JPH08196863A - Oxidation of waste liquid from magnesium process flue gas desulfurization equipment - Google Patents
Oxidation of waste liquid from magnesium process flue gas desulfurization equipmentInfo
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- JPH08196863A JPH08196863A JP7010086A JP1008695A JPH08196863A JP H08196863 A JPH08196863 A JP H08196863A JP 7010086 A JP7010086 A JP 7010086A JP 1008695 A JP1008695 A JP 1008695A JP H08196863 A JPH08196863 A JP H08196863A
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- Prior art keywords
- oxidation
- liquid
- oxidation tower
- tower
- flue gas
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Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は脱硫剤として、水酸化マ
グネシウム〔Ｍｇ（ＯＨ）2 〕または酸化マグネシウム
〔ＭｇＯ〕を使用する湿式の排煙脱硫装置から抜き出さ
れた排水を酸化塔で酸化する方法に関する。BACKGROUND OF THE INVENTION The present invention oxidizes waste water extracted from a wet type flue gas desulfurization device using magnesium hydroxide [Mg (OH) 2 ] or magnesium oxide [MgO] as a desulfurizing agent in an oxidation tower. On how to do.
【０００２】[0002]
【従来の技術】マグネシウム法湿式排煙脱硫装置の概略
フロー例を図７に示す。この装置は処理水（液中浮遊物
質ＳＳ量＜３０ｍｇ／リットル、化学的酸素要求量ＣＯ
Ｄ＜３０ｍｇ／リットル≒液中亜硫酸濃度＜３．７５ｍ
ｍｏｌ／リットル、液ｐＨ：５．５〜８．５）を海に放
流できることから（火力発電所等で一般に利用されてい
る石灰石膏法のような石膏回収装置が不要なため、低イ
ニシャルコストとなる）、一般産業（自家発）ボイラ用
の排煙脱硫装置として広く利用されている。そのため、
機器の主要な構成は、ボイラ排ガス中のＳＯ2 除去及
び除塵を行う吸収塔（脱硫塔）、脱硫排液中のＣＯＤ
源であるＳＯ2 吸収により生成した亜硫酸〔ＭｇＳＯ3
＋Ｍｇ（ＨＳＯ3 ）2 〕を空気酸化（ＭｇＳＯ3 ＋１／
２Ｏ2 →ＭｇＳＯ4 ）して、排液のＣＯＤを低減する酸
化塔、亜硫酸の空気酸化で生成した硫酸塩（イオン）
により低下した排液のｐＨを中性付近に戻すためのアル
カリ液供給システム、排液中の浮遊物質を除去するた
めの排水フィルタなどから成る。2. Description of the Related Art FIG. 7 shows a schematic flow example of a magnesium method wet flue gas desulfurization apparatus. This equipment treats treated water (suspended matter SS in liquid <30 mg / liter, chemical oxygen demand CO
D <30 mg / liter ≈ liquid sulfite concentration <3.75 m
Since it can release mol / liter, liquid pH: 5.5-8.5) into the sea (because it does not require a gypsum recovery device such as the lime gypsum method generally used in thermal power plants, etc., low initial cost and It is widely used as a flue gas desulfurization device for general industrial (in-house) boilers. for that reason,
The main components of the equipment are the absorption tower (desulfurization tower) that removes SO 2 and the dust in the boiler exhaust gas, and the COD in the desulfurization effluent.
Sulfurous acid generated by absorption of SO 2 as a source [MgSO 3
+ Mg (HSO 3 ) 2 ] is air-oxidized (MgSO 3 + 1 /
2O 2 → MgSO 4 ) to reduce COD of the effluent, a sulfate (ion) produced by the air oxidation of sulfurous acid
It consists of an alkaline solution supply system for returning the pH of the drainage lowered to about neutral to a drainage filter for removing suspended matter in the drainage.
