CA1119538A - Process for the production of alcohol - Google Patents
Process for the production of alcoholInfo
- Publication number
- CA1119538A CA1119538A CA000340612A CA340612A CA1119538A CA 1119538 A CA1119538 A CA 1119538A CA 000340612 A CA000340612 A CA 000340612A CA 340612 A CA340612 A CA 340612A CA 1119538 A CA1119538 A CA 1119538A
- Authority
- CA
- Canada
- Prior art keywords
- enzyme
- grain
- protein
- fiber materials
- treated
- 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
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K10/00—Animal feeding-stuffs
- A23K10/30—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms
- A23K10/35—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms from potatoes
-
- 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
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Organic Chemistry (AREA)
- Biotechnology (AREA)
- Polymers & Plastics (AREA)
- Health & Medical Sciences (AREA)
- Wood Science & Technology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Botany (AREA)
- Biochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Microbiology (AREA)
- Molecular Biology (AREA)
- Mycology (AREA)
- Physiology (AREA)
- Animal Husbandry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Food Science & Technology (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
Alcohol preparation from grain is described, in which the fat degradation and the saccharification of the mash is carried out in two separate steps with an intermediate filtra-tion. In the first step the wet-milled grain is degraded with amylolytic enzyme, then filtered, and the protein and fiber-containing filter cake used directly or dried as fodder material.
The filtrate is then treated to an acid and/or enzymatic saccha-rification and used without further filtration in the fermenta-tion.
Alcohol preparation from grain is described, in which the fat degradation and the saccharification of the mash is carried out in two separate steps with an intermediate filtra-tion. In the first step the wet-milled grain is degraded with amylolytic enzyme, then filtered, and the protein and fiber-containing filter cake used directly or dried as fodder material.
The filtrate is then treated to an acid and/or enzymatic saccha-rification and used without further filtration in the fermenta-tion.
Description
1 The invention concerns a process for the preparation of alcohol from grain with recovery of valuable side-products as fodder material.
In the preparation of alcohol from grain seed according to known methods, the first step is the preparation of the so-called wort through the mash process. Malt, grain kernels and bacilli are mashed together with acidified water at temperatures between 30 and 60C, then the materials are peptonized to easily assimilated nitrogen compounds in order to degrade the raw proteins, and finally the mixture is saccharified over a few hours, then acidified and pasteurized. In order to obtain the final wort, the solid components of the mash are removed from the liquids through clarification, i.e., decantation. The recovered spent grain serves as fodder material.
It is also known that the residual grain particles can be separated from the wort through alluvial filtration by means of kieselgur. In this case, the filter cake is discarded. The thus-clarified wort is used as stock wort and is introduced into the fermentation container.
Disadvantages of the clarification process are the amount of time required, the large volumes of the clarification vats necessary, the many intermediate containers for partially clarified worts and the necessary monitoring of the process. A
disadvantage of the kieselgur filtration method is the useless-ness of the filter cake with the valuable proteins contained therein.
All of the known methods have in common the feature that a wort freed of solid materials is prepared only immediately before the fermentation.
It is an object of the invention to provide a process
In the preparation of alcohol from grain seed according to known methods, the first step is the preparation of the so-called wort through the mash process. Malt, grain kernels and bacilli are mashed together with acidified water at temperatures between 30 and 60C, then the materials are peptonized to easily assimilated nitrogen compounds in order to degrade the raw proteins, and finally the mixture is saccharified over a few hours, then acidified and pasteurized. In order to obtain the final wort, the solid components of the mash are removed from the liquids through clarification, i.e., decantation. The recovered spent grain serves as fodder material.
It is also known that the residual grain particles can be separated from the wort through alluvial filtration by means of kieselgur. In this case, the filter cake is discarded. The thus-clarified wort is used as stock wort and is introduced into the fermentation container.
Disadvantages of the clarification process are the amount of time required, the large volumes of the clarification vats necessary, the many intermediate containers for partially clarified worts and the necessary monitoring of the process. A
disadvantage of the kieselgur filtration method is the useless-ness of the filter cake with the valuable proteins contained therein.
All of the known methods have in common the feature that a wort freed of solid materials is prepared only immediately before the fermentation.
It is an object of the invention to provide a process
-2-~9~38 1 for the preparation of a pure stock wort for the production of alcohol, a side product with the high~st possible protein value is recovered from the grain.
This object is achieved according to the invention by a process in which after acid or enzymatic degradation to fer-mentable sugars, a clarifying filtration is carried out to remove protein and fiber materials.
