JP2003342887A - Method and equipment for treating ozone bleaching exhaust gas - Google Patents
Method and equipment for treating ozone bleaching exhaust gasInfo
- Publication number
- JP2003342887A JP2003342887A JP2002152918A JP2002152918A JP2003342887A JP 2003342887 A JP2003342887 A JP 2003342887A JP 2002152918 A JP2002152918 A JP 2002152918A JP 2002152918 A JP2002152918 A JP 2002152918A JP 2003342887 A JP2003342887 A JP 2003342887A
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- Japan
- Prior art keywords
- exhaust gas
- ozone bleaching
- bleaching exhaust
- recovered
- ozone
- 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.)
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Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、製紙工場などにお
いてパルプをオゾン漂白する際に排出されるオゾン漂白
排ガスの処理方法及び処理装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for treating ozone bleaching exhaust gas discharged during ozone bleaching of pulp in a paper mill or the like.
【０００２】[0002]
【従来の技術】近年、パルプのオゾン漂白では、酸素ガ
スを原料としたオゾン化酸素ガスが使用されており、と
くにＰＳＡ式酸素発生装置で発生された酸素を原料とし
たオゾン化酸素でパルプをオゾン漂白した後の排ガス
（以下、オゾン漂白排ガスという）中には、通常、１％
未満の未反応オゾン、８０〜８３％程度の酸素ガス及び
数％の炭酸ガスが含まれている。オゾンは、強い酸化力
をもち、殺菌、漂白、酸化などの目的に用いられている
が、毒性が強く、微量でも長時間吸入すると有害であ
る。その許容濃度は０．１ｐｐｍ未満であるので、オゾ
ン漂白排ガスは、加熱式又は触媒式のオゾン分解器を通
す等の方法によってオゾンを分解してから排気されるか
又は他の酸素利用設備で再利用されている。2. Description of the Related Art In recent years, in ozone bleaching of pulp, ozonized oxygen gas using oxygen gas as a raw material has been used. Especially, pulp produced by ozonized oxygen using oxygen generated by a PSA oxygen generator as a raw material is used. In the exhaust gas after ozone bleaching (hereinafter referred to as ozone bleaching exhaust gas), usually 1%
Less than unreacted ozone, about 80 to 83% oxygen gas and several% carbon dioxide gas are contained. Ozone has a strong oxidizing power and is used for purposes such as sterilization, bleaching and oxidation, but it is highly toxic and even a trace amount is harmful if inhaled for a long time. Since the permissible concentration is less than 0.1 ppm, ozone bleached exhaust gas is exhausted after decomposing ozone by a method such as passing through a heating type or catalytic type ozone decomposing device, or is regenerated by other oxygen utilization equipment. It's being used.
【０００３】しかしながら、加熱式分解器では、オゾン
漂白排ガスを３５０℃以上に加熱するため、多くのエネ
ルギーが必要であり、コストが高くなる。一方、触媒式
分解器では、触媒が劣化するため、触媒の交換が必要と
なり、多大なコストを要するという問題がある。また、
酸素の再利用先の１つである酸素脱リグニン工程では、
酸素濃度８５％以上の酸素ガスを用いることが効果的で
あるが、オゾン漂白排ガスを利用する場合には、酸素濃
度が８５％よりも低いので、酸素脱リグニン効率が低下
するという問題がある。However, in the heating type decomposer, since the ozone bleaching exhaust gas is heated to 350 ° C. or higher, much energy is required and the cost becomes high. On the other hand, in the catalytic decomposing unit, the catalyst is deteriorated, so that the replacement of the catalyst is required, which results in a large cost. Also,
In the oxygen delignification process, which is one of the recycling destinations of oxygen,
It is effective to use oxygen gas having an oxygen concentration of 85% or more, but when using ozone bleaching exhaust gas, the oxygen concentration is lower than 85%, so that there is a problem that the oxygen delignification efficiency decreases.
【０００４】これらの問題を解決するために、特開平９
−２９０６４号公報では、クラフトパルプ製造工程で使
用される還元性物質を含有する液（以下、吸収液とい
う）によりオゾン漂白排ガス中のオゾン分解を行う方法
が提案されている。また、特開平１０−３７０８８号公
報では、アルカリスクラビング処理によりオゾン漂白排
ガス中の炭酸ガスを除去して酸素濃度を上げる方法が提
案されている。In order to solve these problems, Japanese Unexamined Patent Publication No. Hei 9
No. 29064 discloses a method of decomposing ozone in ozone bleaching exhaust gas with a liquid containing a reducing substance used in the kraft pulp manufacturing process (hereinafter referred to as an absorption liquid). Further, Japanese Patent Laid-Open No. 10-37088 proposes a method of removing carbon dioxide gas in ozone bleaching exhaust gas by alkali scrubbing to increase oxygen concentration.
【０００５】特開平９−２９０６４号公報記載の吸収液
を使用した処理方法によるオゾン漂白排ガス処理設備の
一例を図３に示す。オゾン漂白排ガスは、オゾン漂白設
備から同伴されるミスト等がデミスター１１１により除
去された後、吸収塔１０１の下部に導入され、吸収塔１
０１でオゾン及び炭酸ガスが吸収除去される。吸収塔１
０１通過後の処理済み排ガスは、吸収塔１０１の上部か
ら導出され、デミスター１１２によりミストが除去され
た後、排気されるか、又は、必要に応じてブロア１０
５、圧縮機１０８により昇圧され、酸素脱リグニン工
程、排水処理工程、キルン等において利用される。FIG. 3 shows an example of ozone bleaching exhaust gas treatment equipment by a treatment method using an absorbing solution described in JP-A-9-29064. The ozone bleaching exhaust gas is introduced into the lower part of the absorption tower 101 after the mist and the like accompanying the ozone bleaching equipment are removed by the demister 111, and
At 01, ozone and carbon dioxide are absorbed and removed. Absorption tower 1
The treated exhaust gas after passing 01 is discharged from the upper part of the absorption tower 101, and after the mist is removed by the demister 112, it is exhausted or, if necessary, the blower 10
5. The pressure is increased by the compressor 108 and is used in the oxygen delignification process, wastewater treatment process, kiln, and the like.
【０００６】[0006]
【発明が解決しようとする課題】このような吸収液を使
用したオゾン漂白排ガス処理方法によると、吸収液によ
りオゾン漂白排ガス中のオゾンガスや炭酸ガスが除去さ
れて、酸素濃度８５％以上のガスが回収されるが、オゾ
ン漂白排ガスの全量を処理するために必要な吸収液が多
量であるので、コストが高くなってしまうという問題が
ある。同様に、特開平１０−３７０８８号公報記載の方
法においても、炭酸ガスを除去するために多量の吸収液
が必要とされる。本発明は、上記事情を鑑みてなされた
もので、吸収液の使用量が少なく、オゾン漂白排ガスの
処理を低コストで行うことができるオゾン漂白排ガス処
理方法を提供することを目的とする。According to the ozone bleaching exhaust gas treatment method using such an absorbing solution, the absorbing solution removes the ozone gas and the carbon dioxide gas in the ozone bleaching exhaust gas to generate a gas having an oxygen concentration of 85% or more. Although it is recovered, there is a problem that the cost becomes high because the amount of the absorbing solution necessary for treating the entire amount of the ozone bleaching exhaust gas is large. Similarly, in the method described in Japanese Patent Laid-Open No. 10-37088, a large amount of absorbing liquid is required to remove carbon dioxide gas. The present invention has been made in view of the above circumstances, and an object of the present invention is to provide an ozone bleaching exhaust gas treatment method that can treat ozone bleaching exhaust gas at a low cost with a small amount of absorbing liquid used.
