JPH04118002A - Method and device for separating azeotropic solution mixture - Google Patents
Method and device for separating azeotropic solution mixtureInfo
- Publication number
- JPH04118002A JPH04118002A JP19003490A JP19003490A JPH04118002A JP H04118002 A JPH04118002 A JP H04118002A JP 19003490 A JP19003490 A JP 19003490A JP 19003490 A JP19003490 A JP 19003490A JP H04118002 A JPH04118002 A JP H04118002A
- Authority
- JP
- Japan
- Prior art keywords
- distillation column
- distillation
- column
- supplied
- pressure
- 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
- 239000000203 mixture Substances 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 title claims description 15
- 238000004821 distillation Methods 0.000 claims abstract description 111
- 238000009835 boiling Methods 0.000 claims abstract description 12
- 239000011259 mixed solution Substances 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 abstract 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 13
- 239000002994 raw material Substances 0.000 description 4
- 238000005292 vacuum distillation Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000010533 azeotropic distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は共沸混合物を形成する２成分系混合溶液を蒸留
操作により分離する方法とその分離に使用される装置に
関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for separating a two-component mixed solution forming an azeotrope by distillation, and an apparatus used for the separation.
［従来の技術］
共沸混合物を形成する２成分を普通の蒸留で分離するこ
とは不可能であり、通常は共沸蒸留や減圧蒸留を利用し
て分離されている。共沸蒸留は２成分系混合溶液に第３
成分を添加し、前記２成分と断たに２成分または３成分
の共沸混合物をつくることによって分離する方法である
。しかし該第３成分を回収するプロセスが必要であり、
エネルギー効率が悪く、添加される第３成分が有害であ
ることさえある。[Prior Art] It is impossible to separate two components forming an azeotropic mixture by ordinary distillation, and they are usually separated using azeotropic distillation or vacuum distillation. Azeotropic distillation adds a third component to a two-component mixed solution.
This is a method of separation by adding components and creating an azeotropic mixture of two or three components separately from the two components. However, a process to recover the third component is required,
It is energy inefficient and the added third component may even be harmful.
また減圧蒸留は、例えば水とエタノールでは圧力を７０
ｍｍＨｇ以下にした時に共沸点が消滅することを応用し
たものである。第５図に装置の一例を示す。第１塔が１
３０ ｍｍＨｇで運転された場合、塔頂より得られる留
出物のエタノール濃度は９８〜９８．７ｗｔ％であり、
該留出物は常圧操作の第２塔に導かれ、第２塔内で更に
脱水され、第２塔の塔底より９９．９％の無水エタノー
ルを得ることができる。しかしこの方法も低真空域で操
作されるので空気の漏入等操業上程々の困難を伴い、ま
た第２塔に供給されるエタノールの相当量が第１塔に戻
されること等、エネルギー効率が悪いという欠点を有し
ている。更に減圧蒸留法は空気の漏れごみがあるため、
可燃性流体を取り扱う場合には使用できないという欠点
がある。Also, in vacuum distillation, for example, the pressure is 70% for water and ethanol.
This is an application of the fact that the azeotropic point disappears when the temperature is lower than mmHg. FIG. 5 shows an example of the device. The first tower is 1
When operated at 30 mmHg, the ethanol concentration of the distillate obtained from the top of the column is 98 to 98.7 wt%,
The distillate is led to a second column operated at normal pressure, where it is further dehydrated, and 99.9% absolute ethanol can be obtained from the bottom of the second column. However, since this method is operated in a low vacuum region, there are some operational difficulties such as air leakage, and a considerable amount of ethanol supplied to the second column is returned to the first column, resulting in poor energy efficiency. It has the disadvantage of being bad. Furthermore, since the vacuum distillation method has air leakage,
The disadvantage is that it cannot be used when handling flammable fluids.
［発明が解決しようとする課題］
本発明は以上のような事情に鑑みてなされたものであっ
て、第３成分を加える必要がなく、しかも操業が容易な
、共沸混合物を形成する混合溶液の分離方法、及びそれ
に用いる分離装置を提供しようとするものである。[Problems to be Solved by the Invention] The present invention has been made in view of the above circumstances, and provides a mixed solution that forms an azeotrope, which does not require the addition of a third component, and is easy to operate. The present invention aims to provide a separation method for the method and a separation device used therefor.
［課題を解決するための手段］
本発明の共沸混合溶液の分離方法は、加熱器を塔下部に
、凝縮器を塔上部に備えた第１及び第２蒸留塔を用いて
、共沸混合物を形成する２成分系溶液から各成分を分離
する方法において、前記２成分混合溶液を第１及び／又
は第２蒸留塔に供給すると共に、第１蒸留塔には第２蒸
留塔の蒸気または凝縮機で凝縮された凝縮液の一部を供
給し、第１蒸留塔の頂部からの留出物の一部を圧縮器を
通して第２蒸留塔に供給することにより、第２蒸留塔内
圧力を３４１蒸留塔内圧力より高圧に調整しながら蒸留
を行ない、第２蒸留塔の回収部から低沸点側成分を回収
することに要旨がある。[Means for Solving the Problems] The method for separating an azeotropic mixture solution of the present invention uses first and second distillation columns each having a heater at the bottom of the column and a condenser at the top of the column. In the method of separating each component from a binary solution forming By supplying a portion of the condensate condensed in the distillation column and a portion of the distillate from the top of the first distillation column through the compressor to the second distillation column, the pressure inside the second distillation column is increased to 341. The gist is to perform distillation while adjusting the pressure to be higher than the internal pressure of the distillation column, and to recover low-boiling components from the recovery section of the second distillation column.
また上記分離方法に使用される分離装置は前記２成分混
合溶液が′！Ｊ１及び／又は第２蒸留塔に供給されると
共に、第１蒸留塔には第２蒸留塔からの蒸気または凝縮
器で凝縮された凝縮液の一部が供給され、第２蒸留塔に
は第１蒸留塔の頂部からの留出物の一部が圧縮機により
加圧されて供給され、第２蒸留塔内の温度及び圧力が第
１蒸留塔内よりも高温高圧側に調節制御され、第２蒸留
塔の回収部から低沸点成分を回収するものであることに
要旨があり、更に熱効率を高めることを目的として、熱
交換部を介して上部に第１蒸留塔が、下部に第２蒸留塔
が結合して一体化され、更に第１蒸留塔上部には凝縮器
が、第２蒸留塔下部には加熱器が設けられたものも本発
明に含まれる。In addition, the separation device used in the above separation method is used when the two-component mixed solution is '! J1 and/or the second distillation column, the first distillation column is also supplied with steam from the second distillation column or a part of the condensate condensed in the condenser, and the second distillation column is supplied with the steam from the second distillation column or a part of the condensate condensed in the condenser. A part of the distillate from the top of the first distillation column is supplied under pressure by a compressor, and the temperature and pressure in the second distillation column are controlled to be higher in temperature and pressure than in the first distillation column. The main purpose is to recover low-boiling components from the recovery section of the second distillation column, and in order to further increase thermal efficiency, the first distillation column is placed in the upper part and the second distillation column is placed in the lower part via the heat exchange part. The present invention also includes a system in which the columns are combined and integrated, and a condenser is provided at the top of the first distillation column, and a heater is provided at the bottom of the second distillation column.
［作用〕
本発明は加圧することによって、共沸混合物の組成が変
わることを利用したものである。尚、本発明は基本的に
は２成分系溶液を対象としているが、共沸混合物を形成
しない他の成分が入っていても本発明の趣旨により分離
され得る場合は本発明に包含される。また不可避的に混
合する成分がある場合も本発明に包含される。[Function] The present invention utilizes the fact that the composition of the azeotrope changes by applying pressure. Although the present invention is basically directed to two-component solutions, even if other components that do not form an azeotrope are present, the present invention covers cases where they can be separated according to the spirit of the present invention. Furthermore, cases where there are components that are unavoidably mixed are also included in the present invention.
以下第１図に示した基本プロセスに従って説明する。但
し、以下の説明及び実施例では原料を第１蒸留塔に供給
する場合を例にとって説明するが、共沸混合物の組成比
と原料の組成比によフては第２蒸留塔に原料を供給する
こともある。The basic process shown in FIG. 1 will be explained below. However, in the following explanations and examples, the case where the raw material is supplied to the first distillation column will be explained as an example, but depending on the composition ratio of the azeotrope and the composition ratio of the raw material, the raw material may be supplied to the second distillation column. Sometimes I do.
第１図に示される第１蒸留塔１及び第２蒸留塔２として
は棚段塔や充填塔等種々の形式の塔を利用することがで
きるが、第２蒸留塔２としては耐圧構造を備えたものが
使用される。夫々の蒸留塔の上部には凝縮器（４及び６
）が、下部には加熱器（３及び５）が備えつけられてい
て、第１蒸留塔１の塔頂は圧縮器７を介して第２蒸留塔
２につながれ、第２蒸留塔２の塔頂は減圧弁８を介して
第１蒸留塔１につながれている。凝縮器（４及び６）及
び加熱器（３及び５）として種々の形式のものが利用で
き、また設置位置が塔内であってもよい。As the first distillation column 1 and the second distillation column 2 shown in FIG. 1, various types of columns such as plate columns and packed columns can be used, but the second distillation column 2 is equipped with a pressure-resistant structure. is used. Condensers (4 and 6) are installed at the top of each distillation column.
) is equipped with heaters (3 and 5) at the bottom, and the top of the first distillation column 1 is connected to the second distillation column 2 via the compressor 7; is connected to the first distillation column 1 via a pressure reducing valve 8. Various types of condensers (4 and 6) and heaters (3 and 5) can be used, and they may be installed inside the tower.
原料はまず第１蒸留塔１に供給され、常圧下で分離され
た共沸混合物の一部は圧縮機７で圧縮され第２蒸留塔２
に供給される。第２蒸留塔２内は圧縮された蒸気の導入
によって第１蒸留塔１内より高温高圧に保たれるので、
第２蒸留塔２内から留出される共沸混合物中の低沸点成
分の割合は第１蒸留塔１内から留出されるものより少な
くなる。従って第１蒸留塔１内の低沸点成分は徐々に第
２蒸留塔２内に８行し、第１蒸留塔１下部からは高沸点
成分（製品１）が得られ、一方第２蒸留塔２には低沸点
成分が蓄積され、第２蒸留塔２下部より低沸点成分（製
品２）が得られる。蒸留塔内の圧力差が大きい程循環量
は減少するが、第２蒸留塔における成分間の相対揮発度
が小さくなって分離しに＜−くなるので、圧力差は経済
性の面から、更には蒸留塔や圧縮機の能力、操作性等を
考慮して適宜決定される。The raw material is first supplied to the first distillation column 1, and a part of the azeotropic mixture separated under normal pressure is compressed by the compressor 7 and sent to the second distillation column 2.
is supplied to The interior of the second distillation column 2 is maintained at a higher temperature and pressure than the interior of the first distillation column 1 by introducing compressed steam, so that
The proportion of low-boiling components in the azeotrope distilled from the second distillation column 2 is smaller than that distilled from the first distillation column 1. Therefore, the low-boiling components in the first distillation column 1 gradually flow into the second distillation column 2, and the high-boiling components (product 1) are obtained from the lower part of the first distillation column 1, while the second distillation column 2 The low boiling point components are accumulated in the distillation column 2, and the low boiling point components (product 2) are obtained from the lower part of the second distillation column 2. The larger the pressure difference in the distillation column, the smaller the circulating amount, but the relative volatility between the components in the second distillation column becomes smaller and becomes less likely to separate, so the pressure difference is even more important from an economic point of view. is appropriately determined taking into consideration the capacity and operability of the distillation column and compressor.
以上が基本プロセスであるが、より熱効率を高めるため
に、第１ （又は２）蒸留塔のａ縮量より得られる熱エ
ネルギーを第２（又は１）蒸留塔内の加熱に用いること
も可能であるし、更には第２蒸留塔２の濃縮部と第１蒸
留塔１の回収部を１つの熱交換部として兼用し、該熱交
換部を介して第１及び第２蒸留塔を結合させ一体化する
こともてきる。これらの変形態様は後記実施例として説
明する。The above is the basic process, but in order to further improve thermal efficiency, it is also possible to use the thermal energy obtained from the a reduction amount of the first (or second) distillation column to heat the second (or first) distillation column. Furthermore, the concentrating section of the second distillation column 2 and the recovery section of the first distillation column 1 are used as one heat exchange section, and the first and second distillation columns are connected through the heat exchange section to be integrated. It can also become These modifications will be explained later as examples.
［実施例］
実施例１
第２図の装置は基本プロセスの第１蒸留塔と第２蒸留塔
を熱交換部を介して結合させたもので、加熱器３と凝縮
器６が不要となっている。[Example] Example 1 The apparatus shown in Fig. 2 is a device in which the first distillation column and the second distillation column of the basic process are connected via a heat exchange section, and the heater 3 and condenser 6 are unnecessary. There is.
この装置を用いてエタノールと水の混合液を分離したと
ころ効率よく分離することができた。When this device was used to separate a mixture of ethanol and water, it was possible to separate the mixture efficiently.
実施例２
第３図の装置は実施例１の凝縮器４より得られる熱エネ
ルギーを加熱器９のエネルギー源の一部として利用する
ために熱媒体の回路を設けたものである。Embodiment 2 The apparatus shown in FIG. 3 is provided with a heat medium circuit in order to utilize the thermal energy obtained from the condenser 4 of Embodiment 1 as part of the energy source for the heater 9.
この装置を用いてエタノールと水の混合液を分離したと
ころ効率よく分離することができた。When this device was used to separate a mixture of ethanol and water, it was possible to separate the mixture efficiently.
実施例３
第４図の装置は実施例３の熱媒体の代りに第１蒸留塔で
気化された共沸混合物を利用したものである。Example 3 The apparatus shown in FIG. 4 uses the azeotrope vaporized in the first distillation column instead of the heat medium of Example 3.
この装置を用いてエタノールと木の混合液を分離したと
ころ効率よく分離することができた。Using this device, we were able to efficiently separate a mixture of ethanol and wood.
［発明の効果〕
本発明により第３成分を加えることなく、共沸混合物を
形成する混合溶液を効率良く分離することができるよう
になった。また本発明は減圧ではなく加圧を採用してい
るので減圧蒸留法に伴う種々の欠点がなく、操業が容易
で、様々な溶液の分離を効率良く行なうことができる。[Effects of the Invention] According to the present invention, it has become possible to efficiently separate a mixed solution forming an azeotrope without adding a third component. Furthermore, since the present invention employs increased pressure rather than reduced pressure, it does not have the various drawbacks associated with reduced pressure distillation, is easy to operate, and can efficiently separate various solutions.
第１図は本発明の基本プロセスの説明図、第２〜４図は
夫々実施例１〜３の説明図、第５図は減圧蒸留装置の説
明図である。
１・・・第１蒸留塔 ２・・・第２蒸留塔３・・・
第１蒸留塔加熱器
４・・・第１蒸留塔凝縮器
５・・・第２蒸留塔加熱器
６・・・第２蒸留塔凝縮器
７・・・圧縮機 ８・・・減圧弁９・・・加熱
器（熱交換器）
味FIG. 1 is an explanatory diagram of the basic process of the present invention, FIGS. 2 to 4 are explanatory diagrams of Examples 1 to 3, respectively, and FIG. 5 is an explanatory diagram of a vacuum distillation apparatus. 1... First distillation column 2... Second distillation column 3...
First distillation column heater 4...First distillation column condenser 5...Second distillation column heater 6...Second distillation column condenser 7...Compressor 8...Pressure reducing valve 9...・・Heating device (heat exchanger) Taste
Claims (3)
及び第２蒸留塔を用いて、共沸混合物を形成する２成分
系溶液から各成分を分離する方法において、前記２成分
混合溶液を第１及び／又は第２蒸留塔に供給すると共に
、第１蒸留塔には第２蒸留塔の蒸気または凝縮器で凝縮
された凝縮液の一部を供給し、第１蒸留塔の頂部からの
留出物の一部を圧縮機を通して第２蒸留塔に供給するこ
とにより、第２蒸留塔内圧力を第１蒸留塔内圧力より高
圧に調整しながら蒸留を行ない、第２蒸留塔の回収部か
ら低沸点側成分を回収することを特徴とする共沸混合溶
液の分離方法。(1) The first stage has a heater at the bottom of the column and a condenser at the top of the column.
and a method for separating each component from a two-component solution forming an azeotrope using a second distillation column, in which the two-component mixed solution is supplied to the first and/or second distillation column; The distillation column is supplied with the vapor of the second distillation column or a part of the condensate condensed in the condenser, and a part of the distillate from the top of the first distillation column is supplied to the second distillation column through the compressor. By doing so, distillation is performed while adjusting the pressure inside the second distillation column to be higher than the pressure inside the first distillation column, and the low-boiling point component is recovered from the recovery section of the second distillation column. Method of separating solutions.
及び第２蒸留塔を用いて、共沸混合物を形成する２成分
系溶液から各成分を分離する分離装置において、前記２
成分混合溶液が第１及び／又は第２蒸留塔に供給される
と共に、第１蒸留塔には第２蒸留塔の蒸気または凝縮器
で凝縮された凝縮液の一部が供給され、第２蒸留塔には
第１蒸留塔の頂部からの留出物の一部が圧縮機により加
圧されて供給され、第２蒸留塔内の温度及び圧力が第１
蒸留塔内よりも高温高圧側に調節制御され、第２蒸留塔
の回収部から低沸点成分を回収するものであることを特
徴とする共沸混合溶液の分離装置。(2) The first stage has a heater at the bottom of the column and a condenser at the top of the column.
and a separation device for separating each component from a two-component solution forming an azeotrope using a second distillation column;
The component mixed solution is supplied to the first and/or second distillation column, and the first distillation column is supplied with the vapor of the second distillation column or a part of the condensate condensed in the condenser, and the second distillation column is supplied with the component mixture solution. A part of the distillate from the top of the first distillation column is supplied to the column after being pressurized by a compressor, and the temperature and pressure in the second distillation column are equal to that of the first distillation column.
1. An apparatus for separating an azeotropic mixed solution, characterized in that the temperature and pressure are controlled to be higher than that in the distillation column, and the low boiling point components are recovered from the recovery section of the second distillation column.
する２成分系溶液から各成分を分離する分離装置におい
て、熱交換部を介して上部に第１蒸留塔を、下部に第２
蒸留塔を結合して一体化され、更に第１蒸留塔上部には
凝縮器が、第２蒸留塔下部には加熱器が設けられたもの
であり、前記２成分混合溶液が第１及び／又は第２蒸留
塔に供給されると共に、第１蒸留塔には第２蒸留塔から
の蒸気または凝縮液の一部が供給され、第２蒸留塔には
第１蒸留塔の頂部からの留出物の一部が圧縮機により加
圧されて供給され、第２蒸留塔内の温度及び圧力が第１
蒸留塔内よりも高温高圧側に調節制御され、第２蒸留塔
の回収部から低沸点成分を回収するものであることを特
徴とする共沸混合溶液の分離装置。(3) In a separation device that uses first and second distillation columns to separate each component from a two-component solution forming an azeotrope, the first distillation column is placed in the upper part through a heat exchange section, and the first distillation column is placed in the lower part through a heat exchange section. Second
The distillation column is integrated by combining the distillation columns, and is further provided with a condenser at the top of the first distillation column and a heater at the bottom of the second distillation column. At the same time, the first distillation column is supplied with a portion of the vapor or condensate from the second distillation column, and the second distillation column is supplied with the distillate from the top of the first distillation column. A part of the distillation column is pressurized by a compressor and supplied, and the temperature and pressure in the second distillation column are the same as those in the first distillation column.
1. An apparatus for separating an azeotropic mixed solution, characterized in that the temperature and pressure are controlled to be higher than that in the distillation column, and the low boiling point components are recovered from the recovery section of the second distillation column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2190034A JP2903096B2 (en) | 1990-05-17 | 1990-07-17 | Method and apparatus for separating azeotropic mixed solution |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12826390 | 1990-05-17 | ||
| JP2-128263 | 1990-05-17 | ||
| JP2190034A JP2903096B2 (en) | 1990-05-17 | 1990-07-17 | Method and apparatus for separating azeotropic mixed solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04118002A true JPH04118002A (en) | 1992-04-20 |
| JP2903096B2 JP2903096B2 (en) | 1999-06-07 |
Family
ID=26463987
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2190034A Expired - Lifetime JP2903096B2 (en) | 1990-05-17 | 1990-07-17 | Method and apparatus for separating azeotropic mixed solution |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2903096B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009006240A (en) * | 2007-06-27 | 2009-01-15 | Kansai Chemical Engineering Co Ltd | Multicomponent internal heat exchange type distilling apparatus |
| JP2010110759A (en) * | 2009-12-28 | 2010-05-20 | Taiyo Nippon Sanso Corp | Distillation apparatus and concentration method of oxygen isotope |
| CN107428666A (en) * | 2014-10-31 | 2017-12-01 | 陶氏环球技术有限责任公司 | Methanol/methyl methacrylate azeotropic mixture is separated using the transformation way of distillation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4843510A (en) * | 1971-10-05 | 1973-06-23 | ||
| JPS59196833A (en) * | 1983-04-21 | 1984-11-08 | Res Assoc Petroleum Alternat Dev<Rapad> | Method and apparatus for producing anhydrous methanol |
| JPH01179704U (en) * | 1988-06-08 | 1989-12-25 |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3940450A (en) | 1974-12-16 | 1976-02-24 | Texaco Inc. | Preparation and recovery of ethers |
-
1990
- 1990-07-17 JP JP2190034A patent/JP2903096B2/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4843510A (en) * | 1971-10-05 | 1973-06-23 | ||
| JPS59196833A (en) * | 1983-04-21 | 1984-11-08 | Res Assoc Petroleum Alternat Dev<Rapad> | Method and apparatus for producing anhydrous methanol |
| JPH01179704U (en) * | 1988-06-08 | 1989-12-25 |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009006240A (en) * | 2007-06-27 | 2009-01-15 | Kansai Chemical Engineering Co Ltd | Multicomponent internal heat exchange type distilling apparatus |
| JP2010110759A (en) * | 2009-12-28 | 2010-05-20 | Taiyo Nippon Sanso Corp | Distillation apparatus and concentration method of oxygen isotope |
| CN107428666A (en) * | 2014-10-31 | 2017-12-01 | 陶氏环球技术有限责任公司 | Methanol/methyl methacrylate azeotropic mixture is separated using the transformation way of distillation |
| CN107428666B (en) * | 2014-10-31 | 2020-11-03 | 陶氏环球技术有限责任公司 | Separation of methanol/methyl methacrylate azeotropes using pressure swing distillation |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2903096B2 (en) | 1999-06-07 |
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| EXPY | Cancellation because of completion of term |