JPH04349920A - Solvent recovery equipment using dry air - Google Patents
Solvent recovery equipment using dry airInfo
- Publication number
- JPH04349920A JPH04349920A JP2407142A JP40714290A JPH04349920A JP H04349920 A JPH04349920 A JP H04349920A JP 2407142 A JP2407142 A JP 2407142A JP 40714290 A JP40714290 A JP 40714290A JP H04349920 A JPH04349920 A JP H04349920A
- Authority
- JP
- Japan
- Prior art keywords
- solvent
- air
- solvent recovery
- exhaust gas
- heat exchanger
- 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.)
- Granted
Links
- 239000002904 solvent Substances 0.000 title claims abstract description 88
- 238000011084 recovery Methods 0.000 title claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 50
- 230000008929 regeneration Effects 0.000 claims abstract description 13
- 238000011069 regeneration method Methods 0.000 claims abstract description 13
- 238000007791 dehumidification Methods 0.000 claims description 14
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical group CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 8
- 239000003960 organic solvent Substances 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 7
- 230000002745 absorbent Effects 0.000 claims description 5
- 239000002250 absorbent Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 abstract description 6
- 238000004880 explosion Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000013067 intermediate product Substances 0.000 description 5
- 239000012267 brine Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical group O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000011265 semifinished product Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
Landscapes
- Drying Of Gases (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
【０００１】0001
【産業上の利用分野】本発明は，蒸気圧が低く且つ吸湿
性のある有機溶媒が同伴する排ガスから該溶媒を効率良
く回収する設備に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to equipment for efficiently recovering a hygroscopic organic solvent having a low vapor pressure from exhaust gas accompanied by the solvent.
【０００２】0002
【従来の技術】各種の工業製品の製造過程において有機
溶剤の使用が不可欠の場合が多く，半製品や中間品の処
理に使用された溶剤は，産品に残存することが不必要な
場合には産品を加熱や乾燥処理して溶剤を蒸気として分
離することが行われる。この場合，蒸気圧の高い溶剤で
あれば比較的回収が容易であるが，蒸気圧が低く且つ吸
湿性の溶剤の場合には空気中の湿分を吸収する量が大き
くなり，高濃度で且つ効率良く回収することは極めて困
難である。このような溶剤の例としてＮ−メチル−２−
ピロリドンがある。このＮ−メチル−２−ピロリドンは
電池の製造工程で使用されている。この場合，電池中間
品に残存した該溶媒を除去すべく，昇温した処理炉に該
中間品を装入して溶媒を蒸気として蒸発させることが行
われる。[Prior Art] The use of organic solvents is often indispensable in the manufacturing process of various industrial products, and the solvents used in the treatment of semi-finished products and intermediate products may not remain in the products if it is unnecessary. The product is heated or dried to separate the solvent as vapor. In this case, if the solvent has a high vapor pressure, it is relatively easy to recover, but if the solvent has a low vapor pressure and is hygroscopic, it will absorb a large amount of moisture from the air, resulting in a high concentration and It is extremely difficult to recover efficiently. An example of such a solvent is N-methyl-2-
There is pyrrolidone. This N-methyl-2-pyrrolidone is used in the battery manufacturing process. In this case, in order to remove the solvent remaining in the battery intermediate product, the intermediate product is charged into a processing furnace at an elevated temperature and the solvent is evaporated as vapor.
【０００３】0003
【発明が解決しようとする課題】前記のような蒸気圧が
低く吸湿性の溶媒を中間品等から蒸発分離すべく加熱手
段を備えた処理炉を用いて生産性の面から大気雰囲気中
で大量処理する場合，この処理炉の溶媒含有排気を溶媒
が液化する温度にまで冷却して液溶媒を回収するのが最
も便宜であるが，かような冷却液化では排気中の水分も
同時に凝縮し，回収される液は水分含有量の非常に高い
ものになってしまう。このため，そのままで再使用がで
きないので蒸留等の再生操作を必要とし，再生設備に費
用が嵩む結果，溶剤回収を図る経済的メリットが削がれ
，そのまま排気するようなことも行われることがあった
。これは資源の無駄となるばかりか環境上の問題も生ず
る。本発明はこのような問題の解決を目的としたもので
ある。[Problem to be Solved by the Invention] In order to evaporate and separate the above-mentioned hygroscopic solvent with low vapor pressure from intermediate products, etc., it is necessary to use a processing furnace equipped with a heating means to evaporate and separate the hygroscopic solvent from intermediate products, etc. in large quantities in the atmosphere from the viewpoint of productivity. When processing, it is most convenient to recover the liquid solvent by cooling the solvent-containing exhaust gas of this processing furnace to a temperature at which the solvent liquefies, but in such cooling and liquefaction, the moisture in the exhaust gas also condenses, The recovered liquid has a very high water content. Therefore, since it cannot be reused as it is, regeneration operations such as distillation are required, and as a result, the cost of regeneration equipment increases, which reduces the economic merit of recovering the solvent, and sometimes exhausts it as is. there were. This not only wastes resources but also creates environmental problems. The present invention aims to solve such problems.
