JP3069578B2 - Solvent recovery method and apparatus - Google Patents
Solvent recovery method and apparatusInfo
- Publication number
- JP3069578B2 JP3069578B2 JP6317649A JP31764994A JP3069578B2 JP 3069578 B2 JP3069578 B2 JP 3069578B2 JP 6317649 A JP6317649 A JP 6317649A JP 31764994 A JP31764994 A JP 31764994A JP 3069578 B2 JP3069578 B2 JP 3069578B2
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- Prior art keywords
- gas
- organic solvent
- steam
- solvent
- adsorption
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- Separation Of Gases By Adsorption (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は活性炭素繊維（以下ＡＣ
Ｆと言う）を吸着材として、排ガス中の有機溶剤を吸着
回収する溶剤回収方法および装置に関するものである。
更に詳しくは、電子機器製造工場、金属加工工場等に
おける洗浄装置、フィルムコーター装置の排ガス等の中
に含まれる、塩化メチレン・トリクロロエチレン等の比
較的沸点の低い有機溶剤ガスをＡＣＦに吸着させ、排ガ
スを清浄化すると共に、ＡＣＦに吸着した前記有機溶剤
を、水蒸気にて脱着し、回収する方法および装置に関す
るものである。The present invention relates to an activated carbon fiber (hereinafter referred to as AC
F) as an adsorbent, and a method and an apparatus for collecting and recovering an organic solvent in exhaust gas.
More specifically, ACF adsorbs organic solvent gas having a relatively low boiling point, such as methylene chloride and trichloroethylene, contained in exhaust gas from cleaning equipment and film coater equipment in electronic equipment manufacturing factories, metal processing factories, etc. The present invention relates to a method and an apparatus for purifying and recovering the organic solvent adsorbed on the ACF with steam and recovering the same.
【０００２】[0002]
【従来の技術】従来、吸着剤としてＡＣＦを層状に形成
し、溶剤含有ガスをこのＡＣＦ層を通過させて回収す
る、溶剤回収装置に於いては、ＡＣＦに吸着した溶剤を
脱着するには、おおよそ次の様にして行われる。脱着工
程では、水蒸気を最初からＡＣＦ層を通過するように供
給して、ＡＣＦ層を加熱し、ＡＣＦに吸着している溶剤
を脱着する。脱着溶剤を含む水蒸気は凝縮器にて冷却液
化し回収する。2. Description of the Related Art Conventionally, in a solvent recovery apparatus in which ACF is formed in a layer form as an adsorbent and a solvent-containing gas is recovered by passing through the ACF layer, desorption of a solvent adsorbed on the ACF is performed by: It is performed roughly as follows. In the desorption step, water vapor is supplied so as to pass through the ACF layer from the beginning, and the ACF layer is heated to desorb the solvent adsorbed on the ACF . Steam containing the desorbing solvent is cooled and liquefied in a condenser and collected.
【０００３】すなわち、活性炭素繊維を吸着素子として
用いた溶剤回収システムでは、 〔第一工程・吸着工程〕吸着素子に溶剤含有ガス（被処
理ガス・原ガス）を供給し、溶剤ガスを吸着させ、清浄
ガス（清浄空気）は、系外に排出する。 〔第二・脱着工程〕脱着用水蒸気を活性炭素繊維の吸着
素子に供給し、ここに吸着している溶剤を脱着し、吸着
素子を再生すると共に、脱着した溶剤含有水蒸気を系外
に取り出す。 〔第三工程・回収工程〕溶剤含有水蒸気の初期流には、
溶剤、空気、水蒸気を含有する。溶剤含有水蒸気の本流
は、主に水蒸気と脱着溶剤とからなる。この両者は分別
されず、凝縮器で冷却され、水蒸気と溶剤は凝縮され、
回収される。初期流にある空気に溶剤が気化した未凝縮
溶剤ガスは、再度活性炭素繊維に吸着され、溶剤を含ま
ない清浄空気として排出される。[0003] That is, in the Solvent recovered system using activated carbon fiber as the adsorbing element, to supply [first step and adsorption step] solvent-containing gas to the adsorbing element (treated gas-crude gas), the solvent gas Adsorb and clean gas (clean air) is discharged out of the system. [Second Desorption Step] The desorption water vapor is supplied to the activated carbon fiber adsorption element, the solvent adsorbed therein is desorbed, the adsorption element is regenerated, and the desorbed solvent-containing water vapor is taken out of the system. [Third step / recovery step] In the initial flow of the solvent-containing steam,
Solvent, air, containing water vapor. Mainstream solvent-containing steam, consisting mainly of water vapor and desorption SOLVENTS. The two are not separated, are cooled in a condenser, and the water vapor and the solvent are condensed,
Collected. Uncondensed solvent gas solvent is vaporized into the air in the initial stream is adsorbed again activated carbon fibers, it is discharged as clean air free of solvent.
【０００４】また、粒状炭の場合は、吸・脱着缶への充
填量が多く、このため１サイクル当たりの吸着量が多
く、サイクル時間が長い。ＡＣＦを用いた溶剤回収装置
は、吸着材の吸着性能・圧力損失・価格が高い事、脱着
時間が短くて済む事などから、充填するＡＣＦ量を極力
少量に抑え、吸着と脱着のサイクルを、短く且つ速くす
るのが一般的である。その為、吸脱着の工程切替時間を
短く（６分〜２０分）しているのが現状である。[0004] In the case of granular coal, the amount of filling in the adsorption / desorption can is large, so that the adsorption amount per cycle is large and the cycle time is long. Solvent recovery equipment using ACF requires a small amount of ACF to be filled as much as possible because of high adsorption performance, high pressure loss, high price of adsorbent, and short desorption time. It is common to make it short and fast. Therefore, at present, the process switching time of the adsorption / desorption is shortened (6 minutes to 20 minutes).