【０００７】[0007]
【課題を解決するための手段】本発明者らは、上記目的
を達成すべく鋭意研究した結果、オゾン漂白排ガスを吸
収塔内で吸収液と接触させて処理する際に、該吸収塔の
塔頂部から回収されるオゾン漂白排ガス中の酸素濃度よ
りも低い酸素濃度のオゾン漂白排ガスを該吸収塔の中間
部の少なくとも１カ所から回収することにより、オゾン
や炭酸ガスの処理に消費される吸収液の量を減らすこと
ができることを見出し、この知見に基づいて、本発明を
完成した。Means for Solving the Problems As a result of intensive studies aimed at achieving the above object, the present inventors have found that when ozone bleached exhaust gas is treated by bringing it into contact with an absorbing liquid in an absorption tower, the tower of the absorption tower is treated. An absorption liquid consumed for the treatment of ozone and carbon dioxide by recovering ozone bleaching exhaust gas having an oxygen concentration lower than that of the ozone bleaching exhaust gas recovered from the top from at least one location in the middle part of the absorption tower. Based on this finding, the present invention has been completed.
【０００８】すなわち、本発明は、充填材層を有する吸
収塔に、オゾン漂白排ガスを供給し、充填材層中で上昇
させつつ、充填材層中を流下する吸収液に接触させるオ
ゾン漂白排ガス処理方法であって、充填材層中を上昇す
るオゾン漂白排ガスの一部を、充填材層の中間位置にお
いて回収し、他部を、充填材層を通過させて回収するこ
とを特徴とするオゾン漂白排ガス処理方法である。前記
充填材層が少なくとも２層であり、前記中間位置が、各
充填材層の間に設けた空間部分であることが好ましい。
また、前記中間位置において、前記吸収液の再分配を行
うことが好ましい。さらに、本発明のオゾン漂白排ガス
処理方法では、充填材層を通過させて回収したオゾン漂
白排ガス中の酸素濃度を、充填材層の中間位置において
回収したオゾン漂白排ガスを添加することによって調整
することが好ましい。また、本発明のオゾン漂白排ガス
処理方法では、充填材層を通過させて回収したオゾン漂
白排ガス中の酸素濃度を、酸素ガスを添加することによ
って調整することが好ましい。That is, the present invention provides an ozone bleaching exhaust gas treatment in which ozone bleaching exhaust gas is supplied to an absorption tower having a packing material layer, and the ozone bleaching gas is brought into contact with the absorbing liquid flowing down in the packing material layer while rising in the packing material layer. A method, wherein a part of the ozone bleaching exhaust gas rising in the filler layer is recovered at an intermediate position of the filler layer, and the other part is recovered by passing through the filler layer. This is an exhaust gas treatment method. It is preferable that the filler layer is at least two layers and the intermediate position is a space portion provided between the filler layers.
Further, it is preferable that the absorption liquid is redistributed at the intermediate position. Furthermore, in the ozone bleaching exhaust gas treatment method of the present invention, the oxygen concentration in the ozone bleaching exhaust gas recovered by passing through the filler layer is adjusted by adding the ozone bleaching exhaust gas recovered at the intermediate position of the filler layer. Is preferred. Moreover, in the ozone bleaching exhaust gas treatment method of the present invention, it is preferable to adjust the oxygen concentration in the ozone bleaching exhaust gas recovered by passing through the filler layer by adding oxygen gas.
【０００９】また、本発明は、充填材層を有する吸収塔
と、該吸収塔の塔頂部に吸収液を供給する吸収液供給手
段と、該吸収液を該吸収塔の塔底部から回収する吸収液
回収手段と、オゾン漂白排ガスを該吸収塔の塔底部に供
給するオゾン漂白排ガス供給手段とを備え、該充填材層
の中間位置の少なくとも１カ所と塔頂部とに、供給した
オゾン漂白排ガスを回収するオゾン漂白排ガス回収手段
を備えることを特徴とするオゾン漂白排ガス処理装置で
ある。前記充填材層は、少なくとも２層であり、前記中
間位置が、各充填材層の間に設けた空間部分であること
が好ましい。また、前記中間位置に、前記吸収液の再分
配器を備えることが好ましい。さらに、本発明のオゾン
漂白排ガス処理装置は、前記吸収塔の塔頂部のオゾン漂
白排ガス回収手段に対して該吸収塔の中間部のオゾン漂
白排ガス回収手段が連結され、該塔頂部から回収したオ
ゾン漂白排ガスに添加する中間位置から回収したオゾン
漂白排ガスの量を調整するガス量調整手段と、該吸収塔
の塔頂部から回収したオゾン漂白排ガス中の酸素濃度を
測定する酸素濃度計とを備えることが好ましい。また、
本発明のオゾン漂白排ガス処理装置は、前記吸収塔の塔
頂部から回収したオゾン漂白排ガスに酸素ガスを添加し
て該オゾン漂白排ガス中の酸素濃度を調整する酸素ガス
供給弁と、該オゾン漂白排ガス中の酸素濃度を測定する
酸素濃度計とを備えることが好ましい。Further, according to the present invention, an absorption tower having a packing material layer, an absorption liquid supply means for supplying the absorption liquid to the top of the absorption tower, and an absorption liquid for recovering the absorption liquid from the bottom of the absorption tower. A liquid recovery means and an ozone bleaching exhaust gas supply means for supplying ozone bleaching exhaust gas to the tower bottom of the absorption tower are provided, and the supplied ozone bleaching exhaust gas is supplied to at least one intermediate position of the packing material layer and the tower top. It is an ozone bleaching exhaust gas treatment device characterized by comprising ozone bleaching exhaust gas recovery means for recovery. It is preferable that the filler layer is at least two layers, and the intermediate position is a space portion provided between the filler layers. In addition, it is preferable to provide a redistributor of the absorbing liquid at the intermediate position. Further, in the ozone bleaching exhaust gas treatment apparatus of the present invention, the ozone bleaching exhaust gas recovery means in the middle part of the absorption tower is connected to the ozone bleaching exhaust gas recovery means at the top of the absorption tower, and the ozone recovered from the tower top is connected. A gas amount adjusting means for adjusting the amount of ozone bleaching exhaust gas recovered from an intermediate position added to the bleaching exhaust gas, and an oxygen concentration meter for measuring the oxygen concentration in the ozone bleaching exhaust gas recovered from the top of the absorption tower are provided. Is preferred. Also,
The ozone bleaching exhaust gas treatment apparatus of the present invention is an oxygen gas supply valve for adjusting the oxygen concentration in the ozone bleaching exhaust gas by adding oxygen gas to the ozone bleaching exhaust gas recovered from the top of the absorption tower, and the ozone bleaching exhaust gas. An oximeter for measuring the oxygen concentration therein is preferably provided.