【０００４】0004
【課題を解決するための手段】本発明によれば，有機溶
剤の蒸気が発生する処理炉と，この処理炉にドライエア
を送気するための除湿装置と，この処理炉内の雰囲気ガ
スを強制排気するための排気ダクトと，この排気ダクト
に接続された溶剤回収装置と，この溶剤回収装置で溶剤
を分離したあとの気体を前記処理炉に送気する送気ダク
トとからなり，前記の溶剤回収装置が熱交換器と排ガス
冷却器とを備え，この排ガス冷却器で溶剤を液化すると
共に該熱交換器において排ガス冷却器を通過する前後の
気体間の熱交換を行なうようにしたドライエアを用いた
溶剤回収設備を提供する。なお，該溶剤回収装置は再熱
器および／または高性能フイルタを備えることができ，
再熱器には排ガス冷却器および熱交換器を経た気体を導
き，また高性能フイルタを経た排ガスを熱交換器および
排ガス冷却器に送るようにする。さらに，排ガス冷却器
で液化した溶剤は溶剤タンクに導入され，この溶剤タン
クに該除湿装置で除湿されたドライエアの一部を導入す
るようにする。除湿装置としては，除湿経路と再生経路
に跨がって吸湿剤含浸ロータを配置した乾式除湿器であ
って，除湿経路における該ロータの上流側に空気冷却器
を，再生経路における該ロータの上流側に空気加熱器を
配置したものを使用する。本発明設備は，溶媒として例
えばＮ−メチル−２−ピロリドンを用いる電池製造工程
での該溶媒の回収設備として好適である。[Means for Solving the Problems] According to the present invention, there is provided a processing furnace in which organic solvent vapor is generated, a dehumidification device for supplying dry air to this processing furnace, and an atmospheric gas in this processing furnace forcibly. It consists of an exhaust duct for exhausting air, a solvent recovery device connected to this exhaust duct, and an air supply duct that sends the gas after the solvent has been separated by this solvent recovery device to the processing furnace. The recovery device is equipped with a heat exchanger and an exhaust gas cooler, and the exhaust gas cooler liquefies the solvent, and the heat exchanger uses dry air that exchanges heat between the gases before and after passing through the exhaust gas cooler. Provide solvent recovery equipment. Note that the solvent recovery device can be equipped with a reheater and/or a high-performance filter,
Gas that has passed through an exhaust gas cooler and heat exchanger is led to the reheater, and exhaust gas that has passed through a high-performance filter is sent to the heat exchanger and exhaust gas cooler. Furthermore, the solvent liquefied by the exhaust gas cooler is introduced into a solvent tank, and a portion of the dry air dehumidified by the dehumidifier is introduced into this solvent tank. The dehumidifier is a dry dehumidifier in which a rotor impregnated with a moisture absorbent is placed across the dehumidification path and the regeneration path, and an air cooler is installed upstream of the rotor in the dehumidification path, and an air cooler is placed upstream of the rotor in the regeneration path. Use one with an air heater on the side. The equipment of the present invention is suitable as equipment for recovering N-methyl-2-pyrrolidone as a solvent in a battery manufacturing process, for example.