【０００５】[0005]
【本発明が解決しようとする課題】溶剤回収装置一般に
は、缶内に、ＡＣＦにて構成された円筒状の吸着素子を
配設し、吸着は該吸着素子に被処理ガスを供給し吸着
素子通過後、清浄ガスとして取り出し、脱着は水蒸気
を吸着素子に供給し吸着素子通過後、脱着ガスとして回
収する装置が知られている（特開昭６０−７９３９号、
同６１−６８１２２号、特開平１−１３０７１５号）。SUMMARY OF THE INVENTION In general, a solvent recovery device is provided with a cylindrical adsorption element made of ACF in a can, and the adsorption element supplies a gas to be treated to the adsorption element. A device is known which removes the gas after passing therethrough as a clean gas and supplies water vapor to the adsorption element for desorption, and recovers the gas as a desorption gas after passing through the adsorption element (Japanese Patent Application Laid-Open No. 60-7939,
No. 61-68122, JP-A-1-130715).
【０００６】このような装置では、吸着素子を通過する
前のガスが缶内に残るスペースとして、吸着素子の外周
から、脱着ガス取出し口までの空間（仮にこの空間を低
濃度ガス空間と呼ぶ）が必然的に存在し、ここに、被処
理ガス供給停止直後、ＡＣＦ層を通過する前の被処理ガ
ス（原ガス）が充満している。In such an apparatus, the space from the outer periphery of the adsorption element to the desorption gas outlet is temporarily defined as a space where the gas before passing through the adsorption element remains in the can (tentatively, this space is called a low concentration gas space). Is inevitably present, and immediately after the supply of the gas to be treated is stopped, the gas to be treated (raw gas) before passing through the ACF layer is filled.
【０００７】この低濃度ガス空間に充満するガス（原ガ
ス）は、ＡＣＦ層を通過する前であり、数十乃至数百ｐ
ｐｍ単位の溶剤ガスを含んでいる。この低濃度ガス空間
に存在する低濃度ガスは、脱着水蒸気を供給の際、始め
に吹き出されるが、同時に脱着した溶剤を含む事にな
る。この溶剤とガス（空気）との分離は、水蒸気と溶剤
の分離よりも困難であり、溶剤は未凝縮ガスのまま、サ
イクル度ごとに排出されることになる。The gas (original gas) filling the low-concentration gas space before passing through the ACF layer is several tens to several hundreds p.
It contains solvent gas in pm units. The low-concentration gas existing in the low-concentration gas space is blown out first when supplying the desorbed steam, but at the same time contains the desorbed solvent. The separation of the solvent from the gas (air) is more difficult than the separation of the water vapor and the solvent, and the solvent is discharged at each cycle without being condensed.
【０００８】前述のように、ＡＣＦを用いた溶剤回収装
置では、吸脱着のサイクルタイムを短くする事により、
一つの弊害が伴う。それは脱着時に発生するこの未凝縮
ガスが、吸着・脱着サイクルに対応し、その発生回数が
多いと言う事である。As described above, in a solvent recovery apparatus using ACF, the cycle time of adsorption and desorption is shortened,
There is one evil. It is this non-condensed gas generated at the time of desorption, corresponds to the adsorption and desorption cycles, is to say that there are many number of occurrences.
【０００９】未凝縮ガスの発生は次のようなメカニズム
からなる。吸着が終了した状態の缶内には、配設された
ＡＣＦ吸着素子とそれに吸着した溶剤、そして大気圧下
にある缶一杯分のガス（空気）が存在している。そし
て、脱着工程では、吸着工程から脱着工程に移るとすぐ
に水蒸気を吹き込む。吹き込まれた水蒸気はＡＣＦ層を
通過しながら吸着した溶剤を脱着させる。The generation of the uncondensed gas has the following mechanism. The ACF adsorbing element, the solvent adsorbed on the ACF adsorbing element, and gas (air) for one can at atmospheric pressure are present in the can in the state where the adsorption is completed. Then, in the desorption step, water vapor is blown as soon as the process proceeds from the adsorption step to the desorption step. The blown water vapor desorbs the adsorbed solvent while passing through the ACF layer.
【００１０】脱着工程のごく初期の段階では缶内には、
まだ空気が残存しているから、それに脱着した溶剤が気
化し、缶一杯分の空気中に脱着初期の高い濃度で気化し
た溶剤ガスが存在することになる。ＡＣＦの脱着速度が
非常に速い事も作用して、この状況は一気に進む。そし
てこれらは次の凝縮工程に送られる。At the very early stage of the desorption process,
Since the air still remains, the solvent desorbed therein is vaporized, and the solvent gas vaporized at a high concentration in the early stage of desorption exists in the air for one can. The fact that the desorption speed of the ACF is very fast acts, and this situation progresses at once. These are then sent to the next condensation step.
【００１１】凝縮工程に送られるガス類をまとめなおす
と、脱着の為に吹き込んだ水蒸気、ＡＣＦに吸着さ
れていた溶剤であって、水蒸気で脱着されたもの、缶
内にあった缶一杯分の空気等であり、缶内にあった缶
一杯分の空気は、その場所によって、 −ア 前記した、低濃度ガス空間の空気 −イ 吸着素子を通過した後、清浄ガスとして排出さ
れる前の空間の空気 −ウ ＡＣＦ総内の空気 に分けられる。凝縮肯定時は、これらのガスが冷却さ
れ、凝縮するわけであるが、ここで問題になるのが空気
中に気化した溶剤、すなわち溶剤ガスである。[0011] The gases sent to the condensing step are summarized as follows: steam blown for desorption, the solvent adsorbed on the ACF, which has been desorbed by steam, and the amount of the can contained in the can an air or the like, cans single serving of the air that was in the can, by its location, - a above, the low concentration gas space air - after passing through the stomach adsorbing elements, the space before issued exhaust as clean gas Air-C The air in the ACF is divided into air. At the time of positive condensation, these gases are cooled and condensed, but what matters here is the solvent vaporized in the air, that is, the solvent gas.
