JPS6394966A - Concentration and recovery of fermentation alcohol - Google Patents
Concentration and recovery of fermentation alcoholInfo
- Publication number
- JPS6394966A JPS6394966A JP61240850A JP24085086A JPS6394966A JP S6394966 A JPS6394966 A JP S6394966A JP 61240850 A JP61240850 A JP 61240850A JP 24085086 A JP24085086 A JP 24085086A JP S6394966 A JPS6394966 A JP S6394966A
- Authority
- JP
- Japan
- Prior art keywords
- alcohol
- line
- concentration
- extractant
- fermentation
- 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 109
- 238000011084 recovery Methods 0.000 title abstract description 7
- 238000000855 fermentation Methods 0.000 claims abstract description 53
- 230000004151 fermentation Effects 0.000 claims abstract description 53
- 238000000605 extraction Methods 0.000 claims abstract description 33
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 239000007864 aqueous solution Substances 0.000 claims abstract description 19
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 13
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 13
- 244000005700 microbiome Species 0.000 claims abstract description 10
- 238000001704 evaporation Methods 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims description 22
- 238000010438 heat treatment Methods 0.000 claims description 11
- 230000008020 evaporation Effects 0.000 claims description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 2
- 239000005977 Ethylene Substances 0.000 claims description 2
- DNZWLJIKNWYXJP-UHFFFAOYSA-N butan-1-ol;propan-2-one Chemical compound CC(C)=O.CCCCO DNZWLJIKNWYXJP-UHFFFAOYSA-N 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 239000001294 propane Substances 0.000 claims description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 2
- 239000004215 Carbon black (E152) Substances 0.000 claims 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 abstract description 4
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 abstract description 4
- 239000000243 solution Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000001476 alcoholic effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 241000588902 Zymomonas mobilis Species 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 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
- 238000000895 extractive distillation Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野）
この発明はアルコール発酵、アセトン−ブタノール発酵
などにより生成した発酵生産物を、発酵液から省エネル
ギー的にｉｅ縮し、回収する方法に関する。DETAILED DESCRIPTION OF THE INVENTION (Industrial Application Field) The present invention relates to a method for energy-saving ie condensation and recovery of fermentation products produced by alcohol fermentation, acetone-butanol fermentation, etc. from fermentation liquid.
（従来の技術）
一般に、微生物利用の発酵によるアルコール生産の場合
、目的とする発酵生産物の濃度が低いため（通常５〜ｆ
ｏｗ１％）、それをＣ縮分離することが要求されるが、
そのｅ縮分離に多大のエネルギーを必要とする。通常、
アルコール濃縮分離には蒸留法が使用されているが、近
年省エネルギー的な方法として超臨界流体またはそれに
近い状態の抽出剤を用いる高圧抽出法が提案されている
（特開昭５６−５６２０１号など）。(Prior art) In general, in the case of alcohol production by fermentation using microorganisms, the concentration of the target fermentation product is low (usually 5-f
ow1%), it is required to separate it by C condensation,
A large amount of energy is required for the e-condensation separation. usually,
Distillation is used to concentrate and separate alcohol, but in recent years a high-pressure extraction method using supercritical fluid or an extractant in a state close to it has been proposed as an energy-saving method (e.g., JP-A No. 56-56201). .
また、発酵槽における発酵生産速度を向上させつつ、高
濃度のアルコールを発酵槽から連続的に除去しながら発
酵させる減圧発酵法やフラッシュ発酵法が知られている
。Further, vacuum fermentation methods and flash fermentation methods are known in which fermentation is performed while continuously removing high-concentration alcohol from the fermenter while increasing the fermentation production rate in the fermenter.
