JPS6359308A - Separation device for organic liquid - Google Patents
Separation device for organic liquidInfo
- Publication number
- JPS6359308A JPS6359308A JP20148586A JP20148586A JPS6359308A JP S6359308 A JPS6359308 A JP S6359308A JP 20148586 A JP20148586 A JP 20148586A JP 20148586 A JP20148586 A JP 20148586A JP S6359308 A JPS6359308 A JP S6359308A
- Authority
- JP
- Japan
- Prior art keywords
- water
- ethanol
- organic liquid
- distillation column
- pervaporation
- 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
- 239000007788 liquid Substances 0.000 title claims abstract description 19
- 238000000926 separation method Methods 0.000 title claims abstract description 17
- 238000004821 distillation Methods 0.000 claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 29
- 238000005373 pervaporation Methods 0.000 claims abstract description 25
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 37
- 238000000034 method Methods 0.000 description 5
- 239000012466 permeate Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- -1 95 kg of ethanol Chemical compound 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 229920002379 silicone rubber Polymers 0.000 description 1
- 239000004945 silicone rubber Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔発明の技術分野〕
本発明は有機液体の分離装置に関し、浸透気化分離装置
と蒸留塔との組合せによって分離効率を高めた有機液体
の分離装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Technical Field of the Invention] The present invention relates to an organic liquid separation apparatus, and more particularly, to an organic liquid separation apparatus in which separation efficiency is improved by a combination of a pervaporation separation apparatus and a distillation column.
従来、含水有機液体、例えば含水エタノールから水を分
離して実質的に無水のエタノールを製造するに際しては
、（イ）蒸留塔を使用する方法または（ロ）浸透気化膜
を使用する方法が採用されている。Conventionally, when separating water from a water-containing organic liquid, such as water-containing ethanol, to produce substantially anhydrous ethanol, (a) a method using a distillation column or (b) a method using a pervaporation membrane has been adopted. ing.
（イ）では、第１の蒸留塔で水分を共沸混合物として除
去し、第２の蒸留塔で共沸混合物から水分を除去してい
るが、二本の蒸留塔を必要とするので装置的に大型化を
免れず、エネルギー損失も大きい問題点があった。In (a), water is removed as an azeotrope in the first distillation column, and water is removed from the azeotrope in the second distillation column, but since two distillation columns are required, the equipment is However, there was a problem in that it was inevitable to increase the size and the energy loss was large.
また、（ロ）は浸透気化膜の二次側に水を浸透、気化さ
せる方法であるが、通常では水と共ニ少量のエタノール
も浸透、気化されるので、５〜１０％程度のエタノール
水溶液が得られ、このエタノール水溶液の処理に苦慮し
ているのが現状である。In addition, (b) is a method in which water permeates and vaporizes on the secondary side of the pervaporation membrane, but normally a small amount of ethanol is also permeated and vaporized along with water, so a 5 to 10% ethanol aqueous solution is used. Currently, it is difficult to process this ethanol aqueous solution.
本発明はかかる現状に鑑みてなされたものであり、有機
液体の分離効率を高めることができると共に、コンパク
トであり、かつ省エネルギー的である装置を提供するこ
とを目的とするものである。The present invention has been made in view of the current situation, and an object thereof is to provide a device that is compact and energy-saving, as well as capable of increasing the separation efficiency of organic liquids.
上記目的を達成する本発明の有機液体の分離装置は、真
空容器中に配置された浸透気化膜モジュールからなる浸
透気化分離装置と、該モジュールの二次側蒸気が供給さ
れる蒸留塔からなり、該蒸留塔の留出物を前記モジュー
ルの一次側に循環する管路を設けたことを特徴とするも
のである。The organic liquid separation device of the present invention that achieves the above object is composed of a pervaporation separation device consisting of a pervaporation membrane module disposed in a vacuum container, and a distillation column to which the secondary side vapor of the module is supplied, The present invention is characterized in that a pipe line is provided for circulating the distillate of the distillation column to the primary side of the module.
以下、本発明を図面に示した実施例にもとづき説明する
。The present invention will be described below based on embodiments shown in the drawings.
本発明の有機液体分離装置は、浸透気化分離装置ｌと、
蒸留塔２の組合せからなる。The organic liquid separation device of the present invention includes a pervaporation separation device l,
It consists of a combination of two distillation columns.
そして浸透気化分離装置１は、真空容器３と、この中に
配置された浸透気化膜モジュール４．４” とから構成
される。The pervaporation separation apparatus 1 is comprised of a vacuum vessel 3 and a pervaporation membrane module 4.4'' disposed within the vacuum vessel 3.
浸透気化膜モジュール４の数は限定されるものではなく
、処理される有機液体の種類および含水量等によって決
定することができる。The number of pervaporation membrane modules 4 is not limited, and can be determined depending on the type and water content of the organic liquid to be treated.
また、この浸透気化膜モジュール４に使用される浸透気
化膜５の材質も従来から使用されているものの中から選
定することができ、例えばポリビニルアルコール膜やシ
リコンゴム膜を挙げることができる。Furthermore, the material of the pervaporative membrane 5 used in the pervaporative membrane module 4 can be selected from conventionally used materials, such as polyvinyl alcohol membranes and silicone rubber membranes.
真空容器３内は蒸気減圧機６によって減圧下に保持され
ており、浸透気化膜５．５゛の二次側に浸透、気化した
成分、例えば供給含水有機液体を含水エタノールとする
と、水分は共に浸透気化した少量のエタノールと共に蒸
留塔２に、蒸気状のままで供給される。The inside of the vacuum container 3 is maintained under reduced pressure by a steam depressurizer 6, and the components that permeate and vaporize on the secondary side of the pervaporation membrane 5.5゛, for example, if the supplied water-containing organic liquid is water-containing ethanol, both water and water are removed. It is fed in vapor form to the distillation column 2 along with a small amount of pervaporized ethanol.
蒸留塔２としては、通常使用される蒸留塔であれば良く
、例えば充填塔や棚段塔が使用される。The distillation column 2 may be any commonly used distillation column, such as a packed column or a tray column.
蒸留塔２の塔底には、塔内官物の一部を取り出して加熱
するための熱供給源７が設けられ、また塔頂には留出蒸
気を冷却、循環するための冷却器８が設けられている。A heat supply source 7 is provided at the bottom of the distillation column 2 to take out and heat a part of the internal substances in the column, and a cooler 8 is provided at the top of the column to cool and circulate distilled vapor. It is provided.
なお、塔２内はコンデンサー８に設けられた真空ポンプ
９により、減圧状態に保たれている。Note that the inside of the column 2 is maintained at a reduced pressure by a vacuum pump 9 provided in a condenser 8.
更に本発明においては、蒸留塔２の留出物の一部を、コ
ンデンサー８からモジュール４の一次側に循環、供給す
るための管路１０が設けられている。Furthermore, in the present invention, a pipe line 10 is provided for circulating and supplying a portion of the distillate from the distillation column 2 from the condenser 8 to the primary side of the module 4.
なお本実施例では、単数の真空容器について述べたが、
本発明はこれに限定されるものではなく、蒸気圧縮器を
それぞれ、またはまとめて持つ複数の真空容器であって
も良い。Although this example describes a single vacuum container,
The present invention is not limited thereto, and may include a plurality of vacuum vessels each having a vapor compressor or a plurality of vacuum vessels collectively.
またモジュール４における浸透気化膜５は、通常供給液
温度が高い程、浸透量が増加するので、モジュール４に
供給される有機液体を加熱するための加熱器１３が通常
では管路１１に設けられる。Further, in the pervaporation membrane 5 in the module 4, the amount of permeation increases as the temperature of the supplied liquid increases, so a heater 13 for heating the organic liquid supplied to the module 4 is usually provided in the conduit 11. .
次にかかる本発明の装置の機能について、含水エタノー
ルからの水分離を例に説明する。Next, the function of the apparatus of the present invention will be explained using water separation from hydrous ethanol as an example.
含水エタノール、例えばエタノール９５ｋｇ、水５ｋｇ
の組成、が加熱器１３で加熱された後に管路１１を経て
浸透気化膜モジュール４の一次側に供給する。Hydrated ethanol, e.g. 95 kg of ethanol, 5 kg of water
The composition is heated by the heater 13 and then supplied to the primary side of the pervaporation membrane module 4 via the conduit 11.
すると、エタノール中の水分は浸透気化膜５に浸透し、
膜５の二次側に蒸気として取り出されるが、このとき水
と共に少量のエタノールが二次側に蒸気として浸透、気
化される。Then, the water in the ethanol permeates the pervaporation membrane 5,
It is taken out as steam to the secondary side of the membrane 5, and at this time, a small amount of ethanol permeates into the secondary side as steam and is vaporized together with water.
膜５の一次側からは水が分離されたエタノールが取り出
され、更に残存する水分を除去するために、次のモジュ
ール４゛における浸透気化膜５゛の一次側に供給され、
残存する水が除去された後に、例えばエタノール９４ｋ
ｇ、水１ｋｇの組成を有する実質的に無水のエタノール
１２が膜５′の一次側から取り出される。Ethanol from which water has been separated is taken out from the primary side of the membrane 5, and is supplied to the primary side of the pervaporation membrane 5' in the next module 4' in order to further remove remaining water.
After the remaining water has been removed, e.g. ethanol 94k
Substantially anhydrous ethanol 12 having a composition of 1 g and 1 kg of water is removed from the primary side of the membrane 5'.
一方、膜５および５”の二次側に浸透、気化された、例
えばエタノール１ｋｇ、水４ｋｇの組成の含エタノール
水は、蒸気圧縮機６を経て蒸気状態のままで蒸留塔２に
供給され、エタノール分離のための蒸留に付される。On the other hand, the ethanol-containing water having a composition of, for example, 1 kg of ethanol and 4 kg of water, which has permeated and vaporized into the secondary side of the membranes 5 and 5'', is supplied to the distillation column 2 in a vapor state via a vapor compressor 6. Subjected to distillation to separate ethanol.
そして蒸留塔２の頂部に設けたコンデンサー８からは、
例えばエタノール１ｋｇ、水１ｋｇの組成からなる留出
物が管路１０を経て、含水エタノール供給管路１１によ
り供給される含水アルコールに合併され、モジュール４
の一次側に供給される。From the condenser 8 installed at the top of the distillation column 2,
For example, a distillate having a composition of 1 kg of ethanol and 1 kg of water passes through a pipe 10 and is combined with hydrous alcohol supplied by a water-containing ethanol supply pipe 11.
is supplied to the primary side of the
上記のように、管路１１によって、エタノール９５ｋｇ
、水５ｋｇの９５％エタノールが供給されるので、管路
１０によってエタノール１ｋｇ、水１ｋｇが添加されて
も、エタノール９６ｋｇ 、水６ｋｇの９４％エタノー
ルとなるだけであり、蒸留塔２の留出物を添加したこと
によるエタノール濃度低下を最小附にすることができる
。As mentioned above, 95 kg of ethanol is
, 5 kg of water and 95% ethanol are supplied, so even if 1 kg of ethanol and 1 kg of water are added through pipe 10, only 96 kg of ethanol and 6 kg of water will become 94% ethanol, and the distillate in distillation column 2 The decrease in ethanol concentration due to the addition of ethanol can be minimized.
以上述べたように本発明によれば、浸透気化分離装置と
蒸留塔が組み合わされているので、浸透気化膜の二次側
に浸透、気化された蒸気を蒸留塔に供給し、蒸留により
有機液体中の水分を除去することができる。As described above, according to the present invention, since the pervaporation separation device and the distillation column are combined, the vapor that permeates the secondary side of the pervaporation membrane and is vaporized is supplied to the distillation column, and the organic liquid is The moisture inside can be removed.
従って本発明によれば、従来、処理に苦慮していた全有
機液体水から有機液体成分を分離して、廃棄される有機
液体量を極力低減することができる。Therefore, according to the present invention, it is possible to separate organic liquid components from all organic liquid water, which has conventionally been difficult to process, and to reduce the amount of organic liquid to be discarded as much as possible.
また、浸透気化膜の二次側の蒸気をそのまま蒸留塔に供
給するので、熱供給源７は蒸気状態を維持するに足る熱
を供給できれば良く、省エネルギー効果が大きい。In addition, since the steam on the secondary side of the pervaporation membrane is directly supplied to the distillation column, the heat supply source 7 only needs to supply enough heat to maintain the steam state, resulting in a large energy saving effect.
更に、二次側蒸気の供給によって、蒸留塔として従来の
ような大型蒸留塔を使用する必要がなく小型蒸留塔で良
いので、省エネルギー効果と共に、装置のコンパクト化
をはかることができる。Furthermore, by supplying the secondary side steam, there is no need to use a conventional large-scale distillation column as a distillation column, and a small-sized distillation column can be used, thereby saving energy and making the apparatus more compact.
図は本発明の実施例を示す概要図である。
１−浸透気化分離装置、２−・・蒸留塔、３−真空容器
、４．４″−浸透気化膜モジュール、５．５′−浸透気
化膜、６・−蒸気圧縮機、１〇−循環管路。The figure is a schematic diagram showing an embodiment of the present invention. 1 - Pervaporation separation device, 2 - Distillation column, 3 - Vacuum container, 4.4'' - Pervaporation membrane module, 5.5' - Pervaporation membrane, 6 - Vapor compressor, 10 - Circulation pipe Road.
Claims (1)
浸透気化分離装置と、該モジュールの二次側蒸気が供給
される蒸留塔からなり、該蒸留塔の留出物を前記モジュ
ールの一次側に循環する管路を設けたことを特徴とする
有機液体の分離装置。A pervaporation separation device consisting of a pervaporation membrane module placed in a vacuum container, and a distillation column to which the secondary side vapor of the module is supplied, and the distillate of the distillation column is circulated to the primary side of the module. 1. An organic liquid separation device characterized by having a conduit for separating the organic liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20148586A JPS6359308A (en) | 1986-08-29 | 1986-08-29 | Separation device for organic liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP20148586A JPS6359308A (en) | 1986-08-29 | 1986-08-29 | Separation device for organic liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6359308A true JPS6359308A (en) | 1988-03-15 |
Family
ID=16441843
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP20148586A Pending JPS6359308A (en) | 1986-08-29 | 1986-08-29 | Separation device for organic liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6359308A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0610775A1 (en) * | 1993-02-06 | 1994-08-17 | BASF Aktiengesellschaft | Process for separating liquid mixtures having an azeotropic point by combination of pervaporation and distillation |
| WO2001066236A3 (en) * | 2000-03-07 | 2001-11-29 | Fielding Chemical Technologies | Pervaporation apparatus and method |
| WO2009048335A1 (en) | 2007-10-12 | 2009-04-16 | Epcon Energy & Process Control As | Method for dewatering a mixture of mostly ethanol and water |
| EP2247370A1 (en) * | 2008-03-05 | 2010-11-10 | St1 Biofuels Oy | Method and apparatus for dewatering a mixture of ethanol and water |
-
1986
- 1986-08-29 JP JP20148586A patent/JPS6359308A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0610775A1 (en) * | 1993-02-06 | 1994-08-17 | BASF Aktiengesellschaft | Process for separating liquid mixtures having an azeotropic point by combination of pervaporation and distillation |
| WO2001066236A3 (en) * | 2000-03-07 | 2001-11-29 | Fielding Chemical Technologies | Pervaporation apparatus and method |
| WO2009048335A1 (en) | 2007-10-12 | 2009-04-16 | Epcon Energy & Process Control As | Method for dewatering a mixture of mostly ethanol and water |
| EP2247370A1 (en) * | 2008-03-05 | 2010-11-10 | St1 Biofuels Oy | Method and apparatus for dewatering a mixture of ethanol and water |
| JP2011513056A (en) * | 2008-03-05 | 2011-04-28 | エステー１・バイオフューエルズ・オサケユキテュア | Method and apparatus for dehydrating a mixture of ethanol and water |
| EP2247370A4 (en) * | 2008-03-05 | 2012-07-25 | St1 Biofuels Oy | Method and apparatus for dewatering a mixture of ethanol and water |
| US8608966B2 (en) | 2008-03-05 | 2013-12-17 | St1 Biofuels Oy | Method and apparatus for dewatering a mixture of ethanol and water |
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