【００１２】この溶剤ガスは、凝縮工程で冷やされた温
度での飽和ガス濃度として存在し、それ以上の凝縮はで
きない。ここで飽和濃度をより下げようとすれば冷却温
度をより下げることであるが、水分の凍結等の問題が新
たに発生し実用的ではない。その為、実際には未凝縮ガ
スとして容認し、循環させるシステムを組まなければな
らない。この未凝縮ガスは濃度が高い為、そのまま大気
に排出することはできず、吸着側にリサイクルする事に
なる。This solvent gas exists as a saturated gas concentration at the temperature cooled in the condensation step, and cannot be further condensed. Here, if the saturation concentration is to be further lowered, the cooling temperature must be further lowered. However, a problem such as freezing of moisture is newly generated, which is not practical. Therefore, it is necessary to establish a system for actually accepting and circulating uncondensed gas. Since the uncondensed gas has a high concentration, it cannot be discharged to the atmosphere as it is, but is recycled to the adsorption side.
【００１３】このような結果、吸着側にこのリサイクル
分の溶剤が余分な負荷となってしまい、その分に対応し
たＡＣＦを増量しなければならない。特に沸点の低い溶
剤ほど未凝縮ガスの濃度が高いため、吸着側への負荷が
大きくなる。この再度吸着させる未凝縮ガスというのが
本来の目的から言うとムダである。この事から、未凝縮
ガス中の溶剤の絶対量を減らすことが必要である。[0013] As a result, the recycled solvent becomes an extra load on the adsorption side, and the amount of ACF must be increased accordingly. In particular, since the concentration of the uncondensed gas is higher as the solvent has a lower boiling point, the load on the adsorption side increases. The uncondensed gas to be adsorbed again is wasteful from its original purpose. For this reason, it is necessary to reduce the absolute amount of the solvent in the uncondensed gas.
【００１４】未凝縮ガス中の溶剤の絶対量を減らす為の
方策としては、先ず凝縮工程での冷却温度を下げる事に
より、未凝縮ガス濃度を下げる事である。しかし、これ
は前項でも述べたように０℃以下にすると水分の凍結と
いう問題があり、一般的には５℃〜１０℃程度に維持し
ている。As a measure for reducing the absolute amount of the solvent in the uncondensed gas, the concentration of the uncondensed gas is first reduced by lowering the cooling temperature in the condensation step. However, as described in the previous section, when the temperature is set to 0 ° C. or lower, there is a problem of freezing of water, and generally, the temperature is maintained at about 5 ° C. to 10 ° C.
【００１５】本発明は、前記した従来技術の問題点を解
決し、未凝縮ガス中の溶剤絶対量を減少させ、ＡＣＦ吸
着素子への吸着負荷を軽減し、吸着素子の稼働効率を高
めることを目的とする。 The present invention solves the above-mentioned problems of the prior art.
Decrease the absolute amount of solvent in the uncondensed gas,
Reduces the adsorption load on the attached element and increases the operating efficiency of the adsorption element
The purpose is to be.
【００１６】[0016]
【課題を解決するための手段】本発明の有機溶剤回収方
法は、活性炭素繊維層を吸着素子として有する有機溶剤
回収装置を用いて、被処理ガスに含まれる有機溶剤を吸
着する吸着工程、該吸着素子に吸着された有機溶剤を水
蒸気で脱着する脱着工程、及び脱着された有機溶剤を回
収する回収工程を含む有機溶剤回収方法において、該脱
着工程に先立ち、水蒸気を該有機溶剤回収装置に導入し
て、該吸着素子に吸着された有機溶剤を脱着することな
く、有機溶剤回収装置に残存する未処理ガスを水蒸気で
置換して排出することを特徴とする。 SUMMARY OF THE INVENTION The organic solvent recovery method of the present invention
The method uses an organic solvent having an activated carbon fiber layer as an adsorption element.
Using a recovery device, absorb the organic solvent contained in the gas to be treated.
Adsorption step of adhering the organic solvent adsorbed on the adsorption element to water
The desorption step of desorption with steam and the recovery of the desorbed organic solvent
In the organic solvent recovery method including a recovery step of recovering,
Prior to the deposition step, steam is introduced into the organic solvent recovery device.
Therefore, the organic solvent adsorbed on the adsorption element is not desorbed.
The untreated gas remaining in the organic solvent recovery unit with steam
It is characterized by being replaced and discharged.
【００１７】前記本発明の有機溶剤回収方法において、
水蒸気を有機溶剤回収装置に導入して、吸着素子に吸着
された有機溶剤を脱着することなく、有機溶剤回収装置
に残存する未処理ガスを水蒸気で置換して排出する前記
方法は、具体的には、該有機溶剤回収装置内において、
活性炭素繊維層を未通過の被処理ガスが未処理ガスとし
て残存している空間部に、直接、水蒸気を導入して行う
ことが好ましい。また、水蒸気で置換され排出された前
記未処理ガスを、吸着工程に戻すことが好ましい。 In the method for recovering an organic solvent according to the present invention,
Introduces water vapor into the organic solvent recovery unit and adsorbs it on the adsorption element
Organic solvent recovery device without desorbing organic solvent
The untreated gas remaining in
The method is, specifically, in the organic solvent recovery device,
The gas to be processed that has not passed through the activated carbon fiber layer is
By introducing steam directly into the remaining space
Is preferred. Before being replaced by steam and discharged
The untreated gas is preferably returned to the adsorption step.
