があり、酸化塔抜き出し量を常に最大ＳＯ２負荷に設
定して初めて可能となったものである。In other words, in order to cope with rapid SO2 load fluctuations, it is impossible to control the amount of CaCO3 added by using the basicity of the neutralization system as shown in Japanese Patent Publication No. 15835/1983, and the amount of CaCO3 extracted from the oxidation tower must be constantly adjusted. This was only possible after setting the maximum SO2 load.
また、中和槽６への炭酸カルシウムパイプの装入は、中
和槽出口の塩基度を塩基度計ＢＭによって計測してこれ
に応じて制御弁■によってコントロールするようにした
。Furthermore, the charging of the calcium carbonate pipe into the neutralization tank 6 was controlled by the control valve ① by measuring the basicity at the outlet of the neutralization tank using a basicity meter BM.
これにより急激なＳ０２負荷変動があっても、吸収塔出
口ガス中のＳＯ２濃度はあまり変化しないようになった
。As a result, even if there is a sudden change in the S02 load, the SO2 concentration in the gas at the outlet of the absorption tower does not change much.
遠心分離機８は、バスケット内径５５インチの立型遠心
分離機が２台、４８インチが２台、計４台設置されてお
り、１バッチ当りの石膏分離能力は、５５インチが４０
０＠、４８インチが３００に７となっており、常時２台
運転としている。The centrifuge 8 has a total of four centrifuges, two with a 55-inch basket inner diameter and two with a 48-inch basket, and the gypsum separation capacity per batch is 40 centrifuges with a 55-inch basket.
0 @, 48 inch is 7 in 300, and two units are always in operation.
ここで石膏は水分１０〜１３ｏＩ）に脱水される。Here, the gypsum is dehydrated to a moisture content of 10 to 13 oI).
本発明は完全クローズドシステムであるが、製品石膏に
混入したアルミニウム分は補充しなげればならない。Although the present invention is a completely closed system, the aluminum content mixed into the product gypsum must be replenished.
この補充アルミニウム分を製錬所で創製されるアンモニ
ウム明パン中のアルミニウムを使用することができる。The aluminum in the ammonium bright bread produced in the smelter can be used for this supplementary aluminum content.
アンモニウム明パンからアルミニウムイオンとアンモニ
ウムイオンの分離工程を次に示す。The process of separating aluminum ions and ammonium ions from ammonium bread is shown below.
アンモニウム明パン結晶を溶解槽１０で水に溶解し、そ
の溶解液を中和槽１１において炭酸カルシウムにて中和
し、水酸化アルミニウムの沈殿を生成させる。Ammonium bright bread crystals are dissolved in water in a dissolution tank 10, and the solution is neutralized with calcium carbonate in a neutralization tank 11 to form a precipitate of aluminum hydroxide.
そして沈殿槽１２にて固液分離した後、上澄液は鉱水処
理場に送られる。After solid-liquid separation in the settling tank 12, the supernatant liquid is sent to a mineral water treatment plant.
中和工程で生成した水酸化アルミニウムは、中和槽６に
送られ液中の硫酸イオンと反応し硫酸アルミニウムとな
り、これに所定の炭酸カルシウムを加え塩基性硫酸アル
ミニウム溶液とする。The aluminum hydroxide produced in the neutralization step is sent to the neutralization tank 6 and reacts with sulfate ions in the liquid to become aluminum sulfate, and a predetermined amount of calcium carbonate is added to this to form a basic aluminum sulfate solution.
上記の各工程を化学反応式で示すと次の様になる。The chemical reaction formula for each of the above steps is as follows.
このアンモニウム明パンは脱硫率および製品石膏の品質
にも何ら問題はないことがわかった。It was found that this ammonium bright bread had no problems with the desulfurization rate or the quality of the product gypsum.
操業成績の一例を第２図に示すが、本発明による塩基度
の適正な管理と定量抜き出しコントロール方式により、
急激なガス量、およびＳＯ２濃度の変化があっても脱硫
率はほぼ一定となっており、良好な成績が得られている
。An example of the operational results is shown in Figure 2, which shows that due to the proper management of basicity and quantitative extraction control method according to the present invention,
Even with sudden changes in the gas amount and SO2 concentration, the desulfurization rate remained almost constant, and good results were obtained.
産出される石膏の分析例、および粒度分布を第１表およ
び第２表に示すが、品質よくスタートして以来順調な操
業を続けることができた。Tables 1 and 2 show examples of analysis and particle size distribution of the gypsum produced, and since the plant started with good quality, it has been able to continue smooth operations.
操業成績（１ケ月間の平均）
処理ガス量 １１７０００ Ｎｍ３／ Ｈｒ入ロガス
中のＳＯ２１４５０卿
出ロガス中のＳＯ２２０ｐｐ［ｌ
脱 硫 率 ９８．６多Operation results (average for one month) Processed gas amount 117,000 Nm3/Hr SO2 in the log gas containing 1,450 SO2 in the log gas exiting 20 pp [l] Desulfurization rate 98.6
第１図は本発明法の実施例を示すフローシート、第２図
は本発明法の実施例の成績図である。
１．２・・・・・・吸収塔、５・・・・・・酸化塔、６
・・・・・・中和槽、７・・・・・・シックナー ８・
・・・・・遠心分離機。FIG. 1 is a flow sheet showing an example of the method of the present invention, and FIG. 2 is a results chart of an example of the method of the present invention. 1.2... Absorption tower, 5... Oxidation tower, 6
... Neutralization tank, 7 ... Thickener 8.
·····centrifuge.
Claims (1)
とを気液接触させて気相中のＳＯ２を液相に吸収させる
吸収工程と；吸収液中の亜硫酸イオンを硫酸イオンに液
相酸化させる酸化工程と；酸化工程を経た液を吸収工程
に循環すると共に、この酸化工程を経た液の一部を排ガ
ス中のＳＯ２負荷の変動とは無関係に最大ＳＯ２負荷に
合わせて一定量連続的に抜き出す工程と；この抜き出し
液に炭酸カルシウムを加えて中和する工程と；この中和
工程を出た液の塩基度により中和工程で添加する炭酸カ
ルシウム量を制御する工程と；中和工程を経た液をシッ
クナーに導きそのオーバーフローを前記吸収および酸化
工程の循環液に合液させかつそのアンダーフローの少な
くとも１部を中和工程に繰返す工程と；からなるＳＯ２
濃度の変動が激しい排煙の脱硫法。 ２ ＳＯ２含有排ガスと塩基性硫酸アルミニウム水溶液
とを気液接触させて気相中のＳＯ２を液相に吸収させる
吸収工程と；吸収液中の亜硫酸イオンを硫酸イオンに液
相酸化させる酸化工程と；酸化工程を経た液を吸収工程
に循環すると共に、この酸化工程を経た液の一部を排ガ
ス中のＳＯ２負荷の変動とは無関係に最大ＳＯ２負荷に
合わせて一定量連続的に抜き出す工程と；この抜き出し
液に炭酸カルシウムを加えて中和する工程と；この中和
工程を出た液の塩基度により中和工程で添加する炭酸カ
ルシウム量を制御する工程と；アンモニウム明パンを溶
解および中和して水酸化アルミニウムを生成させ、これ
を前記酸化液中の硫酸イオンと反応させて硫酸アルミニ
ウムを生成させ、これを炭酸カルシウムと反応させて系
内袖充用塩基性硫酸アルミニウム水溶液を形成させる工
程と；中和工程を経た液をシックナーに導きそのオーバ
ーフローを前記吸収および酸化工程の循環液に合液させ
かつそのアンダーフローの少なくとも１部を中和工程に
繰返す工程と；からなるＳＯ２濃度の変動が激しい排煙
の脱硫法。[Claims] 1. An absorption step in which SO2-containing exhaust gas and a basic aluminum sulfate aqueous solution are brought into gas-liquid contact and SO2 in the gas phase is absorbed into the liquid phase; An oxidation step in which the liquid that has undergone the oxidation step is circulated to the absorption step, and a portion of the liquid that has undergone the oxidation step is continuously pumped in a constant amount to match the maximum SO2 load, regardless of fluctuations in the SO2 load in the exhaust gas. A step of adding calcium carbonate to the extracted liquid to neutralize it; A step of controlling the amount of calcium carbonate added in the neutralization step depending on the basicity of the liquid exiting the neutralization step; a neutralization step a step of introducing the liquid through a thickener and combining the overflow with the circulating liquid of the absorption and oxidation step, and repeating at least a part of the underflow to the neutralization step;
Desulfurization method for flue gas whose concentration fluctuates widely. 2. An absorption step in which SO2-containing exhaust gas and a basic aluminum sulfate aqueous solution are brought into gas-liquid contact and SO2 in the gas phase is absorbed into the liquid phase; An oxidation step in which sulfite ions in the absorption liquid are oxidized to sulfate ions in the liquid phase; A step in which the liquid that has undergone the oxidation process is circulated to the absorption process, and a part of the liquid that has undergone the oxidation process is continuously extracted in a fixed amount in accordance with the maximum SO2 load, regardless of fluctuations in the SO2 load in the exhaust gas; A process of adding calcium carbonate to the extracted liquid to neutralize it; a process of controlling the amount of calcium carbonate added in the neutralization process depending on the basicity of the liquid exiting the neutralization process; and a process of dissolving and neutralizing the ammonium light bread. producing aluminum hydroxide, reacting this with sulfate ions in the oxidizing solution to produce aluminum sulfate, and reacting this with calcium carbonate to form a basic aluminum sulfate aqueous solution for refilling the system; a step in which the liquid that has undergone the neutralization process is led to a thickener, the overflow is combined with the circulating liquid from the absorption and oxidation process, and at least a part of the underflow is repeated in the neutralization process; the SO2 concentration fluctuates rapidly; Flue gas desulfurization method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55041003A JPS5852685B2 (en) | 1980-03-29 | 1980-03-29 | Desulfurization method for flue gas with large fluctuations in SO↓2 concentration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55041003A JPS5852685B2 (en) | 1980-03-29 | 1980-03-29 | Desulfurization method for flue gas with large fluctuations in SO↓2 concentration |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56136626A JPS56136626A (en) | 1981-10-26 |
| JPS5852685B2 true JPS5852685B2 (en) | 1983-11-24 |
Family
ID=12596218
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP55041003A Expired JPS5852685B2 (en) | 1980-03-29 | 1980-03-29 | Desulfurization method for flue gas with large fluctuations in SO↓2 concentration |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5852685B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7242378B2 (en) * | 2019-03-28 | 2023-03-20 | 三菱重工業株式会社 | Separation and recovery system and separation and recovery method |
| CN114591761A (en) * | 2022-03-17 | 2022-06-07 | 鄂尔多斯职业学院 | Method for preparing hydrogen by coal gasification and acid gas removing device |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5315835A (en) * | 1976-07-28 | 1978-02-14 | Iwatsu Electric Co Ltd | Magnetic latent image recording and its controller |
-
1980
- 1980-03-29 JP JP55041003A patent/JPS5852685B2/en not_active Expired
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5315835A (en) * | 1976-07-28 | 1978-02-14 | Iwatsu Electric Co Ltd | Magnetic latent image recording and its controller |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56136626A (en) | 1981-10-26 |
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