EP2059603A1 - Procédé de production de bioalcool, en particulier de bioéthanol et/ou de biobutanol - Google Patents

Procédé de production de bioalcool, en particulier de bioéthanol et/ou de biobutanol

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Publication number
EP2059603A1
EP2059603A1 EP07801949A EP07801949A EP2059603A1 EP 2059603 A1 EP2059603 A1 EP 2059603A1 EP 07801949 A EP07801949 A EP 07801949A EP 07801949 A EP07801949 A EP 07801949A EP 2059603 A1 EP2059603 A1 EP 2059603A1
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EP
European Patent Office
Prior art keywords
fermentation
biomass
separation
yeast
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.)
Withdrawn
Application number
EP07801949A
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German (de)
English (en)
Inventor
Andre Düx
Andreas Jupke
Dieter Mrotzek
Georg Ronge
Sebastian Schmidt
Matthias Böhm
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bayer AG
Original Assignee
Bayer Technology Services GmbH
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Filing date
Publication date
Application filed by Bayer Technology Services GmbH filed Critical Bayer Technology Services GmbH
Publication of EP2059603A1 publication Critical patent/EP2059603A1/fr
Withdrawn legal-status Critical Current

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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
    • 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
    • C12P7/14—Multiple stages of fermentation; Multiple types of microorganisms or re-use of microorganisms
    • 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
    • C12P7/16—Butanols
    • 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

Definitions

  • the invention relates to a process for the production of bioalcohol, in particular bioethanol and / or biobutanol, from biomass, in particular from cereals and in particular from rye by fractional grinding, saccharification, fermentation and distillation.
  • a special feature of the method is that after saccharification initially undissolved solid components and in a subsequent separation step non-fermentable carbohydrates (NFS: non fermentable sugars) such as pentosans and glucans are separated.
  • NFS non fermentable sugars
  • pentosans and glucans are separated.
  • the separation of valuable feed yeasts or, in the case of butanol the separation of the bacteria for recycling after the fermentation (main fermentation) becomes possible for the production of ethanol.
  • the NFS-rich phase obtained during the separation of non-fermentable carbohydrates is fermented in a separate fermentation step (secondary fermentation), which is carried out parallel to the main fermentation, optionally together with undissolved solid constituents.
  • secondary fermentation which is carried out parallel to the main fermentation, optionally together with undissolved solid constituents.
  • the production of alcohols by fermentation of a biomass is one of the oldest biotechnological processes and is u.a. used for the production of alcoholic beverages, such as beer and wine. Also, the production of alcohol to be used industrially by fermentation of biomass has been known for a long time. At present, corresponding alcohols, especially ethanol, are used as starting material for the preparation of pharmaceutical compositions, cosmetic products, and a variety of chemicals.
  • fermentative ethanol as an energy carrier has long been known, but was not used commercially due to the higher compared to the recovery of oil process costs in the past.
  • microorganisms are added to the biomass and a fermentation is carried out; and (c) The ethanol is separated from the biomass.
  • the steam flow is fed to a plant for the production of the desired ethanol quality.
  • the bottom flow is partially returned to the fermentation tank and partially fed to a power take-off unit in which this part is divided into an ethanol-rich second steam flow and a second liquid bottom flow which is low in ethanol.
  • the ethanol-rich vapor stream can be used together with the first ethanol-rich vapor stream for the recovery of ethanol, for example in a rectification column.
  • a process for the production of ethanol in which the yeast is separated after the fermentation, partially recycled to the fermentation and partially discharged.
  • the starchy raw material used for ethanol production is comminuted by a Vollvermahlung, with a separation of the solids takes place after the saccharification.
  • the separation of the yeast is by sedimentation, but is not described in detail.
  • the invention is therefore based on the object of providing an economical process for producing bioalcohol, in particular bioethanol and / or biobutanol, from biomass, preferably cereals, in particular based on rye, in which no complicated grinding or denaturing of the vinasse is required, in which the valuable feed yeasts can be separated and recycled after the fermentation, and in addition to the main alcohol (ethanol and / or butanol) and valuable feed yeasts can be obtained as possible without elaborate drying.
  • a special challenge is the separation of the yeast after fermentation with the highest possible ethanol yield.
  • NFS non-fermentable sugar
  • the invention relates to a process for the production of alcohol from biomass, in which the biomass is comminuted, the remaining biomass is fed to a fermentation and the alcohol is obtained from the product of the fermentation, characterized in that insoluble solid constituents and / or non-fermentable sugars be separated from the biomass before fermentation and / or bio-organisms (yeast and / or bacteria) after the fermentation.
  • butanol is produced from biomass.
  • the method of the present invention is illustrated in FIG.
  • the comminution of the biomass is usually carried out by complete grinding or fractional grinding.
  • First, the pre-cleaned grain is fed to a milling unit to expose the starch particles contained therein.
  • the mean particle size during milling is usually from 0.1 to 2 mm, preferably from 0.1 to 1 mm.
  • Grain fractions with a low starch content (shell fraction) and a high proportion of viscosity-increasing substances, such as, for example, pentosans and glucans (bran fraction) are preferably separated off (fractional milling).
  • apparatuses corresponding to the state of the art are used (for example, a combination of double roller chairs with a basket sifter, possibly with an upstream sanding machine).
  • step b) d For some raw materials such as sugar cane or sugar beet, step b) d.
  • step b) d H. Starch liquefaction and saccharification optional. For cereals, starch liquefaction and saccharification are again required.
  • the biomass is cereals, in particular rye, and the method comprises the following steps:
  • step (b) optional fractions having a lower starch content (shell fraction) and a high proportion of viscosity-increasing substances (glutinous fraction) are separated off prior to liquefaction prior to step (b).
  • shell fraction starch content
  • glutinous fraction viscosity-increasing substances
  • the starch particles contained in the cereal flour are liquefied, ie converted into dextrins and the mash viscosity is lowered by enzymes (46).
  • the water used in the Anmaischen is added with enzymes and then with the flour below the gelatinization, ie at a temperature of 20 - 80 0 C, preferably but mixed 40-60 ° C.
  • the gelatinization in cereals is from 50 to 8O 0 C, wheat 53-65 0 C and at 55 to 7O 0 Rye by C.
  • a Anmaischesch of 1 -3 kg water / kg flour, but preferably from 1.5 - 2.5 kg of water / kg of flour sought.
  • saccharification of the mash ie the transformation into a sweet mash.
  • the dextrins are converted into glucose, which can then be fermented in the fermentation to alcohol, (ethanol or butanol).
  • alcohol ethanol or butanol
  • unreacted dextrins are still converted into fermentable glucose in the fermentation.
  • the saccharification reaction usually takes place at temperatures between 30 and 70 ° C., preferably between 60 and 65 ° C.
  • the residence time depends on the amount of enzyme used and is usually between 15 and 40 h, preferably 20 and 30 h.
  • the pH is usually between 3 and 7, preferably between 5 and 6, and more preferably between 5.3 and 5.7.
  • the saccharification can take place in one or more stirred stirred tanks (stirred tank cascade) or in a tubular reactor with or without internals.
  • suitable saccharification enzymes glucoamylase, eg the commercial product Spirizyme Fuel
  • phosphoric acid 48
  • other acids such as sulfuric acid, are suitable for adjusting the pH.
  • step c) of the process according to the invention the preparation of the sweet mash follows by separation of undissolved solid constituents in order to minimize the necessary residence time of the subsequent fermentation reaction and secondly to allow the separation of the bioorganism (yeast and / or bacteria) after fermentation.
  • the separation is preferably carried out mechanically e.g. by means of separators or decanters.
  • the amount of the resulting concentrate phase containing a large part of the undissolved solid constituents corresponds to about 2-70% by weight of the supplied mash, depending on the type of milling (fractionating or fully comminuting). In the case of fractional milling this proportion is below 40 wt .-%.
  • the moisture content of this concentrate phase is usually from 30 to 95 wt.%.
  • a wash ratio is preferably adjusted from 0.5 kg water: 1 kg concentrate phase - 5 kg water: 1 kg concentrate phase.
  • the undissolved solid components washed with water, if appropriate recovered from the process, are preferably collected and transported for DDGS drying.
  • the overflow laden with sugar is preferably recycled partly for mashing into starch liquefaction.
  • the other partial flow is preferably used to adjust the sugar concentration in the fermentation.
  • the sugar concentration is usually adjusted so that about 10 wt.% Ethanol or 1-3 wt.% Butanol are achieved during fermentation.
  • the separated, undissolved solids are fed together with NFS to a secondary fermentation. In this way, sugar losses can also be minimized.
  • the separation of non-fermentable carbohydrates is preferably carried out.
  • the NFS phase is usually separated mechanically by decanting or filtering, preferably decanting.
  • the remaining mash (11) exiting in the overflow is fed to the fermentation (hereinafter referred to as main fermentation (14)).
  • main fermentation (14) the fermentation
  • the NFS phase is fed to a secondary fermentation operated parallel to the main fermentation, this secondary fermentation converting the residual sugar and increasing the yield of alcohol production.
  • the amount of flow to the main fermentation and the amount of electricity for Maufermentation in the ratio 0.5: 1 - 20: 1, but preferably in the ratio 1: 1 - divided 10: 1.
  • both anionic and cationic flocculants can be used as flocculants.
  • Acrylamides having a strong cationic copolymer for example Praestol 853 BC, Stockhausen GmbH & Co KG
  • acrylamides having a weakly cationic copolymer for example Praestol 611 BC, Stockhausen GmbH & Co KG
  • Copoylmer acrylamide with acrylate (weak anionic, for example Praestol 2520 from Stockhausen GmbH & Co KG) and medium anionic acrylamide copolymer with acrylate (e.g.
  • the admixing of the flocculant is usually carried out as a 0.01-1% solution in water. In this case, preferably 10 to 1000 ppm, based on solids, are metered in.
  • the mash is usually cooled to temperatures between 25 and 50 ° C., preferably between 30 and 45 ° C.
  • the cooling of the mash can take place both before and after the NFS separation, but preferably after the NFS separation.
  • the main fermentation can be carried out continuously or discontinuously, but preferably continuously.
  • the fermentation commonly used bacteria provides eg Jones, or Woods, Microbiological Reviews, 1986, p. 484-524.
  • immobilized bacteria known in the art is also possible (see, for example, Huang, Ramey, Yan, Applied Biochemistry and Biotechnology, 2004, pp. 887-898, Ramey, DOE Report DE-F-G02- 00ER86106, Production of Butyric Acid and Butanol Frorn Biomass, 2004; US 5,563,069; Zhu, Yang, Biotechn. Progr., 2003, pp. 365-372).
  • the operating temperature is usually 25 to 50 preferably 30 to 42 ° C.
  • the necessary residence time depends on the amount of bacteria used, and is usually between 30 and 60 hours. In this case, a butanol content of 0.5 to 3 wt .-% is usually achieved.
  • the bacterial content is usually between 0.5 and 5% by weight at the start of fermentation.
  • the final sugar content is ldR less than 0.1 wt .-%.
  • the pH is preferably 4-7.
  • the light phase usually has a dry matter content of 0-10% by weight TS.
  • Flocculation aids can be used to improve yeast separation.
  • the use of flocculants on the one hand significantly reduces the sedimentation rate by factors of 1-10 and on the other the sediment volume (30-100% by volume in comparison to the sediment volume without flocculant).
  • the amount of flocculant used is preferably 10-100,000 ppm on solid.
  • the hefereiche phase (yeast milk) obtained in the yeast separation usually has an alcohol content of about 6 to 10 wt .-%, which would mean a loss of alcohol.
  • the alcohol contained in the yeast milk is separated in a particular embodiment of the process in a rectification column. Subsequently, the yeast is usually dried using the prior art methods.
  • the recovery of ethanol or butanol from incurred in the fermentation vinasse is usually carried out by distillation.
  • the fermented mash is preheated and then degassed in the degassing column.
  • the alcohol contained in traces in the gas stream is washed out in the exhaust air scrubber and mixed back into the mash stream.
  • the bottom product is fed to the vaporizing steam.
  • the head vapors are condensed and given up as reflux to the mash column.
  • a liquid side draw so-called crude alcohol, is added directly to the azeotropic column for further concentration and purification steps.
  • a fusel oil fraction is withdrawn as a side stream, condensed in the side stream condenser and passed into a decanter.
  • the aqueous phase of this separation step is returned to the azeotropic column.
  • the concentrated fusel oil is discharged.
  • the distillate consists of an alcohol-water mixture of approximately azeotropic composition.
  • the distillate from the azeotrope column is added to the dewatering column. In this column, pure ethanol (about 99.7%) is withdrawn as bottoms product with cyclohexane as entraining agent.
  • the distillate of the dewatering column is cooled and passed into a decanter where two liquid phases are separated:
  • the latter are preferably used for ethanol drying.
  • the recovery of butanol from the vinasse is usually also by distillation, preferably in a continuous distillation process.
  • a rectification called in a first mash or beer column, at the top the butanol and other by-products of the fermentation (for example ethanol and acetone) and the water content resulting from the thermodynamic equilibrium are removed.
  • acetone and azeotropic ethanol are now separated by distillation.
  • the drying of the azeotropic ethanol can - if necessary - be carried out again by azeotropic rectification or pressure swing adsorption.
  • the remaining water-butanol mixture which forms a heteroazeotrope, can now be worked up by means of heteroazeotrophic rectification or pressure swing distillation. The thereby separated water can be recycled in the process.
  • syrup and / or molasses (41) originating from the sugar production together with the mash (12) freed from NFS are fed to the main fermentation (14) and / or together with the NFS phase to the secondary fermentation (13).
  • the thick juice can be used on the one hand to lower the viscosity and on the other hand to adjust the sugar content of the mash to be fermented.
  • the separated phase in the separation of NFS which is a mixture of NFS and included sugar solution
  • a fermentation parallel to the main fermentation hereinafter referred to as Maufermentation
  • the undissolved solid constituents separated during the solids separation are fed to the secondary fermentation.
  • the sugar end content is i.d.R. ⁇ 0, 1 wt .-%.
  • the pH is usually 4-6.
  • the main task of vaporizing is to concentrate the vinasse from the distillation.
  • the concentration of the vinasse is carried out by single or multi-stage evaporation, with a multi-stage process is usually preferred because of the high energy demand.
  • waste heat from the process eg from DDGS drying.
  • vinasse is concentrated to a TS content (dry matter TS) of 15-60% by weight, but preferably up to a DS content of 25-50% by weight.
  • TS content dry matter TS
  • the degree of concentration depends on the type of raw material used for the production of bioalcohol. As a rule, however, the highest possible TS contents are sought.
  • aid of flow aids which can be added during the Schleppezeindampfung or even further upstream in the process (eg in the fermentation), the flowability of the concentrated stillage and thus the degree of concentration can be increased.
  • the separated water is reintroduced into the process as so-called process water, which reduces the need for fresh water.
  • process water which reduces the need for fresh water.
  • the concentrate obtained during the vaporizing evaporation is dried together with the bran separated during the grinding by means of a process which corresponds to the prior art. This results in a so-called dry vat (DDGS). Details of the production of dry stillage are described, for example, in the journal “Die Branntwein Albany" May 1976, pages 138 to 141.
  • the inventive method provides in a preferred embodiment in addition to the main ingredient ethanol two different feeds, namely DDGS (Distiller's Dried Grains with Solubles) and yeast.
  • DDGS Disistiller's Dried Grains with Solubles
  • yeast yeast
  • the starchy raw material is first subjected to a fractional grinding, grain fractions with a low share of starch (shell fraction) and a high proportion of viscosity-increasing substances such as pentosans and glucans (bran fraction) are separated. Subsequently, the mashing of the flour obtained during the grinding takes place. For this, water recovered from the process (e.g., stillage) is used. The mash is then liquefied and saccharified. Thereafter, the separation of undissolved solid components takes place. These are fed together with the resulting in the fractional grinding shells and bran DDGS drying.
  • Fig. 2 Fractional milling, 1-step husk and slime separation, 2-ée fermentation, two feeds (yeast and DDGS), yeast recycling
  • the undissolved solid components are also fed to the secondary fermentation.
  • Fig. 3 fractionated grinding, husk and slime separation, 2-ée fermentation, two feeds (yeast and DDGS), yeast recycling
  • Va ⁇ ante represented takes into account the fact that when using flocculants both the separation of undissolved solid components and the non-fermentable sugar can be done in one step.
  • Fig. 4 Fractional milling, husk and slime separation, 2- Given fermentation, two feeds (yeast and DDGS), yeast recycling
  • Fig. 5 (butanol fermentation) fractionated grinding, husk and slime separation, 2-ée fermentation, a feed (DDGS), bacterial recycling
  • the processing of the grain until the separation of the NFS is carried out analogously to Fig. 1.
  • suitable bacteria are used for the butanol fermentation. These are fed to both the main fermentation and the secondary fermentation.
  • a separation and recycling of the bacteria can be performed.
  • the mash streams of the two fermentations are fed to the Schlempekolonne. This separates the biomass from the organic products (especially butanol, acetone, ethanol).
  • the organic products are withdrawn in approximately azeotropic composition at the top of the Schlempekolonne and fed to your further work-up.
  • the bottoms of the Schlempekolonne, the vinasse (biomass and water, approximately free of the organic fermentation products) is thickened by evaporation in a further work-up step and then dried.
  • the dry goods are u.a. can be used as feed.
  • Variant 6 differs from Variant 5 in that the undissolved constituents which are obtained in the UF separation are fed to the secondary fermentation.
  • Fig. 7 (butanol fermentation) fractionated grinding, husk and slime separation, 2-ée fermentation, a feed (DDGS), bacterial recycling
  • Variant 7 shows, in deviation to Fig. 6, that the separation of the undissolved solid constituents and the NFS with the addition of flocculants can also take place in one step.
  • Fig. 8 (butanol fermentation) fractionated grinding, husk and slime separation, 2-ée fermentation, a feed (DDGS), bacterial recycling
  • DDGS feed
  • thick juice from sugar production is also used as raw material for alcohol production. Through targeted admixture with the main or secondary fermentation, the viscosity can be lowered and an optimal sugar content for the fermentation can be set.
  • the addition of thick juice is also conceivable in the process variants of FIGS. 5 and 6.
  • the process for producing butanol differs from the process for producing ethanol (FIGS. 1-4) in that
  • yeast bacteria instead of yeast bacteria are used as microorganisms. These are also separated behind the fermentation, but then completely returned, for example.
  • Processing of the products after fermentation must be adjusted accordingly.
  • Example 1 husk, slime and yeast separation
  • the saccharification enzymes used were Novozyme 50024 (500 ⁇ l / kg flour) and Spirizyme Fuel (500 ⁇ l / kg flour).
  • the remaining mash was fed to a fermentation.
  • the fermentation was carried out at 38 0 C and a pH of 5.5 and a residence time of 20 h. In this case, 22 g of yeast were added per liter of fermentation mixture.
  • yeast separation was carried out.
  • 25.3 kg of yeast concentrate having a residual moisture content of 82% by weight were separated by means of a decanter.
  • Example 2 Simulation of the ethanol yield by means of Aspen +
  • the ethanol yield of the inventive method of FIG. 1 was determined by means of a simulation with a process engineering software (Aspen +).
  • the simulation serves, in particular, to map the overall method with the relevant return currents and to determine the energy consumption of the individual method sections.
  • the simulation serves, in particular, to map the overall method with the relevant return currents and to determine the energy consumption of the individual method sections.
  • Radfrac e.g., Radfrac
  • the method according to the invention was simulated as follows.
  • the rye is first fed to a milling unit. It is estimated that an estimated 0.5 kg / h is separated as a shell or bran fraction.
  • the grain is mashed with water returned essentially from the process.
  • the simulation was carried out with a mashing ratio of 2 (2 kg water / kg rye flour).
  • the temperature of the mash is 48 ° C.
  • the process parameters of the liquefaction of rye are also known in the art. Thus, a temperature of about 85 0 C is selected, which is adjusted by admixing water vapor (0.05 kg steam / kg mash).
  • the mixture is first cooled to 63 ° C. by means of flash evaporation and then the saccharification.
  • suitable enzymes are added. Dextrins are converted into sugar.
  • the sugar content after saccharification is estimated to be about 20% by weight.
  • the separation of undissolved solids After saccharification, the separation of undissolved solids.
  • the high solids fraction is estimated at 1.64 kg / hr.
  • the separated undissolved solids are washed with water (1 kg wash water / 2 kg undissolved solids).
  • the sugar-containing wash water is essentially fed to the fermentation. Through the wash, the sugar content of the separated undissolved solids is estimated to be ⁇ 4% by weight.
  • the sweet mash is split in a ratio of 2: 1 into a low-NFS and an NFS-rich stream.
  • the low-NFS stream (about 7.1 kg / h) is fed to the main fermentation, while the NFS-rich stream is fed to the secondary fermentation. In the fermentation occurring CO 2 is fed to avoid ethanol losses of an absorption column.
  • Ethanols are used about 0.74 kg of water. After fermentation, the ethanol content is about 10% by weight.
  • the product of the Maufermentation is fed to ethanol production, while after the main fermentation first yeast is separated. For this purpose, the product of the main fermentation is divided into a yeast-rich and a low-yeast fraction in a ratio of 1: 5.
  • the low-yeast fraction (about 6.5 kg / h) is mixed together with the product of the Maufermentation and fed to ethanol production. This is done in the simulation by distillation, m the mash column alcohol and water are separated at 300 mbar. The bottom of this column, the so-called stillage (estimated at 5 kg / h) is fed to a 6-stage evaporation and there evaporated at different pressures (estimated 0.1 to 0.5 bar).
  • the concentrated vinasse (estimated at 1.8 kg / h), along with the shell and bran fractions from the milling and the undissolved solids separated after saccharification, are sent to drying. The drying process produces 1.51 kg / h of DDGS. The heat produced by condensation of the evaporated water is used for vaporizing.
  • the water separated in DDGS drying and in vaporizing is returned to the process, e.g. for maceration.
  • the distillate of the Schlempekolonne (estimated 1.8 kg / h) is fed to the azeotrope.
  • the ethanol is separated at an estimated 2 bar in azeotropic composition as the top product.
  • the water separated at the bottom of the column (estimated at 0.7 kg / h) is reused in the process.
  • From the azeotrope is a fusel oil fraction as Side stream withdrawn, condensed in the side stream condenser and passed into a decanter.
  • the aqueous phase of this separation step is returned to the azeotropic column.
  • the concentrated fusel oil (estimated 7 g / h) is discharged.
  • the distillate from the azeotrope column is added to the dewatering column.
  • the distillate of the dewatering column (estimated 3.7 kg / h) is cooled in a heat exchanger to an estimated 140 0 C and passed into a separating bottle in which two liquid phases are separated:
  • the organic phase (estimated at 3 kg / h) is added as reflux back into the dewatering column, whereas the aqueous phase is added to the recovery column.
  • the water In the cyclohexane work-up column (operating pressure estimated at 2 bar), the water is separated from the entraining agent and leaves the column as bottom product (estimated at 67 g / h) for wastewater collection. A side stream is passed to the dewatering column containing the recovered entrainer. Low boilers are removed as needed with the top stream of the cyclohexane workup column.
  • the amount of ethanol recovered is estimated to be 1 kg / h in the simulation described.
  • An additional 1.51 kg / h of DDGS and 0.11 kg / h of yeast are estimated to be produced.

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Abstract

La présente invention concerne un procédé de production de bioalcool, en particulier d'éthanol ou de butanol, à partir de biomasse, selon lequel la biomasse est broyée, la biomasse restante est fermentée et l'alcool issu du produit de la fermentation est obtenu. Ce procédé est caractérisé en ce que des composants solides insolubles et/ou des sucres non fermentables sont séparés de la biomasse avant fermentation et/ou de la levure ou des bactéries après la fermentation.
EP07801949A 2006-08-30 2007-08-29 Procédé de production de bioalcool, en particulier de bioéthanol et/ou de biobutanol Withdrawn EP2059603A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102006040567A DE102006040567A1 (de) 2006-08-30 2006-08-30 Verfahren zur Herstellung von Bioethanol
PCT/EP2007/007527 WO2008025522A1 (fr) 2006-08-30 2007-08-29 Procédé de production de bioalcool, en particulier de bioéthanol et/ou de biobutanol

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EP2059603A1 true EP2059603A1 (fr) 2009-05-20

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KR101613754B1 (ko) 2008-10-03 2016-04-19 메타볼릭 익스플로러 강하 막, 와이프드 막, 박막 또는 단경로 증발기를 사용한 발효 브로쓰로부터의 알콜의 정제 방법
RU2405828C2 (ru) 2009-01-29 2010-12-10 Дэвон Инвестмент Лимитед Способ получения органических растворителей
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NO20090950L (no) 2009-05-28
WO2008025522A1 (fr) 2008-03-06
RU2009111200A (ru) 2010-10-10
AR062602A1 (es) 2008-11-19
DE102006040567A1 (de) 2008-03-06

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