【００１８】この方法には、前記空間内に残存している
未処理ガスを水蒸気で置換し、次いで、活性炭素繊維の
吸着素子に吸着用水蒸気を供給して吸着素子に吸着して
いる溶剤を脱着後、脱着溶剤を含む水蒸気を冷却装置に
供給し、溶剤を回収することを特徴とする溶剤回収方法
を含む。According to this method, the liquid remains in the space.
After replacing the untreated gas with water vapor, and then supplying the water vapor for adsorption to the adsorption element of the activated carbon fiber to desorb the solvent adsorbed on the adsorption element, supplying the water vapor containing the desorption solvent to the cooling device, And a method for recovering a solvent.
【００１９】前記溶剤回収方法を実施するための本発明
の有機溶剤回収装置は、活性炭素繊維層を円筒状にした
吸着素子を内部に有し、導入された被処理ガス中の有機
溶剤を吸着素子で吸着し、導入された水蒸気により吸着
素子に吸着されている有機溶剤を脱着し回収することが
できる有機溶剤回収装置において、該吸着素子により有
機溶剤回収装置の内部は２つの空間が形成され、一方の
空間を形成する部分に、被処理ガスを供給するための被
処理ガス供給口及び未処理ガスを水蒸気で置換するため
の水蒸気供給口を設けたことを特徴とする。 The present invention for carrying out the above solvent recovery method.
Organic solvent recovery device made the activated carbon fiber layer cylindrical
Organic substance in the gas to be treated introduced with an adsorption element inside
Solvent is adsorbed by the adsorption element and adsorbed by the introduced water vapor
It is possible to desorb and recover the organic solvent adsorbed on the element.
In organic solvent recovery equipment that can
Two spaces are formed inside the solvent recovery device.
The part for forming the space is supplied with the gas to be treated.
To replace the processing gas supply port and unprocessed gas with steam
Is provided .
【００２０】また、この装置は、活性炭素繊維層にて構
成された円筒状の吸着素子の内側中央より脱着用水蒸気
を供給するための機構を有する。本発明の有機溶剤回収
方法を、前述の従来システムと対比する形で示すと次の
通りである。すなわち 〔Ａ工程・吸着工程〕吸着素子に溶剤含有ガス（被処理
ガス）を供給し、溶剤ガスを吸着させ、清浄ガス（清浄
空気）は、系外に排出する。 〔Ｂ−１工程・置換工程〕脱着ガス取出口と活性炭素繊
維の吸着素子との空間部に水蒸気を供給し、微かに溶剤
を含む空気を追い出し、水蒸気で置換する。 〔Ｂ−２工程・凝縮／吸着工程〕水蒸気で追い出され
た、微かに溶剤を含む空気は、凝縮器を経て後、吸着工
程に戻され、溶剤は吸着分離し、空気は清浄空気として
排出する。 〔Ｂ−３工程・脱着工程〕脱着用水蒸気を活性炭素繊維
の吸着素子に供給し、ここに吸着している溶剤を脱着
し、活性炭素繊維の吸着素子を再生すると共に、脱着し
た溶剤と缶内空気の一部（前記−イ、−ウ相当分）
を含む水蒸気を系外に取り出す。〔Ｃ 工程・凝縮／吸着工程〕缶内空気の一部を含む溶剤
含有水蒸気は、凝縮器で冷却され、未凝縮ガス（缶内空
気の一部とこれに含まれる溶剤ガス）は、吸着工程に戻
される。Further, this device has a mechanism for feeding the inner central I Rida' worn steam cylindrical adsorbing element which is composed of activated carbon fiber layer. The method for recovering an organic solvent of the present invention is shown below in comparison with the conventional system described above. That is, [Step A / adsorption step] A solvent-containing gas (gas to be treated) is supplied to the adsorption element to adsorb the solvent gas, and a clean gas (clean air) is discharged out of the system. [B-1 Step / Substitution Step] Water vapor is supplied to the space between the desorption gas outlet and the activated carbon fiber adsorption element, and air containing a solvent is slightly expelled and replaced with water vapor. [B-2 Step Condensation / Adsorption Step] The air slightly containing the solvent expelled by the water vapor passes through the condenser and is returned to the adsorption step. The solvent is adsorbed and separated, and the air is discharged as clean air. . [B-3 Step / Desorption Step] The desorption water vapor is supplied to the activated carbon fiber adsorption element, the solvent adsorbed here is desorbed, the activated carbon fiber adsorption element is regenerated, and the desorbed solvent and can are removed. Part of the internal air (corresponding to -a and -c above)
Is taken out of the system. [ Step C : Condensation / adsorption step] The solvent-containing steam containing a part of the air in the can is cooled by a condenser, and the uncondensed gas (part of the air in the can and the solvent gas contained therein) is removed by the adsorption step. Is returned to.
【００２１】本発明の有機溶剤回収方法により、〔Ｂ−
２工程〕で空気を水蒸気によって置換すると、缶内の空
気の３０〜５０％ガス濃度が低いままで缶内から抜けて
しまう。この濃度の低いガスは、凝縮工程を経て後、吸
着工程に戻される。この水蒸気で追い出されたガスに
は、脱着ガスは殆ど含まず、濃度が低い分だけＡＣＦ吸
着素子に与える負荷は少ない。また、本発明によると、
溶剤を吸着した活性炭素繊維層を通過した脱着用水蒸気
が、脱着ガスを含んだ高濃度のまま通過する通路である
ところの、活性炭素繊維層から取出口までの空間の空気
が、〔Ｂ−２工程〕ですでに水蒸気で置換されているた
め、凝縮分離の困難な空気中に、脱着した溶剤ガスが拡
散することを、少なくすることができる。According to the organic solvent recovery method of the present invention, [B-
When the air is replaced by steam in the two steps, the air in the can exits the can with a low gas concentration of 30 to 50%. The low-concentration gas is returned to the adsorption step after passing through the condensation step. The gas expelled by the water vapor contains almost no desorbed gas, and the lower the concentration, the less the load applied to the ACF adsorption element. Also, according to the present invention,
The air in the space from the activated carbon fiber layer to the outlet, which is a passage through which the desorbed steam passing through the activated carbon fiber layer adsorbing the solvent remains at a high concentration containing the desorbed gas, is [B- because it is already replaced with water vapor in two steps], the difficult in the air condensed and separated, that desorbed SOLVENTS gas diffusion can be reduced.