【００１０】吸収液を供給した充填材層にオゾン漂白排
ガスを通すと、該オゾン漂白排ガス中のオゾンや炭酸ガ
スが、該吸収液に吸収され、ガス中の酸素濃度が高めら
れる。本発明のオゾン漂白排ガス処理方法では、充填材
層を通過した後の高い酸素濃度のオゾン漂白排ガス（以
下、高Ｏ2回収ガスという）よりも酸素濃度が低いオゾ
ン漂白排ガス（以下、低Ｏ2回収ガスという）の一部
を、充填材層の中間位置から回収するので、オゾン漂白
工程で生じたオゾン漂白排ガスの全量をアルカリ処理し
て酸素濃度を高める必要がなく、吸収液消費量を低減さ
せることができる。なお、「充填材層の中間位置」と
は、充填材層の上下方向の中間位置、すなわち、充填材
層の上端部と下端部との間の位置をいう。回収した低Ｏ
2回収ガスは、そのまま、排水処理、キルン等の比較的
低濃度の酸素ガスが利用できる工程へ供給して再利用す
ることができる。When ozone bleaching exhaust gas is passed through the filler layer supplied with the absorbing liquid, ozone and carbon dioxide gas in the ozone bleaching exhaust gas are absorbed by the absorbing liquid and the oxygen concentration in the gas is increased. In the ozone bleaching exhaust gas treatment method of the present invention, the ozone bleaching exhaust gas (hereinafter, low O 2 ) having a lower oxygen concentration than the ozone bleaching exhaust gas having high oxygen concentration after passing through the filler layer (hereinafter, referred to as high O 2 recovery gas). Part of the recovered gas (collected gas) is collected from the middle position of the filler layer, so there is no need to increase the oxygen concentration by alkali treatment of the total amount of ozone bleached exhaust gas generated in the ozone bleaching process, reducing the consumption of absorbing liquid. Can be made. The "intermediate position of the filler layer" refers to an intermediate position in the vertical direction of the filler layer, that is, a position between the upper end portion and the lower end portion of the filler layer. Low O recovered
2 The recovered gas can be reused as it is by supplying it to a process such as waste water treatment or kiln where oxygen gas of relatively low concentration can be used.
【００１１】本発明の好ましい実施態様では、少なくと
も２層の充填材層の間に空間部分を設け、該空間部分に
おいて、その位置より下部の充填材層でアルカリ処理さ
れたオゾン漂白排ガスの回収を行う。これにより、ガス
回収をより容易且つ迅速に行うことができる。また、前
記空間部分において、流下してきた吸収液の再分配を行
うことにより、吸収液が均一に分散して下部の充填材層
に供給され、排ガスと吸収液との気液接触の効率が向上
して、オゾンや炭酸ガスの吸収効率が向上する。In a preferred embodiment of the present invention, a space portion is provided between at least two filler layers, and in this space portion, the ozone-bleached exhaust gas subjected to alkali treatment by the filler layer below the position is recovered. To do. Thereby, gas recovery can be performed more easily and quickly. Further, by re-distributing the absorbing liquid that has flowed down in the space portion, the absorbing liquid is uniformly dispersed and supplied to the lower filler layer, and the efficiency of gas-liquid contact between the exhaust gas and the absorbing liquid is improved. Then, the absorption efficiency of ozone and carbon dioxide is improved.
【００１２】本発明においては、吸収塔から回収したガ
スを他の工程に送って再利用する際に、ガス中の酸素濃
度を測定して、その値に応じて、高Ｏ2回収ガス中に低
Ｏ2回収ガスを混合して酸素濃度を低下させたり、高Ｏ2
回収ガス中に高純度の酸素ガスを混合して酸素濃度を上
昇させる等の簡単な方法により、ガス中の酸素濃度を望
ましい値に調整することができる。In the present invention, when the gas recovered from the absorption tower is sent to another process and reused, the oxygen concentration in the gas is measured, and the oxygen concentration in the high O 2 recovered gas is measured according to the measured value. A low O 2 recovery gas is mixed to reduce the oxygen concentration, or a high O 2
The oxygen concentration in the gas can be adjusted to a desired value by a simple method such as mixing highly pure oxygen gas into the recovered gas to raise the oxygen concentration.
【００１３】[0013]
【発明の実施の形態】以下、図１を用いて本発明のオゾ
ン漂白排ガスの処理方法及び装置をより詳細に説明する
が、これは本発明を限定するものではない。図１は、本
発明のオゾン漂白排ガス処理装置の一実施形態を示すも
のである。ここに示す処理装置は、２層の充填材層２，
３を有する吸収塔１と、該吸収塔１の塔頂部に吸収液を
供給する吸収液ノズル９（吸収液供給手段）と、該吸収
液を該吸収塔１の塔底部から回収するポンプ２５（吸収
液回収手段）と、オゾン漂白排ガスを吸収塔１の塔底部
に供給する排ガスノズル１０（オゾン漂白排ガス供給手
段）とを備えている。この処理装置には、充填材層２，
３の中間位置すなわち吸収塔中間部２１に、下部充填材
層３を通過したオゾン漂白排ガスの一部を回収する中間
部排ガス回収経路Ｌ１（オゾン漂白排ガス回収手段）が
接続されている。また、吸収塔の塔頂部には、上部充填
材層２を通過したオゾン漂白排ガスを回収する塔頂部排
ガス回収経路Ｌ２（オゾン漂白排ガス回収手段）が接続
されている。充填材層２，３は、セラミック、合成樹
脂、金属等の材料によって構成されるものである。吸収
液としては、白液（ＮａＯＨ水溶液）、酸化白液、緑
液、弱液、黒液、排煙脱硫液等を挙げることができ、特
に白液が好ましく用いられる。BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, the method and apparatus for treating ozone bleaching exhaust gas of the present invention will be described in more detail with reference to FIG. 1, but this does not limit the present invention. FIG. 1 shows one embodiment of the ozone bleaching exhaust gas treatment apparatus of the present invention. The processing device shown here is composed of two filler layers 2,
3, an absorption tower 1 having 3; an absorption liquid nozzle 9 for supplying the absorption liquid to the top of the absorption tower 1 (absorption liquid supply means); and a pump 25 for collecting the absorption liquid from the bottom of the absorption tower 1 ( And an exhaust gas nozzle 10 (ozone bleaching exhaust gas supply device) for supplying the ozone bleaching exhaust gas to the tower bottom of the absorption tower 1. This processing device includes a filler layer 2,
An intermediate portion exhaust gas recovery path L1 (ozone bleaching exhaust gas recovery means) for recovering a part of the ozone bleaching exhaust gas that has passed through the lower filler layer 3 is connected to an intermediate position of 3, that is, the absorption tower intermediate portion 21. Further, a tower top exhaust gas recovery path L2 (ozone bleach exhaust gas recovery means) for recovering the ozone bleaching exhaust gas that has passed through the upper filler layer 2 is connected to the tower top of the absorption tower. The filler layers 2 and 3 are made of a material such as ceramic, synthetic resin or metal. Examples of the absorbing liquid include white liquor (NaOH aqueous solution), oxidized white liquor, green liquor, weak liquor, black liquor, flue gas desulfurization liquor, and white liquor is particularly preferably used.