【０００３】この内の酸化塔及びアルカリ液供給シ
ステムについて、従来のシステムを図８に示す。図８に
おいて、（ａ）脱硫塔底部より抜き出された液８（ｐ
Ｈ：５．５〜６．５）は、酸化塔１へ移送される。
（ｂ）酸化塔１の底部に設置された散気管２にブロワな
どにより酸化空気１０を送気する。（ｃ）酸化塔１内で
は、液中の亜硫酸の酸化が行われると共に、液中に溶解
していたＳＯ2 ガスが気相側に放散する。（ｄ）酸化塔
１内をバブリングさせた空気は前記のとおり、ＳＯ2を
含んでいるため、脱硫塔１１へ戻す。（ｅ）酸化塔１で
ＣＯＤを充分に低減（ＣＯＤ＜３０ｍｇ／リットル、亜
硫酸濃度＜３．７５ｍｍｏｌ／リットル）された液は、
亜硫酸の酸化により生成した硫酸イオンのため、液ｐＨ
が低下（酸化塔出口でｐＨ３前後）する。これを中性付
近に戻すため、酸化塔１出口液ｐＨが５．５〜６．５と
なるようｐＨ電極４及びｐＨ計５に連動した制御弁６の
開度を自動的に変更し、アルカリ液タンク７内のアルカ
リ薬剤を酸化塔１出口液に添加する。（ｆ）ｐＨ調整さ
れた酸化塔１出口液を排液中のＳＳ除去のための排水フ
ィルタ９へ供給する。（ｇ）なお、酸化塔１の底部に沈
降・蓄積した固形物は、適宜ドレン抜き３より排出す
る。上記（ｅ）で使用するアルカリ薬剤は、一般に脱硫
剤として使用しているＭｇ（ＯＨ）2 やＭｇＯスラリが
利用される。また、酸化塔１内での液滞留時間は、３時
間程度である。FIG. 8 shows a conventional system for the oxidizing tower and the alkaline liquid supply system. In FIG. 8, (a) Liquid 8 (p
H: 5.5 to 6.5) is transferred to the oxidation tower 1.
(B) The oxidizing air 10 is sent to the diffuser pipe 2 installed at the bottom of the oxidation tower 1 by a blower or the like. (C) In the oxidation tower 1, the sulfurous acid in the liquid is oxidized and the SO 2 gas dissolved in the liquid is diffused to the gas phase side. (D) Since the air bubbling in the oxidation tower 1 contains SO 2 as described above, it is returned to the desulfurization tower 11. (E) The liquid whose COD has been sufficiently reduced in the oxidation tower 1 (COD <30 mg / liter, sulfur dioxide concentration <3.75 mmol / liter) is
Due to the sulfate ion generated by the oxidation of sulfurous acid, the liquid pH
Decrease (pH of around 3 at the outlet of the oxidation tower). In order to return this to near neutrality, the opening of the control valve 6 linked to the pH electrode 4 and the pH meter 5 is automatically changed so that the pH of the liquid at the outlet of the oxidation tower 1 is 5.5 to 6.5. The alkaline chemical in the liquid tank 7 is added to the outlet liquid of the oxidation tower 1. (F) The pH-adjusted outlet liquid of the oxidation tower 1 is supplied to the drainage filter 9 for removing SS in the waste liquid. (G) The solid matter settled and accumulated at the bottom of the oxidation tower 1 is appropriately discharged from the drainage 3. As the alkaline chemical used in the above (e), Mg (OH) 2 or MgO slurry which is generally used as a desulfurizing agent is used. The liquid retention time in the oxidation tower 1 is about 3 hours.
【０００４】[0004]
【発明が解決しようとする課題】酸化塔１へ供給される
脱硫塔底部抜き出し液８は、脱硫塔循環液と同様ｐＨ
５．５〜６．５の液で、先に提案したとおり（特願平６
−２４１６２）、脱硫効率向上、脱硫剤溶解促進、亜硫
酸塩析出防止の観点から亜硫酸濃度５０〜１００ｍｍｏ
ｌ／リットルの液としている。以下に従来の酸化塔の問
題点を列記する。 （ｉ）酸化塔の容量が大きい、 ・材料費、設置面積が大きくイニシャルコストが高い、 ・保守・点検時に、内部の大量の液を抜き出すピットが
必要である、 （ii）排水規制強化に伴い、更に高効率な酸化塔が必要
である。The desulfurization tower bottom withdrawal liquid 8 supplied to the oxidation tower 1 has the same pH as the desulfurization tower circulating liquid.