【００２２】脱着工程においては、吸着工程終了直後、
まず空気を水蒸気によって置換する。次に活性炭素繊維
の吸着素子の内側から外側に向かってＡＣＦ全体を加熱
するように水蒸気を吹き込み、活性炭素繊維に吸着して
いる溶剤を脱着する。この時は従来方式と同工程のガス
濃度となるが、缶内の残存空気量は、すでに５０〜７０
％と少なくなっている。たのため、再吸着工程に供すべ
き未凝縮ガス量自体が少なくなり、活性炭素繊維吸着素
子の負担を軽減することができる。In the desorption step, immediately after the end of the adsorption step,
First, the air is replaced by steam. Next, water vapor is blown from the inside to the outside of the activated carbon fiber adsorption element so as to heat the entire ACF, and the solvent adsorbed on the activated carbon fiber is desorbed. At this time, the gas concentration becomes the same as in the conventional method, but the amount of air remaining in the can is already 50 to 70%.
%. Therefore, the amount of uncondensed gas itself to be subjected to the re- adsorption step is reduced, and the load on the activated carbon fiber adsorption element can be reduced.
【００２３】本発明の方法および装置について図面を用
いて説明する。図１は、本発明の溶剤回収装置（２缶
式）の脱着方式のフローシートである。図２は、図１の
ＡＣＦ吸着素子を配設した缶の水平方向断面図である。
図１・図２に於いて、１は缶、２はＡＣＦ吸着素子、３
は凝縮器，４は脱着蒸気弁（脱着用水蒸気の吹き込みを
ＯＮ−ＯＦＦする自動弁）、そして５は本発明の要目で
ある置換蒸気弁（置換用水蒸気の吹き込みをＯＮ−ＯＦ
Ｆする自動弁）である。６は脱着時に排出される脱着ガ
スの出口弁、７は送風機、８は清浄空気取出口（弁）、
９は脱着用水蒸気供給ノズル、１０は被処理ガス供給口
（弁）である。The method and apparatus of the present invention will be described with reference to the drawings. FIG. 1 is a desorption type flow sheet of the solvent recovery apparatus (two-can type) of the present invention. FIG. 2 is a horizontal sectional view of a can provided with the ACF adsorption element of FIG.
1 and 2, 1 is a can, 2 is an ACF adsorption element, 3
Is a condenser, 4 is a desorption steam valve (automatic valve that turns on and off the injection of steam for desorption), and 5 is a replacement steam valve (an ON-OF injection of steam for replacement), which is the gist of the present invention.
F automatic valve). 6 is an outlet valve for desorbed gas discharged at the time of desorption, 7 is a blower, 8 is a clean air outlet (valve),
9 is a steam supply nozzle for desorption, and 10 is a gas supply port (valve) to be processed.
【００２４】また、アは、ＡＣＦ吸着素子２と、脱着ガ
ス出口（弁）６との間の空間部である。イは、ＡＣＦ吸
着素子２と、清浄空気取出口（弁）８との間の空間部で
ある。ａは未凝集ガスの循環ルート、ｂは水蒸気置換ル
ートをそれぞれ示す。A is a space between the ACF adsorption element 2 and the desorption gas outlet (valve) 6. A is a space between the ACF adsorption element 2 and the clean air outlet (valve) 8. a represents circular route unaggregated gas, b is the water vapor substitution route, respectively.
【００２５】従来の脱着方法では、脱着工程に入るとす
ぐに脱着蒸気弁４及び出口弁６が開き、弁４から水蒸気
が缶内に吹き込まれる。吹き込まれた水蒸気は、空間イ
の空気とＡＣＦ吸着素子２とを加熱し、ＡＣＦに吸着し
ていた溶剤を脱着し、空間アの空気をも伴い出口弁６を
通り、凝縮器３に送られる。脱着ガスは、凝縮器３で冷
却水により冷却され、水蒸気と一部の溶剤が凝縮する。
しかし、缶１内にあった空気は、凝縮器で冷却される温
度での、ほぼ飽和濃度の溶剤ガスとなって、吸着側への
循環ルートａを通り吸着工程中の缶１' に戻る。In the conventional desorption method, as soon as the desorption step is started, the desorption steam valve 4 and the outlet valve 6 are opened, and steam is blown from the valve 4 into the can. The blown water vapor heats the air in the space A and the ACF adsorption element 2, desorbs the solvent adsorbed on the ACF, and is sent to the condenser 3 through the outlet valve 6 together with the air in the space A. . The desorbed gas is cooled by cooling water in the condenser 3, and water vapor and some of the solvent are condensed.
However, the air in the can 1 becomes almost saturated solvent gas at a temperature cooled by the condenser, and returns to the can 1 'during the adsorption process through the circulation route a to the adsorption side.
