JPS5941400B2 - Anhydrous ethanol manufacturing method and device - Google Patents
Anhydrous ethanol manufacturing method and deviceInfo
- Publication number
- JPS5941400B2 JPS5941400B2 JP57138244A JP13824482A JPS5941400B2 JP S5941400 B2 JPS5941400 B2 JP S5941400B2 JP 57138244 A JP57138244 A JP 57138244A JP 13824482 A JP13824482 A JP 13824482A JP S5941400 B2 JPS5941400 B2 JP S5941400B2
- Authority
- JP
- Japan
- Prior art keywords
- column
- pipe
- concentrating
- ethanol
- heat exchanger
- 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.)
- Expired
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【発明の詳細な説明】
本発明は、無水エタノールの製造方法および装置に関す
る。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method and apparatus for producing absolute ethanol.
更に詳しくは、本発明は、稀薄かつ泥状のエタノール原
料から、直接かつ、省エネルギー的に無水エタノールを
取得することのできる該製造方法｝よび装置に関する。
公知の稀薄原料からの無水アルコール製造方法および装
置は、直列に接続された濃縮塔、共沸蒸留塔｝よび溶剤
回収塔の濃縮塔に稀薄原料を供給し、各塔は夫々独立の
熱源で加熱され、塔頂塔気は夫々独立の冷却源で冷却さ
れている。More specifically, the present invention relates to a production method and apparatus that can directly and energy-savingly obtain anhydrous ethanol from a dilute and muddy ethanol raw material.
In the known method and apparatus for producing absolute alcohol from dilute raw materials, dilute raw materials are supplied to the concentrating columns of a concentrating column, an azeotropic distillation column, and a solvent recovery column that are connected in series, and each column is heated by an independent heat source. The air at the top of each tower is cooled by an independent cooling source.
このため特に濃縮塔で消費する熱量は、たとえば該公知
方法で取得される無水アルコールの熱量とほＹ等量にも
達し、そのコストは今日の省エネルギー時代においては
無視しえない程度のものである。特開昭５６−１１３７
１７号は、この問題に関し、濃縮塔を第１塔（粗濃縮塔
）と第２塔（濃縮塔）に分け、該第２塔の塔頂蒸気を圧
縮昇温させこの蒸気で第１塔の加熱に必要な水蒸気を発
生させ、該加熱後の凝縮液（９４〜９５％アルコール）
の一部を取得し（製品）、一部を該第２塔の還流液とす
る如く構成している。これによ只第１、２塔の所要加熱
量は、上記圧縮に必要な電力をスチーム換算してもな卦
公知の２塔式濃縮装置に軟べて約占量の熱量ですむこと
となつている。しかし、１該方法で得られる製品は９４
〜９５％アルコールであシ、共沸塔以下の熱源の合理化
は達成されていない。For this reason, the amount of heat consumed especially in the concentrating column reaches almost Y equivalent to the amount of heat of anhydrous alcohol obtained by the known method, and its cost cannot be ignored in today's energy-saving era. . Japanese Patent Publication No. 56-1137
Regarding this problem, No. 17 divides the concentration column into a first column (crude concentration column) and a second column (concentration column), compresses and heats the top vapor of the second column, and uses this vapor to feed the first column. Generate the steam necessary for heating, and condensate after heating (94-95% alcohol)
A part of the product is obtained (product), and a part is used as the reflux liquid of the second column. As a result, the amount of heat required for the first and second towers is approximately the same as that of the conventional two-column concentrator, even if the electricity required for the compression is converted into steam. ing. However, the product obtained by this method is 94
With ~95% alcohol, rationalization of the heat source below the azeotropic column has not been achieved.
また、２第２濃縮塔の塔頂圧縮蒸気（１１８℃）で、水
を加熱して蒸気を発生させることについては、エントロ
ピー的にみてなお合理化の余地がある。本発明者等は、
特開５６−１１３７１７号に｝いて残された上記二つの
課題を同時に解決すべく鋭意研究した。Furthermore, there is still room for rationalization in terms of entropy in heating water to generate steam using the top-compressed steam (118° C.) of the second concentrating column. The inventors,
In order to simultaneously solve the above two problems left behind in JP-A No. 56-113717, we conducted intensive research.
