JPH07299301A - Alcohol distillation method - Google Patents
Alcohol distillation methodInfo
- Publication number
- JPH07299301A JPH07299301A JP6096456A JP9645694A JPH07299301A JP H07299301 A JPH07299301 A JP H07299301A JP 6096456 A JP6096456 A JP 6096456A JP 9645694 A JP9645694 A JP 9645694A JP H07299301 A JPH07299301 A JP H07299301A
- Authority
- JP
- Japan
- Prior art keywords
- tower
- column
- heating
- extraction
- 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
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 238000004821 distillation Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000000605 extraction Methods 0.000 claims abstract description 76
- 238000010438 heat treatment Methods 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 238000004807 desolvation Methods 0.000 claims description 14
- 238000009835 boiling Methods 0.000 claims description 12
- 238000000746 purification Methods 0.000 claims description 12
- 239000012535 impurity Substances 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 4
- 238000000855 fermentation Methods 0.000 abstract description 2
- 230000004151 fermentation Effects 0.000 abstract description 2
- 230000001476 alcoholic effect Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 239000001760 fusel oil Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 241000406799 Deto Species 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical class [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000002481 ethanol extraction Methods 0.000 description 1
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】この発明は、発酵後の醪（もろ
み）もしくは粗留アルコールからエタノール等の酒精を
蒸留，分離する酒精蒸留方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an alcohol distillation method for distilling and separating alcohol such as ethanol from fermented mash or crude alcohol.
【０００２】[0002]
【従来の技術】従来から、エタノールの蒸留法は、常圧
下のエタノール−水共沸組成に近い９５〜９６ｖｏｌ％
の含水エタノールを目的製品として、種々提案されてお
り、これに用いる蒸留装置も種々開発されている。この
ようなエタノールの蒸留装置として、図３に示すスーパ
ーアロスパス式蒸留装置がある。この装置を用い、つぎ
のようにして、醪タンク１内に収容された発酵後の醪
（エタノール濃度：約９ｖｏｌ％）を上記目的製品に蒸
留することができる。すなわち、まず、醪タンク１内の
醪を分縮器１２および熱交換器１３で沸点近くまで予熱
したのち低沸点分離塔２に送り、この低沸点分離塔２で
アセトアルデヒド，エステル類等の低沸点成分を分離し
醪塔３の塔頂に送る。この醪塔３内には、その塔底に加
熱用水蒸気Ａが吹き込まれており、この水蒸気により、
醪が塔頂から塔底に落下する間に、醪中のエタノールを
蒸留し、エタノール約４５ｖｏｌ％を含む蒸気を生成す
る。ついで、上記蒸気を醪塔３の塔頂から取り出して濃
縮塔５の塔底に送り、この濃縮塔５でほぼ製品濃度９５
ｖｏｌ％まで濃縮したのち、塔頂から取り出して分縮器
１４，全縮器１５に送り、ここで凝縮，液化して第２抽
出塔７に送る。2. Description of the Related Art Conventionally, the distillation method of ethanol is 95 to 96 vol% which is close to the ethanol-water azeotropic composition under normal pressure.
Various types of hydrous ethanol have been proposed as a target product, and various distillation apparatuses used for this have been developed. As such an ethanol distillation apparatus, there is a super allospath type distillation apparatus shown in FIG. Using this apparatus, the fermented mash (ethanol concentration: about 9 vol%) contained in the mash tank 1 can be distilled into the above-mentioned target product as follows. That is, first, the mash in the mash tank 1 is preheated by the partial condenser 12 and the heat exchanger 13 to a temperature close to the boiling point, and then sent to the low boiling point separation column 2, where the low boiling point of acetaldehyde, esters, etc. The components are separated and sent to the top of the turret 3. The steam A for heating is blown into the bottom of the tower 3 by this steam.
While the mash falls from the top to the bottom of the tower, the ethanol in the mash is distilled to produce a vapor containing about 45 vol% of ethanol. Then, the above vapor is taken out from the top of the turret tower 3 and sent to the bottom of the concentration tower 5, where the concentration of the product is almost 95%.
After concentrating to vol%, it is taken out from the top of the column and sent to the partial condenser 14 and the total condenser 15, where it is condensed and liquefied and sent to the second extraction column 7.
