JPH0763561B2 - Distillation method of acetone, butanol and ethanol fermentation broth - Google Patents
Distillation method of acetone, butanol and ethanol fermentation brothInfo
- Publication number
- JPH0763561B2 JPH0763561B2 JP61255859A JP25585986A JPH0763561B2 JP H0763561 B2 JPH0763561 B2 JP H0763561B2 JP 61255859 A JP61255859 A JP 61255859A JP 25585986 A JP25585986 A JP 25585986A JP H0763561 B2 JPH0763561 B2 JP H0763561B2
- Authority
- JP
- Japan
- Prior art keywords
- butanol
- tower
- acetone
- water
- ethanol
- 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 - Lifetime
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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Description
【発明の詳細な説明】 産業上の利用分野 本発明はアセトン，ブタノール及びエタノールの発酵液
（以下ABE発酵液という）の蒸留法に関する。TECHNICAL FIELD The present invention relates to a method for distilling a fermentation broth of acetone, butanol and ethanol (hereinafter referred to as ABE fermentation broth).
従来技術及び問題点 従来ABE発酵液からアセトン，ブタノール及びエタノー
ルを回収するには発酵液を蒸留してこれら３成分と水か
らなる混合物を得てこれを精留することによって各成分
を分離し製品を得ている。蒸留には多くのエネルギーを
要し、又各成分は純度の高い製品が求められているが発
酵液中には多くの不純物が含まれていて分離しにくい。Conventional technology and problems Conventionally, in order to recover acetone, butanol and ethanol from the ABE fermentation broth, the fermentation broth is distilled to obtain a mixture of these three components and water. Is getting Distillation requires a lot of energy, and each component requires a product with high purity, but the fermentation liquor contains many impurities and is difficult to separate.
従来この３成分の分離には発酵液に水蒸気を加えて３成
分を揮発させ蒸気と共に排出し各成分と水との共沸混合
物を形成させ各成分を分離している。例えば発酵液に水
蒸気を加えてアセトン，ブタノール，エタノール及び水
からなる蒸気を排出させてブタノール塔に導きブタノー
ルと水の共沸混合物を形成排出させて濃縮し、分離器に
導入して２層に分離し上層液はブタノール塔回収部へ戻
し下層液は醪塔へ循環し、ブタノールをブタノール塔の
塔底から回収している。Conventionally, in the separation of these three components, steam is added to the fermentation liquor to volatilize the three components and discharge them together with the steam to form an azeotropic mixture of each component and water to separate each component. For example, steam is added to the fermentation broth to expel steam consisting of acetone, butanol, ethanol and water to lead to the butanol tower to form and expel an azeotropic mixture of butanol and water, which is then concentrated and introduced into a separator to form two layers. The separated upper layer liquid is returned to the butanol tower recovery section, and the lower layer liquid is circulated to the mortar tower to recover butanol from the bottom of the butanol tower.
この方法によれば多くのエネルギー、多量の冷却水を要
する。This method requires a lot of energy and a lot of cooling water.
又従来発酵液中の揮発性の有機酸、還元性物質は上記３
成分の純度に影響を与えるので発酵液にアルカリを加え
て中和することにより醪塔から揮発排出させない方法が
知られているが、多量のアルカリが消費される。Moreover, the volatile organic acids and reducing substances in the conventional fermentation broth are the above 3
It is known to add alkali to the fermentation liquor to neutralize the fermentation liquor to prevent volatilization and discharge from the mortar, since it affects the purity of the components, but a large amount of alkali is consumed.
問題点を解決するための手段 本発明によれば発酵液を醪塔に供給して蒸留する前に発
酵液を蒸留廃液で予熱し、醪塔の塔頂から排出される３
成分と水とからなる留出液を蒸留塔（以下ブタノール塔
という）の上部に供給し、ブタノール塔の中央部に設け
たブタノールと水の混合液貯留部にブタノールと水の混
合液を貯留しその上層液をブタノール回収部へ送り、下
層液を醪塔へ循環することによってエネルギーの節約を
計ることができる。Means for Solving the Problems According to the present invention, the fermented liquor is preheated with the distillation waste liquid before being fed to the turret and distilled, and discharged from the top of the turret.