With the liquids of 5.5 to 6.5, as proposed previously (Japanese Patent Application No.
24162), from the viewpoint of improving the desulfurization efficiency, promoting the dissolution of the desulfurizing agent, and preventing the precipitation of sulfite, the sulfite concentration is 50 to 100 mmo.
It is a 1 / liter liquid. The problems of the conventional oxidation tower are listed below. (I) The capacity of the oxidation tower is large, -The material cost, the installation area is large, and the initial cost is high-A pit for extracting a large amount of liquid inside is required during maintenance / inspection. However, a highly efficient oxidation tower is required.
【０００５】本発明は脱硫剤として、水酸化マグネシウ
ム〔Ｍｇ（ＯＨ）2 〕または酸化マグネシウム〔Ｍｇ
Ｏ〕を使用する湿式の排煙脱硫装置から抜き出された排
水を酸化塔で酸化する方法を改良し、酸化を効率化し、
酸化塔を小型化することを目的とする。The present invention uses magnesium hydroxide [Mg (OH) 2 ] or magnesium oxide [Mg] as a desulfurizing agent.
O] is used to improve the method of oxidizing the wastewater extracted from the wet type flue gas desulfurization device in an oxidation tower to improve the efficiency of the oxidation,
The purpose is to reduce the size of the oxidation tower.
【０００６】[0006]
【課題を解決するための手段】酸化塔内での亜硫酸の酸
化が効率良く行われるよう（空気中の酸素の高い利用率
が得られるよう）、酸化塔内の液ｐＨ及び液滞留時間を
最適制御し、酸化塔の小容量化（ブロワの小型化）を図
るために本発明はなされたものであって、特にアルカリ
薬剤を、酸化塔入口液に添加することを特徴とする。す
なわち、本発明は、マグネシウム法排煙脱硫装置の気泡
塔方式廃液酸化方法において、酸化塔出口液のｐＨを検
知し、酸化塔出口液のｐＨが５．５以上になるように、
酸化塔入口液のｐＨをアルカリ性薬剤により制御するこ
とにより、酸化塔を小容量化（小型化）または酸化空気
導入量を低減（空気供給ブロワを小型化）することを特
徴とする上記方法を提供するものである。[Means for Solving the Problems] The liquid pH and the liquid retention time in the oxidation tower are optimized so that the oxidation of sulfurous acid in the oxidation tower is performed efficiently (to obtain a high utilization rate of oxygen in the air). The present invention has been made in order to control and reduce the capacity of the oxidation tower (downsizing of the blower), and is characterized in that an alkaline chemical is added to the oxidation tower inlet liquid. That is, the present invention, in the bubble column type waste liquid oxidation method of the magnesium method flue gas desulfurization apparatus, detects the pH of the oxidation tower outlet liquid, so that the pH of the oxidation tower outlet liquid is 5.5 or more,
Provided is the above method characterized by reducing the capacity of the oxidation tower (downsizing) or reducing the amount of oxidizing air introduced (downsizing the air supply blower) by controlling the pH of the inlet liquid of the oxidation tower with an alkaline chemical. To do.
