CA1140872A - Method of producing ethanol by continuous fermentation - Google Patents
Method of producing ethanol by continuous fermentationInfo
- Publication number
- CA1140872A CA1140872A CA000355452A CA355452A CA1140872A CA 1140872 A CA1140872 A CA 1140872A CA 000355452 A CA000355452 A CA 000355452A CA 355452 A CA355452 A CA 355452A CA 1140872 A CA1140872 A CA 1140872A
- Authority
- CA
- Canada
- Prior art keywords
- flow
- yeast
- ethanol
- fermentor
- evaporator unit
- 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
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
-
- 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
- Organic Chemistry (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Biotechnology (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
For continuous production of ethanol by fermenta-tion, fermenting liquor is fed directly from a fermentor to a simple evaporator unit where a vacuum is maintained and where the liquor is separated into a first vapor flow en-riched in ethanol, which is processed to the desired ethanol quality, and a yeast-containing bottom flow. Of the latter flow, part is recirculated to the fermentor while the rest is separated into a yeast concentrate flow, which is recir-culated to the fermentor, and a yeast-free flow which is fed to a stripping unit. The second vapor flow, enriched in ethanol, which is thus obtained from the stripping unit can be fed to the simple evaporator unit directly or indirectly.
The method is especially advantageous if the substrate is made by enzymatic break-down of cellulose or starch, as the enzymes in this case are not subjected to excessive tempera-tures but can be recovered.
For continuous production of ethanol by fermenta-tion, fermenting liquor is fed directly from a fermentor to a simple evaporator unit where a vacuum is maintained and where the liquor is separated into a first vapor flow en-riched in ethanol, which is processed to the desired ethanol quality, and a yeast-containing bottom flow. Of the latter flow, part is recirculated to the fermentor while the rest is separated into a yeast concentrate flow, which is recir-culated to the fermentor, and a yeast-free flow which is fed to a stripping unit. The second vapor flow, enriched in ethanol, which is thus obtained from the stripping unit can be fed to the simple evaporator unit directly or indirectly.
The method is especially advantageous if the substrate is made by enzymatic break-down of cellulose or starch, as the enzymes in this case are not subjected to excessive tempera-tures but can be recovered.
Description
This invention relates to a method for producing ethanol by fermentation of a substrate containing carbo-hydrate,a yeast-containing flow being separated into a yeast-concentrate flow and a yeast-free flow.
Such methods are known in which the total flow of fermenting liquor is fed to a centrifugal separator for said separation, the yeast-concentrate flow being recirculated to the fermentor. The centrifugal separator utilized must have a capacity for separation of the total flow of fermenting liquor, from which the ethanol is obtained continuously, which can be a drawback. A method in which no centrifugal separator is needed, but in which the yeast is still pro-tected when recovering ethanol from fermenting liquor with continuous fermentation, is disclosed in Swedish Patent 15 Application No. 7801134. In this method, the fermentation is carried out at normal pressure, but the ethanol is recovered by distillation from a flow of fermenting liquor including yeast at vacuum pressure. Even if this method is suitable in many cases, it has certain drawbacks. The apparatus is rather complicated; and considering the amount of yeast present, the extent to which a flow enriched in ethanol can be evaporated is limited.
The principal object of this invention is to pro-vide a method of the type mentioned above in which the capacity of the utilized separation unit can be relatively low, wherein the yeast is recirculated without being damaged, and wherein there is great freedom in the choice of suitable operation data for the recovery of ethanol by distillation.
According to the invention, fermenting liquor is fed directly to a simple evaporator unit corresponding to one or only a few distilling stages and in which a vacuum is -1- t'','.~
: ~
A
8~
maintained. In the evaporator unit, the fermenting liquor is separated partly into a first vapor flow enriched in ethanol, which is fed to a plant for production of the desired ethanol quality, and partly into a first liquid, yeast-containing bottom flow. Part of the latter flow is recirculated to the fermentor while the residual part is separated into at least one yeast concentrate flow, which is recirculated to the fer-mentor, and into one yeast-free flow which is fed to a stripping unit, where it is separated into a second vapor flow enriched in ethanol and partly into a second liquid bottom flow, exhausted of ethanol.
In a preferred embodiment of the new method, the second vapor flow enriched in ethanol is fed to the simple evaporator unit either directly or as an indirect source of heat. The yeast is not exposed to any excessive temperature, but the temperature in the stripping unit may be higher than what could be tolerated by the yeast. According to the in-vention, heating surfaces in the evaporator unit may be dis-pensed with. Also, no high separator capacity is needed, and the operation conditions for the ethanol recovery may be chosen optimally.
