JPH06114229A - Exhaust gas treatment for towers and vessels - Google Patents
Exhaust gas treatment for towers and vesselsInfo
- Publication number
- JPH06114229A JPH06114229A JP28955392A JP28955392A JPH06114229A JP H06114229 A JPH06114229 A JP H06114229A JP 28955392 A JP28955392 A JP 28955392A JP 28955392 A JP28955392 A JP 28955392A JP H06114229 A JPH06114229 A JP H06114229A
- Authority
- JP
- Japan
- Prior art keywords
- inert gas
- gas
- towers
- upper space
- vessels
- 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
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は塔槽類の排ガス処理方法
に関し、揮発性有機物質を取り扱う塔槽類内上部空間の
酸素濃度を安全濃度に保持するために、当該空間を不活
性ガスでパ−ジする場合に発生する排ガスの処理に使用
するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating exhaust gas in tower tanks, and in order to maintain the oxygen concentration in the upper space in the tower tanks handling volatile organic substances at a safe concentration, the space is treated with an inert gas. It is used to treat the exhaust gas generated when purging.
【０００２】[0002]
【従来の技術】爆発性または有毒性の揮発性有機物質を
取り扱う塔槽類、例えば、貯留タンク，溶解撹拌槽，反
応槽，中継タンク，吸収塔，蒸留塔等においては、塔槽
類内上部空間の酸素濃度を爆発等に対して安全範囲内に
保持するように不活性ガスでパ−ジすることが行われて
いる。2. Description of the Related Art Tower tanks handling explosive or toxic volatile organic substances, such as storage tanks, dissolution stirring tanks, reaction tanks, relay tanks, absorption towers, distillation towers, etc. Purging with an inert gas is performed so that the oxygen concentration in the space is kept within a safe range against explosion or the like.
【０００３】この不活性ガスパ−ジにおいては、塔槽類
内上部空間での酸素濃度が上限濃度になると、ガスパ−
ジが開始され、下限濃度になるとガスパ−ジが停止さ
れ、ガスパ−ジに伴って追い出されるガスには、通常、
有機蒸気が高濃度で含有されている。従って、そのまま
大気中に放出することは、環境衛生上好ましくないばか
りか、有機物質の損失となり、不経済である。In this inert gas purge, when the oxygen concentration in the upper space in the tower tanks reaches the upper limit concentration, the gas purge
Gas is started, the gas purge is stopped when the lower limit concentration is reached, and the gas expelled along with the gas purge is usually
Contains high concentrations of organic vapors. Therefore, it is uneconomical to release it into the atmosphere as it is, not only in terms of environmental hygiene, but also as a loss of organic substances.
【０００４】かかる不利を排除するために、追い出しガ
スをそのガス中の有機物質を回収しつつ大気中に放出す
ることが知られており、その有機物質の回収に、当該有
機蒸気に対して選択透過性を有する分離膜モジュ−ルを
使用することも公知である。また、不活性ガスを回収し
て再使用することも公知である。In order to eliminate such a disadvantage, it is known that the purge gas is released into the atmosphere while recovering the organic substance in the gas, and the organic vapor is selected for the recovery of the organic substance. It is also known to use permeable separation membrane modules. It is also known to collect and reuse an inert gas.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、塔槽類
内上部空間の圧力がガスパ−ジのために変動し、分離膜
モジュ−ルの膜間差圧もこれに伴い変動する結果、分離
膜モジュ−ルの膜間差圧を所望の一定値に保持し難く、
有機物質の効率的な分離（回収）を保障し難い。However, the pressure in the upper space in the column tanks fluctuates due to the gas purge, and the transmembrane pressure difference of the separation membrane module also fluctuates accordingly, resulting in the separation membrane module. -It is difficult to maintain the transmembrane pressure difference of
It is difficult to guarantee efficient separation (recovery) of organic substances.
【０００６】尤も、ガスパ−ジを低速にすれば、塔槽類
内上部空間の圧力変動を軽度にとどめ得るが、周囲条件
の急変或は塔槽類内貯留液の出入り操作によって塔槽類
内上部空間の圧力が急峻に増加したとき、その圧力変動
にガスパ−ジが追いつかずに、塔槽類のシ−ル不良部で
の大気の出入りによる酸素濃度変動や塔槽類の機械的強
度面での安全性に失する。However, if the gas purge is slowed down, the pressure fluctuation in the upper space inside the tower tanks can be kept to a slight level, but the inside of the tower tanks may be changed due to a sudden change in ambient conditions or an operation of the stored liquid in and out of the tower tanks. When the pressure in the upper space suddenly increased, the gas purge could not catch up with the pressure fluctuation, and the oxygen concentration fluctuation due to the inflow and outflow of the atmosphere in the defective sealing part of the tower tank and the mechanical strength of the tower tank Lose in safety.