【０００７】[0007]
【作用】液中亜硫酸の空気酸化による液ｐＨとの関係を
明確にするため、マグネシウムの亜硫酸塩を使用して、
図２に示す平面接触攪拌槽を用いた液中亜硫酸の酸化性
確認実験を実施した。その結果、図３に示すとおり液ｐ
Ｈが６．０〜６．５の時をピークに、液ｐＨの低下に伴
い液中亜硫酸の酸化速度が小さく（酸化性が悪く）なる
ことを確認した。この図は液ｐＨと総括物質移動係数Ｋ
G との関係を示す。また、図４に示す気泡塔を用いて、
本発明の実装置の酸化塔を模擬した液中亜硫酸の酸化試
験を実施した。その結果、図５Ａ及びＢに示すとおり、
酸化塔出口液ｐＨを高く（ｐＨ＝５．５）保つように酸
化塔入口液にアルカリ薬剤〔Ｍｇ（ＯＨ）2 スラリ〕を
添加した場合、これを添加しない（酸化塔出口液のｐＨ
調整なし）場合に比較して、液の酸化塔内滞留時間が短
くて（小さい酸化塔容量）、目標とする液中亜硫酸濃度
（３．７５ｍｍｏｌ／リットル以下）に達することを確
認した。例えば、空気の導入量や処理液量、散気ノズル
形状、気液温度、液中亜硫酸濃度、酸化塔高さなどの条
件が同一であれば、液ｐＨが５．５の時に比較して、液
ｐＨ３．０では液中亜硫酸の酸化速度は約１／２と遅く
なる。[Function] In order to clarify the relationship between the liquid pH of liquid sulfite due to air oxidation, magnesium sulfite is used.
An experiment for confirming the oxidizing property of sulfurous acid in liquid using the flat contact stirring tank shown in FIG. 2 was carried out. As a result, as shown in FIG.
It was confirmed that, when H was 6.0 to 6.5, the oxidation rate of sulfurous acid in the liquid was low (the oxidizing property was poor) as the pH of the liquid decreased. This figure shows liquid pH and overall mass transfer coefficient K
The relationship with G is shown. In addition, using the bubble column shown in FIG.
An oxidation test of sulfurous acid in liquid simulating the oxidation tower of the actual apparatus of the present invention was carried out. As a result, as shown in FIGS. 5A and 5B,
When an alkaline chemical [Mg (OH) 2 slurry] was added to the oxidation tower inlet liquid so as to keep the pH of the oxidation tower outlet liquid high (pH = 5.5), this was not added (pH of the oxidation tower outlet liquid).
It was confirmed that the retention time of the liquid in the oxidation tower was shorter (smaller capacity of the oxidation tower) and the target concentration of sulfurous acid in the liquid (3.75 mmol / liter or less) was reached as compared with the case without adjustment). For example, if the conditions such as the amount of introduced air, the amount of treatment liquid, the shape of the air diffuser nozzle, the gas-liquid temperature, the concentration of sulfurous acid in the liquid, and the height of the oxidation tower are the same, compared with when the liquid pH is 5.5, When the pH of the liquid is 3.0, the oxidation rate of sulfurous acid in the liquid is as slow as about 1/2.
【０００８】また、実際の酸化塔では、亜硫酸の酸化に
伴ない高さ方向（気液の流れ方向）にｐＨの分布（低
下）が生じ、これに準じて液中亜硫酸の酸化速度の分布
（低下）が生じる。すなわち、従来システムでは、酸化
塔の中〜上層部の液ｐＨの低下したところでは、導入し
た酸化空気の有効利用率が低下し、高い酸化効率が得ら
れない（逆説すれば、高い酸化効率を得るためには、酸
化塔容量を大きくし、酸化塔内の液滞留時間を大きく設
計するか、酸化空気導入量を増大する必要がある）。こ
れに対して、本発明に従い、酸化塔出口液のｐＨを高く
保つように酸化塔入口液にアルカリ薬剤を添加すると酸
化塔内の液ｐＨの高さ方向の分布はかさ上げされ、ま
た、酸化塔入口液に添加したアルカリ薬剤であるＭｇ
（ＯＨ）2 スラリやＭｇＯスラリは溶解に時間を要する
ため、酸化塔入口付近での急激な液ｐＨ上昇を起こさず
液流れやガス流れに乗って、酸化塔の中〜上層部で溶解
が進むため、酸化塔内の全層において導入した酸化空気
が有効利用され、高い酸化効率が得られる。[0008] In an actual oxidation tower, pH distribution (decrease) occurs in the height direction (gas-liquid flow direction) accompanying the oxidation of sulfurous acid, and in accordance with this, the distribution of the oxidation rate of liquid sulfurous acid ( Decrease) occurs. That is, in the conventional system, at a place where the liquid pH in the middle to upper layers of the oxidation tower is lowered, the effective utilization rate of the introduced oxidizing air is lowered, and high oxidation efficiency cannot be obtained (paradoxically, high oxidation efficiency is In order to obtain it, it is necessary to increase the capacity of the oxidation tower and design the liquid retention time in the oxidation tower to be large, or to increase the introduction amount of oxidizing air). On the other hand, according to the present invention, when an alkaline chemical is added to the oxidation tower inlet liquid so as to keep the pH of the oxidation tower outlet liquid high, the distribution of the liquid pH in the height direction in the oxidation tower is increased, and the oxidation Mg as an alkaline chemical added to the tower inlet liquid
Since (OH) 2 slurry and MgO slurry take time to dissolve, the dissolution progresses in the middle and upper layers of the oxidation tower without riding on the liquid flow or gas flow without causing a sharp increase in liquid pH near the inlet of the oxidation tower. Therefore, the oxidizing air introduced into all layers in the oxidation tower is effectively used, and high oxidation efficiency can be obtained.