（発明か解決しようとする問題点）
通常、従来の発酵法すなわち回分式発酵法又は固定化微
生物等を用いる連続発酵法により得られる発酵液中のア
ルコール濃度は５〜ｌｏｗｔ％である。この発酵液を特
開昭５６−５６２０１号記載の高圧抽出法により濃縮し
た場合、得られるアルコールの濃度は約７０〜８０ｗｔ
％であり、この後の工程における濃縮のため、さらにエ
ネルギーを必要とする。また、必要とする抽出剤の量も
多くなるという欠点かある。例えば、抽出剤として二酸
化炭素を使用しエタノールを抽出する場合エタノールの
二酸化炭素側の分配係数が低く、抽出エタノール１ｋｇ
当り二酸化炭素的Ｚｏｏ〜２００ｋｇを必要とするため
、抽出剤の循環、調整に多大のエネルギーを必要とする
。(Problems to be Solved by the Invention) Usually, the alcohol concentration in the fermentation liquid obtained by the conventional fermentation method, ie, the batch fermentation method or the continuous fermentation method using immobilized microorganisms, is 5 to low %. When this fermented liquid is concentrated by the high-pressure extraction method described in JP-A No. 56-56201, the concentration of alcohol obtained is approximately 70 to 80 wt.
%, and further energy is required for concentration in the subsequent step. Another drawback is that it requires a large amount of extractant. For example, when extracting ethanol using carbon dioxide as an extractant, the partition coefficient of ethanol on the carbon dioxide side is low, and 1 kg of extracted ethanol
Since approximately 200 kg of carbon dioxide is required per extraction, a large amount of energy is required for circulation and adjustment of the extractant.
一方、減圧発酵法やフラッシュ発酵法による生産物を通
常の蒸留法により濃縮すると、エタノール−水系の共清
点付近でピンチポイントがあるため、高濃度のアルコー
ル水溶液を供給しても蒸留塔の段数はあまり節減されず
、むしろ従来より蒸留塔留出液のエタノール濃度は低下
する場合もある結果となっている。すなわち減圧発酵法
あるいはフラッシュ発酵法の利点が生かされないことと
なった。On the other hand, when products produced by vacuum fermentation or flash fermentation are concentrated using normal distillation, there is a pinch point near the co-clearing point of the ethanol-water system, so even if a highly concentrated aqueous alcohol solution is supplied, the number of plates in the distillation column is limited. The result is that the ethanol concentration in the distillate from the distillation column may be lower than in the past, rather than being saved much. In other words, the advantages of the reduced pressure fermentation method or the flash fermentation method were not utilized.
（問題点を解決するための手段）
発明者らは上記した濃縮アルコールの生産方法の欠点を
克服するため鋭意研究を重ねた結果、高圧抽出工程に供
給するアルコールの濃度を発酵槽の後に設けた蒸発器に
より発酵槽の効率を低下させることなく１５〜４０ｗｔ
％に上昇させることにより、高圧抽出工程において抽出
分離されたアルコール濃度を８５〜９５）Ｌ％に濃縮て
き、かつ、抽出剤の必要量すなわち所要エネルギーの減
少を達成させることかできることを見出した。(Means for Solving the Problems) The inventors have conducted intensive research to overcome the drawbacks of the above-mentioned method for producing concentrated alcohol, and as a result, the inventors have developed a method to increase the concentration of alcohol supplied to the high-pressure extraction process after the fermentation tank. 15-40wt without reducing the efficiency of fermenter with evaporator
%, it has been found that the alcohol concentration extracted and separated in the high-pressure extraction step can be concentrated to 85-95) L%, and the required amount of extractant, that is, the required energy, can be reduced.
この発明において高圧抽出工程への供給アルコール濃度
を上昇させる方法は、発酵液中のアルコールを蒸発器に
より気相へ移行させ、アルコール分の少ない液を発酵槽
へ循環させることによって発酵効率の低下を極力抑えつ
つ、回収されたアルコールの濃度を上げようとする方法
である。In this invention, the method of increasing the alcohol concentration supplied to the high-pressure extraction process is to transfer the alcohol in the fermentation liquid to the gas phase using an evaporator, and to circulate the liquid with a low alcohol content to the fermenter, thereby reducing the fermentation efficiency. This method attempts to increase the concentration of recovered alcohol while suppressing it as much as possible.
この発明において発酵槽の蒸発器側より取り出された高
圧抽出器へ提供される水溶液中のアルコール濃度は通常
、１５〜４０ｗ［％であり、好ましくは２０〜３０ｗｔ
％である。In this invention, the alcohol concentration in the aqueous solution taken out from the evaporator side of the fermenter and provided to the high-pressure extractor is usually 15 to 40 w[%, preferably 20 to 30 wt].
%.
この供給アルコール濃度範囲の下限未満では高圧抽出操
作により得られた濃縮アルコールの濃度は８５ｗｔ％以
下となり、さらに濃縮するための別の操作（例えば、抽
出蒸留法、膜を利用する浸透気化法および吸着脱水法な
ど）が必要となり付加的なエネルギーか必要となる。さ
らに上記濃度範囲の下限未満では、高圧抽出操作に供給
される水溶液中のアルコールの濃度に反比例して必要な
抽出剤の量が急激に増大する０例えば高圧二酸化炭素を
抽出剤とするエタノール水溶液の濃縮の場合、供給エタ
ノール水溶液の濃度が１０ｗｔ％のとき、エタノール濃
度を８５〜９５ｗｔ％とするための抽出剤使用量は供給
エタノール水溶液が上記濃度範囲内にあるときの２〜４
倍、または供給エタノール水溶液濃度が５ｗｔ％のとき
エタノール濃度を７０〜８０ｗＬ％とするためには抽出
剤は４〜８倍量必要とする。ここで、抽出剤の量が増加
することは抽出剤を循環するためのエネルギーの増加、
高圧抽出設備のコストの増大等をまねくので望ましくな
い。Below the lower limit of this feed alcohol concentration range, the concentration of concentrated alcohol obtained by the high-pressure extraction operation is below 85 wt%, and other operations for further concentration (e.g., extractive distillation, membrane-based pervaporation, and adsorption) are required. (e.g. dehydration method), which requires additional energy. Furthermore, below the lower limit of the above concentration range, the amount of extractant required increases rapidly in inverse proportion to the concentration of alcohol in the aqueous solution supplied to the high-pressure extraction operation. In the case of concentration, when the concentration of the supplied ethanol aqueous solution is 10 wt%, the amount of extractant used to make the ethanol concentration 85 to 95 wt% is 2 to 4 when the supplied ethanol aqueous solution is within the above concentration range.
In order to increase the ethanol concentration to 70 to 80 wL% when the concentration of the aqueous ethanol solution supplied is 5 wt%, the amount of the extractant is required to be 4 to 8 times the amount. Here, an increase in the amount of extractant means an increase in energy for circulating the extractant,
This is undesirable because it increases the cost of high-pressure extraction equipment.
なお、高圧抽出工程への供給アルコールが４０ｗｔ％を
越える場合、蒸発器においてこの濃度にまで濃縮するた
めには発酵槽中の発酵液のアルコール濃度を上昇させね
ばならないが、これは発酵槽における発酵速度の低下を
まねき、発酵槽の効率が下がるのて好ましくない。また
このような濃度範囲の上限を越える発酵液を高圧抽出部
へ供給してももはや抽出、分離されるアルコールの濃度
は９０〜９５ｗｔ％で一定であり、アルコール濃度の向
上は望めない。Note that if the alcohol supplied to the high-pressure extraction process exceeds 40 wt%, the alcohol concentration of the fermented liquor in the fermenter must be increased in order to concentrate it to this concentration in the evaporator, but this is because the fermentation in the fermenter This is undesirable because it causes a decrease in speed and reduces the efficiency of the fermenter. Further, even if a fermentation liquid exceeding the upper limit of the concentration range is supplied to the high-pressure extraction section, the concentration of extracted and separated alcohol will remain constant at 90 to 95 wt%, and no improvement in alcohol concentration can be expected.
この発明において、上述した点景外は、通常の発酵法に
従って行われる。その好ましい実施態様を以下に述べる
。In this invention, the above-mentioned fermentation is performed according to a conventional fermentation method. A preferred embodiment thereof will be described below.
この発明において発酵槽の微生物として固定化微生物、
凝集性微生物又は浮遊性微生物が好ましく使用され、微
生物は発酵液が蒸発器に導入される前に分離され発酵槽
へ返送される。In this invention, immobilized microorganisms as microorganisms in the fermenter,
Flocculent or planktonic microorganisms are preferably used, the microorganisms being separated and returned to the fermenter before the fermentation liquor is introduced into the evaporator.
この発明において用いられる微生物としては。Microorganisms used in this invention include:
各種酵母例えばサツカロマイセス セレビシェ（Ｓａｃ
ｃｈｏｒｏｍｙｃｅｓ ｃｅｒｅｖｉｓｉａｅ）、サツ
カロマイセスラバラム（Ｓａｃｃｈｏｒｏｍｙｃｅｓ
ｕｖａｒａｓ）など、あるいは細菌例えばザイモモナス
モビリス（Ｚｇｏ■ｏｎａｓｌｃ）ｂｉｌｉｓ）など
が用いられる。Various yeasts such as Saccharomyces cerevisiae (Sac
chromyces cerevisiae), Sacchoromyces lavalum (Sacchoromyces
or bacteria such as Zymomonas mobilis.
この発明の蒸発工程において用いられる蒸発器は好まし
くは１段の加熱蒸発器あるいは加熱蒸発器のあとの減圧
蒸発器であり、発酵槽との組合せて２基（組）以上設置
することができる。また、加熱蒸発器には好ましくは棚
段等の手段が内蔵されていて、生成したアルコールを加
熱蒸発した発酵液中のアルコール濃度は下げられ１発酵
液が返送された先の発酵槽における発酵効率の低下を防
いでいる。The evaporator used in the evaporation process of the present invention is preferably a one-stage heating evaporator or a reduced pressure evaporator after the heating evaporator, and two or more units (sets) can be installed in combination with a fermenter. In addition, the heating evaporator preferably has a built-in means such as a tray, so that the alcohol concentration in the fermentation liquid obtained by heating and evaporating the generated alcohol is reduced, and the fermentation efficiency in the fermentation tank to which the fermentation liquid is returned is increased. This prevents a decline in
この発明において蒸発器において気相に移行させられた
アルコールを含む蒸気を断熱圧縮して昇温させて蒸発器
の加熱源として利用することにより、アルコールを含む
蒸気の凝縮のための冷却源及び加熱のための蒸気等の加
熱源の節減をはかることかできる。In this invention, the alcohol-containing vapor transferred to the gas phase in the evaporator is adiabatically compressed and heated, and used as a heating source for the evaporator, thereby providing a cooling source and a heating source for condensing the alcohol-containing vapor. It is possible to reduce heating sources such as steam.
この発明において高圧抽出工程で用いられる抽出剤は二
酸炭素またはエタン、エチレン、プロパン、プロピレン
等の炭化水素またはこれらの混合物がそれぞれの超臨界
状態または臨界点に近い状態の流体として使用される。In the present invention, the extractant used in the high-pressure extraction process is carbon dioxide, hydrocarbons such as ethane, ethylene, propane, propylene, or mixtures thereof, and is used as a fluid in a supercritical state or a state close to the critical point.
また抽出剤として二酸化炭素を用いる場合、発酵槽にお
いて発生する二酸化炭素を回収して利用することもでき
る。Furthermore, when carbon dioxide is used as an extractant, the carbon dioxide generated in the fermenter can be recovered and used.
この発明において高圧抽出処理における抽出剤／アルコ
ール水溶液供給液量（Ｓ／Ｆ）比（重量比）は１５以上
でよく、好ましくは１５〜２５の範囲である。Ｓ／Ｆ比
か１５未満ではアルコールの回収率が低くなり、上限は
特に制限はないがＳ／Ｆ比が２５以上になると回収率が
あまり上がらず抽出剤の量が増すため循環に動力が必要
となる。In the present invention, the extraction agent/alcohol aqueous solution supply amount (S/F) ratio (weight ratio) in the high-pressure extraction process may be 15 or more, preferably in the range of 15 to 25. If the S/F ratio is less than 15, the recovery rate of alcohol will be low, and there is no particular upper limit, but if the S/F ratio is 25 or more, the recovery rate will not increase much and the amount of extractant will increase, so power is required for circulation. becomes.
従来このような抽出剤によるアルコールの回収率を９０
％以上とする場合Ｓ／Ｆ比は２０以上である必要があっ
たのに対し、この発明においては、Ｓ／Ｆ比を極めて低
くてきる。Conventionally, the recovery rate of alcohol using such extractants was 90%.
% or more, the S/F ratio had to be 20 or more, whereas in the present invention, the S/F ratio is extremely low.
次にこの発明の好ましい実施態様を図面を参照して詳細
に説明する。Next, preferred embodiments of the present invention will be described in detail with reference to the drawings.
第１図はこの発明の一実施態様の工程図であり、図中１
は固定化微生物を充填した発酵槽であり、グルコース等
を含む発酵原料水溶液がライン２からライン３を通り、
供給されて連続的にアルコール発酵が行われる。５は二
酸化炭素の排出ラインてあり、この二酸化炭素は必要に
より回収装置（図示せず）を設置して回収し、次の高圧
抽出部の抽出剤として利用することもできる。FIG. 1 is a process diagram of one embodiment of this invention, and in the figure 1
is a fermenter filled with immobilized microorganisms, and a fermentation raw material aqueous solution containing glucose etc. passes from line 2 to line 3.
Alcoholic fermentation takes place continuously. Reference numeral 5 denotes a carbon dioxide discharge line, and this carbon dioxide can be recovered by installing a recovery device (not shown) if necessary, and used as an extractant in the next high-pressure extraction section.
一方発酵槽ｌの発酵液にはアルコールが蓄桔してくるが
、この発酵液はライン４から、棚段６ａ及び熱交換器６
ｂを内蔵する蒸発器６へ供給される。発酵液は内蔵熱交
換器６ｂにより加熱源８で加熱蒸発されて、アルコール
を１５〜４０ｗし％含む蒸気を生成し、この蒸気はライ
ン７から凝縮器１２へ送られ、冷却源１３により冷却さ
れ、アルコール水溶液としてライン２１より回収される
。On the other hand, alcohol accumulates in the fermentation liquid in the fermenter L, and this fermentation liquid is transferred from the line 4 to the tray 6a and the heat exchanger 6.
b is supplied to the evaporator 6 containing the evaporator 6. The fermentation liquor is heated and evaporated by a heating source 8 by a built-in heat exchanger 6b to produce steam containing 15 to 40% alcohol, and this steam is sent from a line 7 to a condenser 12 and cooled by a cooling source 13. , is recovered from line 21 as an alcohol aqueous solution.
１４は非凝縮性ガスのラインである。14 is a non-condensable gas line.
一方蒸発器６においてアルコール分を気相へ分離された
発酵液はアルコール分を実質的に含有しない発酵液であ
り、その一部又は大部分はライン９からライン１０を経
由して発酵槽１へ返送される。返送された発酵液によっ
て発酵槽ｌ中のアルコール濃度は低下し１発酵槽内の発
酵速度の低下が防止される。また蒸発器６から排出され
る発酵液の一部はライン９及びライン１１を経由して排
出されるか、又は他の発酵槽へ供給され発酵に付される
。On the other hand, the fermented liquor whose alcohol content has been separated into the gas phase in the evaporator 6 is a fermented liquor that does not substantially contain alcohol, and a part or most of it is sent to the fermenter 1 via line 9 and line 10. It will be sent back. The alcohol concentration in the fermenter 1 is reduced by the returned fermentation liquor, and a decrease in the fermentation rate in the 1 fermenter is prevented. Further, a part of the fermented liquid discharged from the evaporator 6 is discharged via lines 9 and 11, or is supplied to another fermentation tank and subjected to fermentation.
凝縮器１２で回収されたアルコール１５〜４０Ｗ［％を
含むアルコール水溶液はライン２１からポンプ１５によ
り昇圧されて抽出塔２２上部へ供給される。抽出塔２２
下部には、抽出剤が循環圧縮機２７およびライン２８を
経て供給される。抽出塔２２内部において、上部から降
下移動するアルコールを含む水溶液と下部から上昇移動
する抽出剤は向流的に接触して抽出剤は上昇移動しなが
ら水溶液中のアルコールを抽出し、抽出塔２２の上部か
らライン２３によって排出され分離塔２４へ導入される
。一方、抽出塔２２内を下降移動しながらアルコールを
抽出剤に奪われた水溶液は抽出塔２２下部からライン２
９により排出される。The alcohol aqueous solution containing 15 to 40 W [%] of alcohol recovered in the condenser 12 is pressurized by the pump 15 from the line 21 and is supplied to the upper part of the extraction column 22 . Extraction tower 22
In the lower part, extractant is supplied via a circulation compressor 27 and a line 28. Inside the extraction tower 22, the aqueous solution containing alcohol that descends from the top and the extractant that moves upward from the bottom come into contact with each other in a countercurrent manner, and the extractant moves upward to extract the alcohol in the aqueous solution. It is discharged from the top via line 23 and introduced into separation column 24 . On the other hand, the aqueous solution, whose alcohol has been taken away by the extractant while moving downward inside the extraction tower 22, flows from the lower part of the extraction tower 22 to the line 2.