【０００５】[0005]
【実施例】図１は本発明に従う溶媒回収設備の全体を示
したものである。１は処理炉であり，溶媒を具有する産
品２がコンベアベルト３によってこの処理炉１内を連続
的に搬送される。処理炉１内は所定の温度に管理される
が，これは炉内に供給する空気温度を制御することによ
って行なうことができる。また別途加熱手段を備えても
よい。いずれにしても，使用する溶剤の種類や産品に応
じて適切な雰囲気温度に制御され，炉内の溶剤蒸気を含
有する雰囲気ガスは排気フード４を経て排気ダクト５か
ら排出される。７は強制排気を行なうための排気ファン
である。炉内から排出される空気量にほぼ見合う（或い
は漏洩を考慮して若干多い）空気が給気口８から炉内に
供給される。９はこのための給気ファンである。溶媒と
してＮ−メチル−２−ピロリドンを用いる電池製造工程
にこの処理炉１を適用する場合には，この導入空気の温
度を６０℃程度に管理する。このような有機溶剤の蒸気
が発生する処理炉１に対して，本発明設備では，排気ダ
クト５によって排出される溶媒含有排ガスから溶媒を回
収する溶媒回収装置１０と，処理炉１にドライエアを供
給するための除湿装置１１を付設する。DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 shows the entirety of a solvent recovery facility according to the present invention. Reference numeral 1 denotes a processing furnace, through which a product 2 containing a solvent is continuously conveyed by a conveyor belt 3 . The inside of the processing furnace 1 is controlled to a predetermined temperature, which can be achieved by controlling the temperature of the air supplied into the furnace. Further, a separate heating means may be provided. In any case, the ambient temperature is controlled to be appropriate depending on the type of solvent used and the product, and the ambient gas containing solvent vapor in the furnace is exhausted from the exhaust duct 5 via the exhaust hood 4. 7 is an exhaust fan for forced exhaust. Air approximately equal to the amount of air discharged from the furnace (or slightly larger in consideration of leakage) is supplied into the furnace from the air supply port 8. 9 is an air supply fan for this purpose. When this processing furnace 1 is applied to a battery manufacturing process using N-methyl-2-pyrrolidone as a solvent, the temperature of the introduced air is controlled at about 60°C. For the processing furnace 1 that generates such organic solvent vapor, the equipment of the present invention includes a solvent recovery device 10 that recovers the solvent from the solvent-containing exhaust gas discharged through the exhaust duct 5, and a dry air supply to the processing furnace 1. A dehumidifying device 11 is attached for this purpose.
【０００６】溶媒回収装置１０は，一つのケーシング１
２内に熱交換器１３と排ガス冷却器１４を収納したもの
であり，場合によっては， 高性能フイルタ１５および
再熱器１６を具備する（図例ではこの例を示す） 。排
ガス冷却器１４は溶媒含有排ガスを溶媒が凝縮するに十
分な温度に冷却するためのもので，通常のフイン付熱交
換コイルが使用されており，このコイル内には冷凍機で
製造された冷水またはブラインが通液される。その冷却
容量は通液管路に設けられた三方弁１７によって制御さ
れる。熱交換器１３は，気体間の顕熱を間接的に熱交換
する熱交換器である。この熱交換器１３は排ガス冷却器
１４を通過する前の排ガスと該冷却器１４を通過したあ
との排ガスとの間の顕熱を交換するように設置される。
図示の例では，ケーシング１内が仕切板１８によって往
路Ａと還路Ｂとに区分され，排ガス取入口１９から往路
Ａに導入された排ガスは仕切板１８の奥に設けた開口２
０を通じて還路Ｂに入り， 往路とは向流式に還路Ｂを
流れ， 取入口１９と同じ側に設けた流出口２１を経て
装置を出るようにしてあり，排ガス冷却器１４が往路Ａ
の側に設置されたうえ，この冷却器１４の上流側の往路
Ａと， 還路Ｂとに跨がって熱交換器１３が設置されて
いる。なお，還路Ａは還路Ｂの下側となるように構成さ
れ，還路Ａに存在する排ガス冷却器１４で凝縮した溶媒
液は受け器２２に集液される。また，熱交換器１３で凝
縮することもある溶媒液も受け器２２に集液される。往
路Ａでは取入口１９の近傍に高性能フイルタ１５が取付
けされ，排ガス中に同伴する塵埃をここで除去する。さ
らに還路Ｂの流出口２１の近くには再熱器１６が設置さ
れ，装置１０から流出する気体を再加熱する。この再熱
器１６は温水が通水するフイン付熱交換器または電気ヒ
ータを用いられる。[0006] The solvent recovery device 10 includes one casing 1.
2 houses a heat exchanger 13 and an exhaust gas cooler 14, and in some cases is equipped with a high-performance filter 15 and a reheater 16 (this example is shown in the figure). The exhaust gas cooler 14 is used to cool the solvent-containing exhaust gas to a temperature sufficient for condensing the solvent, and uses an ordinary heat exchange coil with fins. Or brine is passed through. Its cooling capacity is controlled by a three-way valve 17 provided in the liquid passageway. The heat exchanger 13 is a heat exchanger that indirectly exchanges sensible heat between gases. The heat exchanger 13 is installed to exchange sensible heat between the exhaust gas before passing through the exhaust gas cooler 14 and the exhaust gas after passing through the cooler 14. In the illustrated example, the inside of the casing 1 is divided into an outgoing path A and a return path B by a partition plate 18, and the exhaust gas introduced into the outgoing path A from the exhaust gas intake port 19 is passed through an opening provided at the back of the partition plate 18.
The exhaust gas cooler 14 enters return path B through 0, flows through return path B in a countercurrent manner to the outgoing path, and exits the device through an outlet 21 provided on the same side as the intake port 19.
In addition, a heat exchanger 13 is installed across the outgoing route A and the return route B on the upstream side of this cooler 14. Note that the return path A is configured to be below the return path B, and the solvent liquid condensed in the exhaust gas cooler 14 present in the return path A is collected in the receiver 22. Further, the solvent liquid that may condense in the heat exchanger 13 is also collected in the receiver 22 . On the outward path A, a high performance filter 15 is installed near the intake port 19 to remove dust entrained in the exhaust gas. Further, a reheater 16 is installed near the outlet 21 of the return path B to reheat the gas flowing out of the device 10. As the reheater 16, a finned heat exchanger or an electric heater through which hot water flows is used.
【０００７】このように構成された溶媒回収装置１０の
取入口１９には，排気口２３に通ずる排気ダクト５から
分岐する分岐ダクト２４を経て， 排気ダクト５内の溶
媒含有排ガスの一部または全部が取入れられる。この排
ガス取入れ量の制御はモータダンパ２５によって行われ
る。また溶媒回収装置１０の流出口２１からは溶媒が分
離され且つ熱交換器１３によって昇温した気体 （空気
） が取り出されるが，これは送気ダクト２６を経て後
述のドライエアと共に処理炉１に送気される。Part or all of the solvent-containing exhaust gas in the exhaust duct 5 is supplied to the intake port 19 of the solvent recovery device 10 configured as described above through a branch duct 24 branching from the exhaust duct 5 leading to the exhaust port 23. will be incorporated. This amount of exhaust gas intake is controlled by the motor damper 25. Further, from the outlet 21 of the solvent recovery device 10, the solvent is separated and gas (air) heated by the heat exchanger 13 is taken out. It bothers me.
【０００８】一方， 処理炉１に導入される新たな空気
は，除湿装置１１によって湿分が除去されドライエアが
使用される。この除湿装置１１は，一つのケーシング２
７内を仕切板２８によって除湿経路Ｃと再生経路Ｄとに
区分し， この除湿経路Ｃと再生経路Ｄに跨がって吸湿
剤含浸ロータ２９が回転可能に設置されると共に， こ
のロータ２９よりも上流側の除湿経路Ｃ内に空気冷却器
３０が，またこのロータ２９よりも上流側の再生経路Ｄ
に空気加熱器３１が配置される。３２は除湿側送風機，
３３は再生側送風機を示している。図例では除湿経路
Ｃと再生経路Ｄとは向流式に形成されている。除湿経路
Ｃの入口３４には外気が取入れられ，フイルタ３５を経
たあと空気冷却器３０で露点温度以下に冷却されて空気
中の湿分がドレンとして分離され，さらにロータ２９を
通過することによって吸湿剤に湿分が吸着されてドライ
エアとなる。そしてこのドライエアは出口３６から取り
出され， 送気路３７を経て処理路１の給気口８から炉
内に吹き出される。また，再生経路Ｄの入口３８からも
外気が取入れられ， フイルタ３９を経たあと空気加熱
器３１で加熱され， この加熱空気がロータ２９を通過
するさいに吸湿剤に吸着した湿分を奪ってこれを再生し
，湿分を同伴した排気は排気口４０から系外に排出され
る。なお，ロータ２９では除湿経路の空気から再生経路
の空気に湿分が移動するだけでなく，両空気の顕熱も熱
交換されるので，除湿経路から出るドライエアは空気冷
却器３０を通過したときの温度より昇温している。空気
加熱器３１としては蒸気または熱媒を流すフイン付熱交
換器または電気ヒータが使用される。On the other hand, fresh air introduced into the processing furnace 1 has its moisture removed by a dehumidifier 11, and dry air is used. This dehumidifier 11 includes one casing 2
7 is divided into a dehumidification path C and a regeneration path D by a partition plate 28, and a desiccant-impregnated rotor 29 is rotatably installed across the dehumidification path C and regeneration path D. There is also an air cooler 30 in the dehumidification path C upstream of the rotor 29, and a regeneration path D upstream of the rotor 29.
An air heater 31 is disposed at. 32 is a dehumidifying side blower,
33 indicates a reproduction side blower. In the illustrated example, the dehumidification path C and the regeneration path D are formed in a countercurrent manner. Outside air is taken in at the inlet 34 of the dehumidification path C, passes through a filter 35, is cooled to below the dew point temperature in the air cooler 30, and the moisture in the air is separated as drain, and further passes through the rotor 29 to absorb moisture. Moisture is absorbed by the agent and becomes dry air. This dry air is then taken out from the outlet 36, passed through the air supply path 37, and blown into the furnace from the air supply port 8 of the processing path 1. In addition, outside air is taken in from the inlet 38 of the regeneration path D, passes through a filter 39, and is then heated by the air heater 31. When this heated air passes through the rotor 29, it removes moisture adsorbed on the moisture absorbent. The exhaust gas containing moisture is discharged from the exhaust port 40 to the outside of the system. In addition, in the rotor 29, not only the moisture is transferred from the air in the dehumidification path to the air in the regeneration path, but also the sensible heat of both airs is exchanged, so when the dry air coming out of the dehumidification path passes through the air cooler 30, The temperature has risen above the temperature of As the air heater 31, a heat exchanger with fins or an electric heater through which steam or heat medium flows is used.
【０００９】空気冷却器３０は冷水またはブラインが通
液するフイン付熱交換器であり，この冷水またはブライ
ンは冷凍機ユニット４２によって製造され，ポンプ４３
によって循環供給される。なお，この冷凍機ユニット４
２に製造された冷水またはブラインは前述の溶媒回収装
置１０の排ガス冷却器１４にも共用することができる。
４４は空気冷却器３０の冷却容量を制御するための三方
弁である。The air cooler 30 is a heat exchanger with fins through which cold water or brine flows, and the cold water or brine is produced by a refrigerator unit 42 and pumped by a pump 43.
Supplied in circulation by In addition, this refrigerator unit 4
The cold water or brine produced in step 2 can also be used in the exhaust gas cooler 14 of the solvent recovery device 10 described above. 44 is a three-way valve for controlling the cooling capacity of the air cooler 30.
【００１０】溶媒回収装置１０で回収された溶媒は受け
器２２から溶媒タンク４６に導かれ，ここに蓄えられる
。そのさい，除湿器１１で製造されたドライエアの一部
が小径ダクト４７を経て溶媒タンク４６に送気され，タ
ンク内雰囲気を乾燥雰囲気として溶媒に水分が吸着する
のを防止する。The solvent recovered by the solvent recovery device 10 is led from the receiver 22 to a solvent tank 46 and stored there. At this time, a portion of the dry air produced by the dehumidifier 11 is sent to the solvent tank 46 through the small-diameter duct 47 to create a dry atmosphere in the tank and prevent moisture from adsorbing to the solvent.
【００１１】以上の構成になる本発明設備では，処理炉
１には除湿器１１で湿分が除去されたドライエアと溶媒
回収装置１０で溶媒が分離された空気が導入されるが，
後者の空気も湿分は実質的に含まず，また前者では再生
用の高温空気から顕熱をロータ２９で受取り，後者も熱
交換器１３で受熱しているので昇温されており，これら
の昇温したドライエアが処理炉１に供給されることにな
る。したがって，処理炉１内で発生した溶媒は低湿分空
気によって排気ダクト５に排出されることになり，この
排気が溶媒回収装置１０に導かれるので，溶媒回収装置
１０でも湿分の少ない溶媒が液状態で回収される。なお
，処理炉へのドライエアの送風量は，使用する溶媒の爆
発限界値を考慮して必要最小限とするように制御するの
がよい。In the equipment of the present invention having the above configuration, dry air from which moisture has been removed by the dehumidifier 11 and air from which the solvent has been separated by the solvent recovery device 10 are introduced into the processing furnace 1.