The first enzymatic step can be carried out together with wet milling. One may employ diastase-containing malt in the customary manner, or diastase or alpha-amylase may be added.
Saccharification in two stages has the advantage that the reac-tion is better controlled, and damage to the valuable proteins through extended presence in the mash is avoided. In the first stage, shorter times and higher temperatures can be used, which is more advantageous than longer times at lower temperatures.
The separation of the solids, which consist principally of protein and fiber materials, follows in an advantageous manner through the use of a vacuum drum filter. The filter cake can be used directly as fodder material, or a preliminary drying may be carried out. From the dried filter cake, the grain oil may also be extracted.
The final saccharification of the clarified filtrate can be carried out with acid alone at elevated temperature or with addition of amyloglucosidase in the acid solution. In comparison to a customarily obtained mash, a minimum of enzyme is required for a pure solution. This has many practical advantages with respect to the efficiency of the entire process.
As a cooling of the saccharified mash, which may also now be called the stock wort, is carried out in a heat exchanger, the absence of solids minimizes the amount of cleaning required.
953~3 1 The use of heat exchangers also allows for recirculation of the heat energy. The recirculated;heat is used to warm the water used in the process.
The novel features which are considered as characteris-tic for the invention are set forth in particular in the appended claims. The invention itself, however, both as to its construction and its method of operation, together with additional objects and advantages thereof, will be best understood from the following de-scription of specific embodiments when read in connection with the accompanying drawing.
FIG. 1 illustrates a schematic flow diagram of an em-bodiment of the inventive process.
FIG. 2 illustrates a variant of the embodiment of FIG. 1.
In FIG. 1, a grain bunker 1 is arranged over a wet mill 2. A forwarding conduit 3 leads to the wet mill 2 for the grain kernels, and a water conduit with sections 4 and 5. Between the two sections a heat exchanger 6 is pro*ided, with a connection 7 for the heating medium and a connection 8 attached to input line 9. A container 10 with mixing or stirring means 11 is provided for the first stage of enzyme treatment. A pipe conduit 12 leads from container 10 to a rotating drum filter 13. A forwarding band 14 leads to a drier 15. A filtrate conduit 16 is provided and connected with container 17, which is provided with a steam connection 18, as well as a conduit 19 ~hich in turn leads to an acid container 20. The container 17 is joined with a subsequent buffer tank 22, from which a conduit 23 runs through heat exchanger 24. The heat exchanger 24 is provided with connection 25 for a cooling medium. Instead of a single heat exchanger, a number of units in sequence may be employed. Conduit 26 leads to a fermenter ~119538 1 27, in which the alcoholic -fermentation is carried out. The fermenter 27 is provided with connections 28 and 29 for cooling medium. From fermenter 27, a conduit 30 leads to a centrifuge 31, a conduit 32 to distillation with thermocompression unit 33, and thereafter to a system for rectification of the alcohol which is not illustrated. The conduit 34 leads back to fermenter 27.
In operation the grain kernels from bunker 1 are intro-duced into the wet mill 2, in which it is pretreated in warm water introduced simultaneously through water conduit 4. The warm water is generated through the use of heat exchanger 6; the heat recovered from the previously heated mash is transferred to the water intro-duced into the mill via conduit 9. The water discharged at connec-tion 7 is then conveyed to a channel system which is not illus-~ trated. From the wet mill 2, in which simultaneously with the sl~ r~h L~ grain and water the ~t-degrading enzyme, such as alpha-amylase, can be added, the suspension is given further treatments in a con-tainer over about 2 hours at above 80C with stirring. During s~r~hQ~
this treatment, the ~ are converted thoroughly into dextrins, without any appreciable degradation of the proteins. For separa-tion ~f the solids in particularly advantageous manner, a rotatingdrum filter 13 is used, which is operated undPr vacuum. Filter aids are not required on account of the fiber materials already present. The filter cake is lead into the drier 15 via a trans-port band 14. The dried filter residues can be used as fodder material, or before such use treated to an oil extraction to recover the grain oil.