It is discharged by 9.
アルコールを含む抽出剤はライン２３より分離塔２４に
導入する前に適宜減圧されるか、又は温度を調節され（
図示せず）、分離塔２４内でアルコールが液化分離され
る。アルコールは８５〜９５ｗし％以上に濃縮されてお
り、ライン２６より回収される。一方、アルコールを分
離した抽出剤は分離塔２４の上部からライン２５を経て
循環圧縮ｆｉ２７に送られる。Before the extractant containing alcohol is introduced into the separation column 24 from the line 23, the pressure is appropriately reduced or the temperature is adjusted (
(not shown), alcohol is liquefied and separated in the separation column 24. Alcohol is concentrated to 85-95% or more and is recovered from line 26. On the other hand, the extractant from which the alcohol has been separated is sent from the upper part of the separation column 24 to the circulation compression fi 27 via a line 25.
第２図はこの発明の他の実施態様を示すものである。FIG. 2 shows another embodiment of the invention.
同図において蒸発器６において加熱蒸発されて得られた
アルコールを含む蒸気はライン７を経て圧縮機１６で断
熱圧縮され、ライン１７を経て蒸発器内蔵熱交換器の加
熱源として使用され凝縮される。さらにライン１日より
冷却源１９を有する気液分離器２０に入り、不活性ガス
はライン３０より排出され、凝縮液はライン２１により
取り出されポンプ１５により昇圧されて抽出塔２２に送
られる。第３図は従来法のフローシートであり、発酵槽
ｌからライン４へ抜出されたアルコールを含む発酵液は
ポンプ１５により昇圧されて、ライン２１から抽出塔２
２へ供給される。第２図、第３図ともその他の構成は第
１図と同じである。第１図と同符号は同じものを示す。In the figure, alcohol-containing vapor obtained by heating and evaporating in the evaporator 6 passes through line 7, is adiabatically compressed in compressor 16, passes through line 17, and is used as a heating source for a heat exchanger with a built-in evaporator, where it is condensed. . Further, the gas enters a gas-liquid separator 20 having a cooling source 19 through line 1, inert gas is discharged through line 30, and condensate is taken out through line 21, pressurized by pump 15, and sent to extraction column 22. FIG. 3 is a flow sheet of the conventional method, in which the fermentation liquid containing alcohol is drawn out from the fermenter 1 to line 4, is pressurized by pump 15, and then sent from line 21 to extraction column 2.
2. The other configurations in both FIGS. 2 and 3 are the same as in FIG. 1. The same symbols as in FIG. 1 indicate the same things.
（発明の効果）
この発明によればアルコール発酵液からアルコールを省
エネルギー的に濃縮し、回収すことができ、濃度８５〜
９５ｗｔ％のアルコールを容易に得ることができる。ま
たこの発明によれば、例えば抽出剤として二酸化炭素を
用いた場合エタノール水溶液よりエタノールを抽出する
とき、同じ抽出効率を得るのに従来法では抽出剤／エタ
ノール供給液量（重量比）が２０前後必要であったもの
が１５前後まで下げることができ、またこれにより抽出
剤の循環に要する圧縮動力は大幅に削減できる。(Effect of the invention) According to this invention, alcohol can be concentrated and recovered from an alcoholic fermentation liquid in an energy-saving manner, and the concentration is 85 to 85%.
95 wt% alcohol can be easily obtained. Furthermore, according to the present invention, when extracting ethanol from an ethanol aqueous solution using carbon dioxide as an extractant, the conventional method would require an extractant/ethanol supply amount (weight ratio) of around 20 to obtain the same extraction efficiency. The required amount can be reduced to around 15,000 yen, and the compression power required for circulating the extractant can be significantly reduced.
（実施例）
次にこの発明の方法を実施例および比較例によりさらに
具体的に説明する。(Examples) Next, the method of the present invention will be explained in more detail with reference to Examples and Comparative Examples.
実施例
第１図に基づいてエタノール発酵液をｅ縮し、エタノー
ルの回収を行った。発酵槽ｌへ、ライン２．３を経て全
糖濃度２５ｗｔ％の原料を９０．４ｋｇ／ｈとラインＩ
Ｏを通って返還発酵液を９０．４ｋｇ／ｈとを供給した
。発酵槽ｌ内には固定化酵母が充填されており、３０℃
てエタノール発酵が行われた。発酵槽ｌ内のエタノール
濃度は６ｗｔ％となった。この発酵液はライン４を通り
、圧力４０ｍｍｌ１ｇ−ａｂｓに保持された蒸発器６に
導入されて加熱蒸発されアルコール分を含む蒸気がライ
ン７より凝縮器１２へ入り凝縮し、アルコール濃度３０
ｗｔ％のアルコール水溶液３４−０ｋｇ／ｈがライン２
１より得られた。一方、蒸発器６でアルコール分を蒸発
除去された発酵液はライン９を経て、ライン１０．３よ
り発酵槽ｌへ返還され、一部はライン１１を経て排出さ
れた。ライン２１から送り出されたアルコール水溶液は
ポンプ１５により昇圧されてライン２１を通り、内部圧
力１００ｋｇ／ｃｒｒｆＧ 、温度３８℃に保持されて
いる抽出塔２２の上部へ供給され、下部からライン２８
より二酸化炭素２６ＯＮゴ／ｈを供給してエタノールの
抽出が行われた。その結果ライン２６よりエタノール濃
度９５Ｗし％の製品が１０．５ｋｇ／ｈで得られた。Example Based on FIG. 1, the ethanol fermentation liquid was subjected to e-condensation and ethanol was recovered. 90.4 kg/h of raw material with a total sugar concentration of 25 wt% is transferred to fermenter L via line 2.3 and line I
90.4 kg/h of returned fermentation liquid was supplied through O. The fermenter l is filled with immobilized yeast and kept at 30°C.
Ethanol fermentation was performed. The ethanol concentration in the fermenter I was 6 wt%. This fermented liquid passes through line 4 and is introduced into evaporator 6 maintained at a pressure of 40 mm/1 g-abs, where it is heated and evaporated. Steam containing alcohol enters condenser 12 through line 7 and is condensed, with an alcohol concentration of 30
wt% alcohol aqueous solution 34-0 kg/h on line 2
Obtained from 1. On the other hand, the fermented liquor from which the alcohol content had been evaporated in the evaporator 6 was returned to the fermenter l via line 9 and line 10.3, and a portion was discharged via line 11. The alcohol aqueous solution sent out from the line 21 is pressurized by the pump 15, passes through the line 21, and is supplied to the upper part of the extraction column 22, which is maintained at an internal pressure of 100 kg/crrfG and a temperature of 38°C, and from the lower part to the line 28.
Ethanol extraction was performed by supplying 26 ON/h of carbon dioxide. As a result, a product with an ethanol concentration of 95 W and % was obtained from line 26 at a rate of 10.5 kg/h.
比較例
第３図に示す発酵槽ｌからのラインを抽出塔２２に直接
接続したフローシートに従い、発酵槽１および抽出塔２
２の運転条件は実施例と同じとしてエタノール発酵を行
った。Comparative Example Fermentation tank 1 and extraction tower 2 were prepared according to the flow sheet in which the line from fermentation tank 1 shown in FIG.
Ethanol fermentation was carried out under the same operating conditions as in Example 2.
発酵原料は実施例の２倍に希釈されライン２より発酵槽
ｌに供給され、ライン４よりエタノール濃度６ｗｔ％の
発酵液１６９．３ｋｇ／ｈが得られた。The fermentation raw material was diluted twice as much as in the example and was supplied to the fermenter 1 from line 2, and 169.3 kg/h of fermentation liquid with an ethanol concentration of 6 wt% was obtained from line 4.
これを高圧抽出操作に付し、エタノール濃度８０ｗｔ％
の製品が得られた。しかし抽出剤（二酸化炭素）の循環
量は１７０ＯＮｒｎ”／ｈであり、実施例の約６．５倍
必要てあった。This was subjected to high-pressure extraction operation, and the ethanol concentration was 80 wt%.
of products were obtained. However, the circulation rate of the extractant (carbon dioxide) was 170 ONrn''/h, which was about 6.5 times that of the example.
第１図はこの発明の一実施態様のフローシートであり、
第２図はこの発明の他の実施態様を示し、第３図は、従
来方法のフローシートを示す。
符号の説明
１−・・発酵槽、６・・・蒸発器、１２・・・凝縮器、
１５・・・ポンプ、１６・・・圧縮機、２０−・気液分
離器、２２・・・抽出塔、２４−・・分離塔、２７・・
・循環圧縮機
特許出願人 新燃料油開発技術研究組合代理人 弁理士
飯 １）敏 三
第１図FIG. 1 is a flow sheet of one embodiment of this invention,
FIG. 2 shows another embodiment of the present invention, and FIG. 3 shows a flow sheet of the conventional method. Explanation of symbols 1 - Fermenter, 6 - Evaporator, 12 - Condenser,
15--pump, 16--compressor, 20--gas-liquid separator, 22--extraction tower, 24--separation tower, 27--
・Circulating compressor patent applicant Representative of New Fuel Oil Development Technology Research Association Patent attorney Ii 1) Toshizo Figure 1
Claims (6)
い発酵液を蒸発処理してアルコール濃度１５〜４０ｗｔ
％のアルコール水溶液を分離し、ついで該アルコール水
溶液を抽出剤の存在下高圧抽出処理に付すことを特徴と
する発酵アルコールの濃縮回収方法。(1) The fermentation liquid extracted from the fermenter and containing substantially no microorganisms is evaporated to have an alcohol concentration of 15 to 40 wt.
% alcohol aqueous solution, and then subjecting the alcohol aqueous solution to high-pressure extraction treatment in the presence of an extractant.
ル等の発酵アルコールである特許請求の範囲第１項記載
の方法。(2) The method according to claim 1, wherein the alcohol is fermented alcohol such as ethanol or acetone-butanol.
圧蒸発処理との組合せである特許請求の範囲第１項記載
の方法。(3) The method according to claim 1, wherein the evaporation treatment is a reduced pressure evaporation treatment or a combination of a heating evaporation treatment and a reduced pressure evaporation treatment.
点に近い状態で存在する特許請求の範囲第１項記載の方
法。(4) The method according to claim 1, wherein the extractant for the high-pressure extraction treatment exists in a supercritical state or a state close to a critical point.
パン、プロピレン等の炭化水素、又はこれらの混合物で
ある特許請求の範囲第１項記載の方法。(5) The method according to claim 1, wherein the extractant is carbon dioxide, a hydrocarbon such as ethane, ethylene, propane, propylene, or a mixture thereof.
給量、Ｆ；アルコール水溶液供給量）（重量比）が１５
〜２５の範囲内である特許請求の範囲第１項記載の方法
。(6) S/F ratio (S: extractant supply amount, F: alcohol aqueous solution supply amount) (weight ratio) in high pressure extraction treatment is 15
25. The method of claim 1 within the range of .about.25.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61240850A JPS6394966A (en) | 1986-10-09 | 1986-10-09 | Concentration and recovery of fermentation alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61240850A JPS6394966A (en) | 1986-10-09 | 1986-10-09 | Concentration and recovery of fermentation alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6394966A true JPS6394966A (en) | 1988-04-26 |
| JPH031000B2 JPH031000B2 (en) | 1991-01-09 |
Family
ID=17065639
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61240850A Granted JPS6394966A (en) | 1986-10-09 | 1986-10-09 | Concentration and recovery of fermentation alcohol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6394966A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008132281A1 (en) * | 2007-04-25 | 2008-11-06 | St1 Biofuels Oy | Method and apparatus for preparing a mixture of ethanol and water by fermentation of fermentable raw material |
| JP2013518720A (en) * | 2010-02-09 | 2013-05-23 | ビュータマックス・アドバンスド・バイオフューエルズ・エルエルシー | Method for removing product alcohol from fermentation by evaporation under vacuum |
-
1986
- 1986-10-09 JP JP61240850A patent/JPS6394966A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008132281A1 (en) * | 2007-04-25 | 2008-11-06 | St1 Biofuels Oy | Method and apparatus for preparing a mixture of ethanol and water by fermentation of fermentable raw material |
| JP2013518720A (en) * | 2010-02-09 | 2013-05-23 | ビュータマックス・アドバンスド・バイオフューエルズ・エルエルシー | Method for removing product alcohol from fermentation by evaporation under vacuum |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH031000B2 (en) | 1991-01-09 |
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