【００１４】次に、上記処理装置を使用した場合を例と
して、本発明のオゾン漂白排ガス処理方法の一実施形態
を説明する。吸収液は、吸収液タンク２３から、ポンプ
２４によって吸収塔１の塔頂部へ送液され、吸収液ノズ
ル９から上部充填材層２の上部に噴射され、吸収塔１内
の充填材層２，３を流下する。Next, one embodiment of the ozone bleaching exhaust gas treatment method of the present invention will be described by taking the case of using the above treatment apparatus as an example. The absorption liquid is sent from the absorption liquid tank 23 to the tower top part of the absorption tower 1 by the pump 24, is injected from the absorption liquid nozzle 9 to the upper part of the upper packing material layer 2, and is filled with the packing material layer 2 in the absorption tower 1. Flow down 3.
【００１５】オゾン漂白装置（図示せず）から回収され
たオゾン漂白排ガスは、デミスター１１でミスト等を除
去した後、吸収塔１の塔底部に導入する。排ガスノズル
１０から吸収塔１の塔底部に導入されたオゾン漂白排ガ
スは、まず、下部充填材層３で吸収液と向流接触する。
このとき、オゾン漂白排ガス中に含まれるオゾンのほぼ
全量と炭酸ガスの一部が吸収液に吸収され、排ガス中か
ら除去される。The ozone bleaching exhaust gas recovered from the ozone bleaching device (not shown) is introduced into the bottom of the absorption tower 1 after removing mist and the like by the demister 11. The ozone bleaching exhaust gas introduced from the exhaust gas nozzle 10 to the tower bottom of the absorption tower 1 first comes into countercurrent contact with the absorbing liquid in the lower filler layer 3.
At this time, almost all of the ozone contained in the ozone bleaching exhaust gas and part of the carbon dioxide gas are absorbed by the absorbing liquid and removed from the exhaust gas.
【００１６】下部充填材層３で吸収液によりオゾンを除
去されたオゾン漂白排ガスの一部は、下部充填材層３と
上部充填材層２との間に設けられた空間部分、すなわち
吸収塔中間部２１から、中間部回収ガス止め弁８を経由
して回収される。回収されたガスは、デミスター１２を
通し、必要に応じてブロア１５で昇圧された後、中間部
回収ガス供給弁７より、排水処理、キルン等の比較的低
濃度の酸素ガスが利用できる工程へ供給されるか又は排
気弁４を経て排気される。A part of the ozone bleaching exhaust gas from which ozone has been removed by the absorbing liquid in the lower filler layer 3 is a space portion provided between the lower filler layer 3 and the upper filler layer 2, that is, in the middle of the absorption tower. It is recovered from the portion 21 via the intermediate portion recovery gas stop valve 8. The recovered gas is passed through the demister 12 and, if necessary, pressurized by the blower 15, and then is transferred from the intermediate recovery gas supply valve 7 to wastewater treatment, to a process where a relatively low concentration oxygen gas such as a kiln can be used. It is supplied or exhausted via the exhaust valve 4.
【００１７】一方、吸収塔中間部２１で回収されなかっ
たオゾン漂白排ガスは、さらに、上部充填材層２で吸収
液と向流接触し、炭酸ガスの一部が除去される。充填材
層２，３を通過した排ガスは、塔頂部排ガス回収経路Ｌ
２から回収され、デミスター１３でミスト等が除去され
た後、塔頂部回収ガス供給弁６を経由して、圧縮機１４
により昇圧されて、パルプの酸素脱リグニン工程等の比
較的高濃度の酸素を必要とする工程に供給される。On the other hand, the ozone bleaching exhaust gas which has not been recovered in the intermediate portion 21 of the absorption tower is further countercurrently contacted with the absorption liquid in the upper filler layer 2 to remove a part of carbon dioxide gas. The exhaust gas that has passed through the filler layers 2 and 3 is the exhaust gas recovery path L at the top of the tower.
2 and the mist etc. are removed by the demister 13, and then the compressor 14 is passed through the tower top recovered gas supply valve 6.
It is pressurized by and is supplied to a process requiring a relatively high concentration of oxygen, such as a pulp oxygen delignification process.
【００１８】パルプ処理において、酸素脱リグニン工程
で使用される酸素の量は、一般的に、オゾン漂白排ガス
として排出される酸素量の約半分である。したがって、
下部充填材層３で処理されたオゾン漂白排ガスの約半分
を吸収塔中間部２１から回収し、上部充填材層２で処理
する排ガス量を減らすことにより、上部充填材層２で消
費される吸収液量を減らすことができる。In pulp treatment, the amount of oxygen used in the oxygen delignification step is generally about half of the amount of oxygen discharged as ozone bleaching exhaust gas. Therefore,
About half of the ozone bleaching exhaust gas treated in the lower filler layer 3 is recovered from the absorption tower middle part 21, and the amount of exhaust gas treated in the upper filler layer 2 is reduced, so that the absorption consumed in the upper filler layer 2 is reduced. The liquid volume can be reduced.
【００１９】また、吸収塔１の塔底部に導入されるオゾ
ン漂白排ガスは、オゾン漂白設備の運転状況によって
は、そのガス組成が安定しない場合がある。本装置で
は、酸素脱リグニン工程に供給する回収ガス中の酸素濃
度を酸素濃度計２２で検出し、この検出値に基づいて、
予め設定された酸素濃度になるように、塔頂部からの回
収ガス（高Ｏ2回収ガス）に対して酸素ガス供給弁２０
から供給する酸素ガスの供給量を制御することができ
る。また、本装置では、酸素濃度計２２で検出した酸素
濃度の値に基づいて、予め設定された酸素濃度になるよ
うに、回収ガスバイパス弁１６から供給する吸収塔中間
部２１からの回収ガス（低Ｏ2回収ガス）量を制御し、
酸素濃度を低下させることもできる。吸収塔中間部２１
からの回収ガスを用いて処理ガスの希釈を行った場合に
は、上部充填材層２での排ガス処理量が減少するため、
吸収液消費量をさらに減らすことができる。The ozone bleaching exhaust gas introduced into the bottom of the absorption tower 1 may not have a stable gas composition depending on the operating conditions of the ozone bleaching equipment. In this device, the oxygen concentration in the recovered gas supplied to the oxygen delignification step is detected by the oxygen concentration meter 22, and based on the detected value,
Oxygen gas supply valve 20 for the recovered gas (high O 2 recovered gas) from the top of the tower so that the oxygen concentration is preset.