【０００７】本発明の目的は、揮発性の有機物質を取り
扱う塔槽類内上部空間を不活性ガスのパ−ジによって安
全なガス状態に保持すると共にそのガスパ−ジによって
追い出されるガスから分離膜モジュ−ルによって有機物
質を回収する場合、塔槽類内上部空間の圧力を該空間の
安全状態を保持しつつ実質上所定の一定圧力として分離
膜モジュ−ルの膜間差圧を所望の一定値に維持し、有機
蒸気の分離回収を効率よく行い得る塔槽類の排ガス処理
方法を提供することにある。The object of the present invention is to keep the upper space in the column tanks handling volatile organic substances in a safe gas state by a page of inert gas and to separate the separation membrane from the gas expelled by the gas page. In the case of recovering an organic substance by a module, the pressure in the upper space in the tower tank is kept substantially constant while maintaining the safety state of the space, and the transmembrane pressure difference of the separation membrane module is set to a desired constant value. An object of the present invention is to provide a method for treating exhaust gas in tower tanks, which can maintain the value and efficiently separate and recover organic vapor.
【０００８】[0008]
【課題を解決するための手段】本発明の塔槽類の排ガス
処理方法は、揮発性有機物質を取り扱う塔槽類内に不活
性ガスをパ−ジして当該塔槽類内上部空間での酸素濃度
を安全濃度に保持すると共に上記不活性ガスのパ−ジに
伴い追い出される有機蒸気含有不活性ガスを分離膜モジ
ュ−ルに通して有機蒸気と不活性ガスとに分離し、有機
物質を回収しつつ不活性ガスを大気に放出する方法にお
いて、上記分離した不活性ガスリッチガスの一部を塔槽
類内に還流させる配管を設け、塔槽類内上部空間圧力を
一定とするように、不活性ガスリッチガスの還流量並び
に大気放出量を調節することを特徴とする構成である。According to the method for treating exhaust gas of a tower tank of the present invention, an inert gas is purged into the tower tank that handles volatile organic substances, so that the upper space in the tower tank is treated. While keeping the oxygen concentration at a safe concentration, the organic vapor-containing inert gas expelled along with the purge of the above-mentioned inert gas is passed through the separation membrane module to separate the organic vapor and the inert gas, and In the method of releasing the inert gas to the atmosphere while recovering, a pipe for refluxing a part of the separated inert gas rich gas into the tower tanks is provided, so that the upper space pressure in the tower tanks is constant, The configuration is characterized in that the amount of recirculation of the inert gas rich gas and the amount of release into the atmosphere are adjusted.
【０００９】[0009]
【作用】不活性ガスリッチガスの還流量または大気放出
量が、塔槽類内上部空間圧力を一定とするように調節さ
れ、その結果、塔槽類内上部空間に連通された分離膜モ
ジュ−ルの高圧側圧力が一定にされ、分離膜モジュ−ル
の膜間差圧が一定に保持される。従って、膜間差圧の変
動による分離効率の低下を排除できる。The flow rate of the inert gas-rich gas or the amount released into the atmosphere is adjusted so as to keep the pressure in the upper space in the tower tanks constant, and as a result, the separation membrane module communicated with the upper space in the tower tanks. The pressure on the high pressure side is kept constant, and the transmembrane pressure difference of the separation membrane module is kept constant. Therefore, it is possible to eliminate a decrease in separation efficiency due to a change in transmembrane pressure difference.
【００１０】[0010]
【実施例】図１は本発明の実施例において使用する排ガ
スの処理装置を示している。図１において、１は揮発性
有機物質、例えばヘキサンの貯槽である。２は不活性ガ
ス供給ライン、３は不活性ガス流量制御弁、４は貯槽内
上部空間に連通された酸素濃度指示調節計であり、この
酸素濃度指示調節計４により貯槽内上部空間の酸素濃度
が検出され、その検出値で不活性ガス流量制御弁３が調
節され、不活性ガス供給量が制御されて酸素濃度が爆発
の畏れのない安全濃度に維持される。FIG. 1 shows an exhaust gas treating apparatus used in an embodiment of the present invention. In FIG. 1, reference numeral 1 is a storage tank for volatile organic substances such as hexane. 2 is an inert gas supply line, 3 is an inert gas flow control valve, 4 is an oxygen concentration indicator controller communicating with the upper space in the storage tank. Is detected, the inert gas flow rate control valve 3 is adjusted by the detected value, the amount of the inert gas supply is controlled, and the oxygen concentration is maintained at a safe concentration without explosion fear.
【００１１】５は凝縮用冷却器、５１は冷却水ラインで
あり、冷却器５の被処理ガス入口と貯槽内上部空間との
間が被処理ガス移送ライン５２によって連通されてい
る。５３は有機物質回収ラインである。６は被処理ガス
中の有機蒸気に対して選択透過性を有する分離膜モジュ
−ルである。７は分離膜モジュ−ル透過側の有機蒸気リ
ッチガスを冷却器５に還流させる透過ガス還流ライン、
７１は透過ガス還流ライン７中に設けられた真空ポンプ
である。Reference numeral 5 is a condenser for cooling, and 51 is a cooling water line. The inlet of the gas to be treated of the cooler 5 and the upper space in the storage tank are connected by a gas to be treated transfer line 52. Reference numeral 53 is an organic substance recovery line. Reference numeral 6 is a separation membrane module having selective permeability for organic vapor in the gas to be treated. 7 is a permeate gas recirculation line for recirculating the organic vapor rich gas on the permeation side of the separation membrane module to the cooler 5,
Reference numeral 71 is a vacuum pump provided in the permeated gas recirculation line 7.
【００１２】８は分離膜モジュ−ル６の非透過ガス出口
からの不活性ガスリッチガスが吸引される非透過ガス吸
引ライン、８１はブロア、９は非透過ガスの一部を貯槽
内上部空間に還流させる非透過ガス還流配管である。8 is a non-permeable gas suction line for sucking the inert gas rich gas from the non-permeable gas outlet of the separation membrane module 6, 81 is a blower, and 9 is a part of the non-permeable gas in the upper space in the storage tank. It is a non-permeable gas recirculation pipe for recirculating.
【００１３】１０は非透過ガス放出ライン、１１は放出
流量制御弁、１２は貯槽内上部空間に連通された圧力指
示調節計であり、この圧力指示調節計１２により貯槽内
上部空間の圧力が検出され、その検出値で放出流量制御
弁１１が調節され、放出量がが制御されて貯槽内上部空
間の圧力が所望の一定値に保持される。Reference numeral 10 is a non-permeate gas discharge line, 11 is a discharge flow control valve, and 12 is a pressure indicating controller communicating with the upper space inside the storage tank. The pressure indicating controller 12 detects the pressure in the upper space inside the storage tank. The discharge flow rate control valve 11 is adjusted by the detected value, the discharge amount is controlled, and the pressure in the upper space in the storage tank is maintained at a desired constant value.
【００１４】上記において、貯槽内上部空間の酸素濃度
は、有機蒸気濃度に無関係に爆発限界濃度外に設定さ
れ、通常０〜１０vol％に設定される。また、貯槽内上
部空間の圧力は、貯槽の耐久圧力値以下で、しかも任意
部分でのシ−ル不良が発生して貯槽内へ大気が多量に吸
引されて酸素濃度が上昇することが起こらないように、
通常、−１００〜＋１００mmH2Oに設定される。In the above, the oxygen concentration in the upper space of the storage tank is set outside the explosion limit concentration regardless of the organic vapor concentration, and is usually set to 0 to 10 vol%. Further, the pressure in the upper space of the storage tank is not more than the durable pressure value of the storage tank, and further, a sealing failure does not occur in any portion, so that a large amount of air is sucked into the storage tank and the oxygen concentration does not rise. like,
Usually set to -100~ + 100mmH 2 O.
【００１５】図１に示す装置により本発明を実施するに
は、酸素濃度指示調節計４により貯槽内上部空間の酸素
濃度を検出させ、その検出値が上記した設定値を越えて
いると、不活性ガス流量制御弁３の自動開通により不活
性ガスをパ−ジさせ、検出ヘキサン蒸気濃度が設定値に
回復するとパ−ジを停止させ、以後、パ−ジ開始と停止
とを繰り返えさせて貯槽内上部空間の酸素濃度を設定値
に維持させる。In order to carry out the present invention with the apparatus shown in FIG. 1, if the oxygen concentration in the upper space of the storage tank is detected by the oxygen concentration indicator controller 4 and the detected value exceeds the above-mentioned set value, it is not possible. The active gas flow control valve 3 is automatically opened to purge the inert gas, and when the detected hexane vapor concentration is restored to the set value, the purge is stopped, and thereafter the purge start and stop are repeated. Maintain the oxygen concentration in the upper space of the storage tank at the set value.
【００１６】この貯槽内上部空間への不活性ガスのパ−
ジに伴い、同空間に存在していたヘキサン蒸気含有不活
性ガスを冷却器５に押出移送させ、冷却器５の温度と圧
力で定まるヘキサン蒸気飽和濃度のもとでその移送ガス
のヘキサン蒸気を凝縮させ、その凝縮液をヘキサン回収
ライン５３で回収させる。Inert gas is supplied to the upper space of the storage tank.
With this, the hexane vapor-containing inert gas existing in the same space was extruded and transferred to the cooler 5, and the hexane vapor of the transferred gas was transferred under the saturated concentration of hexane vapor determined by the temperature and pressure of the cooler 5. It is condensed, and the condensed liquid is recovered in the hexane recovery line 53.
【００１７】一方、凝縮処理を終えたヘキサン蒸気飽和
ガスを、ブロア８１の吸引作用により分離膜モジュ−ル
６に移送させ、真空ポンプ７１による分離膜モジュ−ル
透過側の減圧下、ヘキサン蒸気に対して選択透過性を有
する分離膜モジュ−ル６の膜にヘキサン蒸気を透過濃縮
させ、この透過側のヘキサン蒸気過飽和のガスを冷却器
５に還流させて再度ヘキサン蒸気を凝縮分離させ、以
後、分離膜モジュ−ル６によるヘキサン蒸気の濃縮と冷
却器５によるヘキサン蒸気の凝縮を繰り返えさせてヘキ
サンを回収ライン５３で回収させていく。On the other hand, the hexane vapor saturated gas which has been subjected to the condensation treatment is transferred to the separation membrane module 6 by the suction action of the blower 81, and is converted into hexane vapor under the reduced pressure on the permeation side of the separation membrane module by the vacuum pump 71. On the other hand, hexane vapor is permeated and concentrated in the membrane of the separation membrane module 6 having selective permeability, and the hexane vapor supersaturated gas on the permeate side is refluxed to the cooler 5 to condense and separate the hexane vapor again. The concentration of hexane vapor by the separation membrane module 6 and the condensation of hexane vapor by the cooler 5 are repeated to recover hexane in the recovery line 53.
【００１８】また、分離膜モジュ−ル６の非透過側から
出ていく不活性ガスリッチガスにおいては、ブロア８１
による吸引下、非透過ガス放出ライン１０並びに非透過
ガス還流配管９に向かわせ、貯槽内上部空間圧力を、前
記した所定圧力（大気圧−１００〜＋１００mmH2O）と
するように圧力指示調節計１２により、不活性ガスリッ
チガスの大気への放出量を調節させる。Further, in the case of the inert gas rich gas flowing out from the non-permeation side of the separation membrane module 6, the blower 81
Under suction by directing to the non-permeable gas release line 10 and the non-permeable gas recirculation pipe 9, the pressure indicating controller so that the upper space pressure in the storage tank becomes the above-mentioned predetermined pressure (atmospheric pressure −100 to +100 mmH 2 O). 12, the amount of the inert gas rich gas released to the atmosphere is adjusted.
【００１９】即ち、圧力指示調節計１２により貯槽内上
部空間圧力を検出させ、その検出値が上記した所定圧力
を越えていると、放出流量制御弁１１の自動開閉制御に
より放出量を還流流量よりも多くさせ、検出圧力が所定
値にに回復すると放出流量制御弁１１の自動閉鎖により
不活性ガスリッチガスの大気中放出量を零にしてそのガ
スの全量を貯槽１に還流させる。That is, the pressure indicating controller 12 detects the upper space pressure in the storage tank, and when the detected value exceeds the above-mentioned predetermined pressure, the release flow rate control valve 11 automatically opens and closes the release amount from the reflux flow rate. When the detected pressure is restored to a predetermined value, the discharge flow control valve 11 is automatically closed to reduce the amount of the inert gas rich gas released into the atmosphere to zero, and the entire amount of the gas is returned to the storage tank 1.
【００２０】このように、本発明によれば、貯槽内上部
空間の圧力を所定の一定値に維持しつつ、ヘキサンを高
効率で回収できる。As described above, according to the present invention, hexane can be recovered with high efficiency while maintaining the pressure in the upper space in the storage tank at a predetermined constant value.
【００２１】このことは、次の実施例からも確認でき
る。 実施例１ 図１において、貯槽１には有効容積１００m3のヘキサン
貯留タンクを、分離膜モジュ−ル６には日東電工（株）
製分離膜モジュ−ル，NTGS−2200−S8一本（膜面積１４
m3）を，真空ポンプ７１には３．７KWル−ツ型ドライ式
を，ブロア８１には０．４KW揺動型ドライ式をそれぞれ
使用し、貯留タンク内上部空間の酸素濃度を０〜５VOL
％とするように、窒素ガスのパ−ジ量を１００〜３００
L/minの範囲で調節すると共に貯留タンク内上部空間圧
力をゲ−ジ圧５０mmH2Oとするように分離膜モジュ−ル
６の非透過側からの窒素リッチガスの大気放出量を調節
したところ、ヘキサンの回収効率を８０％以上になし得
た。This can be confirmed from the following examples. Example 1 In FIG. 1, a hexane storage tank having an effective volume of 100 m 3 is provided in the storage tank 1, and a separation membrane module 6 is provided with Nitto Denko Corporation.
Separation membrane module, NTGS-2200-S8 1 piece (membrane area 14
m 3 ), the vacuum pump 71 is a 3.7 KW roots type dry type, and the blower 81 is a 0.4 KW swing type dry type. The oxygen concentration in the upper space of the storage tank is 0 to 5 VOL.
% So that the purge amount of nitrogen gas is 100 to 300.
When the amount of nitrogen-rich gas released from the non-permeate side of the separation membrane module 6 was adjusted to the atmosphere so that the upper space pressure in the storage tank was set to a gate pressure of 50 mmH 2 O while adjusting the L / min range, The recovery efficiency of hexane could be 80% or more.
【００２２】なお、貯留タンク内上部空間のヘキサン蒸
気濃度を測定したところ、３０VOL％以上であった。ま
た、分離膜モジュ−ルの非透過側からの窒素リッチガス
の窒素ガス濃度を測定したところ、９０％以上であっ
た。The hexane vapor concentration in the upper space of the storage tank was measured and found to be 30 VOL% or more. The nitrogen gas concentration of the nitrogen-rich gas from the non-permeate side of the separation membrane module was measured and found to be 90% or more.
【００２３】実施例２ 樹脂をトルエンで溶解する場合に使用する樹脂溶解釜を
対象とし、図２に示すように、並列配設の溶解釜５台に
対し処理装置を併用した（図２において、図１と同一の
符号は、同一の構成要素を示している）。Example 2 As shown in FIG. 2, a resin melting vessel used when dissolving a resin in toluene was used in combination with five dissolving vessels arranged in parallel (in FIG. 2, The same reference numerals as those in FIG. 1 indicate the same components).
【００２４】各樹脂溶解釜１には有効容積４m3のもの
を、分離膜モジュ−ル６には日東電工（株）製分離膜モ
ジュ−ル，NTGS−2200−S4一本（膜面積３m3）を，真空
ポンプ７１には１．５KWル−ツ型ドライ式を，ブロア８
１には０．４KWル−ツ型ドライ式をそれぞれ使用し、釜
内上部空間の酸素濃度を２〜８VOL％とするように、窒
素ガスのパ−ジ量を１０〜２０L/minの範囲で調節する
と共に釜内上部空間圧力をゲ−ジ圧−１００mmH2Oとす
るように分離膜モジュ−ルの非透過側からの窒素リッチ
ガスの大気放出量を調節したところ、トルエンの回収効
率を９０％以上になし得た。Each resin dissolver 1 has an effective volume of 4 m 3 , and the separation membrane module 6 is a NTGS-2200-S4 separation membrane module manufactured by Nitto Denko Corporation (membrane area 3 m 3 ), The vacuum pump 71 is a 1.5 KW roots type dry type, and the blower 8
0.4KW Roots type dry type is used for each, and the nitrogen gas purge amount is in the range of 10 to 20 L / min so that the oxygen concentration in the upper space of the kettle is 2 to 8 VOL%. When the amount of nitrogen-rich gas released from the non-permeate side of the separation membrane module to the atmosphere was adjusted so that the pressure in the upper space inside the kettle was equal to the gauge pressure of -100 mmH 2 O, the recovery efficiency of toluene was 90%. I was able to do the above.
【００２５】なお、貯留タンク内上部空間のトルエン蒸
気濃度を測定したところ、４VOL％以上であった。ま
た、分離膜モジュ−ルの非透過側からの窒素リッチガス
の窒素ガス濃度を測定したところ、９９％以上であっ
た。The concentration of toluene vapor in the upper space of the storage tank was measured and found to be 4 VOL% or higher. The nitrogen gas concentration of the nitrogen-rich gas from the non-permeation side of the separation membrane module was measured and found to be 99% or more.
【００２６】また、上記の実施例においては、有機蒸気
に対して選択透過性を有する分離膜モジュ−ルを使用し
ているが、不活性ガスに対し選択透過性を有する分離膜
モジュ−ルを使用し、透過側ガスを大気放出ライン並び
に貯槽への還流配管側に送り、非透過側のガスを冷却器
に還流させることもできる。Further, in the above embodiment, the separation membrane module having the selective permeability to the organic vapor is used, but the separation membrane module having the selective permeability to the inert gas is used. It is also possible to use the gas on the permeate side to send it to the atmosphere release line and the reflux pipe side to the storage tank, and to recirculate the gas on the non-permeate side to the cooler.
【００２７】更に、適応対象は上記の実施例の貯槽、樹
脂溶解釜に限定されるものではなく、反応槽，中継タン
ク，吸収塔，蒸留塔等の塔槽類にも適用できる。Further, the object of application is not limited to the storage tank and the resin melting tank of the above-mentioned embodiment, but it can be applied to reaction tanks, relay tanks, absorption towers, tower towers and the like.
【００２８】[0028]
【発明の効果】本発明の塔槽類の排ガス処理方法は、揮
発性有機物質を取り扱う塔槽類内に不活性ガスをパ−ジ
して当該塔槽類内上部空間での酸素濃度を安全濃度に保
持すると共に上記不活性ガスのパ−ジに伴い追い出され
る有機蒸気含有不活性ガスを分離膜モジュ−ルに通して
有機蒸気と不活性ガスとに分離し、有機物質を回収しつ
つ不活性ガスを大気に放出する方法において、分離膜モ
ジュ−ルで分離した不活性ガスの一部を塔槽類内上部空
間に還流可能とし、その還流量とその不活性ガスの大気
中放出量とを調節して塔槽類内上部空間圧力を所定の一
定圧力に維持できるようにして、有機物質を効率よく回
収すると同時に不活性ガスの消費量を最小限に押えるこ
とが可能である。According to the method for treating exhaust gas of towers of the present invention, the oxygen concentration in the upper space of the towers is kept safe by purging an inert gas into the towers handling volatile organic substances. The organic vapor-containing inert gas, which is kept at a concentration and is expelled along with the purge of the above-mentioned inert gas, is passed through a separation membrane module to separate into an organic vapor and an inert gas, and an organic substance is recovered while being recovered. In the method of releasing active gas to the atmosphere, a part of the inert gas separated by the separation membrane module can be refluxed to the upper space in the column tanks, and the reflux amount and the amount of the inert gas released to the atmosphere. Is adjusted so that the upper space pressure in the tower tanks can be maintained at a predetermined constant pressure, so that the organic substances can be efficiently recovered and the consumption of the inert gas can be suppressed to the minimum.
【図１】本発明において使用する処理装置の一例を示す
説明図である。FIG. 1 is an explanatory diagram showing an example of a processing device used in the present invention.
【図２】本発明において使用する処理装置の別例を示す
説明図である。FIG. 2 is an explanatory diagram showing another example of the processing device used in the present invention.
１ 塔槽類 ２ 不活性ガス供給ライン ３ 不活性ガス流量制御弁 ４ 酸素濃度指示調節計 ５ 凝縮用冷却器 ５３ 有機物質回収ライン ６ 分離膜モジュ−ル ９ 非透過ガス還流配管 １０ 非透過ガス放出ライン １１ 放出流量制御弁 １２ 圧力指示調節計 1 Tower Tanks 2 Inert Gas Supply Line 3 Inert Gas Flow Control Valve 4 Oxygen Concentration Indicator Controller 5 Condensing Cooler 53 Organic Material Recovery Line 6 Separation Membrane Module 9 Non-Permeate Gas Reflux Pipe 10 Non-Permeate Gas Release Line 11 Discharge flow control valve 12 Pressure indicating controller
Claims (1)
性ガスをパージして当該塔槽類内上部空間での酸素濃度
を安全濃度に保持すると共に上記不活性ガスのパージに
伴い追い出される有機蒸気含有不活性ガスを分離膜モジ
ュールに通して有機蒸気と不活性ガスとに分離し、有機
物質を回収しつつ不活性ガスを大気に放出する方法にお
いて、上記分離した不活性ガスリッチガスの一部を塔槽
類内に還流させる配管を設け、塔槽類内上部空間圧力を
一定とするように、不活性ガスリッチガスの還流量並び
に大気放出量を調節することを特徴とする塔槽類の排ガ
ス処理方法。1. A column tank that handles volatile organic substances is purged with an inert gas to maintain a safe oxygen concentration in the upper space of the column tank, and is purged along with the purge of the inert gas. In the method of separating the organic vapor-containing inert gas passed through the separation membrane module into the organic vapor and the inert gas, and releasing the inert gas to the atmosphere while recovering the organic substance, the separated inert gas-rich gas A column tank is provided which is provided with a pipe for recirculating a part of the gas into the column tank, and the reflux amount of the inert gas rich gas and the amount released into the atmosphere are adjusted so that the upper space pressure in the column tank is constant. Exhaust gas treatment method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28955392A JP3241459B2 (en) | 1992-10-02 | 1992-10-02 | Exhaust gas treatment method for tower tanks |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28955392A JP3241459B2 (en) | 1992-10-02 | 1992-10-02 | Exhaust gas treatment method for tower tanks |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06114229A true JPH06114229A (en) | 1994-04-26 |
| JP3241459B2 JP3241459B2 (en) | 2001-12-25 |
Family
ID=17744730
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP28955392A Expired - Lifetime JP3241459B2 (en) | 1992-10-02 | 1992-10-02 | Exhaust gas treatment method for tower tanks |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3241459B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5537911A (en) * | 1992-04-27 | 1996-07-23 | Gkss-Forschungszentrum Geesthacht Gmbh | Method and device for separating gas mixtures formed above liquids |
| US5611841A (en) * | 1995-09-29 | 1997-03-18 | Membrane Technology And Research, Inc. | Vapor recovery process using baffled membrane module |
| US5985002A (en) * | 1997-03-07 | 1999-11-16 | Vapor Systems Technologies, Inc. | Fuel storage system with vent filter assembly |
| US6293996B1 (en) | 1997-03-07 | 2001-09-25 | Vapor Systems Technologies, Inc. | Fuel storage system with vent filter assembly |
| US6953496B2 (en) | 1997-03-07 | 2005-10-11 | Vapor Systems Technologies, Inc. | Sub-atmospheric fuel storage system |
-
1992
- 1992-10-02 JP JP28955392A patent/JP3241459B2/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5537911A (en) * | 1992-04-27 | 1996-07-23 | Gkss-Forschungszentrum Geesthacht Gmbh | Method and device for separating gas mixtures formed above liquids |
| US5611841A (en) * | 1995-09-29 | 1997-03-18 | Membrane Technology And Research, Inc. | Vapor recovery process using baffled membrane module |
| US5985002A (en) * | 1997-03-07 | 1999-11-16 | Vapor Systems Technologies, Inc. | Fuel storage system with vent filter assembly |
| US6293996B1 (en) | 1997-03-07 | 2001-09-25 | Vapor Systems Technologies, Inc. | Fuel storage system with vent filter assembly |
| US6953496B2 (en) | 1997-03-07 | 2005-10-11 | Vapor Systems Technologies, Inc. | Sub-atmospheric fuel storage system |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3241459B2 (en) | 2001-12-25 |
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