JPS6324734B2 - - Google Patents
Info
- Publication number
- JPS6324734B2 JPS6324734B2 JP54023403A JP2340379A JPS6324734B2 JP S6324734 B2 JPS6324734 B2 JP S6324734B2 JP 54023403 A JP54023403 A JP 54023403A JP 2340379 A JP2340379 A JP 2340379A JP S6324734 B2 JPS6324734 B2 JP S6324734B2
- Authority
- JP
- Japan
- Prior art keywords
- adsorption
- tank
- exhaust
- solvent
- gas
- 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.)
- Expired
Links
- 238000001179 sorption measurement Methods 0.000 claims description 48
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 22
- 238000003795 desorption Methods 0.000 claims description 20
- 239000002904 solvent Substances 0.000 claims description 20
- 239000012159 carrier gas Substances 0.000 claims description 14
- 239000011261 inert gas Substances 0.000 claims description 14
- 238000011084 recovery Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- 238000000034 method Methods 0.000 description 12
- 238000001816 cooling Methods 0.000 description 9
- 238000001035 drying Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000003960 organic solvent Substances 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000006864 oxidative decomposition reaction Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000005453 ketone based solvent Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000935 solvent evaporation Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Description
【発明の詳細な説明】
本発明は活性炭吸着による改良された溶剤回収
装置に関し、更に詳しくは脱着終了後の活性炭層
の冷却と水分の除去を簡便に行なう機能を備えた
溶剤回収装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an improved solvent recovery device using activated carbon adsorption, and more particularly to a solvent recovery device that has the function of easily cooling an activated carbon layer and removing moisture after completion of desorption.
活性炭を使用して排気中の有機溶剤を回収する
方法及び装置は多数あり、特に固定層式の場合、
水蒸気脱着の後、炭層を熱風により乾燥し、更に
冷風により冷却をした後、次の吸着工程に入るの
が原則であるが、従来用いられた乾燥、冷却の設
備は送風機、空気加熱器、ダクト及び調節弁から
なるかなり大規模なものであり、時間的にも冷却
及び乾燥は20〜30分間づゝ行なわれ、乾燥の初
期、白煙と水滴の飛散を伴つていた。近年これ等
の乾燥、冷却工程を用いることは操作が煩雑にな
り、設備費がかゝる割には溶剤の回収率には殆ん
ど影響を与えないことから、乾燥・冷却工程を省
略略することが一般に行なわれている。 There are many methods and devices for recovering organic solvents in exhaust gas using activated carbon, especially for fixed bed systems.
After steam desorption, the coal seam is dried with hot air and then cooled with cold air before entering the next adsorption process. Conventionally, the drying and cooling equipment used is a blower, air heater, or duct. It was quite large-scale, consisting of a control valve and a control valve, and cooling and drying were carried out for 20 to 30 minutes at a time, and white smoke and water droplets were scattered in the early stages of drying. In recent years, the use of these drying and cooling processes has become complicated, and although the equipment costs are high, they have little effect on the recovery rate of the solvent, so the drying and cooling processes are omitted. It is commonly done.