It is possible to control the supply amount of oxygen gas supplied from. Further, in the present apparatus, based on the value of the oxygen concentration detected by the oxygen concentration meter 22, the recovered gas from the absorption tower middle part 21 supplied from the recovered gas bypass valve 16 is adjusted so as to reach a preset oxygen concentration ( Control the amount of low O 2 recovery gas)
It is also possible to reduce the oxygen concentration. Absorption tower middle part 21
When the treated gas is diluted with the recovered gas from the above, the amount of treated exhaust gas in the upper filler layer 2 decreases,
The absorption liquid consumption can be further reduced.
【００２０】また、排気弁４から排気されるガス中のオ
ゾン濃度を常時モニターし、装置異常、あるいはオゾン
漂白排ガスの流量ならびにオゾン濃度の変動等によっ
て、排気されるガス中に許容濃度以上のオゾンが検知さ
れた場合には、中間部回収ガス止め弁８を閉じ、通常運
転中は閉じている回収ガス切替弁５を開いて、オゾン漂
白排ガス全量を吸収塔上部から回収する。これによっ
て、許容濃度以上のオゾンの排出を防止することができ
る。Further, the ozone concentration in the gas exhausted from the exhaust valve 4 is constantly monitored, and due to a device malfunction, fluctuations in the flow rate of ozone bleaching exhaust gas, or ozone concentration, etc. When is detected, the intermediate recovery gas stop valve 8 is closed, the recovery gas switching valve 5 that is closed during normal operation is opened, and the entire amount of ozone bleaching exhaust gas is recovered from the upper part of the absorption tower. This makes it possible to prevent the discharge of ozone above the permissible concentration.
【００２１】また、吸収塔１塔底部から回収される吸収
液は、ポンプ２５によって吸収液回収弁１９を通じ、他
の工程（苛性化工程、蒸解工程、白液酸化装置、酸素脱
リグニン工程等）へ送液し、再利用することもできる。
その際、回収した吸収液の一部を吸収液バイパス弁１７
から吸収液タンク２３に戻して吸収液を循環させ、その
循環量と吸収液補給弁１８からの吸収液補給量を調節す
ることで、各工程に適したアルカリ濃度の吸収液とする
ことができる。Further, the absorption liquid recovered from the bottom of the absorption tower 1 is passed through the absorption liquid recovery valve 19 by the pump 25 to another process (causticizing process, digestion process, white liquor oxidizing device, oxygen delignification process, etc.). It can also be sent to and reused.
At that time, a part of the collected absorption liquid is absorbed into the absorption liquid bypass valve 17
To the absorption liquid tank 23, the absorption liquid is circulated, and the amount of circulation and the absorption liquid replenishment amount from the absorption liquid replenishment valve 18 are adjusted to obtain an absorption liquid having an alkali concentration suitable for each process. .
【００２２】本実施態様のオゾン漂白排ガス処理装置で
は、充填材層２，３中を上昇するオゾン漂白排ガスの一
部を、吸収塔中間部２１（充填材層２，３の中間位置）
において回収するので、排ガス処理に必要な吸収液の使
用量を低減できる。したがって、オゾン漂白排ガス処理
に要するコストが低減される。本実施態様のオゾン漂白
排ガス処理装置では、充填材層を２層とし、前記中間位
置を各充填材層の間に設けた空間部分（吸収塔中間部２
１）とすることにより、ガス回収をより容易且つ迅速に
行うことができる。また、充填材層２，３を通過させて
回収したオゾン漂白排ガス中の酸素濃度を、吸収塔中間
部２１で回収したオゾン漂白排ガスを添加して調整する
ことにより、アルカリ処理される排ガス量が少なくなる
ので、吸収液の使用量をさらに低減することができる。
また、充填材層２，３を通過させて回収したオゾン漂白
排ガス中の酸素濃度を、酸素ガスを添加して調整するこ
とにより、酸素濃度の低いガスが酸素脱リグニン工程に
供給されるのを防ぐことができ、従って、酸素脱リグニ
ン効率の低下を防ぐことができる。In the ozone bleaching exhaust gas treatment apparatus of the present embodiment, a part of the ozone bleaching exhaust gas rising in the packing material layers 2 and 3 is partially absorbed in the absorption tower middle part 21 (the middle position between the packing material layers 2 and 3).
In this case, the amount of the absorbent used for exhaust gas treatment can be reduced. Therefore, the cost required for ozone bleaching exhaust gas treatment is reduced. In the ozone bleaching exhaust gas treatment apparatus of the present embodiment, there are two filler layers, and the intermediate portion is a space portion provided between the filler layers (absorption tower intermediate portion 2).
By setting 1), gas recovery can be performed more easily and quickly. In addition, by adjusting the oxygen concentration in the ozone bleaching exhaust gas recovered by passing through the filler layers 2 and 3 by adding the ozone bleaching exhaust gas recovered in the absorption tower middle part 21, the amount of exhaust gas to be alkali-treated is adjusted. Since the amount is reduced, the amount of the absorbing liquid used can be further reduced.
Further, by adjusting the oxygen concentration in the ozone bleaching exhaust gas collected by passing through the filler layers 2 and 3 by adding oxygen gas, a gas having a low oxygen concentration is supplied to the oxygen delignification step. Therefore, it is possible to prevent a decrease in oxygen delignification efficiency.
【００２３】図２には、本発明のオゾン漂白排ガス処理
装置の別の実施態様として、上部充填材層２と下部充填
材層との間の空間部分に再分配器２６を配した装置を示
す。再分配器２６を配することにより、上部充填材層２
から流下する吸収液が、偏ることなく均一に分散して下
部充填材層３に供給されるので、排ガスと吸収液との気
液接触の効率が向上し、オゾンや炭酸ガスの吸収効率が
向上する。FIG. 2 shows another embodiment of the ozone bleaching exhaust gas treatment apparatus of the present invention, in which a redistributor 26 is arranged in the space between the upper filler layer 2 and the lower filler layer. . By disposing the redistributor 26, the upper filler layer 2
Since the absorbing liquid flowing down from the tank is uniformly dispersed and supplied to the lower filler layer 3, the efficiency of gas-liquid contact between the exhaust gas and the absorbing liquid is improved, and the absorption efficiency of ozone and carbon dioxide is improved. To do.
【００２４】なお、図１には、充填材層を２層設け、そ
の間の一カ所から低Ｏ2回収ガスを回収する例を示して
いるが、本発明においては、充填材層は１層としてもよ
いし３層以上設けてもよい。また、充填材層を３層以上
設ける場合には、各充填材層間の任意の数カ所から低Ｏ
2回収ガスを回収してもよい。FIG. 1 shows an example in which two filler layers are provided and a low O 2 recovery gas is recovered from one place between them, but in the present invention, the filler layer is one layer. Or three or more layers may be provided. In addition, when three or more filler layers are provided, low O can be obtained from any number of places between the filler layers.
2 The recovered gas may be recovered.
【００２５】[0025]
【実施例】以下、実施例を示して本発明およびその効果
を具体的に説明するが、これらは本発明を限定するもの
ではない。
実施例１
図２に示す装置を用い、オゾン漂白排ガスの処理を行っ
た。本実施例では、塔径３００ｍｍ、上部充填材層２の
高さ９００ｍｍ、下部充填材層３の高さ３００ｍｍの吸
収塔１を用いた。オゾン漂白排ガスを吸収塔１の塔底部
から５０Ｎｍ3／ｈで供給し、液温５０℃の吸収液を吸
収塔１の塔頂部から１．２ｍ3／ｈで供給した。このと
き用いた吸収液の組成は、ＮａＯＨ １０８ｇ／Ｌ、Ｎ
ａ2ＣＯ3 ４７．７ｇ／Ｌ、Ｎａ 2Ｓ ３２．７ｇ／
Ｌ、Ｎａ2Ｓ2Ｏ3 ３．６ｇ／Ｌ、Ｎａ2ＳＯ3 ４．７
ｇ／Ｌ、Ｎａ2ＳＯ4 １１．７ｇ／Ｌであった。吸収塔
中間部２１からの回収ガス（以下、中間部回収ガスとい
う。）と塔頂部からの回収ガス（以下、塔頂部回収ガス
という。）とが同量となるように、中間部ガス止め弁８
を調整した。表１に、処理前のオゾン漂白排ガス、中間
部回収ガス及び塔頂部回収ガスの組成を示す。EXAMPLES The present invention and its effects are shown below with reference to examples.
Will be specifically described, but these limit the present invention.
is not.
Example 1
Treatment of ozone bleaching exhaust gas using the equipment shown in Fig. 2
It was In this embodiment, the tower diameter is 300 mm and the upper filler layer 2
900 mm in height and 300 mm in height of the lower filler layer 3
Collection tower 1 was used. Absorbs ozone bleached gas at the bottom of absorption tower 1
To 50 Nm3/ H to absorb the absorption liquid at a liquid temperature of 50 ° C
1.2m from the top of the tower 1.3/ H. This and
The composition of the absorbing solution used was NaOH 108 g / L, N
a2CO3 47.7 g / L, Na 2S 32.7 g /
L, Na2S2O3 3.6 g / L, Na2SO3 4.7
g / L, Na2SOFour It was 11.7 g / L. Absorption tower
Recovery gas from the intermediate part 21 (hereinafter referred to as intermediate recovery gas
U ) And the gas recovered from the tower top (hereinafter referred to as the tower top recovered gas
Say. ) And the same amount, the intermediate gas stop valve 8
Was adjusted. Table 1 shows ozone bleaching exhaust gas before treatment, intermediate
The composition of the partial recovery gas and the column top recovery gas is shown.
【００２６】[0026]
【表１】 [Table 1]
【００２７】中間部回収ガス中のオゾン濃度は、検出下
限未満であり、下部充填材層３においてほぼ完全に除去
されたことが確認された。また、未処理ガス中に４．８
％存在した炭酸ガスは、中間部回収ガス中においては
４．１％にまで除去され、酸素濃度は８３．０％となっ
た。この酸素濃度は、排水処理工程、キルン等での使用
には十分な酸素濃度である。一方、塔頂部回収ガス中の
炭酸ガスは０．５％にまで除去され、酸素濃度は８６．
１％となった。この酸素濃度は、酸素脱リグニン工程で
の使用においても支障はない。The ozone concentration in the intermediate recovered gas was below the lower limit of detection, and it was confirmed that the ozone was almost completely removed in the lower filler layer 3. Also, 4.8 in the untreated gas
% Of the carbon dioxide gas present was removed to 4.1% in the intermediate recovery gas, and the oxygen concentration became 83.0%. This oxygen concentration is sufficient for use in wastewater treatment processes, kilns and the like. On the other hand, carbon dioxide in the recovered gas at the top of the tower was removed to 0.5%, and the oxygen concentration was 86.
It became 1%. This oxygen concentration does not hinder the use in the oxygen delignification step.
【００２８】実施例２
図２に示す装置において、実施例１で使用したのと同様
の吸収塔を用い、オゾン漂白排ガスを吸収塔１の塔底部
から５０Ｎｍ3／ｈで供給し、液温５０℃の吸収液（実
施例１で使用したのと同じ組成のもの）を吸収塔１の塔
頂部から１．２ｍ3／ｈで供給した。そして、下部充填
材層３で処理したオゾン漂白排ガスの半量（約２５Ｎｍ
3／ｈ）を吸収塔中間部２１から回収した。Example 2 In the apparatus shown in FIG. 2, the same absorption tower as used in Example 1 was used, ozone bleaching exhaust gas was supplied from the bottom of the absorption tower 1 at 50 Nm 3 / h, and the liquid temperature was 50. An absorption liquid (having the same composition as that used in Example 1) at 0 ° C. was supplied from the top of the absorption tower 1 at 1.2 m 3 / h. And half of the ozone bleaching exhaust gas treated with the lower filler layer 3 (about 25 Nm
3 / h) was recovered from the absorption tower middle section 21.
【００２９】比較例
オゾン漂白排ガスの処理に必要な吸収液量を比較するた
めに、実施例２に対する比較例として、以下の操作を行
った。図２に示す装置において、実施例１で使用したの
と同様の吸収塔を用い、オゾン漂白排ガスを吸収塔１の
塔底部から５０Ｎｍ3／ｈで供給し、液温６５℃の吸収
液（実施例１で使用したのと同じ組成のもの）を吸収塔
１の塔頂部から１．２ｍ3／ｈで供給した。そして、中
間部回収ガス止め弁８は閉とし、オゾン漂白排ガスの全
量を塔頂部から回収した。（このとき、吸収液の液温を
６５℃としたのは、実施例２よりも上部充填材層で処理
するオゾン漂白排ガス量が増えるので、処理効率を上げ
るためである。）Comparative Example In order to compare the amount of absorbing liquid required for the treatment of ozone bleaching exhaust gas, the following operation was performed as a comparative example to Example 2. In the apparatus shown in FIG. 2, the same absorption tower as that used in Example 1 was used, ozone bleaching exhaust gas was supplied from the bottom of the absorption tower 1 at 50 Nm 3 / h, and the absorption liquid at a liquid temperature of 65 ° C. The same composition as used in Example 1) was fed from the top of the absorption tower 1 at 1.2 m 3 / h. Then, the intermediate portion recovery gas stop valve 8 was closed, and the entire amount of the ozone bleaching exhaust gas was recovered from the tower top. (At this time, the liquid temperature of the absorbing liquid was set to 65 ° C. in order to increase the treatment efficiency because the amount of ozone bleaching exhaust gas treated in the upper filler layer was larger than that in Example 2.)
【００３０】表２に、処理前のオゾン漂白排ガス組成、
実施例２の中間部回収ガス及び塔頂部回収ガス組成、並
びに、比較例の塔頂部回収ガス組成を示す。Table 2 shows the composition of ozone bleaching exhaust gas before treatment,
The composition of the recovered gas and the recovered gas at the top of the column in Example 2 and the composition of the recovered gas at the top of Comparative Example are shown.
【００３１】[0031]
【表２】 [Table 2]
【００３２】実施例２の場合、下部充填材層３で除去さ
れた炭酸ガスは０．５Ｎｍ3／ｈであり、上部充填材層
２で除去された炭酸ガスは０．８８Ｎｍ3／ｈであっ
た。すなわち、除去された炭酸ガスは１．３８Ｎｍ3／
ｈであった。一方、比較例の場合、除去された炭酸ガス
は２．２５Ｎｍ3／ｈであった。なお、５０Ｎｍ3／ｈで
供給されたオゾン漂白排ガス（未処理ガス）中の炭酸ガ
スは、２．５Ｎｍ3／ｈであった。ここで、吸収塔で消
費された吸収液中のＮａＯＨ量は、除去された炭酸ガス
量に比例すると考えられる。したがって、排ガス全量を
塔頂部から回収した比較例の場合の炭酸ガス吸収量すな
わち吸収液消費量を１００とすると、中間部及び塔頂部
から同量のガス量を回収した実施例２の場合のＮａＯＨ
消費量は約６１であり、吸収液消費量が削減できたこと
は明らかである。In the case of Example 2, the carbon dioxide gas removed by the lower filler layer 3 was 0.5 Nm 3 / h, and the carbon dioxide gas removed by the upper filler layer 2 was 0.88 Nm 3 / h. It was That is, the removed carbon dioxide gas is 1.38 Nm 3 /
It was h. On the other hand, in the case of the comparative example, the carbon dioxide gas removed was 2.25 Nm 3 / h. Incidentally, carbon dioxide in the supplied ozone bleaching gas (untreated gas) at 50 Nm 3 / h was 2.5 Nm 3 / h. Here, the amount of NaOH in the absorption liquid consumed in the absorption tower is considered to be proportional to the amount of carbon dioxide gas removed. Therefore, assuming that the carbon dioxide absorption amount in the case of the comparative example in which the total amount of exhaust gas was recovered from the tower top, that is, the absorption liquid consumption amount was 100, the NaOH in the case of Example 2 in which the same amount of gas was recovered from the middle part and the tower top part
The consumption amount was about 61, and it is clear that the absorption liquid consumption amount could be reduced.
【００３３】[0033]
【発明の効果】本発明の処理方法によると、充填材層中
を上昇するオゾン漂白排ガスの一部を、充填材層の中間
位置において回収するので、排ガス処理に必要な吸収液
の使用量を低減できる。したがって、オゾン漂白排ガス
処理に要するコストを低減できる。また、オゾン漂白排
ガス処理を１基の吸収塔で行いながら、排水処理、キル
ン等で使用できる比較的低純度の酸素ガスと、酸素脱リ
グニン工程等で使用できる比較的高純度の酸素ガスとを
得ることができるので、設置スペースが小さいオゾン漂
白排ガス処理装置を提供することができる。According to the treatment method of the present invention, a part of the ozone bleaching exhaust gas rising in the filler layer is recovered at the intermediate position of the filler layer, so that the amount of the absorbent used for exhaust gas treatment can be reduced. It can be reduced. Therefore, the cost required for ozone bleaching exhaust gas treatment can be reduced. In addition, while performing ozone bleaching exhaust gas treatment in one absorption tower, relatively low-purity oxygen gas that can be used in wastewater treatment, kilns, etc., and relatively high-purity oxygen gas that can be used in oxygen delignification processes, etc. Therefore, it is possible to provide an ozone bleaching exhaust gas treatment device having a small installation space.
【図１】 本発明のオゾン漂白排ガス処理装置の一実施
態様を示す概略図である。FIG. 1 is a schematic diagram showing an embodiment of an ozone bleaching exhaust gas treatment apparatus of the present invention.
【図２】 本発明のオゾン漂白排ガス処理装置の一実施
態様を示す概略図である。FIG. 2 is a schematic view showing an embodiment of the ozone bleaching exhaust gas treatment apparatus of the present invention.
【図３】 従来のオゾン漂白排ガス処理装置の一例を示
す概略図である。FIG. 3 is a schematic view showing an example of a conventional ozone bleaching exhaust gas treatment apparatus.
１…吸収塔、２…上部充填材層、３…下部充填材層、４
…排気弁、５…回収ガス切替弁、６…塔頂部回収ガス供
給弁、７…中間部回収ガス供給弁、８…中間部回収ガス
止め弁、９…吸収液ノズル、１０…排ガスノズル、１
１、１２及び１３…デミスター、１４…圧縮機、１５…
ブロア、１６…回収ガスバイパス弁、１７…吸収液バイ
パス弁、１８…吸収液補給弁、１９…吸収液弁、２０…
酸素ガス供給弁、２１…吸収塔中間部、２２…酸素濃度
計、２３…吸収液タンク、２４，２５…ポンプ、２６…
再分配器1 ... Absorption tower, 2 ... Upper packing material layer, 3 ... Lower packing material layer, 4
... Exhaust valve, 5 ... Recovered gas switching valve, 6 ... Tower top recovered gas supply valve, 7 ... Intermediate recovered gas supply valve, 8 ... Intermediate recovered gas stop valve, 9 ... Absorbing liquid nozzle, 10 ... Exhaust gas nozzle, 1
1, 12 and 13 ... Demister, 14 ... Compressor, 15 ...
Blower, 16 ... Recovered gas bypass valve, 17 ... Absorption liquid bypass valve, 18 ... Absorption liquid supply valve, 19 ... Absorption liquid valve, 20 ...
Oxygen gas supply valve, 21 ... Absorption tower middle part, 22 ... Oxygen concentration meter, 23 ... Absorption liquid tank, 24, 25 ... Pump, 26 ...
