WO2009062601A2 - Méthode de préparation de biobutanol à partir de biomasse - Google Patents

Méthode de préparation de biobutanol à partir de biomasse Download PDF

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Publication number
WO2009062601A2
WO2009062601A2 PCT/EP2008/009162 EP2008009162W WO2009062601A2 WO 2009062601 A2 WO2009062601 A2 WO 2009062601A2 EP 2008009162 W EP2008009162 W EP 2008009162W WO 2009062601 A2 WO2009062601 A2 WO 2009062601A2
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WO
WIPO (PCT)
Prior art keywords
fermentation
raw materials
vegetable raw
mash
biobutanol
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PCT/EP2008/009162
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German (de)
English (en)
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WO2009062601A3 (fr
Inventor
Martin Ehrig
Werner BÄCKER
Jürgen BAUSA
Andre Düx
Sebastian Schmidt
Michael Traving
Mitja Medved
Günter OLF
Georg Ronge
Rafael Warsitz
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Bayer Technology Services Gmbh
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Application filed by Bayer Technology Services Gmbh filed Critical Bayer Technology Services Gmbh
Publication of WO2009062601A2 publication Critical patent/WO2009062601A2/fr
Publication of WO2009062601A3 publication Critical patent/WO2009062601A3/fr

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    • 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 biobutanol by fermentation from vegetable raw materials using reverse osmosis as separation step.
  • Biobutanol can be obtained by fermentation from solutions containing sugar and starch, reviewed in D. Jones and D. Woods in their article “Acetone butanol revisited” (Microbiological Reviews, 1986, p.484-524) for the processes described
  • the process is characterized in that the dissolved glucose is converted to butanol in discontinuously operated fermenters, acetone, ethanol, hydrogen and carbon dioxide being produced as byproducts
  • fermentation mashes are limited to about 12-22 g / l, which corresponds approximately to proportions in the fermentation mash of 1.2 to 2.2% by weight, so that the direct product separation from the resulting suspension is quite complicated and influences the Economic efficiency of the process negative.
  • Albert Garcia III also discloses concentrating a butanol-containing ultrafiltration permeate by reverse osmosis (Dissertation, University of Missouri-Columbia, USA, 1984; Biotechnology and Bioengineering, (1986) 28, 785-791).
  • the starting material for fermentation is filtered corn mash.
  • ultrafiltration after fermentation is provided to effect cell retention.
  • the feed for the reverse osmosis should be cleaned to the extent that no fouling occurs in this process step.
  • the effect on the process step of reverse osmosis has been achieved, however, a rapid occupancy of the ultrafiltration membrane is also disclosed. Thus, there is no process step which previously separates those soluble components of the starting material which cause the coating to allow an economical and reliable operation of the process.
  • step ab) separating the microorganisms containing a fermentation product comprising biobutanol and a biomass solution comprising the microorganisms, and optionally at least partially recycling the biomass solution into the fermentation and / or blending the ground vegetable raw materials according to step ab)),
  • step d) separating at least a portion of the biobutanol contained in the fermentation product by a reverse osmosis, and optionally at least partially recycling the remaining fermentation product obtained from step d) into the transformation by a fermentation,
  • step e) optionally further treating the obtained from step d) by reverse osmosis
  • the process according to the invention can be carried out continuously or batchwise. Preference is given to a batchwise procedure.
  • biobutanol in the present invention, all isomers of an alcohol having four carbon atoms and mixtures and solutions containing at least one of these isomers and produced by a process containing at least one process step in which a biological reaction is carried out are referred to.
  • Plant raw materials are, in the context of the present invention, all plants and / or substances obtained from these plants or mixtures thereof, which contain poly-sugars for the purposes of the present invention.
  • Preferred as vegetable raw materials are cereals. Particularly preferred are rye, wheat, barley and corn.
  • Poly-sugars in the present invention designate all substances of the empirical formula (C n (H 2 O) n ) m , where m denotes the number of units of the sugar C n (H 2 O) n in the poly-sugar and a value> 1 has and n can be any number from 3 to 6.
  • the poly-sugars are preferred Hexoses or Pentoses (5 ⁇ n ⁇ 6) Particularly preferred are the poly-sugars, xylans, dextrins and cellulose
