JPS6359331A - System recovering vapor of solvent - Google Patents
System recovering vapor of solventInfo
- Publication number
- JPS6359331A JPS6359331A JP61203434A JP20343486A JPS6359331A JP S6359331 A JPS6359331 A JP S6359331A JP 61203434 A JP61203434 A JP 61203434A JP 20343486 A JP20343486 A JP 20343486A JP S6359331 A JPS6359331 A JP S6359331A
- Authority
- JP
- Japan
- Prior art keywords
- activated carbon
- adsorption tower
- gas
- refrigerant
- valve
- 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 description 34
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 152
- 238000001179 sorption measurement Methods 0.000 claims abstract description 50
- 239000003507 refrigerant Substances 0.000 claims abstract description 26
- 238000003795 desorption Methods 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims description 13
- 239000000463 material Substances 0.000 abstract description 6
- 239000000498 cooling water Substances 0.000 abstract description 5
- 230000001172 regenerating effect Effects 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 11
- 238000004140 cleaning Methods 0.000 description 9
- 239000011232 storage material Substances 0.000 description 6
- AJDIZQLSFPQPEY-UHFFFAOYSA-N 1,1,2-Trichlorotrifluoroethane Chemical compound FC(F)(Cl)C(F)(Cl)Cl AJDIZQLSFPQPEY-UHFFFAOYSA-N 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
【発明の詳細な説明】
皮粟上ｍ１里分黙
本発明は、溶剤蒸気回収装置に係り、特に、蓄冷器と活
性炭吸着塔を組み合わせた溶剤蒸気回収装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a solvent vapor recovery device, and more particularly to a solvent vapor recovery device that combines a regenerator and an activated carbon adsorption tower.
従来少及火
従来、この種の装置では、前段に蓄冷器、後段に活性炭
吸着塔を配し、それぞれを別個の装置として運転してい
る。即ち、前段の蓄冷器では、ガス中の溶剤蒸気が蓄冷
器内の蓄冷材表面温度まで冷却され、溶剤蒸気は、その
温度での平衡濃度まで凝縮する。しかし、その平衡濃度
の分は、ガス中に残存したまま活性炭吸着塔に送られる
。残存する溶剤蒸気は、活性炭に吸着され、はとんど除
去される。蓄冷器を出たガスの温度は低いが、吸着時の
発熱のため、活性炭吸着塔の温度は、はとんど変化しな
い。従って、活性炭による溶剤の吸着特性は、常温での
吸着等混線に支配される。溶剤の吸着が進むと、活性炭
は飽和に達し、活性炭の吸着能力は低下し、再生が必要
となる。Conventionally, this kind of equipment has a regenerator in the front stage and an activated carbon adsorption tower in the latter stage, and each is operated as a separate device. That is, in the pre-stage regenerator, the solvent vapor in the gas is cooled to the surface temperature of the regenerator material in the regenerator, and the solvent vapor is condensed to the equilibrium concentration at that temperature. However, the equilibrium concentration remains in the gas and is sent to the activated carbon adsorption tower. The remaining solvent vapor is adsorbed onto the activated carbon and is mostly removed. Although the temperature of the gas leaving the regenerator is low, the temperature of the activated carbon adsorption tower hardly changes due to heat generation during adsorption. Therefore, the adsorption characteristics of a solvent by activated carbon are dominated by adsorption and crosstalk at room temperature. As the adsorption of solvent progresses, the activated carbon reaches saturation, the adsorption capacity of the activated carbon decreases, and regeneration is required.