【０００９】[0009]
【実施例】本発明の方法の実施例を図１に基づいて以下
に説明する。 脱硫塔底部より抜き出された液８を酸化塔１に導入
した。この際、酸化塔出口液９のｐＨをｐＨ電極４及び
ｐＨ計５により検知した。 酸化空気１０を散気管２より導入（バブリング）す
ると共に、ｐＨ計５の指示値が５．５〜６．５となるよ
うｐＨ計５に連動した制御弁６の開度を自動調整し、ア
ルカリ薬剤タンク７内のアルカリ薬剤〔Ｍｇ（ＯＨ）2
スラリやＭｇＯスラリなど〕を酸化塔入口液（脱硫塔底
部抜出し液）８に添加した。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the method of the present invention will be described below with reference to FIG. The liquid 8 extracted from the bottom of the desulfurization tower was introduced into the oxidation tower 1. At this time, the pH of the oxidation tower outlet liquid 9 was detected by the pH electrode 4 and the pH meter 5. Oxidizing air 10 is introduced (bubbling) from the air diffuser 2, and the opening of the control valve 6 linked to the pH meter 5 is automatically adjusted so that the indicated value of the pH meter 5 is 5.5 to 6.5. Alkaline drug [Mg (OH) 2 in the drug tank 7
Slurry or MgO slurry] was added to the oxidation tower inlet liquid (desulfurization tower bottom extract liquid) 8.
【００１０】実施例１ 酸化塔入口液にアルカリ薬剤を添加した場合の酸化塔小
型化の実施例を以下に示す。石油コークス／重油だきボ
イラで処理ガス量２０万Ｎｍ3 ／ｈ（ｄｒｙ）のマグネ
シウム法排煙脱硫装置（排水量：６０ｍ3 ／ｈ）の酸化
塔寸法、容量を以下に示す。 （本発明方法では、酸化塔出口液ｐＨを５．５に調整） Example 1 An example of reducing the size of the oxidation tower when an alkaline chemical is added to the inlet liquid of the oxidation tower will be described below. The size and capacity of the oxidation tower of a magnesium-type flue gas desulfurization unit (wastewater: 60 m 3 / h) with a processing gas amount of 200,000 Nm 3 / h (dry) in a petroleum coke / heavy oil-fired boiler are shown below. (In the method of the present invention, the pH of the liquid at the outlet of the oxidation tower is adjusted to 5.5)
【００１１】実施例２ 酸化塔容量を同一とした場合の本発明による酸化空気導
入量の低減効果を示す実験データを以下に示す。図４
（気泡塔による液中亜硫酸の酸化性確認試験）におい
て、模擬液供給量＝２３．６１／ｈ（酸化塔内滞留時間
＝１ｈ）とし、空気流量を変化させて酸化塔出口液の亜
硫酸濃度を測定した結果を図６に示す。本発明の方法で
は、従来方法に比べ、空気導入量が少なくてよい。 Example 2 The following is experimental data showing the effect of reducing the introduction amount of oxidizing air according to the present invention when the oxidizing tower volume is the same. FIG.
In the (oxidation confirmation test of sulfurous acid in a liquid by a bubble column), the simulated liquid supply amount = 23.61 / h (residence time in the oxidation tower = 1 h), and the air flow rate was changed to change the sulfurous acid concentration of the outlet liquid of the oxidation tower. The measurement result is shown in FIG. The method of the present invention requires less air than the conventional method.
【００１２】[0012]
【発明の効果】従来方法では、排水規制値の一条件であ
るｐＨ５．５〜８．５をクリアするために酸化塔の下流
側でアルカリ薬剤を添加していたが、これと同等の方法
で、アルカリ薬剤の添加位置を酸化塔の上流側に変更す
ることにより、酸化塔内での液中亜硫酸の酸化効率（導
入空気の酸素利用率）が向上し、処理亜硫酸量および酸
化空気量等が同一であれば、酸化塔の容量は従来方法
（液滞留時間は約３ｈｒ）の１／２〜１／３と小型化が
図れる。また、導入空気の酸素利用率が向上することか
ら、酸化塔容量を同一とすると、酸化空気導入量の低
減、すなわちブロワの小型化が図れる。EFFECTS OF THE INVENTION In the conventional method, an alkaline chemical was added at the downstream side of the oxidation tower in order to clear pH 5.5 to 8.5, which is one condition of the wastewater regulation value. By changing the addition position of the alkaline chemical to the upstream side of the oxidation tower, the oxidation efficiency of sulfurous acid in the liquid (oxygen utilization rate of the introduced air) in the oxidation tower is improved, and the amount of treated sulfurous acid and the amount of oxidizing air are increased. If they are the same, the capacity of the oxidation tower can be reduced to 1/2 to 1/3 of the conventional method (the liquid retention time is about 3 hours). Further, since the oxygen utilization rate of the introduced air is improved, if the oxidizing tower capacity is made the same, the amount of the oxidizing air introduced can be reduced, that is, the blower can be downsized.
【図１】図１は、本発明の実施例１に係る脱硫排液酸化
システムの概略フロー図である。FIG. 1 is a schematic flow diagram of a desulfurization effluent oxidation system according to a first embodiment of the present invention.
【図２】図２は、平面接触攪拌槽による液中亜硫酸の酸
化性確認試験の装置、試験条件を示す概略フロー図であ
る。FIG. 2 is a schematic flow chart showing an apparatus and a test condition for a test for confirming the oxidizing property of sulfurous acid in a liquid by a flat contact stirring tank.
【図３】図３は、平面接触攪拌槽による液中亜硫酸の酸
化性確認試験の結果を示すグラフである。FIG. 3 is a graph showing the result of a test for confirming the oxidizing property of sulfurous acid in a liquid using a flat contact stirring tank.
【図４】図４は、気泡塔による液中亜硫酸の酸化性確認
試験のための装置、試験条件を示す概略フロー図であ
る。FIG. 4 is a schematic flow chart showing an apparatus and a test condition for a test for confirming the oxidizing property of sulfurous acid in a liquid by a bubble column.
【図５】図５Ａ及びＢは夫々気泡塔による液中亜硫酸の
酸化性確認試験の結果を示すグラフであり、Ａはアルカ
リ薬剤を添加してｐＨ調整をした場合、ＢはｐＨ調整を
しない場合の結果を示す。5A and 5B are graphs showing the results of a test for confirming the oxidative property of liquid sulfite by a bubble column, where A is the pH adjustment by adding an alkaline chemical, and B is the pH adjustment not performed. The result is shown.
【図６】図６は図４に示す気泡塔による液中亜硫酸の酸
化性確認試験において空気流量を変化させて酸化塔出口
液の亜硫酸濃度を測定した結果を示すグラフである。FIG. 6 is a graph showing the results of measuring the sulfurous acid concentration in the outlet liquid of the oxidation tower by changing the air flow rate in the test for confirming the oxidizing property of liquid sulfite by the bubble tower shown in FIG.
【図７】図７は、マグネシウム法湿式排煙脱硫装置の概
略フロー図である。FIG. 7 is a schematic flowchart of a magnesium method wet flue gas desulfurization apparatus.