【０００３】上記第２抽出塔７内には、その塔底に加熱
用水蒸気Ａが吹込まれているとともに、その塔頂に、脱
酒精塔８の塔底から取り出された温水が送られてきてお
り、この温水と上記全縮器１５から送られてきた凝縮液
とを水蒸気により蒸発，気化し、この留出ガス（発生蒸
気）の一部を分縮器１８で液化して第２抽出塔７に還流
するとともに、エステル類等の微量の低沸点成分を全縮
器１９を経て第１抽出塔４に送る。このように、第２抽
出塔７では、濃縮塔５から濃度９５ｖｏｌ％で送られて
きたエタノールを１０ｖｏｌ％程度に希釈，抽出蒸留す
る。つぎに、希釈されたエタノールを、第２抽出塔７の
塔底から脱酒精塔８の塔頂に送る。この脱酒精塔８に
は、その上側に精留塔９が一連に形成されており、下側
の脱酒精塔８が回収部として作用し、上側の精留塔９が
濃縮部として作用する。そして、これら脱酒精塔８，精
留塔９で、上記希釈されたエタノールを再びほぼ製品濃
度９５ｖｏｌ％まで濃縮する。つぎに、この濃縮された
エタノールを精留塔９の塔頂から脱メタノール塔１０に
送り、この脱メタノール塔１０で微量のメタノールを分
離したのち、塔底から精製塔１７の塔頂に送り、精製塔
１１で最終的に精製し、製品として塔底から取り出す。
図において、各塔２〜１１内に表示された数字は温度
（℃）を示している。The steam A for heating is blown into the bottom of the second extraction tower 7, and the hot water taken out from the bottom of the desouring tower 8 is sent to the top of the tower. The hot water and the condensate sent from the total compressor 15 are vaporized and vaporized by the steam, and a part of this distillate gas (generated steam) is liquefied by the partial condenser 18 and the second extraction tower While refluxing to 7, a small amount of low boiling point components such as esters are sent to the first extraction column 4 via the total condenser 19. In this way, in the second extraction column 7, ethanol sent from the concentration column 5 at a concentration of 95 vol% is diluted to about 10 vol% and subjected to extractive distillation. Next, the diluted ethanol is sent from the bottom of the second extraction tower 7 to the top of the desolvation distillation tower 8. A rectification column 9 is formed in series on the upper side of the desolvation rectification column 8, the lower rectification column 8 acts as a recovery section, and the upper rectification column 9 acts as a concentration section. Then, the diluted ethanol is concentrated again in the desolvation tower 8 and the rectification tower 9 to a product concentration of 95% by volume. Next, this concentrated ethanol is sent from the top of the rectification tower 9 to the demethanol tower 10, and after a slight amount of methanol is separated by this demethanol tower 10, it is sent from the bottom to the top of the purification tower 17. The product is finally purified in the purification tower 11 and taken out from the bottom of the tower as a product.
In the figure, the number displayed in each of the towers 2 to 11 indicates the temperature (° C).
【０００４】上記蒸留装置において、第１抽出塔４に
は、低沸点分離塔２および第２抽出塔７（分縮器１８）
で分離された低沸点成分を含むエタノールが送り込ま
れ、温水塔６（濃縮塔５の回収部）および脱酒精塔８か
ら供給される温水によって抽出蒸留される。この加水抽
出されたエタノールは第１抽出塔４の塔底から受槽２３
を経て、低沸点分離塔２の塔頂へ還流される。一方、フ
ーゼル油等の高沸点成分を含むエタノールは第１抽出塔
４および濃縮塔５から抜き出されたのち、冷却器１６，
２４を経て分別器１７，２５に送られ、フーゼル油が分
離され、他成分が受槽２３を経て、低沸点分離塔２の塔
頂へ回収される。また、醪塔３で分離された水や固形物
は熱交換器１３を経て廃液される。図において、２０は
製品冷却器、２１，２２は加熱缶（熱交換器）、２６は
分縮器、２７，２８は全縮器、２９は温水受槽、３０，
３１はポンプである。In the above distillation apparatus, the low boiling point separation column 2 and the second extraction column 7 (decompressor 18) are included in the first extraction column 4.
Ethanol containing the low-boiling point component separated in (1) is fed and is extracted and distilled by the hot water supplied from the hot water tower 6 (recovery section of the concentrating tower 5) and the desolventizing tower 8. The water-extracted ethanol is transferred from the bottom of the first extraction tower 4 to the receiving tank 23.
And is refluxed to the top of the low boiling point separation column 2. On the other hand, ethanol containing a high boiling point component such as fusel oil is extracted from the first extraction column 4 and the concentration column 5, and then cooled by the cooler 16.
After being sent to the separators 17 and 25 via 24, the fusel oil is separated, and the other components are collected at the top of the low boiling point separation column 2 via the receiving tank 23. The water and solids separated in the turret 3 are passed through the heat exchanger 13 to be drained. In the figure, 20 is a product cooler, 21 and 22 are heating cans (heat exchangers), 26 is a partial condenser, 27 and 28 are total condensers, 29 is a hot water receiving tank, 30,
31 is a pump.