The latter air also contains virtually no moisture, and the former receives sensible heat from the high-temperature air for regeneration in the rotor 29, and the latter also receives heat in the heat exchanger 13, so its temperature is increased. The heated dry air is supplied to the processing furnace 1. Therefore, the solvent generated in the processing furnace 1 will be discharged into the exhaust duct 5 by the low-humidity air, and this exhaust gas will be led to the solvent recovery device 10, so that the solvent with low moisture will be liquefied in the solvent recovery device 10 as well. recovered in condition. Note that the amount of dry air blown into the processing furnace should be controlled to the minimum necessary, taking into account the explosion limit of the solvent used.
【００１２】0012
【発明の効果】本発明設備によれば，蒸気圧が低く吸湿
性の有機溶媒であっても，これが発生する帯域から水分
含有量の低い高濃度の溶媒液が回収できるので，水分除
去のための蒸留等の操作を経なくてもそのまま再利用で
きる。そして溶媒を回収したあとの気体（空気）も昇温
され且つ低湿分であるから，これを処理炉に再循環でき
る。これによって除湿器の負荷の低減（加熱負荷と除湿
負荷の両者の低減）ができる。さらに，空気冷却器と再
生式乾式除湿器（吸湿剤含浸ロータ）との組み合わせた
除湿器の採用によって，極低湿分で昇温したドライエア
を，外気を用いて作り出すことができ，比較的大型の処
理炉でも安価に昇温ドライエアを供給できる。また溶媒
回収装置に高性能フイルタを設置することによって，溶
媒に不純物が混入することが防止され，純度のよい溶媒
が採取できる。[Effects of the Invention] According to the equipment of the present invention, even if the organic solvent has a low vapor pressure and is hygroscopic, a highly concentrated solvent solution with a low water content can be recovered from the zone where it is generated. It can be reused as is without undergoing operations such as distillation. Since the gas (air) after recovering the solvent is also heated and has low humidity, it can be recycled to the processing furnace. This allows the load on the dehumidifier to be reduced (reduction in both heating load and dehumidification load). Furthermore, by using a dehumidifier that combines an air cooler and a regenerative dry dehumidifier (moisture absorbent impregnated rotor), dry air with extremely low humidity and elevated temperature can be created using outside air. Temperature-heated dry air can be supplied inexpensively even to processing furnaces. Furthermore, by installing a high-performance filter in the solvent recovery device, it is possible to prevent impurities from being mixed into the solvent and to collect a highly pure solvent.
【図１】本発明設備を構成する機器を略断面で示した機
器配置系統図である。FIG. 1 is an equipment layout system diagram showing, in a schematic cross-section, equipment constituting the equipment of the present invention.
１ 処理炉 ２ 溶媒含有産品 ４ 排気フード ５ 排気ダクト ７ 排気ファン ９ 給気ファン １０ 溶媒回収装置 １１ 除湿器 １３ 熱交換器 １４ 排ガス冷却器 １５ 高性能フイルタ １６ 再熱器 ２９ 吸湿剤含浸ロータ ３０ 空気冷却器 ３１ 空気加熱器 ３７ ドライエア送気ダクト ４２ 冷凍機ユニット ４６ 溶媒タンク 1 Processing furnace 2. Products containing solvents 4 Exhaust hood 5 Exhaust duct 7 Exhaust fan 9 Air supply fan 10 Solvent recovery device 11 Dehumidifier 13 Heat exchanger 14 Exhaust gas cooler 15 High performance filter 16 Reheater 29 Moisture absorbent impregnated rotor 30 Air cooler 31 Air heater 37 Dry air supply duct 42 Refrigerator unit 46 Solvent tank
Claims (6)
この処理炉にドライエアを送気するための除湿装置と，
この処理炉内の雰囲気ガスを強制排気するための排気ダ
クトと，この排気ダクトに接続された溶剤回収装置と，
この溶剤回収装置で溶剤を分離したあとの気体を前記処
理炉に送気する送気ダクトと，からなり，前記の溶剤回
収装置が熱交換器と排ガス冷却器とを備え，この排ガス
冷却器で溶剤を液化すると共に該熱交換器において排ガ
ス冷却器を通過する前後の気体間の熱交換を行なうよう
にしたドライエアを用いた溶剤回収設備。[Claim 1] A processing furnace in which organic solvent vapor is generated;
A dehumidifier for supplying dry air to this processing furnace,
An exhaust duct for forcibly exhausting the atmospheric gas in this processing furnace, a solvent recovery device connected to this exhaust duct,
an air supply duct that sends the gas after the solvent has been separated by the solvent recovery device to the processing furnace; the solvent recovery device includes a heat exchanger and an exhaust gas cooler; Solvent recovery equipment that uses dry air to liquefy the solvent and exchange heat between gases before and after passing through the exhaust gas cooler in the heat exchanger.