Redistributor
───────────────────────────────────────────────────── フロントページの続き (72)発明者 岩本 一帆 東京都港区西新橋１丁目16番７号 日本酸 素株式会社内 (72)発明者 古家 順 東京都千代田区丸の内３丁目４番２号 三 菱製紙株式会社内 (72)発明者 北谷 純治 東京都千代田区丸の内３丁目４番２号 三 菱製紙株式会社内 Ｆターム(参考） 4L055 AD08 BB18 CB47 CB60 FA22 FA30 ─────────────────────────────────────────────────── ─── Continued front page (72) Inventor Kazuho Iwamoto 1-16-7 Nishi-Shimbashi, Minato-ku, Tokyo Japan Acid Inside the corporation (72) Inventor Furuya Jun 3-4-2 Marunouchi 3-4-2, Chiyoda-ku, Tokyo Ryo Paper Co., Ltd. (72) Inventor Junji Kitaya 3-4-2 Marunouchi 3-4-2, Chiyoda-ku, Tokyo Ryo Paper Co., Ltd. F-term (reference) 4L055 AD08 BB18 CB47 CB60 FA22 FA30
Claims (10)
排ガスを供給し、充填材層中で上昇させつつ、充填材層
中を流下する吸収液に接触させるオゾン漂白排ガス処理
方法であって、 充填材層中を上昇するオゾン漂白排ガスの一部を、充填
材層の中間位置において回収し、他部を、充填材層を通
過させて回収することを特徴とするオゾン漂白排ガス処
理方法。1. A method for treating ozone bleaching exhaust gas, which comprises supplying ozone bleaching exhaust gas to an absorption tower having a packing material layer, and raising it in the packing material layer to bring it into contact with an absorbing liquid flowing down in the packing material layer. A method for treating ozone bleaching exhaust gas, characterized in that a part of the ozone bleaching exhaust gas rising in the filler layer is recovered at an intermediate position of the filler layer and the other part is recovered by passing through the filler layer.
前記中間位置が、各充填材層の間に設けた空間部分であ
ることを特徴とする請求項１記載のオゾン漂白排ガス処
理方法。2. The filler layer is at least two layers,
The ozone bleaching exhaust gas treatment method according to claim 1, wherein the intermediate position is a space portion provided between the filler layers.
分配を行うことを特徴とする請求項２記載のオゾン漂白
排ガス処理方法。3. The ozone bleaching exhaust gas treatment method according to claim 2, wherein the absorption liquid is redistributed at the intermediate position.
白排ガス中の酸素濃度を、充填材層の中間位置において
回収したオゾン漂白排ガスを添加することによって調整
することを特徴とする請求項１乃至３のいずれか１項に
記載のオゾン漂白排ガス処理方法。4. The oxygen concentration in the ozone bleaching exhaust gas recovered by passing through the filler layer is adjusted by adding the ozone bleaching exhaust gas recovered at an intermediate position of the filler layer. 4. The ozone bleaching exhaust gas treatment method according to any one of 1 to 3.
白排ガス中の酸素濃度を、酸素ガスを添加することによ
って調整することを特徴とする請求項１乃至４のいずれ
か１項に記載のオゾン漂白排ガス処理方法。5. The oxygen concentration in the ozone bleaching exhaust gas recovered by passing through the filler layer is adjusted by adding oxygen gas, according to any one of claims 1 to 4. Ozone bleaching exhaust gas treatment method.
塔頂部に吸収液を供給する吸収液供給手段と、該吸収液
を該吸収塔の塔底部から回収する吸収液回収手段と、オ
ゾン漂白排ガスを該吸収塔の塔底部に供給するオゾン漂
白排ガス供給手段とを備え、 充填材層の中間位置の少なくとも１カ所と塔頂部とに、
供給したオゾン漂白排ガスを回収するオゾン漂白排ガス
回収手段を備えることを特徴とするオゾン漂白排ガス処
理装置。6. An absorption tower having a packing material layer, an absorption liquid supply means for supplying the absorption liquid to the top of the absorption tower, and an absorption liquid recovery means for recovering the absorption liquid from the bottom of the absorption tower. An ozone bleaching exhaust gas supply means for supplying ozone bleaching exhaust gas to the tower bottom of the absorption tower, and at least one intermediate position of the packing material layer and the tower top,
An ozone bleaching exhaust gas treatment device comprising an ozone bleaching exhaust gas recovery means for recovering the supplied ozone bleaching exhaust gas.
前記中間位置が、各充填材層の間に設けた空間部分であ
ることを特徴とする請求項６記載のオゾン漂白排ガス処
理装置。7. The filler layer is at least two layers,
The ozone bleaching exhaust gas treatment device according to claim 6, wherein the intermediate position is a space portion provided between the filler layers.
を備えることを特徴とする請求項７記載のオゾン漂白排
ガス処理装置。8. The ozone bleaching exhaust gas treatment apparatus according to claim 7, further comprising a redistributor for the absorbing liquid provided at the intermediate position.
回収手段に対して該吸収塔の中間部のオゾン漂白排ガス
回収手段が連結され、該塔頂部から回収したオゾン漂白
排ガスに添加する中間位置から回収したオゾン漂白排ガ
スの量を調整するガス量調整手段と、該吸収塔の塔頂部
から回収したオゾン漂白排ガス中の酸素濃度を測定する
酸素濃度計とを備えることを特徴とする請求項６乃至８
のいずれか１項に記載のオゾン漂白排ガス処理装置。9. An intermediate position for adding ozone bleaching exhaust gas to the ozone bleaching exhaust gas collected from the tower top, wherein ozone bleaching exhaust gas collecting means at the middle part of the absorption tower is connected to the ozone bleaching exhaust gas recovery means at the top of the absorption tower. 7. A gas amount adjusting means for adjusting the amount of ozone bleaching exhaust gas recovered from the absorption tower, and an oxygen concentration meter for measuring the oxygen concentration in the ozone bleaching exhaust gas recovered from the top of the absorption tower. Through 8
The ozone bleaching exhaust gas treatment apparatus according to any one of 1.
ン漂白排ガスに酸素ガスを添加して該オゾン漂白排ガス
中の酸素濃度を調整する酸素ガス供給弁と、該オゾン漂
白排ガス中の酸素濃度を測定する酸素濃度計とを備える
ことを特徴とする請求項６乃至９のいずれか１項に記載
のオゾン漂白排ガス処理装置。10. An oxygen gas supply valve for adjusting the oxygen concentration in the ozone bleaching exhaust gas by adding oxygen gas to the ozone bleaching exhaust gas recovered from the tower top of the absorption tower, and the oxygen concentration in the ozone bleaching exhaust gas. An ozone bleaching exhaust gas treatment apparatus according to any one of claims 6 to 9, further comprising an oxygen concentration meter for measuring.
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|---|---|---|---|
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002152918A JP3914820B2 (en) | 2002-05-27 | 2002-05-27 | Method and apparatus for treating ozone bleaching exhaust gas |
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| JP3914820B2 JP3914820B2 (en) | 2007-05-16 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101131074B1 (en) * | 2010-02-03 | 2012-03-30 | 해성엔지니어링 주식회사 | Method for Treatment of Discharged Ozone by Using Alkali Reductive Solution |
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2002
- 2002-05-27 JP JP2002152918A patent/JP3914820B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101131074B1 (en) * | 2010-02-03 | 2012-03-30 | 해성엔지니어링 주식회사 | Method for Treatment of Discharged Ozone by Using Alkali Reductive Solution |
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| Publication number | Publication date |
|---|---|
| JP3914820B2 (en) | 2007-05-16 |
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