JPS634826A - Azeotropic distilling plant - Google Patents
Azeotropic distilling plantInfo
- Publication number
- JPS634826A JPS634826A JP14700586A JP14700586A JPS634826A JP S634826 A JPS634826 A JP S634826A JP 14700586 A JP14700586 A JP 14700586A JP 14700586 A JP14700586 A JP 14700586A JP S634826 A JPS634826 A JP S634826A
- Authority
- JP
- Japan
- Prior art keywords
- azeotropic
- water
- organic compounds
- distillate
- membrane
- 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.)
- Pending
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 150000002894 organic compounds Chemical class 0.000 claims abstract description 24
- 239000012528 membrane Substances 0.000 claims abstract description 19
- 238000000926 separation method Methods 0.000 claims abstract description 15
- 238000010533 azeotropic distillation Methods 0.000 abstract description 16
- 239000000203 mixture Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- KGIGUEBEKRSTEW-UHFFFAOYSA-N 2-vinylpyridine Chemical compound C=CC1=CC=CC=N1 KGIGUEBEKRSTEW-UHFFFAOYSA-N 0.000 description 7
- 238000000034 method Methods 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005373 pervaporation Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- HXEARCOLWPOOFJ-UHFFFAOYSA-N 2-ethenylpyridine;hydrate Chemical compound O.C=CC1=CC=CC=N1 HXEARCOLWPOOFJ-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 235000011148 calcium chloride Nutrition 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
【発明の詳細な説明】
〔発明の技術分野〕
本発明は有機化合物の水を除去するための共沸蒸留装置
に関する。DETAILED DESCRIPTION OF THE INVENTION [Technical Field of the Invention] The present invention relates to an azeotropic distillation apparatus for removing water from organic compounds.
有機化合物中の水分を除去する方法としては、物理的吸
着によって水を除去する方法や化学的反応によって水を
除去する方法等が知られているが、工業的には共沸蒸留
法が最も一般的である。Methods for removing water from organic compounds include methods for removing water by physical adsorption and methods for removing water by chemical reaction, but industrially, azeotropic distillation is the most common method. It is true.
ところで、従来の共沸蒸留法では、共沸蒸留物に第３成
分を添加して共沸蒸留物から水を抽出し、共沸蒸留物を
より水分の少ない有機化合物−水組成物に変え、この組
成物を更に共沸蒸留にかけて残存する水を共沸蒸留物と
して除去する方法が採用されていた。By the way, in the conventional azeotropic distillation method, a third component is added to the azeotropic distillate to extract water from the azeotropic distillate, converting the azeotropic distillate into an organic compound-water composition with lower water content. A method has been adopted in which this composition is further subjected to azeotropic distillation to remove remaining water as an azeotropic distillate.
たとえば、ビニルピリジンの脱水は第２図に示すように
して行なわれていた。For example, vinylpyridine was dehydrated as shown in FIG.
含水のビニルピリジンが第１共沸蒸留器１１に供給され
、共沸蒸留物はコンデンサ１２で冷却された後にデカン
タ１３に導かれる。次いで第３成分としての数％の苛性
ソーダ水溶液、またはＫｃｌ。Water-containing vinylpyridine is supplied to a first azeotropic distiller 11 , and the azeotropic distillate is cooled in a condenser 12 and then led to a decanter 13 . Then a few percent aqueous solution of caustic soda, or Kcl, as a third component.
ＣａＣｌ２等の水溶液が管路１４を経てデカンタ１３に
供給されると、共沸混合物中の水分が苛性ソーダ水溶液
に抽出されて、ビニルピリジンは上層に、苛性ソーダ水
溶液は下層に分液する。When an aqueous solution such as CaCl2 is supplied to the decanter 13 through the pipe 14, water in the azeotrope is extracted into an aqueous caustic soda solution, and the vinyl pyridine is separated into an upper layer and the aqueous sodium hydroxide solution is separated into a lower layer.
上層のビニルピリジンは管路１５によって第２共沸蒸留
器１６に送られ、残存する水はビニルピリジンとの共沸
物として除去されると共に、はぼ無水のビニルピリジン
１７が得られる。The upper layer of vinyl pyridine is sent to a second azeotropic distiller 16 via a pipe 15, and the remaining water is removed as an azeotrope with vinyl pyridine, and anhydrous vinyl pyridine 17 is obtained.
−方、抽出した水によって希釈された苛性ソーダ水溶層
は、濃縮器１８で濃縮された後に、再び管路１４を経て
デカンタ１３に供給され、第２共沸蒸留器１６で除去さ
れたビニルピリジン−水共沸物と、第１共沸蒸留器１１
からのビニルピリジン−水共沸物とからの水抽出に再び
使用される。On the other hand, the aqueous caustic soda layer diluted with the extracted water is concentrated in the concentrator 18 and then supplied to the decanter 13 via the pipe 14 again, where vinylpyridine is removed in the second azeotropic distiller 16. Water azeotrope and first azeotropic distiller 11
The vinylpyridine-water azeotrope from
しかしながら、かかる従来の共沸蒸留器では、第３成分
による共沸蒸留物からの水抽出が行なわれるので、この
水抽出によって希釈された第３成分水溶液の濃縮工程が
当然必要となり、大量エネルギー消費を回避できない欠
点があった。However, in such conventional azeotropic distillers, since water is extracted from the azeotropic distillate by the third component, a step of concentrating the aqueous solution of the third component diluted by this water extraction is naturally required, which consumes a large amount of energy. There was a drawback that could not be avoided.