熱器に排ガス冷却器および熱交換器を経た気体が通過す
る請求項１に記載の溶剤回収設備。2. The solvent recovery equipment according to claim 1, wherein the solvent recovery device includes a reheater, through which the gas that has passed through the exhaust gas cooler and the heat exchanger passes.
，この高性能フイルタを経た気体が熱交換器および排ガ
ス冷却器を通過する請求項１または２に記載の溶剤回収
設備。3. The solvent recovery facility according to claim 1, wherein the solvent recovery device includes a high-performance filter, and the gas that has passed through the high-performance filter passes through a heat exchanger and an exhaust gas cooler.
ンクに導入され，この溶剤タンクに，前記の除湿装置で
除湿されたドライエアの一部が導入される請求項１，２
または３に記載の溶剤回収設備。4. The solvent liquefied by the exhaust gas cooler is introduced into a solvent tank, and a portion of the dry air dehumidified by the dehumidifier is introduced into the solvent tank.
Or the solvent recovery equipment described in 3.
がって吸湿剤含浸ロータを配置した乾式除湿器からなり
，除湿経路における該ロータの上流側に空気冷却器が配
置され，再生経路における該ロータの上流側に空気加熱
器が配置されたものである請求項１，２，３または４に
記載の溶剤回収設備。5. The dehumidification device consists of a dry dehumidifier in which a rotor impregnated with a moisture absorbent is arranged across a dehumidification path and a regeneration path, an air cooler is arranged upstream of the rotor in the dehumidification path, and 5. The solvent recovery equipment according to claim 1, wherein an air heater is arranged upstream of the rotor.
ドンである請求項１，２，３，４または５に記載の溶剤
回収設備。6. The solvent recovery equipment according to claim 1, 2, 3, 4 or 5, wherein the organic solvent is N-methyl-2-pyrrolidone.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2407142A JP2567300B2 (en) | 1990-12-10 | 1990-12-10 | Solvent recovery equipment using dry air |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2407142A JP2567300B2 (en) | 1990-12-10 | 1990-12-10 | Solvent recovery equipment using dry air |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04349920A true JPH04349920A (en) | 1992-12-04 |
| JP2567300B2 JP2567300B2 (en) | 1996-12-25 |
Family
ID=18516767
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2407142A Expired - Fee Related JP2567300B2 (en) | 1990-12-10 | 1990-12-10 | Solvent recovery equipment using dry air |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2567300B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006054408A1 (en) * | 2004-11-17 | 2006-05-26 | Sanyo Electric Co., Ltd. | Distillation apparatus for dry cleaner |
| JP2011125768A (en) * | 2009-12-15 | 2011-06-30 | Taikisha Ltd | Solvent recovery method and apparatus |
| JP2012005956A (en) * | 2010-06-24 | 2012-01-12 | Panasonic Corp | Solvent recovery apparatus |
| JP2017101913A (en) * | 2015-11-24 | 2017-06-08 | 株式会社西部技研 | Dryer |
-
1990
- 1990-12-10 JP JP2407142A patent/JP2567300B2/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006054408A1 (en) * | 2004-11-17 | 2006-05-26 | Sanyo Electric Co., Ltd. | Distillation apparatus for dry cleaner |
| KR100724322B1 (en) * | 2004-11-17 | 2007-06-04 | 산요덴키가부시키가이샤 | Distillation equipment for dry cleaner |
| JP2011125768A (en) * | 2009-12-15 | 2011-06-30 | Taikisha Ltd | Solvent recovery method and apparatus |
| JP2012005956A (en) * | 2010-06-24 | 2012-01-12 | Panasonic Corp | Solvent recovery apparatus |
| JP2017101913A (en) * | 2015-11-24 | 2017-06-08 | 株式会社西部技研 | Dryer |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2567300B2 (en) | 1996-12-25 |
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| Date | Code | Title | Description |
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| LAPS | Cancellation because of no payment of annual fees |