The filtrate is conveyed from filter 13 by conduit 16 into a pressure chamber 17, in to which, for example, 0.05% hyd-rochloric~ acid is dosed via conduit 19 from tank 20. Through direct steaming of about 130C over half an hour the solution is i9S38 1 heated to about 120C and thereby partially saccharified. A
thorough saccharification follows in container 22, into which, such as diastase, can be introduced as well. The pure stock wort is then lead into the fermenter 27 for the alcoholic fermentation after cooling to about 30C in heat exchanger 24 via conduit 26 without additional filtration. The fermentation takes place in conventional manner, as well as the separation of the yeast cells present in the fermenter. These are carried via conduit 30 to separator 31, and then centrifuged from the wort;
in order to maintain the necessary cell concentration in fermenter 27, they are partially returned by means of conduit 34. The alcohol containing wort freed of cells is then treated in evapora-tor 33 to distill the alcohol; the latter is then rectified. The residue from the evaporator is treated in a unit for treatment of waste water with recovery of methane.
In FIG. 2, a variant of the inventive pracess is illus-trated. The major difference between this embodiment and that of FIG. 1 lies in the higher concentration of hydrolysis products which can be achieved, if the hydrolysate before th~ second hydro-lysis is conveyed via conduit 12' into a second wet mill 2' afterfilter 13, which can also be another type of separation device, such as a centrifuge. Into the wet mill 2', new grain is intro-duced from silo 1 and mixed with addition of a small amount of enzyme to compensate for the increased activity requirements.
After the wet milling, the material is conveyed into container 10' and then treated as described in the process of FIG. 1 above. The separation in filter 13' or a centrifuge follows as described above.
The method has the great advantage that with correspond-ing amounts of grain and enzyme, the concentration of the hydroly-- 1119~38 1 sate can be approximately doubled, which leads to a consider-able reduction in thermal energy re~uirements for the further hydrolysis to fermentable sugars. Simultaneously, there is a saving in process water and expensive enzyme.
This object is achieved according to the invention by a process in which after acid or enzymatic degradation to fer-mentable sugars, a clarifying filtration is carried out to remove protein and fiber materials.
The first enzymatic step can be carried out together with wet milling. One may employ diastase-containing malt in the customary manner, or diastase or alpha-amylase may be added.
Saccharification in two stages has the advantage that the reac-tion is better controlled, and damage to the valuable proteins through extended presence in the mash is avoided. In the first stage, shorter times and higher temperatures can be used, which is more advantageous than longer times at lower temperatures.
The separation of the solids, which consist principally of protein and fiber materials, follows in an advantageous manner through the use of a vacuum drum filter. The filter cake can be used directly as fodder material, or a preliminary drying may be carried out. From the dried filter cake, the grain oil may also be extracted.
The final saccharification of the clarified filtrate can be carried out with acid alone at elevated temperature or with addition of amyloglucosidase in the acid solution. In comparison to a customarily obtained mash, a minimum of enzyme is required for a pure solution. This has many practical advantages with respect to the efficiency of the entire process.
As a cooling of the saccharified mash, which may also now be called the stock wort, is carried out in a heat exchanger, the absence of solids minimizes the amount of cleaning required.
953~3 1 The use of heat exchangers also allows for recirculation of the heat energy. The recirculated;heat is used to warm the water used in the process.
The novel features which are considered as characteris-tic for the invention are set forth in particular in the appended claims. The invention itself, however, both as to its construction and its method of operation, together with additional objects and advantages thereof, will be best understood from the following de-scription of specific embodiments when read in connection with the accompanying drawing.
FIG. 1 illustrates a schematic flow diagram of an em-bodiment of the inventive process.
FIG. 2 illustrates a variant of the embodiment of FIG. 1.
In FIG. 1, a grain bunker 1 is arranged over a wet mill 2. A forwarding conduit 3 leads to the wet mill 2 for the grain kernels, and a water conduit with sections 4 and 5. Between the two sections a heat exchanger 6 is pro*ided, with a connection 7 for the heating medium and a connection 8 attached to input line 9. A container 10 with mixing or stirring means 11 is provided for the first stage of enzyme treatment. A pipe conduit 12 leads from container 10 to a rotating drum filter 13. A forwarding band 14 leads to a drier 15. A filtrate conduit 16 is provided and connected with container 17, which is provided with a steam connection 18, as well as a conduit 19 ~hich in turn leads to an acid container 20. The container 17 is joined with a subsequent buffer tank 22, from which a conduit 23 runs through heat exchanger 24. The heat exchanger 24 is provided with connection 25 for a cooling medium. Instead of a single heat exchanger, a number of units in sequence may be employed. Conduit 26 leads to a fermenter ~119538 1 27, in which the alcoholic -fermentation is carried out. The fermenter 27 is provided with connections 28 and 29 for cooling medium. From fermenter 27, a conduit 30 leads to a centrifuge 31, a conduit 32 to distillation with thermocompression unit 33, and thereafter to a system for rectification of the alcohol which is not illustrated. The conduit 34 leads back to fermenter 27.