【００２６】本発明においては、空間部アに水蒸気を供
給するための置換蒸気弁５を有し、脱着に先立ち、先ず
この置換蒸気弁５及び出口弁６を開く。置換蒸気弁５を
開く事により少量の水蒸気（ニードル弁等により流量を
絞り調整する）が缶１に吹き込まれる。吹き込まれた水
蒸気は、空間部アを通りＡＣＦ吸着素子２の外側を図２
のルートｂの如く流れる。その時に空間部アの空気がｂ
ルートの水蒸気によって押し出され、出口弁６を通り凝
縮器３に至る。In the present invention, there is provided a replacement steam valve 5 for supplying steam to the space a , and the replacement steam valve 5 and the outlet valve 6 are first opened prior to desorption. By opening the replacement steam valve 5, a small amount of steam (the flow rate is adjusted by a needle valve or the like) is blown into the can 1. The blown water vapor passes through the space a, and the outside of the ACF adsorption element 2 is shown in FIG.
Flows like the route b. At that time, the air in the space
It is pushed out by the steam of the route and reaches the condenser 3 through the outlet valve 6.
【００２７】そして、この時、ＡＣＦ層が微かにしか加
熱されていない為、脱着は殆ど進んでおらず、この空間
部アに相当する容積分の空気は、極めて低い、被処理ガ
スの溶剤濃度のガスのままで、循環ルートａを通って吸
着工程に戻る。At this time, since the ACF layer is only slightly heated, the desorption has hardly progressed, and the volume of air corresponding to this space A is extremely low, and the solvent concentration of the gas to be treated is extremely low. And returns to the adsorption step through the circulation route a.
【００２８】このようにして、微かな水蒸気量で空間ア
の空気が水蒸気にて置換される。次に、脱着蒸気弁４を
開け脱着を始める。この時には、未凝縮ガスの源となる
缶１内の空気量は、缶の容積から空間部アを減じた容積
分の量となる。残存した空気には、溶剤がガス状態で凝
縮器に送られ、その冷却温度下における未凝縮ガスと凝
縮液とになる。このように脱着時（本発明では、置換工
程と脱着工程をまとめて脱着或いは脱着工程とくく
る。）に発生する未凝縮ガスの量そのものは変わらずと
も、本発明の場合は、未凝縮ガスの濃度を一部低くする
事により未凝縮ガス中の溶剤の絶対量を下げ、吸着側へ
の循環分負荷を約半減させる事ができる。In this manner, the air in the space A is replaced by the steam with a small amount of steam. Next, the desorption steam valve 4 is opened to start desorption. At this time, the amount of air in the can 1, which is a source of the uncondensed gas, is equal to the volume of the can minus the space a. In the remaining air, the solvent is sent to the condenser in a gaseous state, and becomes an uncondensed gas and a condensate at the cooling temperature. As described above, even when the amount of uncondensed gas generated during desorption (in the present invention, the replacement step and the desorption step are collectively referred to as a desorption or desorption step) does not change, in the case of the present invention, the amount of uncondensed gas By partially lowering the concentration, the absolute amount of the solvent in the uncondensed gas can be reduced, and the circulating load on the adsorption side can be reduced by about half.
【００２９】[0029]
［実施例］平面が長方形の箱型缶の内空間に、円筒状の
吸着素子６本を垂直に配設した溶剤回収装置を用いた。
個々の吸着素子には、それぞれ脱着用の水蒸気供給口が
開口して居る。以下に塩化メチレンの排ガスを処理する
実施例を示す。 （１）運転条件 （ａ）対象ガス 塩化メチレン 分子量 ８４．９３ ，沸点 ４０．４℃ 蒸気圧 １０℃のとき ２２９．７ mmHg （ｂ）処理ガス量，濃度 ９０Ｎｍ↑３/min ×４０００ p.p.m （溶剤量 ８１．９ Kg/H） （ｃ）処理温度 常温 缶（箱型） 寸法ｍｍ たて２２５０×よこ１５１０×高さ１４８０の箱型 容積リットル 約 ５０００ （ｅ）ＡＣＦ吸着素子 充填数 ６本／缶 円筒状吸着素子 外径φ６２０、内径φ４００ 高さ１４００ｍｍ ＡＣＦ重量 ２３Kg／本 （ｆ）凝縮条件 冷水温度 ： ７℃ 未凝縮ガス温度 ：１０℃[Embodiment] A solvent recovery apparatus in which six cylindrical adsorption elements were vertically arranged in the inner space of a box-shaped can having a rectangular plane was used.
Each of the adsorption elements has a water supply port for desorption for opening. An example of treating the exhaust gas of methylene chloride will be described below. (1) Operating conditions (a) Target gas: methylene chloride, molecular weight: 84.93, boiling point: 40.4 ° C, vapor pressure: 10 ° C, 229.7 mmHg (b) Processing gas amount, concentration: 90 Nm ↑ 3 / min × 4000 ppm (solvent Amount 81.9 Kg / H) (c) Processing temperature Room temperature Can (box type) Dimensions mm Box type with a length of 2250 x 1510 x 1480 Volume Approx. 5000 (e) ACF adsorption element Filling quantity 6 / can Cylindrical adsorption element Outer diameter φ620, inner diameter φ400 Height 1400mm ACF weight 23kg / piece (f) Condensation conditions Cold water temperature: 7 ° C Non-condensed gas temperature: 10 ° C
【００３０】（２）運転結果 前記条件にて従来法と本発明の脱着方法における、未凝
縮ガス量の比較をした。 （ａ）測定場所 未凝縮ガスの量と濃度を図１のＣ点、詳しくは図３のＣ
点で測定した。（ｂ）測定方法 ガス量−面積式流量計により１０秒間隔で、その時の瞬
時流量を計測した。 ガス濃度−全炭化水素計によ
る連続測定 型式 ＹＡＮＡＣＯ Ｇ−１００４Ｆ （ｃ）測定結果 図４，５に従来法と本発明の脱着時の未凝縮ガス量と、
ガス濃度及び未凝縮溶剤量の測定結果を示す。尚、図４
は従来法，図５は本発明である。この図の中で未凝縮溶
剤量は１０秒間単位の各時間でのガス量に溶剤濃度を乗
じて求めたものである。すなわち、図の中の棒グラフの
面積の和に相当する分の比較となる。(2) Operation Results Under the above conditions, the amount of uncondensed gas was compared between the conventional method and the desorption method of the present invention. (A) Measurement location The amount and concentration of the uncondensed gas are measured at point C in FIG.