【０００５】このような蒸留装置では、蒸気消費量の節
減のため、図４に示すように、加熱缶２１の熱媒体とし
て、第２抽出塔７の塔頂の発生蒸気を利用する方法が用
いられている。この方法では、通常、第２抽出塔７の塔
頂の発生蒸気を加熱缶２１に送り、精製塔１１の塔底か
ら取り出した留出液（エタノール）を間接加熱したの
ち、加熱缶２１から取り出し、第２抽出塔７の塔頂に還
流することが行われている。In such a distillation apparatus, in order to reduce the steam consumption, as shown in FIG. 4, a method of using the vapor generated at the top of the second extraction column 7 as a heating medium of the heating can 21 is used. Has been. In this method, normally, the vapor generated at the top of the second extraction tower 7 is sent to the heating can 21, the distillate (ethanol) taken out from the bottom of the purification tower 11 is indirectly heated, and then taken out from the heating can 21. , Reflux to the top of the second extraction tower 7 is performed.
【０００６】[0006]
【発明が解決しようとする課題】しかしながら、上記蒸
留装置では、目的製品の純度を上げるため、精留塔９の
棚数を多くする場合には、精留塔７の塔圧が上がり［例
えば、通常行われているように、第２抽出塔７の棚数を
５０棚とし、塔圧を０．１５ｋｇｆ／ｃｍ2 とする場合
に、精留塔９の棚数を多くして１００棚にすると、脱酒
精塔８の塔頂（もしくは精留塔９の塔底）付近の圧力が
０．３ｋｇｆ／ｃｍ2 に、脱酒精塔８の塔底の圧力が
０．４ｋｇｆ／ｃｍ2 になり］、第２抽出塔７からの液
が脱酒精塔８に入りにくくなるという問題がある。しか
も、第２抽出塔７の塔頂の発生蒸気を加熱缶２１の熱源
とする場合には、上記発生蒸気と精製塔１１の塔底から
取り出された留出液（エタノール）との温度差が少な
く、上記加熱缶２１として伝熱面積の大きな熱交換器が
必要になり、コスト高になるという問題がある。さら
に、脱酒精塔８から取り出される温水の温度が高く、こ
の温水をそのまま第２抽出塔７の塔頂に送ると、塔頂で
フラッシュ状態になるという問題もある。However, in the above distillation apparatus, if the number of shelves in the rectification column 9 is increased in order to increase the purity of the target product, the column pressure of the rectification column 7 increases [eg, As usual, when the number of shelves in the second extraction tower 7 is 50 and the tower pressure is 0.15 kgf / cm 2 , the number of shelves in the rectification tower 9 is increased to 100. , The pressure near the top of the desolvation tower 8 (or the bottom of the rectification tower 9) becomes 0.3 kgf / cm 2 , and the pressure at the bottom of the desolvation tower 8 becomes 0.4 kgf / cm 2 ], There is a problem that it is difficult for the liquid from the second extraction tower 7 to enter the desolving spirit tower 8. Moreover, when the generated steam at the top of the second extraction tower 7 is used as the heat source of the heating can 21, the temperature difference between the generated steam and the distillate (ethanol) taken out from the bottom of the purification tower 11 is However, there is a problem that a heat exchanger having a large heat transfer area is required as the heating can 21 and the cost becomes high. Further, there is a problem that the temperature of the hot water taken out from the alcoholic distillation tower 8 is high, and if this hot water is sent to the top of the second extraction tower 7 as it is, a flash state occurs at the top of the tower.
【０００７】この発明は、このような事情に鑑みなされ
たもので、精留塔の棚数を多くした場合にも抽出塔（第
２抽出塔）からの液の入りが良く、しかも、加熱缶とし
て伝熱面積の大きな熱交換器を必要とせず、さらに、脱
酒精塔から送られた温水が抽出塔（第２抽出塔）の塔頂
でフラッシュ状態となることのない酒精蒸留方法の提供
を目的とする。The present invention has been made in view of the above circumstances. Even when the number of shelves in the rectification column is increased, the liquid from the extraction column (second extraction column) is well introduced and the heating can is used. As a result, there is no need for a heat exchanger with a large heat transfer area, and furthermore, a method for the distillation of alcohol is provided in which the hot water sent from the dewatering column does not flash at the top of the extraction column (second extraction column). To aim.