その結果、第１濃縮塔を加圧式としその塔頂蒸気（たと
えば１１５℃）で常圧塔である共沸蒸留塔卦よび溶剤回
収塔の缶を加熱し、加熱後の凝縮液を第２濃縮塔に供給
することによつて前記４の問題を解決し、第２濃縮塔の
塔頂蒸気を圧縮した被圧縮ガスでは、該塔の缶液（８３
゜０を加熱することによつて前記２の問題を解決した。
以上のように、本発明は省エネルギー的無水アルコール
の製造法と装置の提供を目的とする。以下本発明の構成
及び効果を図に基づいて詳細に説明する。図に｝いて、
例えば醗酵法によつて製造された醪のようなエタノール
原料（エタノール濃度１〜６ｍ０１％）は、粗濃縮塔Ａ
／）中段へポンプＰ−１および配管１を通じて供給され
る。As a result, the first concentrating column is pressurized, and its top vapor (for example, 115°C) is used to heat the cans of the azeotropic distillation column and the solvent recovery column, which are atmospheric pressure columns, and the heated condensate is transferred to the second concentrating column. By supplying the gas to the column to solve the problem 4 above and compressing the top vapor of the second concentrating column, the bottom liquid (83
Problem 2 above was solved by heating the temperature.
As described above, the present invention aims to provide an energy-saving method and apparatus for producing absolute alcohol. The configuration and effects of the present invention will be explained in detail below based on the drawings. Look at the diagram,
For example, ethanol raw material such as moromi produced by fermentation method (ethanol concentration 1 to 6 m01%) is stored in crude concentration column A.
/) Supplied to the middle stage through pump P-1 and piping 1.
その間該原料は熱交換器Ｅ−１（予熱器）を通じて予熱
される。塔Ａ内圧は２〜６ｋｇ／ＤＧ例えば２．４ｋ９
／〜Ｇで運転される。加熱は塔底に取付けられた熱交換
器Ｅ−２（加熱缶）を通じスチームを用いて行う。今、
塔頂蒸気の留出工タノール濃度を５３．７ｍ０１％とす
ると、その留出濃度は、２．４ｋｇ／ＣＩＬＧにおける
エタノール・水の平衡関係から１１５℃となる。この塔
頂蒸気は、配管２，４、共沸蒸留塔の熱交換器（加熱缶
）Ｅ−４および溶剤回収塔Ｄの熱交換器（加熱缶）Ｅ−
６を経由して凝縮され、凝縮液タンク、ポンプＰ−３お
よび配管５を経由℃て一部は、第２濃縮塔Ｂの中段に供
給▲れ残部は還流としてＡ塔に戻Ｖ．Ｂ塔の塔底液は配
管６およびポンプＰ−２を経て塔々頂へ戻される。Ｂ塔
内は常圧で運転される。エタノール濃度５３．７ｍ０１
％のＡ塔からの凝縮液はＢ塔内で濃縮され、塔頂蒸気の
エタノール濃度を７４．７ｍ０１（ｆ）とする。この蒸
気は、配管７、圧縮機Ｇ於よび熱交換器Ｅ−３通じて凝
縮され、ポンプＰ−４および配管８を経て一部は共沸蒸
留塔Ｃへ供給され、残部は塔Ｂへ還流として戻される。
塔Ｂの塔底液濃度は、エタノール２１ｍ０１０１）であ
り、その沸点は、常圧で８３゜Ｃ１他方、前記圧縮器Ｇ
で圧縮前の塔頂温度は留出濃度を７４．７ｍ０１０Ｉ）
とすれば７８゜Ｃであり、塔底温度は塔底のエタノール
濃度を２１ｍ０１％とすると８３℃でこれに塔内圧損失
による温度上昇｝よび熱伝導に必要な温度差を１５゜Ｃ
とすると圧縮後の蒸気の凝縮温度は９８゜Ｃとなわ、そ
の成績係数η＝１８．６となる。この成績係数を圧縮比
であられすと１．６となるが、常圧１塔式の場合に塔底
液を同じように圧縮蒸気で加熱しようとすると塔底温度
１００℃に必要な１５℃を加えた１１５℃が蒸気の圧縮
後の凝縮温度となジ、これに対応する成績係数は１０．
５、換算した圧縮比は２．８となる。したがつて２塔式
の方が圧縮比が小さくて所要動力も少くてすむ。他方、
１塔式と２塔式の還流比について考察すると、原料中エ
タノール濃度２．４３ｍ０１（Ｌ（平衡蒸気濃度２１．
７ｍ０１０／））、留出濃度を７４．７ｍ０１とすると
１塔式では最小還流比γｍは２．７５となる。他方、２
塔式では、Ｂ塔の原料濃度（５３．７ｍ０１％）（平衡
蒸気濃度６６，９ｍ０１％）留出濃度は７４．７ｍ０１
（Ｆｆ）であり、γｍは０．５９１となる。以上のよう
に１塔式と２塔式では還流量は同じ留出量に対して前者
は後者の４．６倍の還流量が必要となシ、従つて蒸気圧
縮機Ｇが処理する蒸気量も４．５倍となる。Ｂ塔の塔底
液は、前述のように配管６、ポンプＰ−２を経てＡ塔の
塔頂へ還流液として供給される。共沸蒸留塔Ｃは常圧で
運転される。該塔の缶（熱交換器Ｅ−４）は、前述のよ
うにＡ塔の蒸気で加熱され、塔頂近くには、前述のＢ塔
蒸気の凝縮液が配管８から、共沸溶剤が配管１０から、
卦よびデカンタ一Ｆからの共沸溶剤−エタノールが配管
１２から供給され、塔底の配管１１から無水エタノール
が抜き出される。塔底液の温度は７９℃（註、エタノー
ルの沸点）、熱交換器Ｅ一４に供給されるＡ塔々頂蒸気
の温度は前述のように１１５℃であるから、伝熱に必要
な温度差は、充分である。Ｃ塔の塔頂からは、三成分共
沸蒸気が配管９を経て熱交換器Ｅ−５（凝縮器）に導か
れ、冷却水で冷却され生じた凝縮液は、デカンタ一Ｆに
導かれる。該凝縮液は、デカンタ一で共沸溶剤に富む層
と水分に富む層に分けられ、前者は前述のように塔Ｃに
戻され、後者は、配管１３を経て溶剤回収塔へ供給され
る。溶剤回収塔Ｄは常圧で運転される。該塔の缶（熱交
換器Ｅ−６）は、前述のようにＡ塔の蒸気で加熱され、
塔頂近くには、前述のＣ塔デカンタ一の水に富む層液が
配管１３から、塔頂蒸気の凝縮液（溶剤）が配管１６か
ら供給され、塔底の配管１５から水が抜き出される。塔
底液の温度は１０００Ｃ（註水の沸点）、熱交換器Ｅ−
６に供給されるＡ塔々頂蒸気の温度は、前述のように１
１５゜Ｃであるから、伝熱に必要な温度差は充分である
。配管２４からの凝縮液の一部はデカンタ一Ｆに戻され
る。以上のように共沸蒸留塔Ｃ卦よび溶剤回収塔Ｄの缶
の熱源はＡ塔々頂蒸気であるから、公知方法のように独
立の加熱源を全く必要としない。また、本発明は、濃縮
塔を２塔式とした前述の特開昭５６−１１３７１７号と
比較しても、４Ａ塔の塔頂蒸気の潜熱が高度に利用され
ている点および、◎Ｂ塔々頂蒸気の圧縮ガスは、全量Ｂ
塔の缶（熱交換器Ｅ−３）の加熱に利用され、水から蒸
気を発生するのには利用されない点で４場合と同様に熱
利用が高度であわ、およびＯ独立の加熱源は、Ａ塔の缶
（熱交換器Ｅ−２）対するもののみでよいから熱管理が
容易である。Meanwhile, the raw material is preheated through heat exchanger E-1 (preheater). The internal pressure of tower A is 2 to 6 kg/DG, for example 2.4k9
It is driven at /~G. Heating is performed using steam through a heat exchanger E-2 (heating can) attached to the bottom of the column. now,
Assuming that the distillate ethanol concentration in the tower top vapor is 53.7 m01%, the distillate concentration will be 115° C. based on the equilibrium relationship between ethanol and water at 2.4 kg/CILG. This tower top vapor is transferred to the pipes 2 and 4, the heat exchanger (heating can) E-4 of the azeotropic distillation column, and the heat exchanger (heating can) E-4 of the solvent recovery column D.
6, a part of it is supplied to the middle stage of the second concentrating column B via the condensate tank, pump P-3 and pipe 5, and the rest is returned to column A as reflux. The bottom liquid of tower B is returned to the top of the towers via pipe 6 and pump P-2. The inside of the B column is operated at normal pressure. Ethanol concentration 53.7m01
% of the condensate from column A is concentrated in column B, resulting in an ethanol concentration of 74.7 m01(f) in the overhead vapor. This vapor is condensed through pipe 7, compressor G and heat exchanger E-3, and a portion is supplied to azeotropic distillation column C via pump P-4 and pipe 8, and the remainder is refluxed to column B. returned as .
The concentration of the bottom liquid in column B is ethanol 21m0101), and its boiling point is 83°C1 at normal pressure.
The tower top temperature before compression is 74.7m010I)
If the ethanol concentration at the bottom of the column is 21m01%, then the temperature at the bottom of the tower is 83°C, plus the temperature rise due to the pressure loss inside the tower, and the temperature difference required for heat conduction is 15°C.
Then, the condensation temperature of the vapor after compression is 98°C, and its coefficient of performance η=18.6. When this coefficient of performance is expressed as a compression ratio, it becomes 1.6, but if you try to heat the bottom liquid with compressed steam in the same way in the case of a normal-pressure one-column type, the 15°C required for a tower bottom temperature of 100°C will be 1.6. The added 115°C is the condensation temperature after compression of the vapor, and the corresponding coefficient of performance is 10.
5. The converted compression ratio is 2.8. Therefore, the two-column type has a smaller compression ratio and requires less power. On the other hand,
Considering the reflux ratio of the one-column type and the two-column type, the ethanol concentration in the raw material is 2.43 m01 (L (equilibrium vapor concentration 21.0 m).
7m010/)) and the distillate concentration is 74.7m01, the minimum reflux ratio γm is 2.75 in a one-column system. On the other hand, 2
In the column type, the raw material concentration in the B column (53.7 m01%) (equilibrium vapor concentration 66.9 m01%) and the distillate concentration is 74.7 m01
(Ff), and γm is 0.591. As mentioned above, the reflux amount for the one-column type and the two-column type is the same, but the former requires 4.6 times the reflux amount of the latter. Therefore, the amount of vapor processed by vapor compressor G is It also becomes 4.5 times. The bottom liquid of the B column is supplied as a reflux liquid to the top of the A column via the pipe 6 and the pump P-2, as described above. Azeotropic distillation column C is operated at normal pressure. The can of the column (heat exchanger E-4) is heated by the steam from column A as described above, and near the top of the column, the condensate of the vapor from column B is supplied from pipe 8, and the azeotropic solvent is supplied from pipe 8. From 10,
The azeotropic solvent-ethanol from the column and decanter 1F is supplied through a pipe 12, and anhydrous ethanol is extracted from a pipe 11 at the bottom of the tower. The temperature of the bottom liquid is 79°C (note: the boiling point of ethanol), and the temperature of the vapor at the top of the A column supplied to heat exchanger E-4 is 115°C as mentioned above, so the temperature required for heat transfer is The difference is sufficient. From the top of the C tower, the three-component azeotropic vapor is led to a heat exchanger E-5 (condenser) via a pipe 9, and the condensate produced by cooling with cooling water is led to a decanter 1F. The condensate is separated into an azeotropic solvent-rich layer and a water-rich layer in a decanter, the former being returned to column C as described above, and the latter being fed via pipe 13 to the solvent recovery column. Solvent recovery column D is operated at normal pressure. The can of the column (heat exchanger E-6) is heated by the steam of the A column as described above,
Near the top of the tower, the water-rich layer liquid from the C tower decanter is supplied from pipe 13, the condensate (solvent) of the tower vapor is supplied from pipe 16, and water is extracted from pipe 15 at the bottom of the tower. . The temperature of the bottom liquid is 1000C (the boiling point of water), and the heat exchanger E-
As mentioned above, the temperature of the A tower top steam supplied to 6 is 1.
Since the temperature is 15°C, the temperature difference necessary for heat transfer is sufficient. A portion of the condensate from the pipe 24 is returned to the decanter 1F. As mentioned above, since the heat source for the cans of the azeotropic distillation column C and the solvent recovery column D is the overhead steam of the A column, there is no need for any independent heating source unlike the known method. In addition, the present invention has the advantage that the latent heat of the top steam of the 4A column is utilized to a high degree, even compared to the above-mentioned Japanese Patent Application Laid-open No. 56-113717, which uses a two-column type concentrating column. The total amount of compressed gas of top steam is B
Similar to case 4, the heat utilization is high in that it is used to heat the column can (heat exchanger E-3) and not used to generate steam from water, and the O independent heating source is Heat management is easy because only the one for the can of tower A (heat exchanger E-2) is needed.
図は本発明の無水エタノール製造装置のフローシートを
示す。The figure shows a flow sheet of the anhydrous ethanol production apparatus of the present invention.
Claims (1)
装置を用いてエタノール原料から無水エタノールを製造
する方法において、濃縮塔を直列に２塔とし、第１濃縮
塔を加圧蒸留塔としてその塔頂蒸気を共に常圧で操作す
る共沸蒸留塔と溶剤回収塔の缶の加熱に使用できる如く
し、該使用後の凝縮液は、常圧で操作する第２濃縮塔の
中段へ供給し、該塔の塔頂蒸気は、該塔に付設した圧縮
機で圧縮して被圧縮ガスが該塔の缶の加熱に使用できる
如くし、該加熱後の凝縮液の一部を共沸蒸留塔へ他の一
部を第２濃縮塔々頂への環流液とし、第２濃縮塔の塔底
液を前記第１濃縮塔への環流液とすることを特徴とする
無水エタノールの製造方法。 ２ 特許請求の範囲第１項において、第１濃縮塔の塔内
圧力を２〜６ｋｇ／ｃｍ＾２Ｇとする方法。 ３ 特許請求の範囲第１項において、第２濃縮塔の塔頂
蒸気を２〜４ｋｇ／ｃｍ＾２Ｇまで圧縮する方法。 ４ 濃縮塔、共沸蒸留塔および溶剤回収塔からなる蒸留
装置であつてエタノール原料から無水エタノールを製造
するものにおいて、濃縮塔を加圧式粗濃縮塔Ａと該塔で
発生させたエタノールを濃縮する濃縮塔Ｂとし、該塔で
発生させたエタノール蒸気を圧縮する圧縮機Ｇ、共沸蒸
留塔Ｃおよび洗剤回収塔Ｄからなり、加圧式粗濃縮塔Ａ
には、原料供給管１、熱交換器Ｅ−２および缶液抜出管
３を有し、該塔と濃縮塔Ｂ間には、エタノール蒸気配管
２および４、熱交換器Ｅ−４およびＥ−６、凝縮液タン
クＶ、凝縮液配管５、凝縮液ポンプＰ−３、抜出液配管
６および還流液ポンプＰ−２を有し、濃縮塔Ｂと圧縮機
Ｇ間にはエタノール蒸気配管７を圧縮機Ｇと共沸蒸留塔
Ｃ間には圧縮ガス配管７′、熱交換器Ｅ−３、濃縮液配
管８、凝縮液ポンプＰ−４を濃縮塔Ｂと凝縮液ポンプＰ
−４間には濃縮液配管８を有し、共沸蒸留塔Ｃには熱交
換器Ｅ−４および無水エタノール抜出管１１を塔底部に
有し、該塔Ｃと溶剤回収塔Ｄ間には共沸蒸気配管９、熱
交換器Ｅ−５、デカンターＦ、デカンター抜出液配管１
２および１３を有し、溶剤回収塔Ｄには、熱交換器Ｅ−
６および水抜出管１５を塔底部に有し、該塔々頂とデカ
ンターＦ間には、溶剤蒸気配管１４、熱交換器Ｅ−７お
よび溶剤配管１６を熱交換器Ｅ−７と溶剤回収塔Ｄ間に
も溶剤配管１６を、それぞれ結合若しくは設置したこと
を特徴とする無水エタノールの製造装置。 ５ 原料供給管１と水抜出管１７を交差させた位置に熱
交換器Ｅ−１を有する特許請求の範囲第４項の装置。 ６ 加圧式粗濃縮塔Ａ、濃縮塔Ｂ、共沸蒸留塔Ｃおよび
溶剤回収塔Ｄにそれぞれ加熱缶としての熱交換器Ｅ−２
、Ｅ−３、Ｅ−４およびＥ−６を設置してなる特許請求
の範囲第４項の装置。[Claims] 1. A method for producing anhydrous ethanol from an ethanol raw material using a distillation apparatus consisting of a concentrating column, an azeotropic distillation column, and a solvent recovery column, in which two concentrating columns are connected in series, and the first concentrating column is As a pressurized distillation column, the top vapor can be used to heat the cans of the azeotropic distillation column and the solvent recovery column, both of which are operated at normal pressure, and the condensate after the use is transferred to the second condensation column, which is operated at normal pressure. The top vapor of the column is compressed by a compressor attached to the column so that the compressed gas can be used to heat the can of the column, and part of the condensate after heating is An anhydrous product characterized in that one part is sent to the azeotropic distillation column and the other part is used as the reflux liquid to the top of the second concentration column, and the bottom liquid of the second concentration column is used as the reflux liquid to the first concentration column. Method for producing ethanol. 2. The method according to claim 1, wherein the internal pressure of the first concentrating column is 2 to 6 kg/cm^2G. 3. A method according to claim 1, in which the top vapor of the second concentrating column is compressed to 2 to 4 kg/cm^2G. 4. In a distillation apparatus consisting of a concentrating column, an azeotropic distillation column, and a solvent recovery column that produces anhydrous ethanol from an ethanol raw material, the concentrating column is a pressurized crude concentrating column A and the ethanol generated in the column is concentrated. The concentrating column B consists of a compressor G that compresses the ethanol vapor generated in the column, an azeotropic distillation column C, and a detergent recovery column D, and a pressurized crude concentrating column A.
has a raw material supply pipe 1, a heat exchanger E-2, and a bottom liquid withdrawal pipe 3, and between the column and the concentration column B, there are ethanol vapor pipes 2 and 4, heat exchangers E-4 and E -6, has a condensate tank V, a condensate pipe 5, a condensate pump P-3, an extracted liquid pipe 6 and a reflux pump P-2, and an ethanol vapor pipe 7 between the concentrating column B and the compressor G. Between the compressor G and the azeotropic distillation column C, there is a compressed gas pipe 7', a heat exchanger E-3, a concentrate pipe 8, a condensate pump P-4, and a condensate pump P between the concentrator B and the condensate pump P.
The azeotropic distillation column C has a heat exchanger E-4 and an anhydrous ethanol extraction pipe 11 at the bottom of the column. are azeotropic steam piping 9, heat exchanger E-5, decanter F, decanter extraction liquid piping 1
2 and 13, and the solvent recovery column D has a heat exchanger E-
A solvent vapor pipe 14, a heat exchanger E-7 and a solvent pipe 16 are connected between the heat exchanger E-7 and the solvent recovery tower between the top of the tower and the decanter F. An apparatus for producing anhydrous ethanol, characterized in that solvent piping 16 is also connected or installed between D and D. 5. The apparatus according to claim 4, which has a heat exchanger E-1 at a position where the raw material supply pipe 1 and the water withdrawal pipe 17 intersect. 6 A heat exchanger E-2 as a heating can is installed in each of the pressurized crude concentration column A, concentration column B, azeotropic distillation column C, and solvent recovery column D.
, E-3, E-4 and E-6.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57138244A JPS5941400B2 (en) | 1982-08-09 | 1982-08-09 | Anhydrous ethanol manufacturing method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57138244A JPS5941400B2 (en) | 1982-08-09 | 1982-08-09 | Anhydrous ethanol manufacturing method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5927841A JPS5927841A (en) | 1984-02-14 |
| JPS5941400B2 true JPS5941400B2 (en) | 1984-10-06 |
Family
ID=15217436
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57138244A Expired JPS5941400B2 (en) | 1982-08-09 | 1982-08-09 | Anhydrous ethanol manufacturing method and device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5941400B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60226837A (en) * | 1983-12-01 | 1985-11-12 | Res Assoc Petroleum Alternat Dev<Rapad> | Apparatus for producing absolute ethanol and production of absolute ethanol |
| KR100348781B1 (en) * | 2000-08-17 | 2002-08-14 | 에스케이건설 주식회사 | Process controller for reducing energy in potable ethanol distillation |
| JP5313482B2 (en) * | 2007-10-31 | 2013-10-09 | 株式会社日本触媒 | Process for producing fatty acid alkyl ester and / or glycerin |
| US8350109B2 (en) * | 2010-12-13 | 2013-01-08 | Lummus Technology Inc. | Production of styrene from ethylbenzene using azeotropic vaporization and low overall water to ethylbenzene ratios |
-
1982
- 1982-08-09 JP JP57138244A patent/JPS5941400B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5927841A (en) | 1984-02-14 |
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