Measured in points. (B) Measurement method The instantaneous flow rate at that time was measured at intervals of 10 seconds by a gas amount-area flow meter. Gas concentration-Continuous measurement by total hydrocarbon meter Model YANACO G-1004F (c) Measurement results Figs. 4 and 5 show the amount of uncondensed gas at the time of desorption according to the conventional method and the present invention.
The measurement results of gas concentration and uncondensed solvent amount are shown. FIG.
5 shows the conventional method, and FIG. 5 shows the present invention. In this figure, the amount of uncondensed solvent is obtained by multiplying the amount of gas at each time in units of 10 seconds by the solvent concentration. In other words, the comparison is equivalent to the sum of the areas of the bar graphs in the figure.
【００３１】この実施例では、水蒸気脱着前に２４６０
リットルの空気が水蒸気で置換された結果、当該装置に
おける未凝縮ガスとして吸着側に戻る溶剤絶対量は、従
来法では４．３５Kgなのに対し本発明では２．０７Kgと
なった。 因みに、実施例の場合、従来法と本発明での
発生する未凝縮ガスの溶剤量の差（４．３５Kg−２．０
７Kg＝２．２８Kg）を受け止めるＡＣＦ量を低減でき
る。ＡＣＦの塩化メチレン操作吸着率を１５％とする
と、１５．２KgのＡＣＦ量を減らす事ができる。In this embodiment, before desorption of steam, 2460
As a result of replacing one liter of air with water vapor, the absolute amount of solvent returning to the adsorption side as uncondensed gas in the apparatus was 2.07 kg in the present invention, compared with 4.35 kg in the conventional method. Incidentally, in the case of the embodiment, the difference between the solvent amount of the uncondensed gas generated in the conventional method and the present invention (4.35 kg-2.0
(7 kg = 2.28 kg) can be reduced in ACF amount. If the methylene chloride adsorption rate of ACF is 15%, the amount of ACF of 15.2 kg can be reduced.
【００３２】[0032]
【発明の効果】（１）本発明により、溶剤回収装置の装
置内を循環する未凝縮ガス中の溶剤絶対量を３０〜５０
％低減できる。この未凝縮ガスの減少によって、ＡＣＦ
吸着素子への負荷を軽減し、吸着素子の稼働効率を高
め、結果的にＡＣＦ充填量の低減につなげることができ
る。 （２）ＡＣＦ原料に伴い脱着に使用する水蒸気量も低減
できる。 （３）処理風量の大きい装置ほど缶内のガスの流れ空間
を確保せねばならなく、缶が大きくなり、図１のアの空
間部はＡＣＦ吸着素子が多くなるほど、本発明は、より
大きくなり効果は増加する。(1) According to the present invention, the absolute amount of the solvent in the uncondensed gas circulating in the solvent recovery device is reduced to 30 to 50.
%. This reduction in uncondensed gas results in ACF
It is possible to reduce the load on the adsorption element, increase the operation efficiency of the adsorption element, and consequently reduce the ACF filling amount. (2) The amount of steam used for desorption can be reduced with the ACF raw material. (3) process air volume of large apparatus as without Senebanara ensure the flow space of the gas in the can, the can is increased, the space portion of the A 1 The more ACF adsorption element, the present invention will become greater The effect increases.
【００３３】[0033]
図１ 本発明のフロー図 図２ 図１の缶の断面図 図３ 実施例での未凝縮ガスの流量及び濃度測定個所 図４ 従来方法で発生する未凝縮ガスの流量，濃度及び
溶剤量 図５ 本発明で発生する未凝縮ガスの流量，濃度及び溶
剤量Fig. 1 Flow diagram of the present invention Fig. 2 Cross-sectional view of the can of Fig. 1 Fig. 3 Measurement location of flow rate and concentration of uncondensed gas in the embodiment Fig. 4 Flow rate, concentration and solvent amount of uncondensed gas generated by conventional method Fig. 5 Flow rate, concentration and solvent amount of uncondensed gas generated in the present invention
１．缶 １' 吸着工程中の缶 ２．ＡＣＦ吸着素子 ２' 吸着工程中のＡＣＦ吸着素
子 ３．凝縮器 ４．脱着蒸気（弁） ５．置換用水蒸気（弁） ６．出口蒸気（弁） ７．送風機 ８．清浄空気取出口（弁） ９．脱着用水蒸気供給ノズル、 １０．被処理ガス供給口（弁）である。 １１．水蒸気 １２ 被処理ガス（原ガス） １３．清浄空気 １４．凝縮液1. 1. Can 1 'Can during adsorption process. 2. ACF adsorption element 2 'ACF adsorption element during adsorption step Condenser 4. 4. Desorption steam (valve) 5. Steam for replacement (valve) 6. Outlet steam (valve) 7. Blower 8. Clean air outlet (valve) 9. Desorption steam supply nozzle, This is the gas supply port (valve) to be processed. 11. Water vapor 12 Gas to be treated (raw gas) 13. Clean air 14. Condensate
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ Ｂ０１Ｊ 20/34 (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 53/44 B01D 53/04 B01D 53/34 B01D 53/81 ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 7 identification code FI B01J 20/34 (58) Investigated field (Int.Cl. 7 , DB name) B01D 53/44 B01D 53/04 B01D 53/34 B01D 53/81
Claims (5)
有機溶剤回収装置を用いて、被処理ガスに含まれる有機
溶剤を吸着する吸着工程、該吸着素子に吸着された有機
溶剤を水蒸気で脱着する脱着工程、及び脱着された有機
溶剤を回収する回収工程を含む有機溶剤回収方法におい
て、 該脱着工程に先立ち、水蒸気を該有機溶剤回収装置に導
入して、該吸着素子に吸着された有機溶剤を脱着するこ
となく、有機溶剤回収装置に残存する未処理ガスを水蒸
気で置換して排出することを特徴とする有機溶剤回収方
法。 1. An activated carbon fiber layer as an adsorption element.