【図８】図８は、従来の脱硫排液酸化システムを示す概
略フロー図である。FIG. 8 is a schematic flow diagram showing a conventional desulfurization effluent oxidation system.
【符号の説明】 １．酸化塔 ２．散気管 ３．ドレン抜き ４．ｐＨ電
極 ５．ｐＨ計 ６．制御弁 ７．アルカリ液タンク
８．脱硫塔（吸収塔）底部抜き出し液 ９．排水フィル
タへ １０．酸化空気 １１．脱硫塔（吸収塔）へ[Explanation of Codes] Oxidation tower 2. Air diffuser 3. Without drain 4. pH electrode 5. pH meter 6. Control valve 7. Alkaline liquid tank
8. Liquid drawn out from the bottom of the desulfurization tower (absorption tower) 9. To drain filter 10. Oxidizing air 11. To desulfurization tower (absorption tower)
フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 53/34 １２５ Ｒ (72)発明者 滝本 新一 兵庫県神戸市兵庫区和田崎町一丁目１番１ 号 三菱重工業株式会社神戸造船所内Continuation of the front page (51) Int.Cl. 6 Identification number Office reference number FI technical display location B01D 53/34 125 R (72) Inventor Shinichi Takimoto 1-1-1, Wadazaki-cho, Hyogo-ku, Kobe-shi, Hyogo No. Mitsubishi Heavy Industries, Ltd.Kobe Shipyard
Claims (1)
式廃液酸化方法において、酸化塔出口液のｐＨを検知
し、酸化塔出口液のｐＨが５．５以上になるように、酸
化塔入口液のｐＨをアルカリ性薬剤により制御すること
により、酸化塔を小容量化または酸化空気導入量を低減
することを特徴とする上記方法。1. In a bubble column type waste liquid oxidation method for a magnesium-type flue gas desulfurization apparatus, the pH of the oxidation tower outlet liquid is detected, and the oxidation tower inlet liquid is adjusted so that the pH of the oxidation tower outlet liquid is 5.5 or more. The method as described above, wherein the capacity of the oxidation tower is reduced or the introduction amount of oxidizing air is reduced by controlling the pH of the solution with an alkaline chemical.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7010086A JPH08196863A (en) | 1995-01-25 | 1995-01-25 | Oxidation of waste liquid from magnesium process flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7010086A JPH08196863A (en) | 1995-01-25 | 1995-01-25 | Oxidation of waste liquid from magnesium process flue gas desulfurization equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH08196863A true JPH08196863A (en) | 1996-08-06 |
Family
ID=11740538
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7010086A Withdrawn JPH08196863A (en) | 1995-01-25 | 1995-01-25 | Oxidation of waste liquid from magnesium process flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH08196863A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100902018B1 (en) * | 2007-08-01 | 2009-06-15 | 한국동서발전(주) | Method for Treating Industrial Waste Water by Using Neutralizing Chemical Agent |
| CN104857838A (en) * | 2015-04-09 | 2015-08-26 | 北京廷润膜技术开发有限公司 | System and method for flue gas desulfurization through bipolar membrane electrodialysis |
| KR20230044491A (en) | 2021-03-23 | 2023-04-04 | 후지 덴키 가부시키가이샤 | Exhaust gas treatment device and exhaust gas treatment method |
-
1995
- 1995-01-25 JP JP7010086A patent/JPH08196863A/en not_active Withdrawn
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100902018B1 (en) * | 2007-08-01 | 2009-06-15 | 한국동서발전(주) | Method for Treating Industrial Waste Water by Using Neutralizing Chemical Agent |
| CN104857838A (en) * | 2015-04-09 | 2015-08-26 | 北京廷润膜技术开发有限公司 | System and method for flue gas desulfurization through bipolar membrane electrodialysis |
| KR20230044491A (en) | 2021-03-23 | 2023-04-04 | 후지 덴키 가부시키가이샤 | Exhaust gas treatment device and exhaust gas treatment method |
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| A300 | Withdrawal of application because of no request for examination |
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