本発明は上記従来の欠点にかんがみ、エネルギー消費を
著しく削減した共沸蒸留装置を提供することを目的とす
るものである。In view of the above-mentioned conventional drawbacks, the present invention aims to provide an azeotropic distillation apparatus that significantly reduces energy consumption.
上記目的を達成する本発明の共沸蒸留装置は、有機化合
物と水との共沸混合物を得るための第１共沸蒸留器と、
該共沸蒸留物を前記有機化合物と水に分離するための膜
分離装置と、該膜分離装置において得られた前記有機化
合物中に残存する水を共沸蒸留物として除去するための
第２共沸蒸留器とからなることを特徴とするものである
。The azeotropic distillation apparatus of the present invention that achieves the above object includes a first azeotropic distiller for obtaining an azeotropic mixture of an organic compound and water;
a membrane separation device for separating the azeotropic distillate into the organic compound and water; and a second membrane separation device for removing water remaining in the organic compound obtained in the membrane separation device as an azeotropic distillate. It is characterized by consisting of a boiling distiller.
以下、本発明を図面に示した実施例にもとづき説明する
。第１図は本発明の実施例を示し、含水有機化合物が第
１共沸蒸留器１に供給されて共沸蒸留に付される。第１
共沸蒸留器ｌは特に限定されるものではなく、従来使用
されているものを使用することができる。共沸蒸留物は
管路２を経てコンデンサ３に送され、凝縮した共沸蒸留
物は膜分離装置４、たとえばパーベーバレション分離装
置に供給される。The present invention will be described below based on embodiments shown in the drawings. FIG. 1 shows an embodiment of the present invention, in which a water-containing organic compound is fed to a first azeotropic distiller 1 and subjected to azeotropic distillation. 1st
The azeotropic distiller l is not particularly limited, and any conventionally used one can be used. The azeotropic distillate is sent via line 2 to a condenser 3, and the condensed azeotropic distillate is fed to a membrane separation device 4, for example a pervaporation separation device.
そして、分離膜を透過した水は管路５から排出され、−
方、大部分め水分が除された有機化合物は管路６を経て
第２共沸蒸留器７に送られる。Then, the water that has passed through the separation membrane is discharged from the pipe 5, and -
On the other hand, the organic compound from which most of the moisture has been removed is sent to a second azeotropic distiller 7 via a pipe 6.
なお、膜分離装置４は、パーベーパレーション分離装置
に限定されるものではなく、有機化合物−水共沸蒸留物
を有機化合物と水とに分離できるものであれば、いかな
る装置であっても使用することができ、たとえば逆浸透
膜、限外濾過膜、ガス分離膜またはメンブレン蒸留によ
る分離装置を挙げることができる。Note that the membrane separation device 4 is not limited to a pervaporation separation device, and any device can be used as long as it can separate an organic compound-water azeotropic distillate into an organic compound and water. For example, a separation device using a reverse osmosis membrane, an ultrafiltration membrane, a gas separation membrane or a membrane distillation can be mentioned.
第２共沸蒸留器７においては、前記第１共沸蒸留器ｌと
同様に共沸蒸留が行なわれ、有機化合物に残存する水は
有機化合物との共沸蒸留物として除去され、管路８を経
て膜分離装置４に循環され、第１共沸燕留器１からの共
沸蒸留物と共に再び膜による水除去操作にかけられる。In the second azeotropic distiller 7, azeotropic distillation is performed in the same manner as in the first azeotropic distiller 1, water remaining in the organic compound is removed as an azeotropic distillate with the organic compound, and the pipe 8 The water is circulated through the membrane separator 4 and subjected to the water removal operation using the membrane again together with the azeotropic distillate from the first azeotropic distiller 1.
第２共沸蒸留器７において、共沸蒸留物が除去された後
に、実質的に無水の有機化合物９が得られる。In the second azeotropic distiller 7, after the azeotropic distillate has been removed, a substantially anhydrous organic compound 9 is obtained.
なお、かかる本発明の共沸蒸留器において共沸蒸留に共
される有機化合物は、共に共沸蒸留可能な種類であれば
、いかなる種類であっても良く、特に限定されず、たと
えばエタノール、イソプロパツール等を挙げることがで
きる。The organic compound used in the azeotropic distillation in the azeotropic distillation apparatus of the present invention may be of any type as long as it can be distilled azeotropically with the organic compound, and is not particularly limited. For example, ethanol, isopropylene, Patur etc. can be mentioned.
以上述べたように従来の共沸蒸留装置では、第１共沸蒸
留器で得られる共沸蒸留物から水を抽出して共沸蒸留物
の組成を変えるために第３成分を添加していた。As mentioned above, in conventional azeotropic distillation equipment, water is extracted from the azeotropic distillate obtained in the first azeotropic distillation device, and a third component is added to change the composition of the azeotropic distillate. .
この結果、第３成分の希釈された水溶液を濃縮し循環使
用するために多大のエネルギーを消費していた。As a result, a large amount of energy is consumed to concentrate and circulate the diluted aqueous solution of the third component.
しかるに本発明によれば、第１共沸蒸留器からの共沸蒸
留物から膜分離装置によって水を除、去するので、従来
の第３成分の濃縮工程が全く不要となり、消費エネルギ
ー量を大巾に削減することができる。However, according to the present invention, since water is removed from the azeotropic distillate from the first azeotropic distillation device using a membrane separation device, the conventional step of concentrating the third component is completely unnecessary, and the amount of energy consumed can be greatly reduced. can be reduced in width.
また、第３成分の種類によっては、有機化合物中に第３
成分が混入する可能性もあったが、本発明によれば、か
かるトラブルも完全に解消することができる。Also, depending on the type of the third component, there may be a third component in the organic compound.
Although there was a possibility that components would be mixed in, according to the present invention, such troubles can be completely eliminated.
第１図は本発明の実施例を示す配置図、第２図は従来の
共沸蒸留装置を示す配置図である。
１．１１・・・第１共沸蒸留器、４・・・膜分離装置、
７．１６・・・第２共沸蒸留器、１３・・・デカンタ、
１８・・・濃縮器。FIG. 1 is a layout diagram showing an embodiment of the present invention, and FIG. 2 is a layout diagram showing a conventional azeotropic distillation apparatus. 1.11... first azeotropic distiller, 4... membrane separation device,
7.16...Second azeotropic distiller, 13...Decanter,
18...Concentrator.
Claims (1)
留器と、該共沸蒸留物を前記有機化合物と水に分離する
ための膜分離装置と、該膜分離装置において得られた前
記有機化合物中に残存する水を共沸蒸留物として除去す
るための第２共沸蒸留器とからなることを特徴とする共
沸蒸留装置。a first azeotropic distiller for obtaining an azeotropic distillate of an organic compound and water; a membrane separation device for separating the azeotropic distillate into the organic compound and water; and a second azeotropic distiller for removing water remaining in the organic compound as an azeotropic distillate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14700586A JPS634826A (en) | 1986-06-25 | 1986-06-25 | Azeotropic distilling plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14700586A JPS634826A (en) | 1986-06-25 | 1986-06-25 | Azeotropic distilling plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS634826A true JPS634826A (en) | 1988-01-09 |
Family
ID=15420406
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14700586A Pending JPS634826A (en) | 1986-06-25 | 1986-06-25 | Azeotropic distilling plant |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS634826A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06145083A (en) * | 1992-11-02 | 1994-05-24 | Nippon Gosei Arco-Le Kk | Production of dehydrated ethanol |
| EP0793997A1 (en) * | 1996-03-04 | 1997-09-10 | Ciba SC Holding AG | Method and apparatus for separating liquid mixtures |
| JP2016030233A (en) * | 2014-07-29 | 2016-03-07 | オルガノ株式会社 | Organic solvent refining system and method |
| JP6682053B1 (en) * | 2018-10-25 | 2020-04-15 | 木村化工機株式会社 | Solvent recovery system |
| WO2020084803A1 (en) * | 2018-10-25 | 2020-04-30 | 木村化工機株式会社 | Solvent recovery system |
| WO2020085432A1 (en) * | 2018-10-25 | 2020-04-30 | 木村化工機株式会社 | Solvent recovery system |
-
1986
- 1986-06-25 JP JP14700586A patent/JPS634826A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06145083A (en) * | 1992-11-02 | 1994-05-24 | Nippon Gosei Arco-Le Kk | Production of dehydrated ethanol |
| EP0793997A1 (en) * | 1996-03-04 | 1997-09-10 | Ciba SC Holding AG | Method and apparatus for separating liquid mixtures |
| JP2016030233A (en) * | 2014-07-29 | 2016-03-07 | オルガノ株式会社 | Organic solvent refining system and method |
| CN106132516A (en) * | 2014-07-29 | 2016-11-16 | 奥加诺株式会社 | Organic solvent purifying system and method |
| CN106132516B (en) * | 2014-07-29 | 2021-09-24 | 奥加诺株式会社 | Organic solvent purification system and method |
| JP6682053B1 (en) * | 2018-10-25 | 2020-04-15 | 木村化工機株式会社 | Solvent recovery system |
| WO2020084803A1 (en) * | 2018-10-25 | 2020-04-30 | 木村化工機株式会社 | Solvent recovery system |
| WO2020085432A1 (en) * | 2018-10-25 | 2020-04-30 | 木村化工機株式会社 | Solvent recovery system |
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