In operation the grain kernels from bunker 1 are intro-duced into the wet mill 2, in which it is pretreated in warm water introduced simultaneously through water conduit 4. The warm water is generated through the use of heat exchanger 6; the heat recovered from the previously heated mash is transferred to the water intro-duced into the mill via conduit 9. The water discharged at connec-tion 7 is then conveyed to a channel system which is not illus-~ trated. From the wet mill 2, in which simultaneously with the sl~ r~h L~ grain and water the ~t-degrading enzyme, such as alpha-amylase, can be added, the suspension is given further treatments in a con-tainer over about 2 hours at above 80C with stirring. During s~r~hQ~
this treatment, the ~ are converted thoroughly into dextrins, without any appreciable degradation of the proteins. For separa-tion ~f the solids in particularly advantageous manner, a rotatingdrum filter 13 is used, which is operated undPr vacuum. Filter aids are not required on account of the fiber materials already present. The filter cake is lead into the drier 15 via a trans-port band 14. The dried filter residues can be used as fodder material, or before such use treated to an oil extraction to recover the grain oil.
The filtrate is conveyed from filter 13 by conduit 16 into a pressure chamber 17, in to which, for example, 0.05% hyd-rochloric~ acid is dosed via conduit 19 from tank 20. Through direct steaming of about 130C over half an hour the solution is i9S38 1 heated to about 120C and thereby partially saccharified. A
thorough saccharification follows in container 22, into which, such as diastase, can be introduced as well. The pure stock wort is then lead into the fermenter 27 for the alcoholic fermentation after cooling to about 30C in heat exchanger 24 via conduit 26 without additional filtration. The fermentation takes place in conventional manner, as well as the separation of the yeast cells present in the fermenter. These are carried via conduit 30 to separator 31, and then centrifuged from the wort;
in order to maintain the necessary cell concentration in fermenter 27, they are partially returned by means of conduit 34. The alcohol containing wort freed of cells is then treated in evapora-tor 33 to distill the alcohol; the latter is then rectified. The residue from the evaporator is treated in a unit for treatment of waste water with recovery of methane.
In FIG. 2, a variant of the inventive pracess is illus-trated. The major difference between this embodiment and that of FIG. 1 lies in the higher concentration of hydrolysis products which can be achieved, if the hydrolysate before th~ second hydro-lysis is conveyed via conduit 12' into a second wet mill 2' afterfilter 13, which can also be another type of separation device, such as a centrifuge. Into the wet mill 2', new grain is intro-duced from silo 1 and mixed with addition of a small amount of enzyme to compensate for the increased activity requirements.
After the wet milling, the material is conveyed into container 10' and then treated as described in the process of FIG. 1 above. The separation in filter 13' or a centrifuge follows as described above.
The method has the great advantage that with correspond-ing amounts of grain and enzyme, the concentration of the hydroly-- 1119~38 1 sate can be approximately doubled, which leads to a consider-able reduction in thermal energy re~uirements for the further hydrolysis to fermentable sugars. Simultaneously, there is a saving in process water and expensive enzyme.
Claims (10)
1. In a process for the preparation of alcohol from grain with recovery of valuable side products for use as fodder, in which a mash is prepared and treated to peptide degradation and sacchari-fication to prepare a wort for alcoholic fermentation, the im-provement comprising a clarifying filtration to separate out the protein and fiber materials after an acid and/or enzymatic degrada-tion to form fermentable sugars.
2. A process as described in claim 1, additionally com-prising a second acid and/or enzymatic degradation to form fer-mentable sugars after said clarifying filtration.
3. A process as defined in claim 1, wherein the grain is treated to wet milling prior to enzyme treatment.
4. A process as defined in claim 3, wherein enzyme is added during said wet milling.
5. A process as defined in claim 1, wherein after said filtration said protein and fiber materials are dried.
6. A process as defined in claim 1, wherein said protein and fiber materials are treated to an oil extraction.
7. A process as defined in claim 1, wherein heat gener-ated in the enzyme treatments is used to warm water for the process.
8. A process as defined in claim 1, wherein the total hydrolysate or a portion thereof after separation of the protein and fiber materials is used in wet milling of fresh grain and enzyme before a final saccharification, whereby yield of hydrolysis product is increased.
9. A process as described in claim 2, wherein the step of preparation and treatment is carried out in the presence of wash water;
and further comprising the step of adding amylolytic enzymes to said wash water subsequent to said clarifying filtration.
and further comprising the step of adding amylolytic enzymes to said wash water subsequent to said clarifying filtration.
10. A process as described in claim 9, and further comprising recirculating the enzyme-containing wash water back into the process.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CH1233378A CH637990A5 (en) | 1978-12-01 | 1978-12-01 | Process for the production of alcohol |
| CH12333/78 | 1978-12-01 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1119538A true CA1119538A (en) | 1982-03-09 |
Family
ID=4382027
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000340612A Expired CA1119538A (en) | 1978-12-01 | 1979-11-26 | Process for the production of alcohol |
Country Status (6)
| Country | Link |
|---|---|
| AT (1) | AT370440B (en) |
| AU (1) | AU5330879A (en) |
| CA (1) | CA1119538A (en) |
| CH (1) | CH637990A5 (en) |
| FR (1) | FR2442887A1 (en) |
| ZA (1) | ZA796438B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4810647A (en) * | 1985-08-07 | 1989-03-07 | Valpi | Process of producing ethanol and various other by-products from cereals |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2944483C2 (en) * | 1979-11-03 | 1984-05-30 | Supraton F.J. Zucker GmbH, 4040 Neuss | Process for the continuous production of alcohol from starch or raw materials containing starch |
| DE3023874A1 (en) * | 1980-06-26 | 1982-01-21 | Supraton F.J. Zucker GmbH, 4040 Neuss | METHOD FOR OBTAINING A CONCENTRATED SLUDGE IN THE PRODUCTION OF ALCOHOL FROM STARCH OR RAW MATERIALS CONTAINING STRENGTH |
| EP0049994A3 (en) * | 1980-10-10 | 1982-08-11 | Biosynthetics, Inc. | Continuous process for producing alcohol solution |
| IT1211714B (en) * | 1987-08-12 | 1989-11-03 | Technipetrol Spa | PROCEDURE, APPARATUS AND RELATED OPERATING METHOD FOR THE PRODUCTION OF ETHANOL FROM CEREALS WITH CONTINUOUS PROCESS |
| US5559031A (en) * | 1987-08-12 | 1996-09-24 | Technipetrol S.P.A. | Apparatus for the continuous production of ethanol from cereals |
| AT398981B (en) * | 1991-03-14 | 1995-02-27 | Vogelbusch Gmbh | Prodn. of ethanol from raw material contg. starch and rich in protein - by mashing ground raw material in liq. compsn., washing out protein sepg. solid particles contg. starch, saccharifying and fermenting, and sepg. proteins from wash liq. |
| CZ9902389A3 (en) * | 1999-07-01 | 2000-10-11 | Karel Ing. Šašek | Process for preparing spirit without formation of alcohol stillage |
| DE102006047782A1 (en) * | 2006-10-06 | 2008-04-10 | Licher Privatbrauerei Ihring-Melchior Gmbh | Producing ethanol from amylaceous crops comprises separating solids between mashing and fermentation and separating yeast between fermentation and distillation |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2348451A (en) * | 1941-03-27 | 1944-05-09 | Nat Agrol Company Inc | Method of producing alcohol |
| US2663718A (en) * | 1950-04-20 | 1953-12-22 | Laval Separator Co De | Clarification of distillery slop and the like |
| GB1109311A (en) * | 1963-08-07 | 1968-04-10 | Hiram Walker & Sons Scotland L | Improvements in or relating to the production of grain whisky |
-
1978
- 1978-12-01 CH CH1233378A patent/CH637990A5/en not_active IP Right Cessation
-
1979
- 1979-11-26 CA CA000340612A patent/CA1119538A/en not_active Expired
- 1979-11-27 ZA ZA00796438A patent/ZA796438B/en unknown
- 1979-11-29 FR FR7929916A patent/FR2442887A1/en not_active Withdrawn
- 1979-11-29 AU AU53308/79A patent/AU5330879A/en not_active Abandoned
- 1979-11-30 AT AT0760779A patent/AT370440B/en not_active IP Right Cessation
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4810647A (en) * | 1985-08-07 | 1989-03-07 | Valpi | Process of producing ethanol and various other by-products from cereals |
Also Published As
| Publication number | Publication date |
|---|---|
| CH637990A5 (en) | 1983-08-31 |
| ZA796438B (en) | 1980-11-26 |
| AT370440B (en) | 1983-03-25 |
| ATA760779A (en) | 1982-08-15 |
| AU5330879A (en) | 1980-06-05 |
| FR2442887A1 (en) | 1980-06-27 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |