JPH0557151A - Selective permeation separator for organic substances - Google Patents
Selective permeation separator for organic substancesInfo
- Publication number
- JPH0557151A JPH0557151A JP22047291A JP22047291A JPH0557151A JP H0557151 A JPH0557151 A JP H0557151A JP 22047291 A JP22047291 A JP 22047291A JP 22047291 A JP22047291 A JP 22047291A JP H0557151 A JPH0557151 A JP H0557151A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- permeate
- organic
- room temperature
- organic substances
- 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.)
- Withdrawn
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
(57)【要約】
【目的】 高沸点有機物を管路を閉塞せずに透過させ補
集することができる有機物選択透過分離装置を提供す
る。
【構成】 パーベーパレーション膜を用いる有機物選択
透過分離装置において、該膜透過後の透過物管路を加熱
装置および室温冷却器を経てメカニカルブースターポン
プに導き、次いでこの管路を冷媒による冷却補集装置を
経て真空ポンプに接続する。
【効果】 膜の分離性能を向上させると共に、有機物の
高濃度透過物（室温冷却装置）と低濃度透過物（主とし
て冷却補集装置）に分離、補集して管路の閉塞を完全に
防止することができる。
(57) [Abstract] [PROBLEMS] To provide a permselective permeation device for organic substances, which is capable of permeating and collecting high-boiling organic substances without blocking the pipeline. In an organic permselective permeation separation apparatus using a pervaporation membrane, the permeate pipe line after permeating the membrane is led to a mechanical booster pump through a heating device and a room temperature cooler, and then this pipe line is cooled and collected by a refrigerant. Connect to the vacuum pump through the device. [Effect] The separation performance of the membrane is improved and the blockage of the pipeline is completely prevented by separating and collecting the high concentration permeate of organic matter (room temperature cooling device) and the low concentration permeate (mainly the cooling and collecting device). can do.
Description
【０００１】[0001]
【産業上の利用分野】本発明は特に高沸点の有機物を管
路の閉塞なしで分離することができる、改善された分離
性能を有する有機物選択透過分離装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus for selectively permeating an organic substance which has an improved separation performance and is capable of separating an organic substance having a high boiling point without blocking a pipe line.
【０００２】[0002]
【従来の技術】パーベーパレーション膜（以下、膜と略
記することがある）を用いる従来の有機物選択透過分離
装置においては、膜の一方に分離対象液を供給し、他方
側（透過側）を真空ポンプを用いて減圧とし、その圧力
差によって有機物を選択的に透過させ、透過した有機物
の蒸気を冷却、補集していた。2. Description of the Related Art In a conventional organic permselective permeation separation apparatus using a pervaporation membrane (hereinafter sometimes abbreviated as a membrane), a liquid to be separated is supplied to one side of the membrane and the other side (permeation side) is fed to the other side. The pressure was reduced using a vacuum pump, the organic substances were selectively permeated by the pressure difference, and the vapor of the permeated organic substances was cooled and collected.
【０００３】水選択透過性の膜では透過側を10Torr程度
の真空度とすれば良いが、有機物選択透過性の膜では透
過側を１Torr以下に保持する必要があった。In the case of a water selective permeable membrane, the permeation side should have a vacuum degree of about 10 Torr, but in the organic matter selective permeable membrane, the permeation side needs to be maintained at 1 Torr or less.
【０００４】[0004]
【発明が解決しようとする課題】特に高沸点の有機物の
場合には、透過側圧力を高真空に保って有機物を透過さ
せ、液体窒素等の極低温冷媒によって透過物を凝固、ト
ラップしているので透過物が透過側管路に折出して管路
を閉塞することなしで透過物をトラップすることは極め
て困難であった。本発明は高沸点有機物の場合において
も、管路を閉塞せずに透過物を補集することができる装
置を提供することを目的とする。Particularly in the case of an organic substance having a high boiling point, the permeate is coagulated and trapped by a cryogenic refrigerant such as liquid nitrogen by keeping the pressure on the permeation side high vacuum to permeate the organic substance. Therefore, it was extremely difficult to trap the permeate without the permeate protruding into the permeate-side conduit and blocking the conduit. It is an object of the present invention to provide an apparatus capable of collecting permeate without blocking a pipe line even in the case of a high boiling point organic substance.
【０００５】[0005]
【課題を解決するための手段】上記課題を解決する本発
明は、パーベーパレーション膜を用いる有機物選択透過
分離装置において、該膜透過後の透過物管路を、加熱装
置および室温冷却器を経てメカニカルブースタポンプに
導き、次いでこの管路を冷媒による冷却補集装置を経て
真空ポンプに接続することを特徴とするものである。SUMMARY OF THE INVENTION The present invention for solving the above-mentioned problems provides, in an organic substance permselective separation apparatus using a pervaporation membrane, a permeate conduit after passing through the membrane, through a heating device and a room temperature cooler. It is characterized in that it is led to a mechanical booster pump, and then this pipe is connected to a vacuum pump via a cooling and collecting device with a refrigerant.
【０００６】以下、本発明の装置を図１に示した実施例
により説明する。膜１はフランジ２, ２間にセットされ
ており、膜１の上の攪拌機付容器３に処理対象液４が供
給される。膜１の透過側（裏側）は、真空ポンプ５の駆
動によって減圧に保持される。膜１としては、有機物選
択透過性があれば、いかなる膜でも用いることができ、
たとえば選択透過性能が非常に優れているシリコーン系
膜（特開昭58-84005号）、ポリアセチレン系膜（特開昭
61-174905号および特開平1-194903号）、ポリアクリル
酸系膜およびポリエーテル系膜を挙げることができる。The apparatus of the present invention will be described below with reference to the embodiment shown in FIG. The membrane 1 is set between the flanges 2 and 2, and the liquid to be treated 4 is supplied to the container 3 with a stirrer on the membrane 1. The permeate side (back side) of the membrane 1 is kept at a reduced pressure by driving the vacuum pump 5. As the membrane 1, any membrane can be used as long as it has a permselectivity of organic matter,
For example, silicone-based membranes (JP-A-58-84005) and polyacetylene-based membranes (JP-A-58-84005), which have extremely excellent selective permeation performance.
61-174905 and JP-A 1-194903), polyacrylic acid-based films and polyether-based films.
【０００７】なお、攪拌機付容器３において16はヒータ
ーであり、17は容器３内の処理対象液４の温度制御器で
あり、18は膜１の透過側の減圧センサー、19は後述する
冷却装置11内の温度制御器である。本発明の装置におい
ては、膜透過後の透過物管路６に加熱装置７を設ける。
加熱装置７は、たとえば電熱加熱、または蒸気加熱装置
であり、その加熱温度は、透過物に含まれる有機物の種
類により決定され、有機物が固化せずに気体状である温
度を選択する。In the container 3 with a stirrer, 16 is a heater, 17 is a temperature controller for the liquid 4 to be treated in the container 3, 18 is a pressure reducing sensor on the permeate side of the membrane 1, and 19 is a cooling device described later. 11 is a temperature controller. In the device of the present invention, the heating device 7 is provided in the permeate conduit 6 after permeation through the membrane.
The heating device 7 is, for example, an electric heating device or a steam heating device, and its heating temperature is determined by the type of organic substance contained in the permeate, and the temperature at which the organic substance is in a gaseous state without solidifying is selected.
【０００８】管路６は室温冷却器８を経て、メカニカル
ブースターポンプ９に導かれる。室温冷却器８はメカニ
カルブースターポンプ９の保護機能を有すると共に、通
常は室温下において液体状の透過物を分離するが、必要
によっては管路６と同様に透過物の凝固を防止するため
に、加熱装置により加熱することもできる。メカニカル
ブースターポンプ９は透過側を高真空にするために使用
するものであり、たとえばルーツ式やスクリュー式が用
いられる。ブースターポンプ９から管路10を冷媒による
冷却補集装置11を経て真空ポンプ５に接続する。The pipe line 6 is led to a mechanical booster pump 9 via a room temperature cooler 8. The room temperature cooler 8 has a function of protecting the mechanical booster pump 9 and normally separates a liquid permeate at room temperature, but if necessary, in order to prevent coagulation of the permeate like the pipe line 6, It can also be heated by a heating device. The mechanical booster pump 9 is used to create a high vacuum on the permeate side, and for example, a roots type or a screw type is used. The pipe line 10 is connected from the booster pump 9 to the vacuum pump 5 via a cooling and collecting device 11 using a refrigerant.
【０００９】冷却装置11は特に限定されず、従来の膜を
用いる有機溶剤選択透過分離装置の透過側に用いられて
いたものを用いることができるが、高沸点有機溶媒の場
合には冷媒として10〜20℃の水を用いれば良く、トラッ
プ12および13で有機物を液化あるいは凝固させ、補集す
る。次に上記本発明の装置の機能について述べる。The cooling device 11 is not particularly limited, and the one used on the permeation side of the conventional organic solvent selective permeation separation device using a membrane can be used. It suffices to use water at -20 ° C, and the traps 12 and 13 liquefy or solidify the organic substances and collect them. Next, the function of the apparatus of the present invention will be described.
【００１０】まず、膜１として有効面積 22.04cm2 のポ
リエーテルブロックアミド（ＰＥＢＡ）をセットした。
処理対象液としてフェノールの5.92wt％水溶液を供給
し、経時的に変化するフェノールを補充して濃度変化を
極力抑え、ヒーターおよび温度制御器17によって50℃に
調整した。一方、真空ポンプ５を始動すると共に、メカ
ニカルブースターポンプ９および電磁弁20によって室温
冷却器８および冷却補集装置11を含む透過側を常に１To
rr以下に保った。室温冷却器８により液体状透過物を分
離すると共に、加熱装置７により透過物の温度を....℃
に保持し、一方、冷却装置11の冷媒には15℃の水道水を
用いて有機物を凝固させ補集した。透過物の液組成をガ
スクロマトグラフあるいは吸光光度計により測定し、膜
の透過性能を単位面積、単位時間当りの全透過量（kg/m
2h)と分離係数αにより求めた。なお、分離係数αは以
下に式により求めた。First, a polyether block amide (PEBA) having an effective area of 22.04 cm 2 was set as the membrane 1.
A 5.92 wt% aqueous solution of phenol was supplied as a solution to be treated, and phenol that changes over time was replenished to suppress the concentration change as much as possible, and the temperature was adjusted to 50 ° C by a heater and a temperature controller 17. On the other hand, the vacuum pump 5 is started, and the mechanical booster pump 9 and the solenoid valve 20 are used to constantly set the permeation side including the room temperature cooler 8 and the cooling collector 11 to 1 To.
kept below rr. The room temperature cooler 8 separates the liquid permeate, and the heating device 7 controls the temperature of the permeate ...
On the other hand, tap water at 15 ° C. was used as the refrigerant of the cooling device 11 to solidify and collect the organic matter. The liquid composition of the permeate was measured by a gas chromatograph or an absorptiometer, and the permeation performance of the membrane was determined by the total area per unit area and unit time (kg / m
2 h) and the separation factor α. The separation coefficient α was calculated by the following equation.
【００１１】 [0011]
【００１２】ここでＦph、Ｆwはそれぞれ処理対象液中
のフェノール濃度（wt％）と水分濃度（wt％）を表わ
し、Ｐph、Ｐwはそれぞれ透過液中のフェノール濃度（w
t％）と水分濃度（wt％）を表わす。結果を下記表１に
示す。Here, Fph and Fw represent the phenol concentration (wt%) and water concentration (wt%) in the liquid to be treated, and Pph and Pw represent the phenol concentration (w in the permeate).
t%) and water concentration (wt%). The results are shown in Table 1 below.
【００１３】 [0013]
【００１４】表１から明らかなとおり、液体状透過物分
離装置の性能は分離係数α＝515.6、補集量655.3g/m2h
であり、メカニカルブースターポンプと冷却補集装置お
よび真空ポンプの組合せによる分離係数α＝4.91、補集
量372.3g/m2h であった。As is clear from Table 1, the performance of the liquid permeate separation device has a separation coefficient α = 515.6 and a collection amount of 655.3 g / m 2 h.
The separation coefficient α was 4.91 and the collection amount was 372.3 g / m 2 h due to the combination of the mechanical booster pump, the cooling collector and the vacuum pump.
【００１５】[0015]
【発明の効果】本発明の装置は膜の分離性能を向上させ
ると共に、有機物の高濃度透過物（室温冷却装置）と低
濃度透過物（主として冷却補集装置）に分離、補集して
管路の閉塞を完全に防止することができ、かつ省エネル
ギーでコンパクトな装置であることが明白である。The apparatus of the present invention improves the separation performance of the membrane, and separates and collects the high-concentration permeate of organic matter (room temperature cooling device) and the low-concentration permeate (mainly the cooling and collecting device) for pipes. It is obvious that the device can completely prevent the blockage of the road and is energy-saving and compact.
【図１】本発明装置の実施例を示す概要図である。FIG. 1 is a schematic view showing an embodiment of the device of the present invention.
１ パーベーパレーション膜 ４ 処理対象液 ７ 加熱装置 ８ 室温冷却器 ９ メカニカルブースターポンプ 11 冷媒による
冷却補集装置1 Pervaporation film 4 Liquid to be treated 7 Heating device 8 Room temperature cooler 9 Mechanical booster pump 11 Cooling and collecting device by refrigerant
Claims (1)
選択透過分離装置において、該膜透過後の透過物管路を
加熱装置および室温冷却器を経てメカニカルブースタポ
ンプに導き、次いでこの管路を冷媒による冷却補集装置
を経て真空ポンプに接続することを特徴とする有機物選
択透過分離装置。1. In an organic permselective permeation separation apparatus using a pervaporation membrane, a permeate pipe line after permeating the membrane is led to a mechanical booster pump through a heating device and a room temperature cooler, and then this pipe line is cooled by a refrigerant. An organic permselective separation device characterized by being connected to a vacuum pump via a collector.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22047291A JPH0557151A (en) | 1991-08-30 | 1991-08-30 | Selective permeation separator for organic substances |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22047291A JPH0557151A (en) | 1991-08-30 | 1991-08-30 | Selective permeation separator for organic substances |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0557151A true JPH0557151A (en) | 1993-03-09 |
Family
ID=16751643
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP22047291A Withdrawn JPH0557151A (en) | 1991-08-30 | 1991-08-30 | Selective permeation separator for organic substances |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0557151A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014147882A (en) * | 2013-01-31 | 2014-08-21 | Sumitomo Bakelite Co Ltd | Method for concentrating phenol |
| WO2017204254A1 (en) * | 2016-05-27 | 2017-11-30 | 三菱ケミカル株式会社 | Dehydration system for aqueous organic compounds, operation method therefor, and dehydration method |
-
1991
- 1991-08-30 JP JP22047291A patent/JPH0557151A/en not_active Withdrawn
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014147882A (en) * | 2013-01-31 | 2014-08-21 | Sumitomo Bakelite Co Ltd | Method for concentrating phenol |
| WO2017204254A1 (en) * | 2016-05-27 | 2017-11-30 | 三菱ケミカル株式会社 | Dehydration system for aqueous organic compounds, operation method therefor, and dehydration method |
| CN109195688A (en) * | 2016-05-27 | 2019-01-11 | 三菱化学株式会社 | Dehydration system for water-containing organic compound, operation method thereof, and dehydration method |
| JPWO2017204254A1 (en) * | 2016-05-27 | 2019-03-28 | 三菱ケミカル株式会社 | Dehydration system for water-containing organic compound, method of operating the same, and method of dehydration |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A300 | Withdrawal of application because of no request for examination |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 19981112 |