従来技術による活性炭の再生は、スチームを用いる加熱
脱着操作によって行われる。即ち、活性炭が加熱される
と、吸着されていた溶剤は、ガス中の溶剤蒸気の濃度と
活性炭の吸着量がその温度における平衡関係を保ちなが
ら脱着される。充分に脱着が行われると、活性炭は再生
される。脱着された溶剤蒸気は、スチームとの混合ガス
となっているが、コンデンサで冷却水により冷却され、
凝縮して溶剤となる。溶剤とスチームが凝縮して生じた
水は、重力分離器で分離され、溶剤は回収される。一方
、水はドレン水として排出される。Regeneration of activated carbon according to the prior art is carried out by thermal desorption operations using steam. That is, when the activated carbon is heated, the adsorbed solvent is desorbed while maintaining an equilibrium relationship between the concentration of solvent vapor in the gas and the amount of adsorption on the activated carbon at that temperature. When sufficient desorption occurs, the activated carbon is regenerated. The desorbed solvent vapor becomes a mixed gas with steam, but it is cooled by cooling water in a condenser.
It condenses to become a solvent. The water resulting from condensation of the solvent and steam is separated in a gravity separator and the solvent is recovered. On the other hand, water is discharged as drain water.
■が”°しよ゛と るう 占
しかし、前記の従来技術では、洗浄等で用いるフロン１
１３等のような溶剤の場合、活性炭の脱着時に１２０℃
程度まで加熱する必要があり、スチームを大量に使用す
ること及び脱着ガスの凝縮において含まれるスチームの
潜熱が大きく冷却水を大量に使用すること等の欠点が有
ある。However, in the above-mentioned conventional technology, the Freon 1 used for cleaning etc.
In the case of a solvent such as No. 13, the temperature is 120°C during desorption of activated carbon.
However, there are drawbacks such as the need to heat the desorbed gas to a certain extent, the use of a large amount of steam, and the large latent heat of the steam contained in the condensation of the desorbed gas, which requires the use of a large amount of cooling water.
従って、本発明は、前記の従来技術の欠点を解消し、多
量のスチーム及び冷却水を使用しない、蓄冷器及び活性
炭吸着塔を組み合わせた溶剤蒸気回収装置を提供するこ
とを目的とする。SUMMARY OF THE INVENTION Accordingly, it is an object of the present invention to overcome the drawbacks of the prior art described above and to provide a solvent vapor recovery apparatus that combines a regenerator and an activated carbon adsorption tower without using a large amount of steam or cooling water.
。 占 ”° るための −
本発明は、溶剤蒸気を活性炭に吸着させて回収する場合
、吸着時の温度を低くすれば、加熱による脱着温度を相
対的に低くしても、脱着性能は大きくは低下しないこと
に着目してなされたものである。そして、吸着温度を低
くする手段として、蓄冷器による対象ガスの冷却及び活
性炭吸着塔内に設置した伝熱管による冷却を用い、コン
プレッサで加圧した冷媒をコンデンサで凝縮して蓄冷器
及び活性炭吸着塔に供給し、コンプレッサで加圧した冷
媒のホットガスを活性炭吸着塔に直接供給して加熱でき
るようにすることによって前記の問題点を解決したもの
である。これらの配管は、吸着時、脱着時及び蓄冷時の
操作別にバルブ操作により連結するようにした。. The present invention provides that when solvent vapor is adsorbed onto activated carbon and recovered, if the adsorption temperature is lowered, even if the desorption temperature by heating is relatively lowered, the desorption performance will not be significantly improved. This was done with the aim of lowering the adsorption temperature by cooling the target gas with a regenerator and cooling with a heat exchanger tube installed in an activated carbon adsorption tower, and by pressurizing it with a compressor. The above problem is solved by condensing the refrigerant in a condenser and supplying it to the regenerator and activated carbon adsorption tower, and then supplying the hot gas of the refrigerant pressurized by the compressor directly to the activated carbon adsorption tower for heating. These pipes were connected by valve operations for each operation during adsorption, desorption, and cold storage.