然しながら、乾燥、冷却を省略する慣用の方法
には次の様な欠点がある。即ち高温、高湿度の炭
層に直接吸着用ガスを導入することにより、一時
に多量の水蒸気が排出され、白煙となつて立昇る
と同時に、装置周辺に凝縮した水滴をまきちら
し、又脱着打切時の吸着槽内に残留する脱着蒸気
に含まれる有機溶剤分が、通常約1vol前後の濃度
で排出され、更に、炭層が高温である間は吸着用
ガスから炭層えの吸着が行なわれず、一部素通り
で排出されてしまう。これらは時間的には極めて
短時間であるが、瞬間的に排気中の有機溶剤濃度
が上り、装置の周辺に息気ガスを撒き散らす。更
に又ケトン系溶剤及びTHF，DMFなどの如く、
活性炭の触媒作用により酸化又は分解を起し易い
溶剤の場合は、炭層の温度が高い程この酸化分解
反応速度が速く、従つて回収されるべき溶剤の損
失や好ましくない過酸化物等の混入を招く。これ
らの欠点は環境保護や安全の立場から望ましくな
いものである。 However, conventional methods that omit drying and cooling have the following drawbacks. In other words, by introducing adsorption gas directly into the high-temperature, high-humidity coal bed, a large amount of water vapor is discharged at once, rising as white smoke, and at the same time scattering condensed water droplets around the equipment, and when desorption is terminated. The organic solvent contained in the desorption vapor remaining in the adsorption tank is normally discharged at a concentration of around 1 vol. Furthermore, while the coal bed is at a high temperature, the adsorption gas is not absorbed by the coal bed, and some It will be ejected straight away. Although these events are extremely short-lived, the concentration of organic solvent in the exhaust air increases instantly, and breath gas is scattered around the equipment. Furthermore, ketone solvents, THF, DMF, etc.
In the case of solvents that are likely to undergo oxidation or decomposition due to the catalytic action of activated carbon, the higher the temperature of the carbon bed, the faster the oxidative decomposition reaction rate, which reduces the loss of solvent to be recovered and the contamination of undesirable peroxides. invite These drawbacks are undesirable from the standpoint of environmental protection and safety.
本発明は従来の装置に簡単な設備を附加するこ
とによつて、これらの欠点を一挙に解決すること
を目的としている。 The present invention aims to solve these drawbacks all at once by adding simple equipment to the conventional device.
本発明の特徴は脱着工程終了後の蒸気を含む高
温の吸着槽にキヤリヤーガスを通じつつ吸着槽内
の蒸気を凝縮冷却器を通して排気して活性炭層の
冷却と水分の除去をはかることにある。これによ
つて、吸着槽は吸着開始時の白煙や微量の溶剤及
び水滴の飛散を防止し、回収溶剤の酸化分解の抑
制、キヤリヤーガスの循環使用等を可能とし産業
上極めて有利となる。 A feature of the present invention is that a carrier gas is passed through a high-temperature adsorption tank containing steam after the desorption process is completed, and the steam in the adsorption tank is exhausted through a condensing cooler to cool the activated carbon layer and remove moisture. This prevents the adsorption tank from scattering white smoke and minute amounts of solvent and water droplets at the start of adsorption, suppresses oxidative decomposition of the recovered solvent, and allows the carrier gas to be recycled, which is extremely advantageous industrially.
次にこの本発明を図面にもとづいて説明する。
本発明に於いてキヤリヤーガスは常温の空気又は
窒素の如き不活性ガスである。図面は本発明を２
槽式の吸着装置に適用した一実施例を示すもので
ある。有機溶剤を含有した原ガスは、通常フイル
ター、ガスクーラー（図示せず）を経由してブロ
ワー１より吸着槽２或いは２′（図面は２槽吸着
の場合を示すが、２槽以上でもさしつかえない。）
から入り原ガス中の溶剤は活性炭層に吸着され、
残余の排ガスは弁３或いは３′を通つて上方に排
出される。吸着槽２が吸着工程にあるときには、
他方の吸着槽２′は脱着工程にあり、バルブ４′よ
りスチームが流入し、吸着槽２′内で活性炭層に
吸着されていた溶剤はスチームで脱着され、溶剤
とスチームの混合蒸気はバルブ５′、導管６を経
て凝縮冷却器７で凝縮し、通常凝縮液はデカンタ
ー１０で溶剤層と水層とに分離され、夫々次の工
程に送られ別途処理される。 Next, this invention will be explained based on the drawings.
In the present invention, the carrier gas is room temperature air or an inert gas such as nitrogen. The drawings illustrate the present invention.
This shows an example in which the present invention is applied to a tank-type adsorption device. The raw gas containing the organic solvent is normally passed through a filter and gas cooler (not shown) from the blower 1 to the adsorption tank 2 or 2' (the drawing shows a case of two tank adsorption, but two or more tanks may be used). .)
The solvent in the raw gas is adsorbed by the activated carbon layer,
The remaining exhaust gas is discharged upwardly through valve 3 or 3'. When the adsorption tank 2 is in the adsorption process,
The other adsorption tank 2' is in the desorption process, steam flows in from valve 4', the solvent adsorbed on the activated carbon layer in adsorption tank 2' is desorbed by the steam, and the mixed vapor of solvent and steam flows through valve 5. ', the condensate is condensed in a condensing cooler 7 through a conduit 6, and the condensate is usually separated into a solvent layer and an aqueous layer in a decanter 10, each of which is sent to the next step and treated separately.
脱着時間は通常吸着時間に比して１／２以下で
充分であるので、図面の如く２槽式で運転を行な
つた場合でも吸着槽２が、例えば60分間吸着を行
なつている間に吸着槽２′は脱着を30分間で終了
し、次の吸着に切換わる迄に約30分間の待ち時間
がある。それ故この余裕時間を利用して吸着槽
２′の冷却と乾燥を行なうことが出来る。 Since the desorption time is normally 1/2 or less of the adsorption time, it is sufficient that the adsorption time is 1/2 or less compared to the normal adsorption time. The adsorption tank 2' completes desorption in 30 minutes, and there is a waiting time of about 30 minutes before switching to the next adsorption. Therefore, this extra time can be used to cool and dry the adsorption tank 2'.
このため、本発明に於いては一般の溶剤回収装
置に設けられている凝縮冷却器７と、デカンター
１０の間にシールタンク９、遮断弁１５を配設
し、このシールタンク９に導管で排気ブロワー１
３を接続し、且つ吸着槽２，２′の上部に弁１６，
１６′を有する不活性ガス導入管１７を設けた。
キヤリヤーガスとしては一般には常温の空気が用
いられるが、回収されるべき溶剤が酸化や分解を
受け易いケトンやT.H.Fであるときは窒素等の不
活性ガスを用いることが望ましい。キヤリヤーガ
スは吸着槽内に滞留する水蒸気を搬出し温度を低
下させる媒体となるものである。排気ブロワーと
しては静圧約300mm水柱の比較的低圧風量のター
ボブロワーが利用できる。又遮断弁１５は排気ブ
ロワー１３を始動して吸着槽２，２′内の蒸気を
吸引、排気する際にデカンター１０以降の系を遮
断して、圧力の変動と溶剤の蒸発による損失を防
止する役目をもつ。さらにシールタンク９は凝縮
冷却器７で凝縮する吸引ガス中の凝縮液を貯え、
排気ブロワー１３に凝縮液が吸入されるのを防止
する役目をもつ。 For this reason, in the present invention, a seal tank 9 and a shutoff valve 15 are provided between a condensing cooler 7 and a decanter 10, which are installed in a general solvent recovery device, and a conduit is used to exhaust air into the seal tank 9. Blower 1
3 is connected, and a valve 16,
An inert gas inlet pipe 17 having a diameter of 16' was provided.
Air at room temperature is generally used as the carrier gas, but when the solvent to be recovered is a ketone or THF that is susceptible to oxidation or decomposition, it is desirable to use an inert gas such as nitrogen. The carrier gas serves as a medium that carries out the water vapor remaining in the adsorption tank and lowers the temperature. As an exhaust blower, a turbo blower with relatively low air pressure and a static pressure of about 300 mm of water column can be used. Also, the shutoff valve 15 shuts off the system after the decanter 10 when the exhaust blower 13 is started to suck in and exhaust the vapor in the adsorption tanks 2, 2', thereby preventing loss due to pressure fluctuations and solvent evaporation. have a role. Furthermore, the seal tank 9 stores the condensate in the suction gas condensed in the condensation cooler 7,
It has the role of preventing condensate from being sucked into the exhaust blower 13.
本発明の装置を説明するに、今吸着槽２は吸着
工程を開始して30分を経過し、更に30分間の吸着
工程を続行中とする。このとき他方の吸着槽２′
は脱着工程を終了し、続いて本発明の乾燥、冷却
の工程を開始する。即ち、脱着工程時に開の状態
にあつた脱着蒸気弁４′を閉ぢ、脱着蒸気排出弁
５′は開の状態のまゝとし、遮断弁１５を閉ぢ、
次いで吸着排ガス弁３′を開いて排気ブロワー１
３を始動させる。こうしてキヤリヤーガスとして
の常温の空気は吸着排ガス弁３′から吸着槽２′に
入り活性炭槽層の水分を同伴して脱着蒸気排出弁
５′から、凝縮冷却器７に達し、ここで水分を凝
縮し凝縮液をシールタンク９に分離して排気ブロ
ワー１３から排出する。この排気ブロワー１３を
出る排気は必要に応じて原ガスブロワー１の吸入
側に戻すことも出来る。この排ガス中に微量の溶
剤が含まれるときはとくに有利である。 To explain the apparatus of the present invention, it is assumed that 30 minutes have passed since the adsorption process started in the adsorption tank 2, and the adsorption process is continuing for another 30 minutes. At this time, the other adsorption tank 2'
completes the desorption process, and then begins the drying and cooling process of the present invention. That is, the desorption steam valve 4' that was open during the desorption process is closed, the desorption steam exhaust valve 5' remains open, and the cutoff valve 15 is closed.
Next, open the adsorption exhaust gas valve 3' and turn on the exhaust blower 1.
Start 3. In this way, room temperature air as a carrier gas enters the adsorption tank 2' from the adsorption exhaust gas valve 3', carries with it the moisture in the activated carbon tank layer, and reaches the condensation cooler 7 through the desorption steam discharge valve 5', where the moisture is condensed. The condensate is separated into a sealed tank 9 and discharged from an exhaust blower 13. The exhaust gas exiting the exhaust blower 13 can be returned to the suction side of the raw gas blower 1 if necessary. This is particularly advantageous if the exhaust gas contains trace amounts of solvent.
以上はキヤリヤーガスとして常温の空気を用い
る場合の説明であるが、溶剤の種類によりキヤリ
ヤーガスとして窒素の如き不活性ガスを用いる場
合には、上述の排気弁３′のかわりに不活性ガス
導入弁１６′を開いて不活性ガス導入管１７から
不活性ガスを導入して上記と同様の操作を行なう
ことが出来る。不活性ガスをキヤリヤーガスとし
て使用する場合は、排気ブロワー１３の排出ガス
を原ガスブロワー１の吸入側に導くことも出来る
が、排気ブロワー１３と不活性ガス管入管１７の
間にガスホルダー（図示せず）を設けて不活性ガ
スを貯え、循環使用することも出来る。このよう
にして本発明によれば、目的とする吸着槽の冷却
と水分の減少を容易に達成することが出来る。吸
着槽の耐圧は一般的に300〜400mm水柱の負圧に対
して安全に設計されて居り、本発明のようにキヤ
リヤーガスを導入しつつ300mm水柱程度のターボ
ブロワーで吸引排気する場合、とくに耐圧に問題
はない。又本発明の実施に於いて0.5vol％の原ガ
ス濃度でトルエンを50Kg／Ｈを処理した際に、脱
着終了後の吸着槽内の温度は約100℃で、水分含
有量は活性炭重量の40〜50％である。この脱着後
の吸着槽に原ガス量の約1/15、即ち160m3の常温
空気を20分間にわたつて通じたところ、この吸着
槽の温度は約40℃に冷却され、同時に活性炭に対
する水分含有量は30％以下に減少して、次の吸着
工程開始時の白煙発生と有機溶剤の排出は実質的
に解消された。 The above explanation is for the case where room temperature air is used as the carrier gas, but if an inert gas such as nitrogen is used as the carrier gas depending on the type of solvent, the inert gas inlet valve 16' may be used instead of the exhaust valve 3' described above. The same operation as above can be performed by opening the inert gas inlet pipe 17 and introducing an inert gas from the inert gas inlet pipe 17. When using an inert gas as a carrier gas, the exhaust gas from the exhaust blower 13 can be guided to the suction side of the raw gas blower 1. It is also possible to store inert gas and use it for circulation. In this way, according to the present invention, the desired cooling of the adsorption tank and reduction of water content can be easily achieved. The pressure resistance of an adsorption tank is generally designed to be safe against a negative pressure of 300 to 400 mm of water column, and when sucking and exhausting with a turbo blower of about 300 mm of water column while introducing a carrier gas as in the present invention, it is especially difficult to withstand pressure. No problem. Furthermore, in carrying out the present invention, when toluene is processed at 50 kg/H with a raw gas concentration of 0.5 vol%, the temperature inside the adsorption tank after desorption is approximately 100°C, and the water content is 40% of the weight of activated carbon. ~50%. When room temperature air of about 1/15 of the raw gas amount, that is, 160 m 3 , was passed through the adsorption tank after desorption for 20 minutes, the temperature of the adsorption tank was cooled to about 40°C, and at the same time the moisture content of the activated carbon was reduced. The amount was reduced to less than 30%, and the white smoke generation and organic solvent emissions at the beginning of the next adsorption step were virtually eliminated.
本発明ではキヤリヤーガスを排気ブロワー１３
で吸引するが、吸引式のかわりに押し込み式を用
いることも出来る。又吸引手段として大気脚や水
流を用いるジエツトポンプも使用可能であるが、
併し排気ブロワーによる吸引排気の方が風量調節
や排出ガスの循環使用に便利であり、又この吸引
排気式は負圧のため水の蒸発潜熱が大きいので吸
着槽の水分減少及び冷却の効率がよい。 In the present invention, the carrier gas is discharged by the exhaust blower 13.
It is possible to use a push type instead of a suction type. It is also possible to use a jet pump that uses atmospheric legs or water flow as a suction means, but
However, suction and exhaust using an exhaust blower is more convenient for adjusting the air volume and circulating exhaust gas, and this suction and exhaust type has a large latent heat of evaporation of water due to negative pressure, so it is more efficient in reducing moisture in the adsorption tank and cooling it. good.
以上のように、本発明によれば吸着装置に安価
で、構造簡単な設備を付設することによつて、吸
着槽内の冷却と水分減少が出来、従つて吸着開始
時の白煙発体、溶剤のリーク及び水滴の飛散を解
消し、又吸引フアンによりキヤリヤーガスを循環
出来るのでリークする微量の溶剤を周辺に放出す
ることもなく、又不活性ガスを経済的に利用出来
て産業上極めて有利である。 As described above, according to the present invention, by attaching inexpensive and simple-structured equipment to the adsorption device, it is possible to cool the inside of the adsorption tank and reduce water content. It eliminates solvent leaks and water droplet scattering, and since the carrier gas can be circulated using a suction fan, there is no leakage of small amounts of solvent into the surrounding area. Also, inert gas can be used economically, making it extremely advantageous industrially. be.
第１図は本発明の一実施例を示す２槽吸着式の
固定層型吸着装置である。
１……原ガス、２，２′……第１及び第２吸着
槽、３，３′……第１及び第２吸着排気弁、４，
４′……脱着蒸気弁、５，５′……脱着蒸気排出
弁、６，６′……第１及び第２吸着槽原ガス入口
弁、７……凝縮冷却器、８……導管、９……シー
ルタンク、１０……デカンター、１１……溶剤
層、１２……水層、１３……排気ブロワー、１４
……キヤリヤーガス排気導管、１５……遮断弁、
１６，１６′……第１及び第２吸着槽用不活性ガ
ス導入弁、１７……不活性ガス導入管、１８……
脱着用蒸気導管、１９……脱着蒸気導管。
FIG. 1 shows a two-tank fixed bed adsorption device showing an embodiment of the present invention. 1... Raw gas, 2, 2'... First and second adsorption tanks, 3, 3'... First and second adsorption/exhaust valves, 4,
4'... Desorption steam valve, 5, 5'... Desorption steam discharge valve, 6, 6'... First and second adsorption tank raw gas inlet valve, 7... Condensing cooler, 8... Conduit, 9 ... Seal tank, 10 ... Decanter, 11 ... Solvent layer, 12 ... Water layer, 13 ... Exhaust blower, 14
...Carrier gas exhaust pipe, 15...Shutoff valve,
16, 16'... Inert gas introduction valve for the first and second adsorption tanks, 17... Inert gas introduction pipe, 18...
Desorption steam conduit, 19... Desorption steam conduit.
Claims (1)
着し次いで水蒸気で脱着を行なう工程を交互に行
なう二槽以上からなる溶剤回収装置に於いて、凝
縮冷却器７とデカンター１０との間に、シールタ
ンク９と遮断弁１５を設けると共に該シールタン
ク９に導管を介して排気ブロワー１３を配設し、
且つ吸着槽２，２′の上部に不活性ガス導入管１
７を設け、脱着工程終了後の吸着槽内にキヤリヤ
ーガスを導入しつつ吸着槽内の蒸気を凝縮冷却器
を通して排気するように構成した溶剤回収装置。1. In a solvent recovery device consisting of two or more tanks that alternately adsorbs the solvent in the raw gas using an activated carbon fixed bed and then desorbs it with steam, there is a , a seal tank 9 and a shutoff valve 15 are provided, and an exhaust blower 13 is provided to the seal tank 9 via a conduit,
In addition, an inert gas introduction pipe 1 is installed at the top of the adsorption tanks 2 and 2'.
7, and is configured to introduce a carrier gas into the adsorption tank after the desorption step and exhaust the vapor in the adsorption tank through a condensing cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2340379A JPS55116421A (en) | 1979-03-02 | 1979-03-02 | Solvent reclaiming system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2340379A JPS55116421A (en) | 1979-03-02 | 1979-03-02 | Solvent reclaiming system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS55116421A JPS55116421A (en) | 1980-09-08 |
| JPS6324734B2 true JPS6324734B2 (en) | 1988-05-23 |
Family
ID=12109532
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2340379A Granted JPS55116421A (en) | 1979-03-02 | 1979-03-02 | Solvent reclaiming system |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS55116421A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58153503A (en) * | 1982-03-08 | 1983-09-12 | Mitsubishi Heavy Ind Ltd | Recovering method of solvent |
| JPS58156308A (en) * | 1982-03-15 | 1983-09-17 | Mitsubishi Heavy Ind Ltd | Recovery of solvent |
| JPH0634897B2 (en) * | 1986-07-11 | 1994-05-11 | 東邦化工建設株式会社 | Adsorption and desorption method with activated carbon |
| JP2003071235A (en) * | 2001-08-30 | 2003-03-11 | Sumitomo Chem Co Ltd | Method for separating combustible organic solvent in gas to be treated |
| JP5835662B2 (en) * | 2011-10-18 | 2015-12-24 | 株式会社栗本鐵工所 | Control method of volatile organic compound processing apparatus |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS51119381A (en) * | 1975-04-14 | 1976-10-19 | Mitsubishi Heavy Ind Ltd | A method for preventing initial breaking of adsorbent and recovering a dsorbility in the treatment of waste gas |
-
1979
- 1979-03-02 JP JP2340379A patent/JPS55116421A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS51119381A (en) * | 1975-04-14 | 1976-10-19 | Mitsubishi Heavy Ind Ltd | A method for preventing initial breaking of adsorbent and recovering a dsorbility in the treatment of waste gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS55116421A (en) | 1980-09-08 |
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