  • Microorganisms according to the invention include species from the domain of the bacteria and / or the domain of the eukaryotes and the kingdom of fungi. Species of the genus Clost ⁇ dien are preferred. The species Clostridium acetobutyhcum, Clostridium beije ⁇ nckn, Clostridium saccharobutyhcum or Clostridium saccharoperbutylacetonicum and / or mixed cultures thereof are particularly preferred.
  • the preferred microorganisms are listed under the following numbered species in the German Collection of Microorganisms and Cell Cultures (DSMZ), and optionally the American Type Culture Collection (ATCC).
  • the preferred strains of the species Clostridium acetobutyhcum are available under the numbers DSM792 ( ATCC824), DSM1731 (ATCC4259), DSM1732, DSM1733, DSM1737 (ATCC3625), DSM1738 (ATCC8529), DSM4685 and DSM6228 (ATCC39236) deposited in the DSMZ
  • the preferred strains of the species Clostridium beije ⁇ nckii are under the numbers DSM51 (ATCC 7797), DSM53 (ATCC14949), DSM552, DSM791 (ATCC25752), DSM1739 (ATCC10132), DSM 1820 (ATCC858), DSM6422, DSM6423 and DSM 13821 deposited in the DSMZ
  • Usable sugars are poly-sugars according to the invention for which the microorganisms which can be used according to the invention have a metabolism for their utilization.
  • Poly-sugars of the hexoses and / or pentoses with m ⁇ 3 are preferred
  • the milling of the vegetable raw materials according to step aa) of the inventive method is preferably carried out by fractional milling, the detailed execution of which is known in the art a fractional grinding the interconnection of a mill known to the expert with a Klassiervor ⁇ chtung known in the art are very particularly preferred as mills known to those skilled in the buzzword mill types of Walzenstuhle, Hammer Mills and Impact Mills Also very particularly preferred are the Klassiervor ⁇ chtept known to those skilled in the buzzwords in their details Klassierertypen the drum screens, Plansichter and throw sieves
  • non-fermentable vegetable raw materials can be separated.
  • These non-fermentable vegetable raw materials may comprise, depending on the enzymes used in step ad) of the process according to the invention, for example proteins, cellulose or lignocellulosic raw material constituents
  • the Ve ⁇ nengen the ground vegetable raw materials from step aa) with water according to step ab) of the inventive method is preferably such that a mixture with 10 to 50% by weight ground vegetable raw material in water results particularly preferred is a resulting mixture with 20 to 40 wt -% ground plant raw material in water is further preferred blending elevated under compared to room temperature (20 0 C) temperature more preferably, the temperature amounts to at blending between 30 0 C and 70 0 C. most preferably, the temperature amounts to at blending about 55 ° C also the mixing of the ground vegetable raw materials from aa) with water according to (a) of the process according to the invention is preferred at a pH of less than 7. Mixing at a pH of from 5 to 6 is particularly preferred
  • the preferred proportions of ground vegetable raw material in water are particularly advantageous because the resulting mash is concentrated high enough to achieve economical space-time yields in the process, but is not yet so concentrated that its further treatment by the increased viscosity and Sedimentation is process technically too complex and thus uneconomical
  • the increase of the temperature to the very particularly preferred about 55 ° C is particularly advantageous because this difficult soluble poly-sugar fractions of the mash are better dissolved in the water and thus for the enzymatic treatment according to step ad) of the inventive
  • the particularly preferred reduction of the pH to 5 to 6 is particularly advantageous because it allows parts of the poly-sugars to be split by means of acidic hydrolysis the pH optimum of the at least one enzyme used in the slightly acidic to acidic, so that hereby a presetting of the pH value for the following process steps can be achieved This and the partial cleavage of poly-sugar lead to a further increase in the space-time yield of the overall process and are thus economically particularly advantageous
  • the process according to the invention can be carried out with or without separation of dissolved and / or dispersed non-fermentable substances from the mash and drying of the dissolved and / or dispersed non-fermentable substances according to step a).
  • the separation of dissolved and / or or dispersed, non-fermentable substances from the mash and drying of the dissolved and / or dispersed, non-fermentable substances Preferably separated, dissolved and / or dispersed, non-fermentable substances include gluten and / or lignin and / or cellulose. Particular preference is given to the separation of gluten
  • non-fermentable substances are substances which can not be converted into biobutanol by the microorganisms according to the invention in any further process step or in a combination of other process processes.
  • cellulose is a non-fermentable substance for the purposes of the present invention if it is not converted into usable sugars in step ad) by means of an enzyme (eg cellulase)
  • the separation according to step ac) is usually carried out using separators and / or hydrocyclones in their customary, known to those skilled embodiments
  • separators and / or hydrocyclones in their customary, known to those skilled embodiments
  • Particularly preferred conventional Embodiments for separators are Dusenseparatoren, press screw separators, chamber separators, Tellerseparatoren and / or Vollmanteltellerseparatoren
  • the drying according to step ac) is particularly preferably carried out by thermal and / or pressure treatment of the separated gluten.
  • thermal treatment at elevated temperatures (20 ° C.) together with a pressure treatment at pressures below ambient pressure (1013 hPa).
  • step ac) If a separation according to step ac) of the method according to the invention takes place, then the sequence of steps ac) and ad) is selectable. However, step ad) is preferably carried out after step ac)
  • step ac) The implementation of step ac) of the inventive method is particularly advantageous because achieved by the prior separation of z B also dissolved non-fermentable substances and the unresolved from the prior art remaining object of reducing or preventing the formation of deposits on membranes or surfaces subsequent Anlagenssch ⁇ tte can be (Fouhng)
  • the treatment of mash in Wass ⁇ gen with at least one enzyme for cleavage of poly-sugars according to step ad) of the inventive method can be carried out in one or two steps Preferably, a procedure in two steps
  • at least one enzyme the class of amylases and / or cellulases and / or xylanases and / or glucosidases are added preferred amylases sold under the trade name Novozyme 0O 50024 (Novozymes Germany GmbH) marketed enzyme and / or the (under the brand name Liquozyme °° SC DS Fa Novozymes GmbH) sold enzyme is particularly preferred as amylase Novozyme w 50024 in a ratio of 20 to 80 .mu.l per kg of ground vegetable raw material in the mash and / or milled as another amylase Liquozyme SC DS in a ratio of 150 to 250 .mu.l per kg vegetable raw material used in the
  • amylases are the enzyme marketed under the brand name Novozyme®50024 and / or the enzyme marketed under the brand name Spi ⁇ zyme®Fuel.
  • Amylase Novozyme® °° 50024 is preferred in a ratio of 400 to 600 ⁇ l per kg of ground vegetable raw material in the mash and / or as further e Amylase Spinzyme ⁇ uel (Fa Novozymes Germany GmbH) used in a ratio of 400 to 600 .mu.l per kg of ground vegetable raw material in the mash
  • This second step is preferably carried out at a temperature of 50 0 C to 70 0 C
  • this second Step at a pH value less than 6 is particularly preferably carried out this second step is carried out at a pH of 4 to 5.
  • the residence time of the mash in the second step is preferably between 12 and 36 hours, more preferably between 24 and 32 hours
  • the treatment of mash in Wass ⁇ gen with at least one enzyme for cleavage of poly-sugars according to step ad) of the inventive method in one step preferably the same enzyme classes or preferred enzymes from these classes of the two-stage process or mixtures thereof are used
  • the procedure for cleaving poly-sugars according to step ad) of the process according to the invention is preferably carried out using the same preferred proportions of ground vegetable raw materials in water as in a two-stage procedure. For carrying out the single-stage process, pH values less than 7 are preferred.
  • the temperature of the one-stage process for cleavage of poly-sugars according to step ad) of the inventive method amounts to between 50 0 C and 70 0 C
  • the preferred residence time of the mash in a one-step process is preferably between 24 and 32 hours
  • the procedure described in two steps for the cleavage of poly-sugars according to step ad) of the inventive method is particularly advantageous because the pre-treatment prevents the not yet completely split poly-sugar, which simplifies the process engineering treatment of the mash for both Processes (one or two steps) for the cleavage of poly-sugars according to step ad) of the inventive method given temperatures and pH values are particularly advantageous because they include the pH values and temperatures in which the enzymes used are particularly effective, so that a maximum space-time yield can be achieved
  • the separation of the solids fraction remaining after ad) in step ae) of the process according to the invention can be carried out with or without the use of a flocculant.
  • Possible separation processes include filtration, sedimentation, classification, decantation or centrifugation. Combinations and / or repetitions of the abovementioned separation processes with or without are also possible Use of a flocculant
  • Suitable flocculants include cationic and / or anionic and / or nonionic polymers. Preferred are cationic polymers, most preferably the flocculant Praestol® 853 BC, Stockhausen GmbH & Co. KG
  • the separated remaining solids fraction is fed to a biogas production
  • a biogas production This preferred embodiment is advantageous because the recovered biogas can be burned and the energy obtained from it can be used directly in the inventive process in the form of heat or electricity.
  • the separated remaining solids fraction is dried and further processed into animal feed.
  • This further preferred embodiment of the invention is advantageous because the sale of the animal feed the cost of the process can be increased.
  • the at least partially converting the usable in the glucose-rich fraction usable sugars in biobutanol by microorganisms by a fermentation according to step b) of the method according to the invention is preferably carried out in an anaerobic, operated at room temperature (20 0 C) elevated temperature fermentation.
  • the fermentation is particularly preferably operated anaerobically at an oxygen partial pressure of not more than 1 hPa at ambient pressure (1013 hPa) and a temperature of 30 ° C to 50 0 C.
  • the fermentation is operated anaerobically at an oxygen partial pressure of not more than 0.5 hPa at ambient pressure (1013 hPa) and a temperature of about 35 ° C.
  • the residence time in the fermentation according to step b) of the process according to the invention is preferably between 24 and 72 hours, more preferably about 48 hours.
  • step b) of the process according to the invention is carried out so that in the fermenter, the proportion of the high-glucose fraction in the total mass of the reactor contents is between 10 and 30% by weight. Particularly preferably, the proportion is between 20 and 25% by weight. Further preferably, step b) of the process according to the invention is carried out at a pH of between 4 and 5, more preferably at about 4.5.
  • step b) of the method according to the invention are particularly advantageous because the anaerobic operation of the fermenter, the microorganisms produce by means of a fermentation metabolism alcohols, especially butanol, in an increased amount.
  • the preferred temperatures and pH values are particularly advantageous conditions for the microorganisms and consequently also lead to an increased amount of produced biobutanols.
  • the separation of the microorganisms according to step c) to obtain a fermentation product comprising biobutanol and a biomass solution comprising the microorganisms can be carried out with or without at least partial recycling of the biomass solution into the fermentation and / or into the fermentation
  • the separation takes place by one of the abovementioned separation processes preferred for step ae) of the process according to the invention and / or by an ultrafiltration
  • step c) it is preferred to provide at least partial transfer of the biomass solution from step c) into the conversion by fermentation and / or mixing of the ground vegetable raw materials according to step ab) of the process according to the invention.
  • This embodiment is advantageous because it keeps the microorganisms as producers Dead microorganisms can be used at least partially as a substrate of the living microorganisms. This results in a higher space-time yield of the overall process. Furthermore, the separation of the microorganisms poses the risk of leaving the process in step d) of the process according to the invention used at least reduced membrane
  • step d) of the inventive method can be carried out with or without at least partial slaughteruck the obtained from step d) residual fermentation product in the conversion by a fermentation is preferably an at least partial return of the Step d) obtained residual fermentation product in the
  • Suitable membranes include film membranes
  • Preferred film membranes include cellulose or cellulose membranes, polyamides, polysulfones and / or polysiloxanes.
  • Preferred film membranes are film membranes sold by the company Lenntech under the name FiInUeC 00 BWGO
  • Cellulose derivatives in this context denote chemical compounds in which further chemical groups are covalently bound to the basic cellulose skeleton.
  • Carboxymethylcellulose is to be regarded as such (a part of the hydroxyl groups of the cellulose is as ether with a - CH 2 - COOH (carboxymethyl)) group linked) and hydroxypropylmethylcellulose (a part of the hydroxyl groups of the cellulose is linked as ether with a - CH 3 group, another than ether with - CH 2 - CHOH - CH 3 )
  • Reverse osmosis is usually operated in such a way that a predetermined proportion of biobutanol is obtained in the retentate.
  • the reverse osmosis is operated at a pressure of at least 30 bar, more preferably of at least 40 bar, most preferably of at least 50 bai
  • the reverse osmosis is carried out until the retentate contains between 3 and 30% by weight, more preferably between 5 and 10% by weight, of biobutanol
  • this z B comprises the further concentration of the biobutanol by extraction and / or distillation and / or rectification according to customary methods known to the person skilled in the art Forming of these Processes Further concentration of the biobutanol is preferred by distillation and / or rectification according to customary embodiments of these processes known to the person skilled in the art, wherein in a particularly preferred variant of the process the bottoms product of the distillation and / or rectification predominantly consists of water , in the fermentation according to step b) or the blending of the ground vegetable raw materials from step aa) with water according to step ab) of the inventive method is recycled
  • step e) of the inventive method is particularly advantageous because by this further treatment and the resulting bottom product of the distillation and / or rectification of the energy expenditure of the entire invention Process is reduced per unit of obtained biobutanol, in that parts of the process streams in the process can be demanded in a circle and thus the energy content of these process streams is not removed from the process
  • Grain is first subjected to a fractional grinding z B using a hammer and a drum screen, the bran being separated. Subsequently, in one step (mashing), the product of the fractional grinding is mixed with water (eg recycled water, rec).
  • water eg recycled water, rec
  • the subsequent treatment with enzymes is carried out here in two steps, wherein in the first (liquefying) and second (saccharification) step in addition to the enzymes used Auxiliary substances, for example in the form of co-enzymes, are added.
  • the product of the enzymatic treatment is then largely freed from solid with the prior addition of flocculants (solid-liquid separation), the solid fraction being dried and used as animal feed
  • the liquid fraction of the solid-liquid separation, comprising the usable sugar is therefore together with further water (eg Rec-water), which may also come from the reverse osmosis, but also from the distillation, the conversion (fermentation) fed in the Fermentation contains microorganisms to convert the usable sugars, for example, into biobutanol, CO 2 and hydrogen.
  • further nutrient media and auxiliaries are added to the fermentation.
  • Nutrient media and auxiliaries may here include yeast extract, salt solutions or the like
  • the entire product of the fermentation is a Bakte ⁇ enabtrennung, eg fed in the form of an ultrafiltration and the stream containing the larger proportion of microorganisms is the
  • the distillation is followed by a further step (product preparation) in which by-products which could not be separated from the biobutanol by means of the previous separation processes are separated.
  • by-products include, for example, other alcohols, such as ethanol and Methanol, or acetone and other ketones, or aldehydes of the alcohols produced in the process, and possibly also the acids of the alcohols.
  • a further step is interposed between mashing and enzymatic conversion (liquefaction, saccharification) (gluten separation).
  • the gluten separation leads to an already prepared product stream which is passed into the enzymatic conversion. so that after these two steps, no addition of flocculants for solid-liquid separation is necessary
  • the separated gluten is dried and thus represents another by-product of the inventive method, which increases the efficiency of the entire process z B for use in the Lifter technology for pasta can be sold
  • the solid fraction obtained from the solid-liquid separation is not supplied here for further utilization in the form of animal feed, but used for the production of biogas
  • the biogas can, for example, by fermenting the solids fraction with similar microorganisms, such as those in the Fermentation, but also done by means of other microorganisms or chemical-physical processes
  • the resulting biogas can be used in the sequence either in the form of a direct combustion to produce heat, which z is returned to the novel process in the distillation or fermentation, or the resulting biogas is burned and used to generate electricity, eg by evaporating water and passing it into a steam turbine.
  • the power generated can either be made available again to the process according to the invention in which, for example, the reverse osmosis pump is operated here in the sense of Steiger the economy of the whole process will be sold 4:
  • Example 1 Butanol fermentation with cereals in general (non-fermentable by-products to feed)
  • the liquefaction was carried out at 92 ° C and a residence time of 2 h. After cooling to 63 ° C, the saccharification took place with a residence time of 28 h.
  • the saccharification enzymes used were Novozyme Q ⁇ 50024 (500 ⁇ l / kg flour) and Spirizyme ⁇ uel (500 ⁇ l / kg flour).
  • the pH during the saccharification was 4.2 and was adjusted by the addition of 10 mol% phosphoric acid.
  • the permeate resulting from the ultrafiltration was treated batchwise by means of reverse osmosis.
  • a flat membrane from Lenntech of the type Filmtec °° BW30 with a membrane area of 0.0045 m 2 was used.
  • the reverse osmosis was operated at a

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Abstract

La présente invention concerne une méthode de préparation de biobutanol par fermentation à partir de matières premières végétales, une osmose inverse servant d'étape de séparation.
PCT/EP2008/009162 2007-11-12 2008-10-30 Méthode de préparation de biobutanol à partir de biomasse WO2009062601A2 (fr)

Applications Claiming Priority (2)

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DE102007054150.5 2007-11-12
DE102007054150A DE102007054150A1 (de) 2007-11-12 2007-11-12 Verfahren zur Herstellung von Biobutanol aus Biomasse

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WO2009062601A2 true WO2009062601A2 (fr) 2009-05-22
WO2009062601A3 WO2009062601A3 (fr) 2009-08-06

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JP2015503328A (ja) * 2011-12-22 2015-02-02 ザイレコ，インコーポレイテッド バイオマス処理

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FR2974311A1 (fr) * 2011-04-21 2012-10-26 Metabolic Explorer Sa Recyclage de l'eau par osmose inverse dans un procede de production d'un produit d'interet par fermentation
CN102978274A (zh) * 2012-12-09 2013-03-20 哈尔滨工业大学宜兴环保研究院 一种应用厌氧干发酵技术处理水稻秸秆制取生物絮凝剂的方法
US10427996B2 (en) 2013-12-02 2019-10-01 Braskem S.A. Fermentation hydrocarbon gas products separation via membrane

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US4361651A (en) * 1980-07-18 1982-11-30 Keim Carroll R Process for making fermentable sugars and high-protein products
DE3438024A1 (de) * 1983-10-17 1985-04-25 Institut National de Recherche Chimique Appliquée, Paris Verfahren zur konzentrierung von vergorenen saeften durch umkehrosmose
US20070031919A1 (en) * 2005-04-12 2007-02-08 Dunson James B Jr Treatment of biomass to obtain a target chemical
WO2008025522A1 (fr) * 2006-08-30 2008-03-06 Bayer Technology Services Gmbh Procédé de production de bioalcool, en particulier de bioéthanol et/ou de biobutanol
US20080102502A1 (en) * 2006-10-25 2008-05-01 Brian Foody Inorganic salt recovery during processing of lignocellulosic feedstocks

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4361651A (en) * 1980-07-18 1982-11-30 Keim Carroll R Process for making fermentable sugars and high-protein products
DE3438024A1 (de) * 1983-10-17 1985-04-25 Institut National de Recherche Chimique Appliquée, Paris Verfahren zur konzentrierung von vergorenen saeften durch umkehrosmose
US20070031919A1 (en) * 2005-04-12 2007-02-08 Dunson James B Jr Treatment of biomass to obtain a target chemical
WO2008025522A1 (fr) * 2006-08-30 2008-03-06 Bayer Technology Services Gmbh Procédé de production de bioalcool, en particulier de bioéthanol et/ou de biobutanol
US20080102502A1 (en) * 2006-10-25 2008-05-01 Brian Foody Inorganic salt recovery during processing of lignocellulosic feedstocks

Non-Patent Citations (1)

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Title
GARCIA III, A. ET AL.: "Butanol Fermentation Liquor Production and Separation by Reverse Osmosis" BIOTECHNOLOGY AND BIOENGINEERING, Bd. 28, Nr. 6, 1986, Seiten 785-791, XP002529134 in der Anmeldung erwähnt *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2015503328A (ja) * 2011-12-22 2015-02-02 ザイレコ，インコーポレイテッド バイオマス処理
JP2017192388A (ja) * 2011-12-22 2017-10-26 ザイレコ，インコーポレイテッド バイオマス処理

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AR069259A1 (es) 2010-01-06
DE102007054150A1 (de) 2009-05-14
WO2009062601A3 (fr) 2009-08-06

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