If the substrate has been manufactured by enzy-matic break-down of cellulose or starch raw material, it is an advantage that the simple evaporator unit operate at a low pressure and thus at a low temperature. In that case the enzymes are not damaged but can be recovered. Also, the ten-dency of deposit formation is less in the simple evaporator unit if it is operated at a low temperature.
It is suitable to separate the yeast-containing bottom flow by a centrifugal separator into a yeast concen-trate flow and a yeast-free flow.
Such methods are known in which the total flow of fermenting liquor is fed to a centrifugal separator for said separation, the yeast-concentrate flow being recirculated to the fermentor. The centrifugal separator utilized must have a capacity for separation of the total flow of fermenting liquor, from which the ethanol is obtained continuously, which can be a drawback. A method in which no centrifugal separator is needed, but in which the yeast is still pro-tected when recovering ethanol from fermenting liquor with continuous fermentation, is disclosed in Swedish Patent 15 Application No. 7801134. In this method, the fermentation is carried out at normal pressure, but the ethanol is recovered by distillation from a flow of fermenting liquor including yeast at vacuum pressure. Even if this method is suitable in many cases, it has certain drawbacks. The apparatus is rather complicated; and considering the amount of yeast present, the extent to which a flow enriched in ethanol can be evaporated is limited.
The principal object of this invention is to pro-vide a method of the type mentioned above in which the capacity of the utilized separation unit can be relatively low, wherein the yeast is recirculated without being damaged, and wherein there is great freedom in the choice of suitable operation data for the recovery of ethanol by distillation.
According to the invention, fermenting liquor is fed directly to a simple evaporator unit corresponding to one or only a few distilling stages and in which a vacuum is -1- t'','.~
: ~
A
8~
maintained. In the evaporator unit, the fermenting liquor is separated partly into a first vapor flow enriched in ethanol, which is fed to a plant for production of the desired ethanol quality, and partly into a first liquid, yeast-containing bottom flow. Part of the latter flow is recirculated to the fermentor while the residual part is separated into at least one yeast concentrate flow, which is recirculated to the fer-mentor, and into one yeast-free flow which is fed to a stripping unit, where it is separated into a second vapor flow enriched in ethanol and partly into a second liquid bottom flow, exhausted of ethanol.
In a preferred embodiment of the new method, the second vapor flow enriched in ethanol is fed to the simple evaporator unit either directly or as an indirect source of heat. The yeast is not exposed to any excessive temperature, but the temperature in the stripping unit may be higher than what could be tolerated by the yeast. According to the in-vention, heating surfaces in the evaporator unit may be dis-pensed with. Also, no high separator capacity is needed, and the operation conditions for the ethanol recovery may be chosen optimally.
If the substrate has been manufactured by enzy-matic break-down of cellulose or starch raw material, it is an advantage that the simple evaporator unit operate at a low pressure and thus at a low temperature. In that case the enzymes are not damaged but can be recovered. Also, the ten-dency of deposit formation is less in the simple evaporator unit if it is operated at a low temperature.
It is suitable to separate the yeast-containing bottom flow by a centrifugal separator into a yeast concen-trate flow and a yeast-free flow.
-2-8~2 The invention will now be described more in detail, reference being made to the accompanying drawing in which the single illustration is a schematic view of a system for carrying out the method.
The system as illustrated comprises at least one fermentor 1, a simple evaporator unit 2 corresponding to one or a few distilling stages, a centrifugal separator 3 and a simple stripping unit 4. A plant for production of the de-sired ethanol quality is indicated with a condenser 5 and a distilling column 6. A pipe 7 connects the fermentor 1 to the evaporator unit 2, from which a bottom line 8 divides into two branches 9 and 10. Branch 9 is connected to the centrifugal separator 3, and branch 10 is connected to the fermentor 1. The centrifugal separator 3 is provided with a sludge discharge 13. A line 14 connects the simple stripping unit 4 with the simple evaporator unit 2, from which a line 15 leads to the condenser 5. A feed pipe 16 delivers sub-strate to the fermentor, and a discharge pipe 17 is provided to discharge carbon dioxide formed in the fermentor. The simple evaporator unit 2 and the simple stripping unit 4 are provided with heating coils 18 and 19, respectively.