A distillate composed of components and water was supplied to the upper part of a distillation column (hereinafter referred to as butanol column), and a butanol / water mixture was stored in a butanol / water mixture storage section provided in the center of the butanol column. Energy can be saved by sending the upper layer liquid to the butanol recovery section and circulating the lower layer liquid to the turret.
さらに醪塔の発酵液供給段の上に精留部を設けその上部
に苛性ソーダ溶液を供給することによって製品の純度を
上げることができる。Further, by providing a rectification section on the fermentation liquid supply stage of the turret and supplying a caustic soda solution to the upper section, the purity of the product can be increased.
即ち本発明は蒸留廃液によって予備加熱したABE発酵液
を醪塔（Ｍ塔という）に供給し、アセトン，ブタノー
ル，エタノール及び水からなる留出液をブタノール塔
（Ｂという）に導き、Ｂ塔にはその中央部にブタノール
と水の混合液貯留部を設けて上層液をブタノール回収部
へ送り、下層液をＭ塔へ循環させることを特徴とするAB
E発酵液の蒸留法に関する。That is, in the present invention, the ABE fermentation liquor preheated by the distillation waste liquid is supplied to a mash tower (referred to as M tower), and a distillate composed of acetone, butanol, ethanol and water is introduced to a butanol tower (referred to as B), and then to a B tower. AB is characterized by providing a butanol / water mixture storage section at its central portion, sending the upper layer solution to the butanol recovery section, and circulating the lower layer solution to the M tower AB
E Distillation method of fermentation liquid.
本発明の理解を容易にするために第１図に蒸留装置を示
す。この図によって本発明方法を詳細に説明する。A distillation apparatus is shown in FIG. 1 to facilitate understanding of the present invention. The method of the present invention will be described in detail with reference to this drawing.
発酵液は熱交換器５で予熱されＭ塔１に供給されＭ塔下
部より蒸気が供給され、アセトン，ブタノール及びエタ
ノールの３成分（以下ABE3成分という）と水の混合蒸気
が塔頂より排出される。The fermented liquor is preheated in the heat exchanger 5 and supplied to the M tower 1 and steam is supplied from the lower part of the M tower, and a mixed vapor of acetone, butanol and ethanol (hereinafter referred to as ABE3 component) and water is discharged from the top of the tower. It
発酵液供給段の上部に苛性ソーダ液供給口を設けて必要
により苛性ソーダ液を供給する。苛性ソーダは５〜20％
の濃度の液が用いられる。この添加によって発酵液中の
揮発性有機酸、アセトアルデヒド等の還元性物質をＭ塔
上部精留部分で中和して揮発性を失わせ副生物をＭ塔塔
頂から排出しないようにすることができ、製品の純度向
上がもたらされ、ブタノール塔２の脱水操作が簡単とな
る。A caustic soda solution supply port is provided above the fermentation solution supply stage to supply caustic soda solution as needed. 5-20% of caustic soda
A liquid having a concentration of is used. By this addition, it is possible to neutralize reducing substances such as volatile organic acids and acetaldehyde in the fermentation broth in the upper rectification part of the M tower to lose volatility and prevent the by-products from being discharged from the top of the M tower. As a result, the purity of the product is improved, and the dehydration operation of the butanol tower 2 is simplified.
苛性ソーダをＭ塔上部精留部に添加することにより苛性
ソーダの使用量が発酵液全体を中和するときの使用量よ
りはるかに少くて済み経済的である。苛性ソーダは蒸発
しないからＭ塔塔底から排出される。By adding caustic soda to the rectification section of the upper part of the M tower, the amount of caustic soda used is much smaller than the amount used when neutralizing the entire fermentation liquor, which is economical. Since caustic soda does not evaporate, it is discharged from the bottom of the M tower.
Ｍ塔１の塔底からは蒸留廃液が排出され、この廃液の熱
によって発酵液が熱交換器５で予熱される。Distillation waste liquid is discharged from the bottom of the M tower 1, and the fermentation liquid is preheated in the heat exchanger 5 by the heat of this waste liquid.
Ｍ塔頂から排出される蒸気は熱交換器により凝縮した後
一部Ｍ塔へ還流させ一部はブタノール塔（Ｂ塔）２の上
部に供給される。Ｍ塔頂の操作条件は通常90℃で還流比
１である。The vapor discharged from the top of the M tower is condensed by a heat exchanger and then partly refluxed to the M tower and partly supplied to the upper part of the butanol tower (B tower) 2. The operating conditions at the top of the M tower are usually 90 ° C. and a reflux ratio of 1.
Ｍ塔から留出してＢ塔上部に送られた留出液は精留され
ブタノールより軽い成分は塔頂から排出される。The distillate distilled from the M tower and sent to the upper part of the B tower is rectified and components lighter than butanol are discharged from the top of the tower.
Ｂ塔においてはその中央部にブタノール貯留部15を設
け、ここにブタノールと水の混合物が貯留しブタノール
に水が溶解した層と、水にブタノールが溶解した層に分
離する。液中にこの２層が混在する限り最低共沸混合物
を作り沸点は92.6℃前後であってその蒸気組成はブタノ
ール57.6％、水42.4％である。In the tower B, a butanol storage portion 15 is provided in the central portion thereof, and a mixture of butanol and water is stored therein, and a layer in which water is dissolved in butanol and a layer in which butanol is dissolved in water are separated. As long as these two layers are mixed in the liquid, the lowest azeotrope is formed and the boiling point is around 92.6 ° C, and the vapor composition is 57.6% butanol and 42.4% water.
共沸温度92.6℃付近でも前記２層は比重の差が大きいの
で静置することによって上層液18及び下層液19の２層に
分離できる。この性質を利用して２層を分離するために
例えば第２図に示すような貯留部をブタノール塔の中央
部に設け必要量に見合う下層液のみその温度で醪塔に移
送し上層は溢流管17を通してＢ塔下部へ送られブタノー
ルが回収される。つまりＢ塔においては、高沸点留分が
連続的に除去されている状態で蒸留が行われるため、低
沸点成分の蒸留を少量の蒸気量で行うことができる。Even when the azeotropic temperature is around 92.6 ° C., the two layers have a large difference in specific gravity, so that the two layers, the upper layer liquid 18 and the lower layer liquid 19, can be separated by standing. In order to separate the two layers by utilizing this property, for example, a storage part as shown in FIG. 2 is provided in the central part of the butanol column, and only the lower layer liquid corresponding to the required amount is transferred to the dairy tower at that temperature and the upper layer overflows. It is sent to the lower part of the B tower through a pipe 17 and butanol is recovered. That is, in the B tower, the distillation is performed in a state where the high boiling fraction is continuously removed, so that the low boiling component can be distilled with a small amount of vapor.
Ｂ塔のブタノール貯留部15は上下を仕切る仕切り板16及
び貯留したブタノール濃縮液をＢ塔回収部へ送る溢流管
17が板を貫通して設けられ、板は下層液取出口が最下部
となるように若干傾斜して設けられる。The butanol storage section 15 of the B tower is a partition plate 16 for partitioning the upper and lower parts and an overflow pipe for sending the stored butanol concentrate to the B tower recovery section.
17 is provided so as to penetrate the plate, and the plate is provided with a slight inclination so that the lower layer liquid outlet is at the bottom.
ブタノールと水の２層の関係は第３図に示される。ブタ
ノールと水の均一相の範囲は比較的小さく、図において
均一相以外の範囲ではその温度で静置すれば２相に分離
し、上層と下層の量の比はx2−x1/x3−x1,及びx3−x2/x
3−x1〔x1,x2,x3はそれぞれ水過剰中のブタノール濃
度、全溶液中のブタノール濃度、ブタノール過剰中のブ
タノール濃度（いずれも重量％）〕で表わされる。The relationship between the two layers of butanol and water is shown in FIG. The range of the uniform phase of butanol and water is relatively small, and in the range other than the uniform phase in the figure, if it is allowed to stand at that temperature, it will separate into two phases, and the ratio of the amount of the upper layer to the lower layer will be x 2 −x 1 / x 3 −x 1 and x 3 −x 2 / x
3 −x 1 [x 1 , x 2 and x 3 are respectively represented by butanol concentration in excess water, butanol concentration in total solution, butanol concentration in excess butanol (all are wt%)].
Ｍ塔からＢ塔への留出液中の水分量が多い程下層液の量
は増加し、貯留部が設けられる場合下層液量が増加して
もＢ塔の蒸気消費量は殆んど増えない。しかしブタノー
ル回収のためのアセトン塔（Ａ塔）３における蒸気消費
量は下層液量の増加に伴って増加するが、従来法の如く
同じ条件下共沸蒸留混合物を蒸気で取出しブタノールを
回収する方法に比較すれば、本発明方法はＡ塔の蒸気消
費量の増加は極めて小さく全体の蒸気消費量は大きな節
約となる。さらに本発明方法においては共沸混合物の凝
縮器及び分離器を設ける必要がない。As the amount of water in the distillate from the M tower to the B tower increases, the amount of the lower layer liquid increases, and when the storage part is provided, the vapor consumption of the B column almost increases even if the amount of the lower layer liquid increases. Absent. However, the amount of steam consumed in the acetone column (A column) 3 for recovering butanol increases with an increase in the amount of the lower layer liquid. However, a method for recovering butanol by extracting an azeotropic distillation mixture with steam under the same conditions as in the conventional method. Compared with the above, the method of the present invention has a very small increase in the steam consumption of the tower A, and a large saving in the overall steam consumption. Furthermore, it is not necessary in the process of the invention to provide an azeotrope condenser and separator.
又Ｍ塔からＢ塔へ入る水分はＭ塔頂の還流比及び精留部
分の棚段数によっても影響されるので実験、計算等によ
り経済的条件を選ぶことが好ましい。Further, the water content entering from the M tower to the B tower is also influenced by the reflux ratio at the top of the M tower and the number of trays in the rectification section, so it is preferable to select economic conditions by experiments, calculations and the like.
Ｂ塔からの留出液はアセトン塔、エタノール塔（Ｅ塔）
４へ順次送られアセトン、エタノールが従来法に従って
回収される。The distillate from the B tower is an acetone tower, an ethanol tower (E tower)
4, and acetone and ethanol are recovered according to a conventional method.
本発明の態様を実施例によって説明する。Aspects of the invention are described by way of examples.
実施例１ アセトン、ブタノール発酵醪55,000kg/H,32℃（アセト
ン0.54％，ブタノール1.21％，エタノール0.07％，水そ
の他98,18％）をＭ塔の蒸留廃液とヒーターにて75℃に
予熱し、Ｍ塔の上部に供給する。Example 1 Acetone, butanol fermentation mash 55,000 kg / H, 32 ° C (acetone 0.54%, butanol 1.21%, ethanol 0.07%, water and other 98,18%) was preheated to 75 ° C with a distillation waste liquid of the M tower and a heater. , M tower top.
Ｍ塔は塔頂温度90℃、還流比１にて稼働し廃液は熱交換
器を通り系外へ排出され、留出液2148kg/H,85℃（アセ
トン13.78％，ブタノール34.31％，エタノール1.91％，
水50％）はＢ塔（ブタノール塔）上部へ供給する。The M tower operates at a tower top temperature of 90 ° C and a reflux ratio of 1, and the waste liquid is discharged out of the system through a heat exchanger. The distillate is 2148 kg / H, 85 ° C (acetone 13.78%, butanol 34.31%, ethanol 1.91%). ，
50% of water) is supplied to the upper part of the B tower (butanol tower).
Ｂ塔は塔頂温度60℃、還流比５にて稼働し且つＢ塔中央
部に設けた分離器に下降液2012kg/H,92℃（ブタノール3
6.63％，水63.37％）を貯えて上層液と下層液に分離し
上層液870kg/H（ブタノール76.21％，水23.79％）は溢
流管よりＢ塔の回収部へ下層液1142kg/H（ブタノール6.
48％，水93.52％）はＭ塔上部に返送する。そして塔底
よりブタノール製品663kg/Hを取得し、また留出液343kg
/H,55℃（アセトン86.30％，エタノール11.95％，水1.7
5％）はＡ塔の下部に供給する。The tower B was operated at a tower top temperature of 60 ° C and a reflux ratio of 5 and a descending liquid was added to a separator provided at the center of the tower B at 2012 kg / H, 92 ° C (butanol 3
6.63%, water 63.37%) is stored and separated into upper and lower liquids, and the upper liquid 870kg / H (butanol 76.21%, water 23.79%) flows from the overflow pipe to the recovery part of the B tower 1142kg / H (butanol). 6.
48%, water 93.52%) are returned to the upper part of the M tower. Then, 663 kg / H of butanol product was obtained from the bottom of the tower, and 343 kg of distillate was obtained.
/ H, 55 ℃ (acetone 86.30%, ethanol 11.95%, water 1.7
5%) is supplied to the lower part of Tower A.
Ａ塔は塔頂温度56℃、還流比1.2にて稼働し上部留出液
よりアセトン製品296kg/Hを取得し塔底液47kg/H,82℃
（エタノール87.23％，水12.77％）はＥ塔下部へ供給す
る。The tower A operates at a tower top temperature of 56 ° C and a reflux ratio of 1.2, and obtains 296 kg / H of acetone product from the upper distillate and 47 kg / H, 82 ° C of the bottom liquid.
(Ethanol 87.23%, water 12.77%) is supplied to the lower part of E tower.
Ｅ塔は塔頂温度80℃、還流比1.2.にて稼働し上部留出液
よりエタノール製品44kg/Hを取得し塔下部液はＢ塔下部
に返送する。The E tower operates at a tower top temperature of 80 ° C and a reflux ratio of 1.2., And 44 kg / H of ethanol product is obtained from the upper distillate, and the lower tower liquid is returned to the lower part of the B tower.
上記の操作条件においてソルベント製品１本当りの蒸気
消費量（4kg/cm2G飽和）は次のとおりであった。Under the above operating conditions, the vapor consumption per solvent product (4 kg / cm 2 G saturation) was as follows.
実施例２ 実施例１に示した操作条件に於いてＭ塔の醪供給段の上
部から10％苛性ソーダ水溶液10/Hを連続的に供給した
場合の製品の品質は次の通りであった。 Example 2 Under the operating conditions shown in Example 1, the quality of the product when 10% caustic soda aqueous solution 10 / H was continuously supplied from the upper part of the mashing stage of the M tower was as follows.
第１図は本発明方法を適用した装置の１例を示す。各装
置の記号は次の意義を示す。 1:醪塔、2:ブタノール塔、3:アセトン塔、4:エタノール
塔、５〜14:熱交換器、15:ブタノール貯留部、16:仕切
り板、17:溢流管、18:上層液、19:下層液。 第２図はブタノール貯留部の詳細を示す。20は下層液出
口を示す。 第３図は水とブタノールの相互溶解度の関係図を示す。FIG. 1 shows an example of an apparatus to which the method of the present invention is applied. The symbol of each device has the following meaning. 1: Tofu tower, 2: Butanol tower, 3: Acetone tower, 4: Ethanol tower, 5-14: Heat exchanger, 15: Butanol reservoir, 16: Partition plate, 17: Overflow pipe, 18: Upper layer liquid, 19: Lower layer liquid. FIG. 2 shows details of the butanol reservoir. 20 shows the lower layer liquid outlet. FIG. 3 shows the relationship between the mutual solubility of water and butanol.
Claims (1)
液を醪塔で蒸留濃縮して得られるアセトン、ブタノー
ル、エタノール及び水からなる蒸気を凝縮した後中央へ
貯留部を設けたベタノール塔へ導入し、該貯留部でブタ
ノールと水の混合液を貯留させることにより、ブタノー
ルに水が溶解した上層と水にブタノールが溶解した下層
に分離し、その下層液を醪塔へ共沸温度付近で循環し、
上層液からブタノールを回収し、要すればブタノール塔
からの排出蒸気からアセトン又はエタノールを蒸留によ
って回収することを特徴とするアセトン、ブタノール及
びエタノール発酵液の蒸留法。1. A steam comprising acetone, butanol, ethanol and water obtained by distilling and concentrating an acetone, butanol and ethanol fermented liquid in a turret is condensed and then introduced into a betaanol column having a reservoir in the center, By storing a mixed solution of butanol and water in the storage section, it is separated into an upper layer in which water is dissolved in butanol and a lower layer in which butanol is dissolved in water, and the lower layer liquid is circulated to a turret tower near the azeotropic temperature,
A method for distilling an acetone, butanol, and ethanol fermentation liquor, characterized in that butanol is recovered from the upper layer liquid, and if necessary, acetone or ethanol is recovered from the exhaust vapor from the butanol column by distillation.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61255859A JPH0763561B2 (en) | 1986-10-29 | 1986-10-29 | Distillation method of acetone, butanol and ethanol fermentation broth |
| IN1027/DEL/87A IN172028B (en) | 1986-10-29 | 1987-12-01 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61255859A JPH0763561B2 (en) | 1986-10-29 | 1986-10-29 | Distillation method of acetone, butanol and ethanol fermentation broth |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63109766A JPS63109766A (en) | 1988-05-14 |
| JPH0763561B2 true JPH0763561B2 (en) | 1995-07-12 |
Family
ID=17284572
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61255859A Expired - Lifetime JPH0763561B2 (en) | 1986-10-29 | 1986-10-29 | Distillation method of acetone, butanol and ethanol fermentation broth |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JPH0763561B2 (en) |
| IN (1) | IN172028B (en) |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2006025355A1 (en) * | 2004-08-31 | 2006-03-09 | Kyowa Hakko Kogyo Co., Ltd. | Rectification apparatus and method of rectification with the same |
| JP2009045573A (en) * | 2007-08-21 | 2009-03-05 | Nippon Kagaku Kikai Seizo Kk | Purification method and system for fermented ethanol |
| EP2238098A4 (en) * | 2007-12-27 | 2016-06-01 | Gevo Inc | Recovery of higher alcohols from dilute aqueous solutions |
| JP2009240305A (en) * | 2008-03-10 | 2009-10-22 | Nippon Kagaku Kikai Seizo Kk | Method of dehydrating and purifying fermentation liquid and system therefor |
| WO2010126847A1 (en) * | 2009-04-28 | 2010-11-04 | Cobalt Technologies Inc. | Vapor compression distillation thermodynamic control |
| WO2010151706A1 (en) | 2009-06-26 | 2010-12-29 | Cobalt Technologies, Inc. | Integrated system and process for bioproduct production |
| US8968522B2 (en) * | 2009-07-15 | 2015-03-03 | Butamax Advanced Biofuels Llc | Recovery of butanol isomers from a mixture of butanol isomers, water, and an organic extractant |
| US8968523B2 (en) * | 2009-07-15 | 2015-03-03 | Butamax Advanced Biofuels Llc | Recovery of butanol isomers from a mixture of butanol isomers, water, and an organic extractant |
| AU2014225436B2 (en) * | 2013-03-07 | 2018-05-10 | Genomatica, Inc. | Downstream processing of fatty alcohol compositions produced by recombinant host cells |
| CN103641683B (en) * | 2013-12-11 | 2015-09-16 | 褚雅志 | The propyl carbinol retrieving arrangement of BDO device |
| CN104311389B (en) * | 2014-09-19 | 2016-06-22 | 利晟生物科技（北京）有限公司 | A kind of method producing thick n-butyl alcohol |
| CN104355964B (en) * | 2014-09-19 | 2017-01-18 | 利晟生物科技（北京）有限公司 | Method for producing crude n-butanol and equipment thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5696687A (en) * | 1979-12-27 | 1981-08-04 | Suntory Ltd | Distilling method of ethanol |
-
1986
- 1986-10-29 JP JP61255859A patent/JPH0763561B2/en not_active Expired - Lifetime
-
1987
- 1987-12-01 IN IN1027/DEL/87A patent/IN172028B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| IN172028B (en) | 1993-03-13 |
| JPS63109766A (en) | 1988-05-14 |
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