【０００８】[0008]
【課題を解決するための手段】上記の目的を達成するた
め、この発明の酒精蒸留方法は、発酵後の醪もしくは粗
留アルコールを醪塔で加熱し、この加熱により蒸発，気
化された留出ガスを醪塔から取り出して凝縮器に導入
し、この凝縮器内で凝縮，液化してこの凝縮液を加圧抽
出塔に導入し、この加圧抽出塔で上記凝縮液を加圧抽出
塔内の温水とともに加熱し、この加熱により蒸発，気化
された留出ガスから低沸点成分等の不純物を分離すると
ともに、この留出ガスを液化して加圧抽出塔内に還流
し、この不純物を分離した還流液を脱酒精塔に導入して
加熱し、この加熱により蒸発，気化された留出ガスを精
留塔に導入したのち、精留塔から取り出して精製塔に導
入し、上記精留塔内の留出ガスの一部を液化して脱酒精
塔に還流し、この還流された温水を加圧抽出塔に供給す
るようにしたという構成をとる。In order to achieve the above-mentioned object, the alcoholic distillation method of the present invention comprises heating the mash or crude distilled alcohol after fermentation in a mash tower, and evaporating and vaporizing the distilled liquor by this heating. The gas is taken out from the turret and introduced into a condenser, condensed and liquefied in the condenser and introduced into the pressurized extraction tower, and the condensed liquid is introduced into the pressurized extraction tower by the pressurized extraction tower. And the impurities such as low boiling point components are separated from the distillate gas evaporated and vaporized by this heating, and the distillate gas is liquefied and refluxed in the pressure extraction tower to separate the impurities. The refluxed liquid was introduced into the desolvation rectification column and heated, and the distillate gas evaporated and vaporized by this heating was introduced into the rectification column, and then taken out from the rectification column and introduced into the purification column. Part of the distillate gas in the inside is liquefied and returned to the desouring tower, and this reflux The the hot water take a configuration that has to be supplied to the pressurized pressure extraction Deto.
【０００９】[0009]
【作用】すなわち、この発明の酒精蒸留装置は、抽出塔
（従来例における第２抽出塔）を、例えば、この抽出塔
の塔頂から加熱缶に送る蒸気の流量を絞る等することに
より、加圧抽出塔にしている。したがって、この発明の
酒精蒸留装置では、加圧抽出塔の塔圧が脱酒精塔の塔圧
より大きくなり、目的製品の純度を上げるため精留塔の
棚数を多くする場合にも、加圧抽出塔の圧力で塔内の液
を精留塔内に入りやすくすることができる。しかも、こ
の流入の際に上記液は精留塔内にフラッシュ状態で流入
するため、脱酒精塔の能力が軽減され、省エネルギーに
なる。さらに、このように抽出塔を加圧抽出塔にするこ
とにより、その塔頂の発生蒸気を高温にすることができ
るため、この蒸気と精製塔の塔底から取り出される留出
液との温度差が大きくなり、この留出液の加熱缶の熱源
として充分に利用することができるようになる。したが
って、精製塔の加熱缶として伝熱面積の小さな熱交換器
を使用することができ、低コストになる。そのうえ、加
圧抽出塔の塔頂の発生蒸気を塔外に取り出して上記加熱
缶の熱媒体として利用する等したのち、脱酒精塔の温水
に混入させる場合には、この温水の温度が抽出塔の塔頂
温度くらいになり、蒸留に適したものになる。さらに、
加圧抽出塔の温度が高くなって不純物の排出が良くなる
うえ、蒸気量を多く流すことができ（例えば、同じ流速
でも常圧と０．５ｋｇｆ／ｃｍ2 とではその流量が異な
り、０．５ｋｇｆ／ｃｍ2 の方が常圧の場合より約１．
４倍の流量となる）、装置の処理能力をアップすること
ができる。In other words, the alcoholic distillation apparatus of the present invention can be added to the extraction column (the second extraction column in the conventional example) by, for example, reducing the flow rate of steam sent from the top of the extraction column to the heating can. It is a pressure extraction tower. Therefore, in the alcoholic distillation apparatus of the present invention, the column pressure of the pressure extraction column is larger than the column pressure of the desolvation column, and even when the number of shelves in the column is increased to increase the purity of the target product, the pressure is increased. The pressure in the extraction column can make it easier for the liquid in the column to enter the rectification column. Moreover, at the time of this inflow, since the liquid flows into the rectification column in a flush state, the capacity of the desolvation rectification column is reduced and energy is saved. Furthermore, by making the extraction tower a pressure extraction tower in this way, the steam generated at the top of the tower can be heated to a high temperature, so the temperature difference between this steam and the distillate taken out from the bottom of the purification tower is high. Becomes large and can be fully utilized as a heat source for the heating can of the distillate. Therefore, a heat exchanger having a small heat transfer area can be used as a heating can of the refining tower, resulting in low cost. In addition, when the generated steam at the top of the pressurized extraction tower is taken out of the tower and used as the heating medium of the heating can, etc. The temperature is about the column top temperature, which makes it suitable for distillation. further,
The temperature of the pressure extraction column becomes higher to improve the discharge of impurities, and a large amount of vapor can be made to flow (for example, even at the same flow rate, the flow rate differs between normal pressure and 0.5 kgf / cm 2 , About 5 kgf / cm 2 is about 1.
The flow rate is four times higher), and the processing capacity of the device can be increased.
【００１０】つぎに、この発明を実施例にもとづいて詳
しく説明する。Next, the present invention will be described in detail based on embodiments.
【００１１】[0011]
【実施例１】図１はこの発明に用いる蒸留装置の一実施
例の要部を示している。この実施例１では、精製塔１１
と加熱缶２１とを連結するエタノール取出用配管３７に
圧力指示調節計４０付き第１流量調節弁３９を取付け、
圧力指示調節計４０で第２抽出塔７の塔頂と加熱缶２１
の蒸気入口２１ａとを連結する第１配管３５内の圧力を
検出し、この検出結果により第１流量調節弁３９の流量
調節を行うようにしている。また、加熱缶２１の蒸気出
口２１ｂから第２配管３６を延ばし、この第２配管３６
を、脱酒精塔８の塔底と第２抽出塔７の塔頂とを連結す
る温水供給管４６に連結するとともに、第２配管３６と
分縮器４３（この分縮器４３は、第２配管３６内の蒸気
を凝縮，液化するためのものであり、戻し用配管４２を
介して第２配管３６に連結するとともに、全縮器４４に
連結している。上記分縮器４３，全縮器４４、配管４
１，４２等は、図４に示す従来例においても設けられて
いたものである）とを連結する蒸気取出用配管４１に第
２流量調節弁４５を取付けている。そして、上記第１お
よび第２の流量調節弁３９，４５の流量を絞り、第２抽
出塔７の塔圧を、図３に示す従来例（常圧のもの）より
も０．３５ｋｇｆ／ｃｍ2 アップして、０．５ｋｇｆ／
ｃｍ2 に設定し、これにより、第２抽出塔７を加圧抽出
塔にしている。すなわち、第１流量調節弁３９の流量を
絞る（従来の流量よりも少なくする）ことで、加熱缶２
１内のエタノール液面Ｂを低くして加熱缶２１内におけ
る伝熱面積を少なくし、これにより、第１配管３５内の
蒸気の流量を絞ることができる。また、第２の流量調節
弁４５の流量を絞ることにより、分縮器４３に送られる
蒸気の流量を少なくし、第１配管３５内の蒸気の流量を
絞ることができる。これにより、第２抽出塔７を加圧抽
出塔にしている。図において、３８は戻し用配管であ
る。それ以外の部分は、図３に示す従来例と同様であ
り、同様の部分には同じ符号を付している。Embodiment 1 FIG. 1 shows a main part of an embodiment of a distillation apparatus used in the present invention. In this Example 1, the purification tower 11
The first flow rate control valve 39 with the pressure indicating controller 40 is attached to the ethanol extraction pipe 37 that connects the heating can 21 with the heating can 21,
With the pressure indicating controller 40, the top of the second extraction tower 7 and the heating can 21
The pressure in the first pipe 35 connecting to the steam inlet 21a is detected, and the flow rate of the first flow rate control valve 39 is adjusted based on the detection result. Further, the second pipe 36 is extended from the steam outlet 21b of the heating can 21.
Is connected to a hot water supply pipe 46 that connects the bottom of the desolvation tower 8 and the top of the second extraction column 7, and the second pipe 36 and the dephlegmator 43 (the dephlegmator 43 is the second It is for condensing and liquefying the vapor in the pipe 36, and is connected to the second pipe 36 via the return pipe 42 and is also connected to the total compressor 44. Container 44, piping 4
1, 42, etc. are also provided in the conventional example shown in FIG. 4), and a second flow rate control valve 45 is attached to the steam extraction pipe 41. Then, the flow rates of the first and second flow rate control valves 39 and 45 are reduced, and the column pressure of the second extraction column 7 is set to 0.35 kgf / cm 2 more than that of the conventional example (normal pressure) shown in FIG. Up, 0.5kgf /
The pressure is set to cm 2 , whereby the second extraction tower 7 is a pressure extraction tower. That is, by reducing the flow rate of the first flow rate control valve 39 (decreasing the flow rate as compared with the conventional flow rate), the heating can 2
By lowering the ethanol liquid level B in 1 to reduce the heat transfer area in the heating can 21, the flow rate of steam in the first pipe 35 can be reduced. Further, by narrowing the flow rate of the second flow rate adjusting valve 45, the flow rate of steam sent to the demultiplexer 43 can be reduced and the flow rate of steam in the first pipe 35 can be narrowed. As a result, the second extraction tower 7 is a pressure extraction tower. In the figure, 38 is a return pipe. The other parts are the same as those of the conventional example shown in FIG. 3, and the same parts are denoted by the same reference numerals.
【００１２】上記実施例１によれば、第２抽出塔７の塔
圧が０．５ｋｇｆ／ｃｍ2 となり、脱酒精塔８の塔頂の
圧力より大きくなることから、精留塔９の棚数を多くす
る（例えば、１００棚にする）場合にも、第２抽出塔７
の塔圧で塔内の液が精留塔９内に流入しやすくなる。し
かも、第２抽出塔７の塔頂のベーパーが高温になること
から、精製塔９の塔底から取り出される留出液（エタノ
ール）との温度差が大きくなる。このため、精製塔１１
の加熱缶２１として、伝熱面積の小さな熱交換器を使用
することができにようになる。さらに、第２抽出塔７の
塔頂のベーパーを上記加熱缶２１を経たのち、温水供給
管４６に混入させるようにしたため、この温水供給管４
６の温水の温度が第２抽出塔７の塔頂温度（１００℃）
くらいになり、蒸留に適したものになる。そのうえ、両
流量調節弁３９，４５を第１および第２の配管３５，３
６に取付けないようにしているため、両配管３５，３６
内の蒸気等の流れが、従来と同様に、スムーズである。According to the above-mentioned Example 1, the column pressure of the second extraction column 7 is 0.5 kgf / cm 2 , which is larger than the pressure at the top of the desolvation rectification column 8, so that the number of rectification columns 9 is increased. Even when increasing the number (for example, 100 shelves), the second extraction tower 7
The liquid in the tower is likely to flow into the rectification tower 9 due to the tower pressure. Moreover, since the vapor at the top of the second extraction column 7 becomes high in temperature, the temperature difference with the distillate (ethanol) taken out from the bottom of the purification column 9 becomes large. Therefore, the purification tower 11
As the heating can 21, a heat exchanger having a small heat transfer area can be used. Further, since the vapor at the top of the second extraction tower 7 passes through the heating can 21 and is then mixed into the hot water supply pipe 46, the hot water supply pipe 4
The temperature of the hot water of 6 is the top temperature of the second extraction tower 7 (100 ° C)
It will be suitable for distillation. In addition, both flow rate control valves 39, 45 are connected to the first and second pipes 35, 3
Both pipes 35 and 36 are not attached to
The flow of steam, etc. inside is smooth, as in the past.
【００１３】[0013]
【実施例２】図２は実施例２の要部を示している。この
実施例２では、第２抽出塔７の塔頂と加熱缶２１の蒸気
入口２１ａとを連結する第１配管３５に流量調節弁４７
を取付けている。そして、上記流量調節弁４７で蒸気の
流量を絞り、第２抽出塔７の塔圧を、図２に示す従来例
（常圧のもの）よりも０．３５ｋｇｆ／ｃｍ2 アップし
て、０．５ｋｇｆ／ｃｍ2 に設定し、これにより、第２
抽出塔７を加圧抽出塔にしている。それ以外の部分は、
図１に示す従来例と同様であり、同様の部分には同じ符
号を付している。この実施例２によっても、上記実施例
１と同様の効果を奏する。Second Embodiment FIG. 2 shows the essential parts of the second embodiment. In the second embodiment, the flow control valve 47 is provided in the first pipe 35 that connects the top of the second extraction tower 7 and the steam inlet 21a of the heating can 21.
Is installed. Then, the flow rate of the steam is reduced by the flow rate control valve 47, and the tower pressure of the second extraction tower 7 is increased by 0.35 kgf / cm 2 from that of the conventional example (normal pressure) shown in FIG. Set to 5 kgf / cm 2 , and the second
The extraction tower 7 is a pressure extraction tower. Other than that,
This is the same as the conventional example shown in FIG. 1, and the same parts are denoted by the same reference numerals. The second embodiment also has the same effect as the first embodiment.
【００１４】[0014]
【発明の効果】以上のように、この発明の酒精蒸留方法
によれば、加圧抽出塔の塔圧が脱酒精塔の塔圧より大き
くなり、目的製品の純度を上げるため精留塔の棚数を多
くする場合にも、加圧抽出塔の圧力で塔内の液を精留塔
内に入りやすくすることができる。しかも、この流入の
際に、上記液は精留塔内にフラッシュ状態で流入するた
め、脱酒精塔の能力が軽減され、省エネルギーになる。
さらに、この酒精蒸留方法によれば、加圧抽出塔の塔頂
の発生蒸気を高温にすることができるため、この蒸気と
精製塔の塔底から取り出される留出液との温度差が大き
くなり、この留出液の加熱缶の熱源として充分に利用す
ることができるようになる。したがって、精製塔の加熱
缶として伝熱面積の小さな熱交換器を使用することがで
き、低コストになる。そのうえ、加圧抽出塔の塔頂の発
生蒸気を塔外に取り出して上記加熱缶の熱媒体として利
用する等したのち、脱酒精塔の温水に混入させる場合に
は、この温水の温度が抽出塔の塔頂温度くらいになり、
蒸留に適したものになる。さらに、加圧抽出塔の温度が
高くなって不純物の排出が良くなるうえ、蒸気量を多く
流すことができ、装置の処理能力をアップすることがで
きる。As described above, according to the alcohol distillation method of the present invention, the column pressure of the pressure extraction column becomes higher than the column pressure of the desolvation column, so that the purity of the target product is increased and the rack of the fractionation column is increased. Even when the number is increased, the pressure in the pressure extraction column can facilitate the liquid in the column to enter the rectification column. Moreover, at the time of this inflow, since the liquid flows into the rectification column in a flush state, the capacity of the desolvation rectification column is reduced and energy is saved.
Furthermore, according to this alcoholic distillation method, since the vapor generated at the top of the pressure extraction column can be heated to a high temperature, the temperature difference between this vapor and the distillate taken out from the bottom of the purification column becomes large. , Can be fully utilized as a heat source for a heating can of this distillate. Therefore, a heat exchanger having a small heat transfer area can be used as a heating can of the refining tower, resulting in low cost. In addition, when the generated steam at the top of the pressurized extraction tower is taken out of the tower and used as the heating medium of the heating can, etc. It will be about the top temperature of
It is suitable for distillation. Further, the temperature of the pressure extraction tower becomes high, the discharge of impurities is improved, and a large amount of vapor can be passed, so that the processing capacity of the apparatus can be improved.
【図１】この発明に用いられる蒸留装置の実施例１を示
す要部の説明図である。FIG. 1 is an explanatory view of a main part showing a first embodiment of a distillation apparatus used in the present invention.
【図２】実施例２を示す要部の説明図である。FIG. 2 is an explanatory diagram of a main part showing a second embodiment.
【図３】従来例を示す蒸留装置の説明図である。FIG. 3 is an explanatory view of a distillation apparatus showing a conventional example.
【図４】従来例の変形例の要部の説明図である。FIG. 4 is an explanatory diagram of a main part of a modified example of the conventional example.
１ 醪タンク ２ 低沸点分離塔 ３ 醪塔 ４ 第１抽出塔 ５ 濃縮塔 ６ 温水塔 ７ 第２抽出塔（加圧抽出塔） ８ 脱酒精塔 ９ 精留塔 １０ 脱メタノール塔 １１ 精製塔 ２１，２２ 加熱缶 DESCRIPTION OF SYMBOLS 1 Mug tank 2 Low boiling point separation tower 3 Miritsu tower 4 1st extraction tower 5 Concentration tower 6 Hot water tower 7 2nd extraction tower (pressurized extraction tower) 8 Destaining rectification tower 9 Fractionation tower 10 Demethanol tower 11 Purification tower 21, 22 heating cans
─────────────────────────────────────────────────────
─────────────────────────────────────────────────── ───
【手続補正書】[Procedure amendment]
【提出日】平成６年９月１４日[Submission date] September 14, 1994
【手続補正１】[Procedure Amendment 1]
【補正対象書類名】明細書[Document name to be amended] Statement
【補正対象項目名】００１３[Correction target item name] 0013
【補正方法】変更[Correction method] Change
【補正内容】[Correction content]
【００１３】[0013]
【実施例２】図２は実施例２の要部を示している。この
実施例２では、第２抽出塔７の塔頂と加熱缶２１の蒸気
入口２１ａとを連結する第１配管３５に流量調節弁４７
を取付けている。そして、上記流量調節弁４７で蒸気の
流量を絞り、第２抽出塔７の塔圧を、図２に示す従来例
（常圧のもの）よりも０．３５ｋｇｆ／ｃｍ2 アップし
て、０．５ｋｇｆ／ｃｍ2 に設定し、これにより、第２
抽出塔７を加圧抽出塔にしている。それ以外の部分は、
図１に示す従来例と同様であり、同様の部分には同じ符
号を付している。この実施例２によっても、上記実施例
１と同様の効果を奏する。また、上記実施例１では、圧
力指示調節計４０で第１配管３５内の圧力を検出し、こ
の検出結果により第１流量調節弁３９の流量調節を行う
ようにしているが、これに限定するものではなく、上記
圧力指示調節計４０で第１配管３５内の圧力を検出し、
この検出結果により第２流量調節弁４５の流量調節を行
うようにすることも考えられる。この場合にも、加熱缶
２１の圧力を上げ、第２抽出塔７を加圧抽出塔にするこ
とができるようになる。Second Embodiment FIG. 2 shows the essential parts of the second embodiment. In the second embodiment, the flow control valve 47 is provided in the first pipe 35 that connects the top of the second extraction tower 7 and the steam inlet 21a of the heating can 21.
Is installed. Then, the flow rate of the steam is reduced by the flow rate control valve 47, and the tower pressure of the second extraction tower 7 is increased by 0.35 kgf / cm 2 from that of the conventional example (normal pressure) shown in FIG. Set to 5 kgf / cm 2 , and the second
The extraction tower 7 is a pressure extraction tower. Other than that,
This is the same as the conventional example shown in FIG. 1, and the same parts are denoted by the same reference numerals. The second embodiment also has the same effect as the first embodiment. Further, in the first embodiment, the pressure in the first pipe 35 is detected by the pressure indicating controller 40, and the flow rate of the first flow rate adjusting valve 39 is adjusted based on the detection result, but the present invention is not limited to this. However, the pressure in the first pipe 35 is detected by the pressure indicating controller 40,
It is also possible to adjust the flow rate of the second flow rate adjusting valve 45 based on this detection result. Also in this case, the pressure of the heating can 21 can be increased to make the second extraction tower 7 a pressure extraction tower.
Claims (1)
コールを醪塔で加熱し、この加熱により蒸発，気化され
た留出ガスを醪塔から取り出して凝縮器に導入し、この
凝縮器内で凝縮，液化してこの凝縮液を加圧抽出塔に導
入し、この加圧抽出塔で上記凝縮液を加圧抽出塔内の温
水とともに加熱し、この加熱により蒸発，気化された留
出ガスから低沸点成分等の不純物を分離するとともに、
この留出ガスを液化して加圧抽出塔内に還流し、この不
純物を分離した還流液を脱酒精塔に導入して加熱し、こ
の加熱により蒸発，気化された留出ガスを精留塔に導入
したのち、精留塔から取り出して精製塔に導入し、上記
精留塔内の留出ガスの一部を液化して脱酒精塔に還流
し、この還流された温水を加圧抽出塔に供給するように
したことを特徴とする酒精蒸留方法。1. Fermented mash (moromi) or crude distilled alcohol is heated in a turret tower, and the distillate gas evaporated and vaporized by this heating is taken out from the turret tower and introduced into a condenser. The condensed liquid is condensed and liquefied into the pressurized extraction tower, and the condensed liquid is heated together with hot water in the pressurized extraction tower in the pressurized extraction tower, and the distillation gas evaporated and vaporized by this heating is heated. While separating impurities such as low boiling point components from the
The distillate gas is liquefied and refluxed in the pressure extraction column, and the reflux liquid from which the impurities have been separated is introduced into the desolvation rectification column and heated, and the distillation gas evaporated and vaporized by this heating is rectified in the rectification column. After being introduced into the rectification column, it is taken out from the rectification column and introduced into the purification column, and a part of the distillate gas in the rectification column is liquefied and refluxed to the desolvation rectification column. A method for distilling alcohol which is characterized in that it is supplied to.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP09645694A JP3648267B2 (en) | 1994-05-10 | 1994-05-10 | Alcoholic distillation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP09645694A JP3648267B2 (en) | 1994-05-10 | 1994-05-10 | Alcoholic distillation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07299301A true JPH07299301A (en) | 1995-11-14 |
| JP3648267B2 JP3648267B2 (en) | 2005-05-18 |
Family
ID=14165534
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP09645694A Expired - Fee Related JP3648267B2 (en) | 1994-05-10 | 1994-05-10 | Alcoholic distillation method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3648267B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010506574A (en) * | 2006-10-18 | 2010-03-04 | ゲーエーアー・ヴィーガント・ゲーエムベーハー | Plant for the distillation of drinking alcohol, especially whiskey |
| CN116873885A (en) * | 2023-07-12 | 2023-10-13 | 湖北三峡实验室 | Method for deep dearsenification of high-purity yellow phosphorus through reactive distillation |
-
1994
- 1994-05-10 JP JP09645694A patent/JP3648267B2/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010506574A (en) * | 2006-10-18 | 2010-03-04 | ゲーエーアー・ヴィーガント・ゲーエムベーハー | Plant for the distillation of drinking alcohol, especially whiskey |
| JP4773563B2 (en) * | 2006-10-18 | 2011-09-14 | ゲーエーアー・ヴィーガント・ゲーエムベーハー | Plant for the distillation of drinking alcohol, especially whiskey |
| CN116873885A (en) * | 2023-07-12 | 2023-10-13 | 湖北三峡实验室 | Method for deep dearsenification of high-purity yellow phosphorus through reactive distillation |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3648267B2 (en) | 2005-05-18 |
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