すなわち、本発明による溶剤蒸気回収装置は、伝熱管を
有する蓄冷器と内部に伝熱管を設けた活性炭吸着塔が配
管により連結され、蓄冷器及び活性炭吸着塔の伝熱管に
は、冷媒コンプレッサからバルブを介して膨張弁及びコ
ンデンサを経て冷媒が供給され、活性炭吸着塔の伝熱管
には、更に前記コンプレッサから直接、高温の冷媒ホン
トガスを供給する配管が付設されており、更に、活性炭
吸着塔からの流出配管と蓄冷器への流入配管とが、脱着
ガス循環配管によって連結されていることを特徴とする
。That is, in the solvent vapor recovery apparatus according to the present invention, a regenerator having a heat transfer tube and an activated carbon adsorption tower provided with a heat transfer tube inside are connected by piping, and a valve is connected to the heat transfer tube of the regenerator and the activated carbon adsorption tower from a refrigerant compressor. The refrigerant is supplied through the expansion valve and the condenser, and the heat transfer tube of the activated carbon adsorption tower is further equipped with piping that supplies high-temperature refrigerant real gas directly from the compressor. The outflow pipe and the inflow pipe to the regenerator are connected by a desorption gas circulation pipe.
詐ｌ−
活性炭吸着塔内に設けた活性炭用伝熱管は、吸着時には
、活性炭を冷媒によって冷却して吸着温度を低下する。False - During adsorption, the activated carbon heat transfer tube provided in the activated carbon adsorption tower cools the activated carbon with a refrigerant to lower the adsorption temperature.
吸着が低い温度で行われることにより、加熱による脱着
も低い温度で可能になる。Since adsorption is performed at low temperatures, thermal desorption is also possible at low temperatures.
コンプレッサで加圧した冷媒をコンデンサで凝縮して蓄
冷器及び活性炭吸着塔内の伝熱管に供給することによっ
て蓄冷材及び活性炭の冷却を行い、その冷媒のホットガ
スによって活性炭の加熱脱着を行う。The refrigerant pressurized by the compressor is condensed by the condenser and supplied to the heat transfer tubes in the regenerator and activated carbon adsorption tower to cool the regenerator material and activated carbon, and the activated carbon is thermally desorbed by the hot gas of the refrigerant.
実施貫 次に、図面に基づいて本発明の詳細な説明する。implementation Next, the present invention will be explained in detail based on the drawings.
第１図は、本発明による溶剤蒸気回収装置の１実施例を
示すフローシートである。FIG. 1 is a flow sheet showing one embodiment of the solvent vapor recovery apparatus according to the present invention.
第１図に示した装置は、フロン１１３を溶剤として用い
た洗浄装置から排出される排ガス中の溶剤蒸気を回収す
るため設置されたものであり、活性炭吸着塔１、蓄冷器
２、コンプレフサ３、コンデンサ４、ファン５、溶剤回
収槽６及びこれらを連結する配管系から構成されている
。The device shown in FIG. 1 was installed to recover solvent vapor in exhaust gas discharged from a cleaning device using Freon 113 as a solvent, and includes an activated carbon adsorption tower 1, a regenerator 2, a compressor 3, It consists of a condenser 4, a fan 5, a solvent recovery tank 6, and a piping system connecting these.
洗浄装置２１は、バルブ１１、ファン５及び流入配管２
２を介して蓄冷器２と連結され、この蓄冷器２は配管２
３により活性炭吸着塔１と連結され、バルブ１２を経て
外気と連通されている。更に、活性炭吸着塔１とバルブ
１２との間で脱着ガス循環配管２４が分岐し、ファン２
０及びバルブ１７を介して蓄冷器２への流入配管２２と
連結されている。The cleaning device 21 includes a valve 11, a fan 5, and an inflow pipe 2.
The regenerator 2 is connected to the regenerator 2 via the pipe 2.
3 is connected to the activated carbon adsorption tower 1, and communicated with the outside air via a valve 12. Further, a desorption gas circulation pipe 24 branches between the activated carbon adsorption tower 1 and the valve 12, and a fan 2
0 and an inflow pipe 22 to the regenerator 2 via a valve 17.
活性炭吸着塔１の内部には、活性炭用伝熱管７が設置さ
れており、その伝熱管７の間に活性炭８が充填されてい
る。また、蓄冷器２の内部にも、蓄冷材用伝熱管９が設
置されており、その伝熱管９の間に蓄冷材１０が充填さ
れている。Heat exchanger tubes 7 for activated carbon are installed inside the activated carbon adsorption tower 1, and activated carbon 8 is filled between the heat exchanger tubes 7. Moreover, heat exchanger tubes 9 for regenerator material are also installed inside the regenerator 2, and a regenerator material 10 is filled between the heat exchanger tubes 9.
活性炭用伝熱管７に対しては、コンプレッサ３からバル
ブ１３、コンデンサ４、バルブ１９及びバルブ１４を経
て冷媒が供給されるようになっており、また、活性炭吸
着塔の再生サイクルでは、コンプレッサ３からバルブ１
６を経てホットガスを供給できるようになっている。Refrigerant is supplied from the compressor 3 to the activated carbon heat exchanger tube 7 via a valve 13, a condenser 4, a valve 19, and a valve 14. In addition, in the regeneration cycle of the activated carbon adsorption tower, refrigerant is supplied from the compressor 3 through a valve 13, a condenser 4, a valve 19, and a valve 14. Valve 1
6, hot gas can be supplied.
一方、蓄冷材用伝熱管９に対しては、バルブ１４と１９
との間で、冷媒用配管を分岐させた分岐配管からバルブ
１５を経て冷媒が供給される。On the other hand, for the heat exchanger tube 9 for cold storage material, the valves 14 and 19
A refrigerant is supplied through a valve 15 from a branch pipe that is a branched refrigerant pipe.
活性炭用伝熱管７及び蓄冷材用伝熱管９中の冷媒及び／
又はホー／ トガスは、コンプレッサ３の吸引側に戻さ
れる。The refrigerant in the heat exchanger tube 7 for activated carbon and the heat exchanger tube 9 for cold storage material and/or
Alternatively, the hot/gas is returned to the suction side of the compressor 3.
次に、第１図に示した装置の動作について述べる。洗浄
装置２１では、被洗物の洗浄は、投入、スプレー、乾燥
及び取り出しの工程で行われるが、スプレーの工程では
、溶剤のフロン１１３が気化するため、洗浄装置２１の
内圧が上昇する。この際、内圧の上界を抑えるため、圧
力制御装置１８が作動し、バルブ１１が開くと共にファ
ン５が起動し、洗浄装置２１内のフロン１１３の蒸気を
２０〜３０容量％含むガスは、流入配管２２からまず蓄
冷器２に送られる。Next, the operation of the apparatus shown in FIG. 1 will be described. In the cleaning device 21, cleaning of the object to be washed is performed in the steps of loading, spraying, drying, and taking out. In the spraying step, the solvent Freon 113 is vaporized, so that the internal pressure of the cleaning device 21 increases. At this time, in order to suppress the upper limit of the internal pressure, the pressure control device 18 is activated, the valve 11 is opened, and the fan 5 is activated, and the gas containing 20 to 30% by volume of Freon 113 vapor in the cleaning device 21 is inflowed. It is first sent to the regenerator 2 from the pipe 22.
蓄冷器２内の蓄冷材１０は、コンプレッサ３からバルブ
１３、コンデンサ４、膨張弁１９及びバルブ１５を経て
蓄冷材用伝熱管９に供給された低温の冷媒によって一２
０℃に冷却される。従って、蓄冷器２内でガスは冷却さ
れ、ガス中に含まれるフロンは、そのガス濃度が約５容
量％となるまで凝縮される。凝縮されたフロンは、溶剤
回収槽６へ導入され、貯蔵される。The cold storage material 10 in the cold storage device 2 is cooled by the low-temperature refrigerant supplied from the compressor 3 to the cold storage material heat transfer tube 9 via the valve 13, the condenser 4, the expansion valve 19, and the valve 15.
Cooled to 0°C. Therefore, the gas is cooled in the regenerator 2, and the fluorocarbon contained in the gas is condensed until the gas concentration becomes about 5% by volume. The condensed fluorocarbon is introduced into the solvent recovery tank 6 and stored.
更に、蓄冷器２内のガスは、配管２３により活性炭吸着
塔１へ供給される。活性炭吸着塔１内の活性炭８は、コ
ンプレフサ３からバルブ１３、コンデンサ４、膨張弁１
９及びバルブ１４を経て活性炭用伝熱管７に供給された
低温の冷媒によって一２０℃に冷却されている。ここで
、ガス中のフロン１１３の蒸気は一２０℃の活性炭８と
接触し、活性炭８の細孔に吸着される。この時の活性炭
のフロン吸着量は、温度とガス中のフロンガス濃度によ
って支配され、第２図に示すような吸着等混線に従う。Furthermore, the gas in the regenerator 2 is supplied to the activated carbon adsorption tower 1 through a pipe 23. The activated carbon 8 in the activated carbon adsorption tower 1 is transported from the compressor 3 to the valve 13, the condenser 4, and the expansion valve 1.
It is cooled to -20° C. by a low-temperature refrigerant supplied to the activated carbon heat exchanger tube 7 through the tube 9 and the valve 14. Here, the vapor of the freon 113 in the gas comes into contact with the activated carbon 8 at -20° C., and is adsorbed into the pores of the activated carbon 8. At this time, the amount of fluorocarbon adsorbed by the activated carbon is controlled by the temperature and the concentration of fluorocarbon gas in the gas, and follows the adsorption equicross line as shown in FIG.
すなわち、−２０℃では、２０℃の常温の場合に比べて
同一のガス濃度での平衡な活性炭フロン吸着量は高（な
っており、多くのフロンを吸着することができる。活性
炭吸着塔１でフロンを吸着除去されたガスは、バルブ１
２を経て外気へ放出される。That is, at -20°C, the equilibrium amount of CFCs adsorbed by activated carbon is higher at the same gas concentration than at room temperature of 20C, and more CFCs can be adsorbed. The gas from which the fluorocarbons have been adsorbed and removed is transferred to valve 1.
2 and then released to the outside air.
このような動作により洗浄時に発生するフロン蒸気は、
活性炭吸着塔１に回収される。しかし、洗浄の回数が多
くなり、活性炭のフロン吸着量が増すと、活性炭のフロ
ン吸着能力はなくなる。従って、活性炭の脱着による再
生が必要となる。Freon vapor generated during cleaning due to this operation,
It is collected in the activated carbon adsorption tower 1. However, as the number of washings increases and the amount of fluorocarbon adsorbed by the activated carbon increases, the activated carbon loses its ability to adsorb fluorocarbons. Therefore, regeneration by desorption of activated carbon is required.
脱着の動作は、次のように行われる。The operation of attaching and detaching is performed as follows.
まず、バルブ１１及び１２が閉じられ、バルブ１７が開
放され、ファン２０は起動して、ガスは系内をゆっくり
循環する。蓄冷器２には、吸着時と同様に低温の冷媒が
供給され、蓄冷材１０は低温に維持される。一方、活性
炭吸着塔１に対してはコンプレ・ノサ３から出た冷媒が
ホットガスのままバルブ１６を経て加熱ガスとして活性
炭用伝熱管７に供給され、活性炭８を徐々に加熱し、吸
着されていたフロンを脱着する。このような操作で活性
炭８の温度は、約６０℃まで上昇し、蓄冷材１０は最も
温度の低い部分で一２０°Ｃとなる。従って、循環ガス
の活性炭吸着塔１の入口のフロンガス濃度は、蓄冷材１
０の温度−２０°Ｃでの平徐ｉ濃度約５容量％となり、
活性炭８のフロン吸着量は、第２図に示す６０℃での吸
着等温線においてガス濃度５容量％と平衡な吸着量まで
脱着される。First, valves 11 and 12 are closed, valve 17 is opened, fan 20 is started, and gas is slowly circulated through the system. A low-temperature refrigerant is supplied to the regenerator 2 as in the case of adsorption, and the regenerator material 10 is maintained at a low temperature. On the other hand, for the activated carbon adsorption tower 1, the refrigerant discharged from the compre-nosa 3 is supplied as a hot gas to the activated carbon heat transfer tube 7 through the valve 16, gradually heating the activated carbon 8 and absorbing it. Remove and install the Freon. By such an operation, the temperature of the activated carbon 8 rises to about 60°C, and the temperature of the cold storage material 10 becomes -20°C at its lowest temperature. Therefore, the fluorocarbon gas concentration at the inlet of the activated carbon adsorption tower 1 of the circulating gas is
At a temperature of 0 -20°C, the concentration of Heishu i is approximately 5% by volume,
The amount of fluorocarbon adsorbed by the activated carbon 8 is desorbed to the amount that is in equilibrium with the gas concentration of 5% by volume in the adsorption isotherm at 60° C. shown in FIG.
脱着されたフロン蒸気は、前記濃度となるまで蓄冷器２
で凝縮され、溶剤回収槽６に回収される。The desorbed fluorocarbon vapor is stored in the regenerator 2 until it reaches the above concentration.
The solvent is condensed and collected in a solvent recovery tank 6.
充分に脱着が行われたら、バルブ１６が閉鎖され、活性
炭吸着塔１へのホットガスの吸着は停止され、代わって
冷却された冷媒が供給され、活性炭８の温度は下がる。When sufficient desorption is performed, the valve 16 is closed, the adsorption of hot gas to the activated carbon adsorption tower 1 is stopped, and instead a cooled refrigerant is supplied, and the temperature of the activated carbon 8 is lowered.
活性炭８の温度が下がると、循環ガス中の残存フロン蒸
気は再び活性炭８に吸着され、ガス濃度は低下し、系外
に放出しろる）温度になった後、脱着操作は完了する。When the temperature of the activated carbon 8 decreases, the residual fluorocarbon vapor in the circulating gas is adsorbed by the activated carbon 8 again, the gas concentration decreases, and after reaching a temperature at which it can be released outside the system, the desorption operation is completed.
このようにして、洗浄装置から出るガス中の溶剤（フロ
ン）の蒸気を回収できる。In this way, the solvent (fluorocarbon) vapor in the gas exiting the cleaning device can be recovered.
光五互肱果
本発明の溶剤回収装置によれば、活性炭の再生の際に活
性炭の加熱のため、冷媒のホットガスを使用するので、
スチーム及び冷却水は全（必要なく、著しく省エネルギ
ーが達成される。According to the solvent recovery device of the present invention, hot gas as a refrigerant is used to heat the activated carbon when regenerating the activated carbon.
No steam or cooling water is required and significant energy savings are achieved.
第１図は、本発明の溶剤回収装置の一実施例を示すフロ
ーシート、第２図は、活性炭のフロンの吸着等混線図で
ある。
１・・・活性炭吸着塔、２・・・蓄冷器、３・・・コン
プレッサ、４・・・コンデンサ、６・・・溶剤回収槽、
７・・・活性炭用伝熱管、９・・・蓄冷材用伝熱管FIG. 1 is a flow sheet showing an embodiment of the solvent recovery apparatus of the present invention, and FIG. 2 is a crosstalk diagram of fluorocarbon adsorption on activated carbon. 1...Activated carbon adsorption tower, 2...Regenerator, 3...Compressor, 4...Condenser, 6...Solvent recovery tank,
7... Heat transfer tube for activated carbon, 9... Heat transfer tube for cold storage material
Claims (1)
存する溶剤を更に活性炭吸着塔で回収する溶剤蒸気回収
装置において、伝熱管を有する蓄冷器と内部に伝熱管を
設けた活性炭吸着塔が配管により連結され、蓄冷器及び
活性炭吸着塔の伝熱管には、冷媒コンプレッサからバル
ブを介して膨張弁及びコンデンサを経て冷媒が供給され
、活性炭吸着塔の伝熱管には、更に前記コンプレッサか
ら直接、高温の冷媒ホットガスを供給する配管が付設さ
れており、更に、活性炭吸着塔からの流出配管と蓄冷器
への流入配管とが、脱着ガス循環配管によって連結され
ていることを特徴とする溶剤蒸気回収装置。In a solvent vapor recovery device, the vaporized solvent is passed through a regenerator to partially condense and recovered, and the remaining solvent is further collected in an activated carbon adsorption tower. The towers are connected by piping, and the regenerator and the heat transfer tubes of the activated carbon adsorption tower are supplied with refrigerant from a refrigerant compressor via a valve via an expansion valve and a condenser, and the heat transfer tubes of the activated carbon adsorption tower are supplied with refrigerant from the compressor. A pipe is attached to directly supply high-temperature refrigerant hot gas, and the outflow pipe from the activated carbon adsorption tower and the inflow pipe to the regenerator are connected by a desorption gas circulation pipe. Solvent vapor recovery equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61203434A JPH0624606B2 (en) | 1986-08-29 | 1986-08-29 | Solvent vapor recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61203434A JPH0624606B2 (en) | 1986-08-29 | 1986-08-29 | Solvent vapor recovery device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6359331A true JPS6359331A (en) | 1988-03-15 |
| JPH0624606B2 JPH0624606B2 (en) | 1994-04-06 |
Family
ID=16474027
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61203434A Expired - Lifetime JPH0624606B2 (en) | 1986-08-29 | 1986-08-29 | Solvent vapor recovery device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0624606B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102728093A (en) * | 2012-07-05 | 2012-10-17 | 苏州龙杰特种纤维股份有限公司 | Environment-friendly gas exhaust device of vacuum furnace |
| WO2021132071A1 (en) * | 2019-12-26 | 2021-07-01 | 東洋紡株式会社 | Organic solvent recovery system |
-
1986
- 1986-08-29 JP JP61203434A patent/JPH0624606B2/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102728093A (en) * | 2012-07-05 | 2012-10-17 | 苏州龙杰特种纤维股份有限公司 | Environment-friendly gas exhaust device of vacuum furnace |
| WO2021132071A1 (en) * | 2019-12-26 | 2021-07-01 | 東洋紡株式会社 | Organic solvent recovery system |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0624606B2 (en) | 1994-04-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4197713A (en) | Process and plant for the recovery of water from humid air | |
| KR101250769B1 (en) | Hybrid air conditioning system | |
| US4336159A (en) | Method and arrangement for the thermal regeneration of charged adsorption materials | |
| JP2001317307A (en) | Method of removing carbon dioxide from exhaust gas of gas turbine plant and device for carrying out the method | |
| Szarzynski et al. | Study of different internal vapour transports for adsorption cycles with heat regeneration | |
| KR20130039185A (en) | Dry sorbent co2 capturing device with improving energy efficiency | |
| JPH10508682A (en) | Thermal compression device | |
| CN112105441B (en) | Carbon dioxide separation and recovery system and method | |
| JPH0126737B2 (en) | ||
| JPS6359331A (en) | System recovering vapor of solvent | |
| JP2005172380A (en) | Adsorption-type heat pump | |
| CN115388616B (en) | Mars surface carbon dioxide continuous capturing system adopting pressurizing liquefaction and method thereof | |
| JPH02104988A (en) | Cryopump and reclaiming process thereof | |
| JPH06272989A (en) | Refrigerator | |
| JPH0854184A (en) | Method and apparatus for drying closed-type washer | |
| JP6061462B2 (en) | Chemical heat storage device | |
| JP2590729Y2 (en) | Activated carbon solvent recovery equipment with hot air desorption | |
| JPH0639670Y2 (en) | Solvent recovery device | |
| JPH05288485A (en) | Waste heat temperature increasing and recovering device | |
| JP2997939B2 (en) | Recovery and utilization of evaporative gas in low-temperature storage tank | |
| JPS58170518A (en) | Operation of adsorbing tower | |
| JPH07228545A (en) | Dehydrating method of alcohol | |
| JPH0319934Y2 (en) | ||
| JPH08327188A (en) | Device for removing non-condensed gas of adsorption type freezer | |
| JP2004232928A (en) | Adsorption type refrigerator and method of operating the same |