The organic solvent contained in the gas to be treated is
An adsorption step of adsorbing the solvent, the organic adsorbed by the adsorption element
Desorption step of desorbing solvent with water vapor, and desorbed organic
Organic solvent recovery method including a recovery step to recover the solvent
Prior to the desorption step, water vapor is introduced into the organic solvent recovery device.
To remove the organic solvent adsorbed on the adsorption element.
Untreated gas remaining in the organic solvent recovery unit
Organic solvent recovery method characterized by replacement with air and discharging
Law.
吸着素子に吸着された有機溶剤を脱着することなく、有
機溶剤回収装置に残存する未処理ガスを水蒸気で置換し
て排出する前記方法は、 該有機溶剤回収装置内において、該活性炭素繊維層を未
通過の被処理ガスが未処理ガスとして残存している空間
部に、直接、水蒸気を導入して行うことを特徴とする請
求項１記載の有機溶剤回収方法。 2. Introducing steam into an organic solvent recovery device,
Without desorbing the organic solvent adsorbed on the adsorption element,
Replace the untreated gas remaining in the solvent recovery unit with steam.
The above method of discharging the activated carbon fiber layer in the organic solvent recovery device
Space in which the gas to be processed remains as unprocessed gas
The contract is characterized by the introduction of steam directly into the
The method for recovering an organic solvent according to claim 1.
ガスを、吸着工程に戻すことを特徴とする請求項１又は
２記載の有機溶剤回収方法。 3. The untreated exhaust gas which has been replaced by steam and discharged.
2. The method according to claim 1, wherein the gas is returned to the adsorption step.
3. The method for recovering an organic solvent according to 2.
を内部に有し、導入された被処理ガス中の有機溶剤を吸
着素子で吸着し、導入された水蒸気により吸着素子に吸
着されている有機溶剤を脱着し回収することができる有
機溶剤回収装置において、該吸着素子により有機溶剤回
収装置の内部は２つの空間が形成され、一方の空間を形
成する部分に、被処理ガスを供給するための被処理ガス
供給口及び未処理ガスを水蒸気で置換するための水蒸気
供給口を設けたことを特徴とする有機溶剤回収装置。 4. An adsorption element having a cylindrical activated carbon fiber layer.
Inside to absorb the organic solvent in the introduced gas to be treated.
Adsorbed by the adsorption element and absorbed by the adsorbed element by the introduced water vapor.
Organic solvent attached can be desorbed and recovered
In the solvent recovery device, the organic solvent is recovered by the adsorption element.
Two spaces are formed inside the collecting device, and one space is formed.
The gas to be treated for supplying the gas to be treated
Steam for replacing feed ports and untreated gas with steam
An organic solvent recovery device having a supply port.
着するための水蒸気を導入することができる脱着用水蒸
気供給口が、円筒状吸着素子の内部に直接通ずるように
設けられている請求項４記載の有機溶剤回収装置。 5. An organic solvent adsorbed on an adsorption element is removed.
Dewatering steam that can introduce water vapor to wear
So that the air supply port directly communicates with the inside of the cylindrical adsorption element.
The organic solvent recovery device according to claim 4, which is provided.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6317649A JP3069578B2 (en) | 1994-11-28 | 1994-11-28 | Solvent recovery method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6317649A JP3069578B2 (en) | 1994-11-28 | 1994-11-28 | Solvent recovery method and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08150319A JPH08150319A (en) | 1996-06-11 |
| JP3069578B2 true JP3069578B2 (en) | 2000-07-24 |
Family
ID=18090504
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6317649A Expired - Lifetime JP3069578B2 (en) | 1994-11-28 | 1994-11-28 | Solvent recovery method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3069578B2 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4596110B2 (en) * | 2001-07-19 | 2010-12-08 | 東洋紡績株式会社 | Gas processing apparatus and gas processing method |
| JP2003071235A (en) * | 2001-08-30 | 2003-03-11 | Sumitomo Chem Co Ltd | Method for separating flammable organic solvent in gas to be treated |
| JP2007519520A (en) | 2004-01-27 | 2007-07-19 | ピュリフィツス エンヴイロンメンタル テクノロジーズ インコーポレーテッド | Advanced pollutant treatment system |
| JP5106198B2 (en) * | 2008-03-25 | 2012-12-26 | 千代田化工建設株式会社 | Method for removing methyl iodide from methanol-containing gas |
| JP6229267B2 (en) * | 2013-01-29 | 2017-11-15 | 東洋紡株式会社 | Gas processing apparatus and gas processing method |
| CN103691254A (en) * | 2013-12-10 | 2014-04-02 | 武汉旭日华科技发展有限公司 | Method for reducing energy consumption of wet-process organic solvent recovering device |
| CN105854512A (en) * | 2016-06-13 | 2016-08-17 | 何莉 | Activated carbon fiber adsorption device |
| CN110898609B (en) * | 2019-05-15 | 2024-09-10 | 上海摩萃蒂环保科技有限公司 | Active carbon adsorption purifier of desorption regeneration |
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1994
- 1994-11-28 JP JP6317649A patent/JP3069578B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH08150319A (en) | 1996-06-11 |
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