In the operation of the illustrated system, sub-strate is fed continuously through feed pipe 16, and a suit-able yeast concentration is maintained in fermentor 1. Fer-menting liquor including yeast is discharged continuously ~' through line 7 and is evaporated at a relatively low tem-.' perature under vacuum in the simple evaporator unit 2. The bottom flow is discharged through line 8 and is divided so . that one part is recirculated to fermentor 1 through line 10, and the residual part is fed to the centrifugal separa-tor 3 through line 9. In the centrifugal separator 3, the
The system as illustrated comprises at least one fermentor 1, a simple evaporator unit 2 corresponding to one or a few distilling stages, a centrifugal separator 3 and a simple stripping unit 4. A plant for production of the de-sired ethanol quality is indicated with a condenser 5 and a distilling column 6. A pipe 7 connects the fermentor 1 to the evaporator unit 2, from which a bottom line 8 divides into two branches 9 and 10. Branch 9 is connected to the centrifugal separator 3, and branch 10 is connected to the fermentor 1. The centrifugal separator 3 is provided with a sludge discharge 13. A line 14 connects the simple stripping unit 4 with the simple evaporator unit 2, from which a line 15 leads to the condenser 5. A feed pipe 16 delivers sub-strate to the fermentor, and a discharge pipe 17 is provided to discharge carbon dioxide formed in the fermentor. The simple evaporator unit 2 and the simple stripping unit 4 are provided with heating coils 18 and 19, respectively.
In the operation of the illustrated system, sub-strate is fed continuously through feed pipe 16, and a suit-able yeast concentration is maintained in fermentor 1. Fer-menting liquor including yeast is discharged continuously ~' through line 7 and is evaporated at a relatively low tem-.' perature under vacuum in the simple evaporator unit 2. The bottom flow is discharged through line 8 and is divided so . that one part is recirculated to fermentor 1 through line 10, and the residual part is fed to the centrifugal separa-tor 3 through line 9. In the centrifugal separator 3, the
-3-. -., ~' ' '.'' :
~ ~ 4~372 incoming flow is separated into a yeast concentrate flow,which is recirculated to fermentor 1 through line 12, a yeast-free flow which is fed to the simple stripping unit 4 through line 11, and an intermittent sludge flow which is discharged through pipe 13. The vapor flow (enriched in ethanol) from the simple stripping unit 4 is conducted through line 14 to the simple evaporator unit 2 and contri-butes to the heat feed to this unit. Vapor is fed as needed through heating coil 18 as well as through heating coil 19, which heats the simple stripping unit 4. The combined vapor flow, enriched in ethanol, from the simple evaporator unit 2 is discharged through line 15 to condenser 5 and is then fed to the distilling column 6 for production of the desired ethanol quality.
The following is an example of the operation of a system for carrying out the method according to the inven-tion:
Example Cane sugar molasses, 40Bx, is fed continuously through feed pipe 16 to fermentor 1, where a yeast concentra~
tion of 2.5% (weight) is maintained by recirculation. Under these conditions, a residence time of 6 hours is needed to obtain complete fermentation. A flow of fermenting liquor, containing 0.1-0.5% (weight) of non-fermented sugar and about 5% (weight) ethanol, is pumped continuously to simple evapo-rator unit 2, where a pressure of 50 mm Hg is maintained.
The fermented mash boils at 35 C, and vapor containing 30-35% (weight) ethanol is driven off and condensed in con-denser 5. The diluted ethanol is concentrated and further purified in distilling column 6.
.
:
~ ~ 4~372 incoming flow is separated into a yeast concentrate flow,which is recirculated to fermentor 1 through line 12, a yeast-free flow which is fed to the simple stripping unit 4 through line 11, and an intermittent sludge flow which is discharged through pipe 13. The vapor flow (enriched in ethanol) from the simple stripping unit 4 is conducted through line 14 to the simple evaporator unit 2 and contri-butes to the heat feed to this unit. Vapor is fed as needed through heating coil 18 as well as through heating coil 19, which heats the simple stripping unit 4. The combined vapor flow, enriched in ethanol, from the simple evaporator unit 2 is discharged through line 15 to condenser 5 and is then fed to the distilling column 6 for production of the desired ethanol quality.
The following is an example of the operation of a system for carrying out the method according to the inven-tion:
Example Cane sugar molasses, 40Bx, is fed continuously through feed pipe 16 to fermentor 1, where a yeast concentra~
tion of 2.5% (weight) is maintained by recirculation. Under these conditions, a residence time of 6 hours is needed to obtain complete fermentation. A flow of fermenting liquor, containing 0.1-0.5% (weight) of non-fermented sugar and about 5% (weight) ethanol, is pumped continuously to simple evapo-rator unit 2, where a pressure of 50 mm Hg is maintained.
The fermented mash boils at 35 C, and vapor containing 30-35% (weight) ethanol is driven off and condensed in con-denser 5. The diluted ethanol is concentrated and further purified in distilling column 6.
.
:
4~872 The bottom flow from simple evaporator unit 2 is divided into two flows so that about 80% is recirculated through pipe 10 to fermentor 1, and 20% is centrifuged in centrifugal separator 3, which operates at a high rotational speed. The yeast concentrate is pumped to fermentor 1 through line 12 while the yeast-free flow is fed through pipe 11 to simple stripping unit 4, which is designed as a short column. The vapor, enriched in ethanol, from stripping unit 4 is led either directly to simple evaporator unit 2 or indirectly for heating of same, whereby the energy losses can be minimized. The bottom flow from simple stripping unit 4 contains about 35% (weight) soluble dry solids and can be treated further in a simple way, as in a combustion oven.
-5-., .
Claims (4)
1. In the production of ethanol by fermentation of a carbohydrate-containing substrate in a fermentor, the method which comprises feeding fermenting liquor directly from the fermentor to a simple evaporator unit, maintaining a vacuum in the evaporator unit while separating said liquor therein partly into a first liquid yeast-containing bottom flow, treating said first vapor flow to produce ethanol of a desired quality, recirculating part of said first bottom flow to the fermentor, separating the remaining part of said first bottom flow into a yeast concentrate flow and a yeast-free flow, recirculating said yeast concentrate flow to the fermentor, and feeding said yeast-free flow to a stripping unit and there separating the yeast-free flow partly into a second vapor flow enriched in ethanol and partly into a second liquid bottom flow exhausted of ethanol.
2. The method of claim 1, which comprises also feeding said second vapor flow to said simple evaporator unit.
3. The method of claim 1, in which said separating of the remaining part of said first bottom flow is effected by centrifugal separation.
4. The method of claim 2, in which said separating of the remaining part of said first bottom flow is effected by centrifugal separation.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE7905916-8 | 1979-07-06 | ||
| SE7905916A SE432442B (en) | 1979-07-06 | 1979-07-06 | PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS SPRAYING OF A CARBOHYDRATE-SUBSTRATE, WHICH AN ETHANOLANRICATED FLUID IS SEPARATED UNDER VACUUM BEFORE DISTRIBUTING THE VETERINARY WINE |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1140872A true CA1140872A (en) | 1983-02-08 |
Family
ID=20338463
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000355452A Expired CA1140872A (en) | 1979-07-06 | 1980-07-04 | Method of producing ethanol by continuous fermentation |
Country Status (13)
| Country | Link |
|---|---|
| JP (1) | JPS56113295A (en) |
| AU (1) | AU515814B2 (en) |
| BR (1) | BR8004159A (en) |
| CA (1) | CA1140872A (en) |
| DE (1) | DE3023120A1 (en) |
| DK (1) | DK289680A (en) |
| FR (1) | FR2461005A1 (en) |
| GB (1) | GB2054645B (en) |
| NL (1) | NL8003504A (en) |
| NZ (1) | NZ194151A (en) |
| PH (1) | PH15742A (en) |
| SE (1) | SE432442B (en) |
| ZA (1) | ZA803706B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0114161B1 (en) * | 1983-01-13 | 1989-06-07 | VOEST-ALPINE Aktiengesellschaft | Process for the preparation of ethanol out of fermentable sugar solutions |
| AT388174B (en) * | 1987-03-10 | 1989-05-10 | Vogelbusch Gmbh | METHOD FOR THE FERMENTATION OF CARBOHYDRATE-CONTAINING MEDIA USING BACTERIA |
| GB2438617A (en) * | 2006-06-03 | 2007-12-05 | Edward Arthur Jackman | Continuous fermentation process for the production of ethyl alcohol |
| GB0905234D0 (en) | 2009-03-26 | 2009-05-13 | Agri Ltd Ab | Protien recovery |
| US9963671B2 (en) | 2009-03-26 | 2018-05-08 | Ab Agri Limited | Protein recovery |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2440925A (en) * | 1944-04-27 | 1948-05-04 | Chemprotin Producs | Fermenting method |
| SE432441B (en) * | 1979-02-27 | 1984-04-02 | Alfa Laval Ab | PROCEDURE FOR PREPARING ETHANOL BY CONTINUOUS SPRAYING OF A CARBOHYDRATE-SUBSTRATE, WHICH A DRINK WITH RELATIVE HIGH RATE OF SOLID SUBSTANCE RECOVERY |
-
1979
- 1979-07-06 SE SE7905916A patent/SE432442B/en not_active IP Right Cessation
-
1980
- 1980-06-17 NL NL8003504A patent/NL8003504A/en not_active Application Discontinuation
- 1980-06-20 ZA ZA00803706A patent/ZA803706B/en unknown
- 1980-06-20 DE DE19803023120 patent/DE3023120A1/en not_active Withdrawn
- 1980-06-20 GB GB8020240A patent/GB2054645B/en not_active Expired
- 1980-06-23 PH PH24183A patent/PH15742A/en unknown
- 1980-06-26 NZ NZ194151A patent/NZ194151A/en unknown
- 1980-07-01 FR FR8014664A patent/FR2461005A1/en active Granted
- 1980-07-03 BR BR8004159A patent/BR8004159A/en not_active IP Right Cessation
- 1980-07-04 CA CA000355452A patent/CA1140872A/en not_active Expired
- 1980-07-04 AU AU60120/80A patent/AU515814B2/en not_active Ceased
- 1980-07-04 DK DK289680A patent/DK289680A/en not_active Application Discontinuation
- 1980-07-04 JP JP9079980A patent/JPS56113295A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| ZA803706B (en) | 1981-06-24 |
| DK289680A (en) | 1981-01-07 |
| FR2461005B1 (en) | 1983-07-18 |
| PH15742A (en) | 1983-03-18 |
| GB2054645B (en) | 1983-07-06 |
| SE432442B (en) | 1984-04-02 |
| BR8004159A (en) | 1981-01-21 |
| GB2054645A (en) | 1981-02-18 |
| AU6012080A (en) | 1981-01-15 |
| NZ194151A (en) | 1983-05-10 |
| DE3023120A1 (en) | 1981-02-12 |
| AU515814B2 (en) | 1981-04-30 |
| JPS56113295A (en) | 1981-09-07 |
| NL8003504A (en) | 1981-01-08 |
| FR2461005A1 (en) | 1981-01-30 |
| SE7905916L (en) | 1981-01-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP1019519B1 (en) | Method for conversion of biomass to chemicals and fuels | |
| US4460687A (en) | Fermentation method | |
| US8906204B2 (en) | Methods for alcohol recovery and concentration of stillage by-products | |
| Maiorella et al. | Alcohol production and recovery | |
| US8722911B2 (en) | Process and method for improving the water reuse, energy efficiency, fermentation, and products of an ethanol fermentation plant | |
| US4822737A (en) | Process for producing ethanol by fermentation | |
| US7625728B2 (en) | Process for the simultaneous production of xylitol and ethanol | |
| FI86440B (en) | FRAME FOR SAMPLING OF XYLITOL OR ETHANOL. | |
| GB2054643A (en) | Fermentation process for the manufacture of an organic compound | |
| NO163868B (en) | PROCEDURE FOR THE PREPARATION OF ETHANOL. | |
| EP3479886A1 (en) | Method and system for distilling alcohol in an alcohol production process | |
| WO1989001522A1 (en) | Process and apparatus for the continuous production of ethanol from cereals and method of operating said apparatus | |
| CA1140873B (en) | Production of volatile organic compound by continuous fermentation | |
| CA1140872A (en) | Method of producing ethanol by continuous fermentation | |
| CN212356909U (en) | Fermented mash evaporation concentration and rectification protein powder co-production system | |
| CA1282358C (en) | Method of continuously recovering fermentation products | |
| CN111908691A (en) | Method and system for co-producing protein powder by evaporation concentration and rectification of fermented liquor | |
| WO2015085012A1 (en) | Methods and systems for production of bioproducts | |
| CN101941886B (en) | Method for producing fermentation product | |
| AU2018100802B4 (en) | A method and system for the concentration of juice | |
| CA1175370A (en) | Fermentation method | |
| CN217418690U (en) | Ethanol production system | |
| JPS6394966A (en) | Concentration and recovery of fermentation alcohol | |
| SU582274A1 (en) | Method of producing alcohol | |
| JPH01218592A (en) | Continuous production of fermented alcohol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |