WO2011070061A1 - Verfahren zur gewinnung von ethanol während einer fermentation - Google Patents
Verfahren zur gewinnung von ethanol während einer fermentation Download PDFInfo
- Publication number
- WO2011070061A1 WO2011070061A1 PCT/EP2010/069161 EP2010069161W WO2011070061A1 WO 2011070061 A1 WO2011070061 A1 WO 2011070061A1 EP 2010069161 W EP2010069161 W EP 2010069161W WO 2011070061 A1 WO2011070061 A1 WO 2011070061A1
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- WIPO (PCT)
- Prior art keywords
- ethanol
- fermentation
- gas
- column
- adsorption
- Prior art date
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 347
- 238000000855 fermentation Methods 0.000 title claims abstract description 105
- 230000004151 fermentation Effects 0.000 title claims abstract description 105
- 238000000034 method Methods 0.000 title claims abstract description 76
- 239000007789 gas Substances 0.000 claims abstract description 84
- 238000001179 sorption measurement Methods 0.000 claims abstract description 39
- 239000012159 carrier gas Substances 0.000 claims abstract description 37
- 238000003795 desorption Methods 0.000 claims abstract description 24
- 235000000346 sugar Nutrition 0.000 claims description 58
- 150000008163 sugars Chemical class 0.000 claims description 31
- 239000010457 zeolite Substances 0.000 claims description 26
- 239000000203 mixture Substances 0.000 claims description 25
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 23
- 229910021536 Zeolite Inorganic materials 0.000 claims description 22
- 239000003463 adsorbent Substances 0.000 claims description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000001569 carbon dioxide Substances 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 7
- 238000012856 packing Methods 0.000 claims description 2
- 238000002336 sorption--desorption measurement Methods 0.000 claims 2
- 238000010521 absorption reaction Methods 0.000 claims 1
- 239000000758 substrate Substances 0.000 abstract description 15
- 150000001720 carbohydrates Chemical class 0.000 abstract description 11
- 239000000243 solution Substances 0.000 description 48
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 29
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 20
- 238000011065 in-situ storage Methods 0.000 description 14
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 12
- 239000008103 glucose Substances 0.000 description 12
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- 238000002474 experimental method Methods 0.000 description 11
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- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 description 10
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 description 10
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 241000235647 Pachysolen tannophilus Species 0.000 description 5
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- 235000010633 broth Nutrition 0.000 description 3
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 3
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- 229910052757 nitrogen Inorganic materials 0.000 description 3
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- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
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- HNSDLXPSAYFUHK-UHFFFAOYSA-N 1,4-bis(2-ethylhexyl) sulfosuccinate Chemical compound CCCCC(CC)COC(=O)CC(S(O)(=O)=O)C(=O)OCC(CC)CCCC HNSDLXPSAYFUHK-UHFFFAOYSA-N 0.000 description 1
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- 241001507497 Ogataea thermophila Species 0.000 description 1
- 241000521557 Pichia cactophila Species 0.000 description 1
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- 241000191477 Scheffersomyces segobiensis Species 0.000 description 1
- 241000209056 Secale Species 0.000 description 1
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- 241000209072 Sorghum Species 0.000 description 1
- 235000011684 Sorghum saccharatum Nutrition 0.000 description 1
- 241000694025 Sorghum x drummondii Species 0.000 description 1
- 235000021536 Sugar beet Nutrition 0.000 description 1
- 241001025522 Suhomyces emberorum Species 0.000 description 1
- 241000207200 Thermoanaerobacter acetoethylicus Species 0.000 description 1
- 241001147775 Thermoanaerobacter brockii Species 0.000 description 1
- 241000186337 Thermoanaerobacter ethanolicus Species 0.000 description 1
- 241000204649 Thermoanaerobacter kivui Species 0.000 description 1
- 241001603561 Thermoanaerobacter mathranii Species 0.000 description 1
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- 241000222124 [Candida] boidinii Species 0.000 description 1
- 241000037109 [Candida] picachoensis Species 0.000 description 1
- 241000512905 [Candida] sonorensis Species 0.000 description 1
- 241000192282 [Candida] tenuis Species 0.000 description 1
- 238000007171 acid catalysis Methods 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 150000004645 aluminates Chemical class 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- -1 aluminum silicates Chemical class 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
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- 239000010905 bagasse Substances 0.000 description 1
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- 230000000035 biogenic effect Effects 0.000 description 1
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- 229940041514 candida albicans extract Drugs 0.000 description 1
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- ULHPJBAQOMZNCP-UJPDDDSFSA-N ethanol;(2r,3s,4r)-2,3,4,5-tetrahydroxypentanal Chemical compound CCO.OC[C@@H](O)[C@H](O)[C@@H](O)C=O ULHPJBAQOMZNCP-UJPDDDSFSA-N 0.000 description 1
- 125000000816 ethylene group Chemical group [H]C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 238000012262 fermentative production Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 150000002402 hexoses Chemical class 0.000 description 1
- 238000004128 high performance liquid chromatography Methods 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 229940031154 kluyveromyces marxianus Drugs 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000010871 livestock manure Substances 0.000 description 1
- 239000010445 mica Substances 0.000 description 1
- 229910052618 mica group Inorganic materials 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
- C07C29/84—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by extractive distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- 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
- C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
- C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
-
- 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 ethanol by fermentation. Background of the invention
- yeasts or bacteria may convert the sugar monomers consisting of five (“C5 sugars”, pentoses) and / or six carbon atoms ("C6 sugars", hexoses) to ethanol ⁇ Huber et al., Chem. Rev , 2006, Vol. 106, pp. 4044-4098). Ethanol is called "Bioethano! If it is made from biogenic raw materials.Bioethano!
- LCB lignocellulosic biomass
- ethanol For the production of ethanol by fermentation, separation of the ethanol from the fermentation solution is required. These techniques include pervaporation, extraction, adsorption, reverse osmosis, and gas stripping (Windsperger et al., Aidstechnik, 1989, Vol. 23, pp. 16-21; Qureshi et al., Bioprocess Biosyst. Eng., 2005, Vol. 27, pp. 215-222).
- the ethanol can be converted into the gas phase.
- Gas stripping is a selective removal of volatile substances from the fermentation solution (Ezeji et al., J. Ind. Microbiol. Biotechnol., 2007, Vol. 34, 771- The ethanol must be separated from the ethanol-gas mixture after the conversion into the gas phase.
- CA 1 195 258 describes a process in which, after fermentation, the fermentation solution is subjected to gas stripping and the ethanol-carrier gas mixture is then adsorbed on a molecular sieve under conditions in which the capillary condensation of water is avoided.
- this method does not allow to control the ethanol concentration during the fermentation.
- Walsh et al. discloses a process in which C6 sugar is fermented to ethanol and the ethanol is separated in situ from the fermenter by gas stripping and adsorbed on activated carbon. This method allows to adjust the ethanol concentration in the range of 6% (w / v) during the fermentation.
- activated carbon is not suitable for an economical process.
- Dominguez et al. (Biotech. Bioeng., 2000, Vol. 67, pp. 336-343) show that the conversion of C5 sugars to ethanol with the yeast Pichia stipitis is inhibited in only 2% (w / v) ethanol. Dominguez et al.
- the object was to provide an economical process for the production of ethanol by fermentation, which has a high ethanol yield when using mixtures of C5 and C6 sugars, as e.g. from lignocellulosic biomass.
- a process for producing ethanol comprising: a. the fermentative conversion of C5 and / or C6 sugars to ethanol in a fermentation solution;
- FIGs 1a and 1b show embodiments of the method according to the invention with gas stripping in the fermenter (1a) and in an external gas stripping column (1b).
- Figure 2 shows the course of the ethanol concentration during the fermentation according to Example 1A.
- FIG. 3 shows the course of the glucose, xylose and ethanol concentration during the fermentation according to Game 1 B.
- Figure 4 shows the course of the glucose, xylose and ethanol concentration during the fermentation according to Example! 1C.
- FIG. 5 shows the course of the glucose, xylose and ethanol concentration during the fermentation according to Example 1 D.
- Figure 6 shows a comparison between the zeolite used according to the invention and activated carbon with respect to the ethanol selectivity.
- Figure 7 shows an embodiment of the invention with turret configuration.
- the solution initially contains less than 200 g / L of sugar, less than 100 g / L of C6 sugar, more preferably less than 80 g / L of C6 sugar, most preferably less than 70 g / L C6 sugar, and less than 100 g / L C5 sugar, more preferably less than 35 g / L C5 sugar, most preferably less than 30 g / L C5 sugar.
- the solution contains less than 120 g / L of sugar, with 90% or more of the sugars being C6 sugars.
- the solution contains less than 120 g / L of sugar, with 90% or more of the sugars being C5 sugars.
- the solution contains less than 200 g / l of sugar, preferably less than 120 g / l of sugar, where 20 to 40% of the sugars are C5 sugars and correspondingly 60 to 80% C6 sugars.
- This solution is obtained regularly from carbohydrate-based raw substrates. It may be necessary to digest these raw substrates by means of suitable pretreatment processes and / or to enzymatically or carbohydrate the carbohydrates into sugar monomers by acid catalysis. Before the fermentation, the solution can optionally be concentrated.
- Carbohydrate-containing raw substrate includes carbohydrate-containing pure substances, mixtures of various carbohydrates as well as complex mixtures of substrates containing carbohydrates.
- Carbohydrate-containing material also includes waste products from the forestry and agriculture and food processing industries as well as municipal waste.
- carbohydrate-containing materials are, in particular, lignocellulosic biomass (LCB), which contains cellulose, hemicellulose and lignin.
- LCB lignocellulosic biomass
- Agricultural LCBs include cereal straws and husks (wheat, rye, barley, oats), corn straw and spindein, manure, sugar cane press cake (bagasse), sugar beet pulp (beet pulp!), And herbaceous materials and grasses such as barley grass , Sericea Lespedeza, Gray Millet (Panicum virgatum, Switchgrass), Elephant Grass (Miscanthus, Miscanthus), and Sudan Grass (Sorghum sudananse, Sorghum drummondii).
- LCB in the form of forestry waste products includes tree bark, wood chips and wood waste.
- LCB in the form of raw food industry substrates, includes fruit pulp, agave residues, coffee residues and mill oil wastes such as rapeseed press cake and mill effluents.
- LCB in the form of raw substrates from the Pulp and paper industry includes pulp and paper mill wastewater.
- the fermentation solution is preferably obtained from LCB by hydrolysis.
- the solution further additives such as pH adjusters can be added.
- the C5 and / or C6 sugars released during the hydrolysis preferably C5 sugars, optionally together with C6 sugars, are converted to ethanol by fermentation.
- yeasts or bacteria are used.
- Particularly preferred are C5- and C6-sugar-metabolizing yeasts and in particular those whose fermentation activity is inhibited at ethanol concentrations above 5% (w / v).
- the temperature of the fermenter is between 10 and 100 ° C, preferably between 10 and 50 ° C, more preferably between 20 and 50 ° C, most preferably between 20 and 40 ° C.
- mesophilic yeasts such as Pichia stipitis, Pichia segobiensis, Candida shehatae, Candida tropicalis, Candida boidinii, Candida tenuis, Pachysolen tannophilus, Hansenula polymorph, Candida famata, Candida parapsilosis, Candida rugosa, Candida sonorensis, Issatchenkia terricola, Kloeckera apis , Pichia barken, Pichia cactophila, Pichia deserticola, Pichia norvegensis, Pichia membranaefaciens, Pichia mexicana and Torulaspora delbrueckii.
- thermophilic microorganisms are used.
- Thermophilic yeasts include, for example, Candida bovina, Candida picachoensis, Candida emberorum, Candida pintolopesii, Candida thermophila, Kluyveromyces marxianus, Kluyveromyces fragilis, Kazachstania telluris, Issatchenkia orientalis and Lachancea thermotolerans.
- Thermophilic bacteria include Clostridium thermocellum, Clostridium thermohydrosuiphuricum, Clostridium thermosaccharolyticium, Thermoanaerobium brockii, Thermobacteroides acetoethylicus, Thermoanaerobacter ethanolicus, Clostridium thermoaceticum, Clostridium thermoautotrophicum, Acetogenium kivui, Desulfotomaculurn nigrificans, and Desulfovibrio thermophilus, Thermoanaerobacter tengcongensis, Bacillus stearothermophilus and Thermoanaerobacter mathranii.
- the following mesophilic yeasts are particularly preferably used: Saccharomyces cerevisiae, Pichia stipitis, Pachysols tannophilus, Candida shehatae
- the fermentation is preferably carried out in batch mode (batchwise), in fed-batch mode or in continuous operation. Particularly preferably, the fermentation is carried out in batch mode.
- the volatile constituents in particular the product ethanol, are converted in-situ into the gas phase, in particular by stripping with an inert carrier gas.
- / n-s / ii / removal of the ethanol refers to the removal of the ethanol, for example by gas stripping, parallel to its fermentative production. This can be done either continuously or intermittently.
- sugar is simultaneously reacted in ethanol and at least a portion of this ethanol, for example by gas stripping, removed.
- at least a portion of the sugar in ethanol is first converted by fermentation and then at least a portion of this ethanol is removed, for example by gas stripping. Thereafter, again at least a portion of the sugar is converted to ethanol, etc.
- sugar is continuously converted into ethanol, but the ethanol removed only periodically, for example by gas stripping.
- In situ removal of the ethanol may be by gas stripping, by pervaporation, or by similar methods to convert the ethanol to the gas phase.
- the conversion into the gas phase can take place either in the fermentation vessel or in a separate apparatus.
- a carrier gas is preferably used. Suitable carrier gases are gases such as carbon dioxide, helium, hydrogen, nitrogen or air, as well as mixtures of these gases. Particularly preferred are carbon dioxide and mixtures of carbon dioxide and air, whereby microaerobic conditions can be adjusted if necessary.
- An advantage of this embodiment of the method according to the invention is that the carbon dioxide formed during the fermentation can be used directly as a carrier gas.
- the fermentation takes place in a stirred tank reactor or in a reactor or in an air-lift reactor.
- the gas exchange is also possible via an external gas stripping column connected to the fermenter, which is fed continuously with the fermentation solution and whose outlet is led back into the fermenter.
- an external gas stripping column in countercurrent and / or in combination with Füil analysesnpern for increased mass transfer, such. Raschigingen operated.
- the specific gassing rate is preferably between 0.1 and 10 ⁇ m, more preferably between 0.5 and 5 ⁇ m.
- the stripping is preferably carried out at a pressure between 0.1 and 2 bar, more preferably between 0.5 and 1, 1 bar. Stripping at reduced pressure is particularly preferred.
- the gas bubbles are preferably dispersed. This can be done with a stirrer, which is arranged so that fine bubbles of the carrier gas arise.
- the ethanol is removed from the fermentation broth at the fermentation temperature. Thus, no additional thermal energy for heating the fermentation solution is necessary.
- a further advantage of the method according to the invention is that the enthalpy of vaporization transferred from the liquid into the gas phase by the transfer of the volatile substances contributes to the cooling of the fermenter and thus the required cooling capacity for keeping the temperature constant in the fermenter is reduced.
- the gas stream leaving the fermenter is passed through one or more columns filled with one or more types of adsorbents.
- At least one of the columns contains zeolite as adsorber.
- Further adsorbents are silicas, bentonites, silicalites, clays, hydrotalcites, aluminum silicates, oxide powders, mica, glasses, aluminates, clinoptolites, gismondines, quartzes, activated carbons, bone charcoal, montmorillonites, polystyrenes, polyurethanes, polyacrylamides, polymethacrylates or polyvinylpyridines.
- only zeolites are used as adsorbents.
- the zeolite has a Si0 2 / Al 2 O 3 ratio of 200 to 000, and particularly preferably a Si0 2 / Al 2 O 3 ratio of 400 to 800.
- Particularly preferred are the synthetic zeolites according to US 7,244,409.
- the mass ratio of adsorbent to adsorbed ethanol is preferably between 1 and 1000, more preferably between 5 and 20.
- the temperature can be influenced and kept constant via the Schuschin within the column, whereby the selectivity of the adsorbent can be influenced.
- the selectivity is controlled not only by the temperature but also by the pressure within the column.
- the temperature during the adsorption of the ethanol is preferably between 10 and 100 ° C., more preferably between 20 and 50 ° C.
- the pressure is preferably between 0.5 and 10 bar, more preferably between 1 and 2 bar.
- adsorption it is particularly preferred to carry out the adsorption at a temperature which is not above the temperature of the ethanol-carrier gas mixture at the exit from the fermentation solution.
- neither the ethanol-gas mixture nor the adsorber are heated prior to adsorption.
- the adsorption takes place at overpressure.
- At least one C5 sugar is present in the fermentation solution in this process.
- This also includes fermentation solutions comprising mixtures of at least one C5 sugar and at least one C6 sugar. It is particularly preferred that the at least one C5 sugar present in the fermentation solution is converted to ethanol.
- the amount of adsorbent material used is preferably adjusted to the amount of ethanol produced by the fermentation.
- the amount of adsorbed ethanol at the end of the fermentation is at least 20%, preferably at least 50% and more preferably at least 90% of the maximum ethanol uptake amount of the adsorber. Both the amount of ethanol produced by the fermentation and the maximum ethanol uptake of the adsorber can be determined prior to fermentation.
- the gas stripping and the adsorption is carried out exactly as described in Example 2, ie a solution with known ethanol concentration is introduced and then stripped continuously. During this time, the ethanol concentration in the template is measured hourly. If this does not change (at the latest after 24 hours) the capacity of the adsorber material is exhausted. Then, the experiment is stopped and the volume of the original and the concentration of the ethanol obtained therein are determined, so that the masses of ethanol and water can be calculated. The differences between the initially given masses and those after the end of the test give the adsorbed masses of ethanol and water (mass balance). These values can be used to determine the adsorbed ethanol concentration and the capacity of the adsorber material.
- the maximum amount of ethanol formed in the fermentation can be estimated using the theoretical yield coefficients.
- the theoretical yield coefficients are 0.51 g ethanol per 1 g glucose or 0.46 g ethanol per 1 g xylose (Lee et al., J. Microbiol. Biotechn., 2001, Vol. 11 (3), p -388).
- the ethanol yields achieved in practice are 70-100%, typically 90-95% of the theoretical yields. With the help of the expected amount of ethanol and a surcharge of typically 10-20%, the calculation of the required amount of adsorber.
- the adsorber material may be contained in one or more columns. Preferably, several, more preferably 2 to 6 columns are used. These columns can be connected in series or in parallel. Advantages of the parallel connection are firstly that thus a quasi-continuous operation is made possible by two or more columns alternating between adsorption and desorption, and secondly that the released thermal energy can be transferred in the adsorption for desorption in another column So adsorption and desorption can be performed simultaneously on different columns.
- the columns are preferably provided in a turret arrangement.
- 2 to 6 columns are switched so that the column or columns in which the adsorption takes place is switched in parallel to the column (s) in which the desorption proceeds. If adsorption occurs in more than one column, these columns can be connected in series.
- 6 columns e.g. in the "turret configuration" in columns 1 to 3, the adsorption is carried out, column 4 is heated for desorption, the desorption takes place in column 5, and column 6 is allowed to cool down.
- the adsorbent column is changed when the amount of adsorbed ethanol is at least 90%, more preferably at least 95% of the maximum ethanol uptake amount of the adsorbent in this column.
- the Erftndungssiee method with multiple adsorption also opens up the possibility of switching two or more columns in series, each filled with different adsorbents having different selectivities and / or capacities.
- the adsorbent preferably flows through the adsorber in the order of increasing ethanol binding selectivities (with respect to water).
- the gas stream depleted of ethanol can be fed back into the fermenter after leaving the adsorption column and is then available again for gas stripping.
- the adsorption can be carried out in fluidized bed operation.
- the ethanol concentration in the fermentation solution can be maintained below 5% (w / v), preferably below 2% (w / v) throughout the fermentation period.
- the fermentation is preferably carried out as long as ethanol is produced. Preferred fermentation times are 20 to 120 hours, more preferably 30 to 80 hours.
- the process of the invention allows the selective desorption of the ethanol from the adsorbent by increasing the temperature and / or reducing the pressure within the column.
- the thermal energy is introduced directly onto the adsorbent pack via the acid wall and optionally additionally via the heating coils in the interior of the column.
- Preference is given to temperatures between 25 and 300 ° C and absolute pressures between 0 and 10 bar.
- Particularly preferred are temperatures between 80 and 180 ° C, and absolute pressures at reduced pressure, preferably between 0.1 and 1 bar.
- a carrier gas is used for the discharge of the desorbed ethanol from the column.
- the same inert carrier gas is used here, which is also used for gas stripping.
- the temperature and the absolute pressure of the carrier gas are adjusted according to the above-described temperatures and absolute pressures within the column.
- upstream heat exchangers and / or throttles or compressors are suitable.
- the desorption can be carried out in fluidized bed operation.
- a preferred embodiment of the method according to the invention provides for the condensation of the desorbed ethanol gas.
- the gas stream is compressed and / or cooled by using one or more compressors and / or one or more heat exchangers and / or one or moredefailen. Particularly preferred are countercurrent heat exchangers.
- condensates are obtained with different ethanol concentrations by the series connection of two or more heat exchangers and / ordefalien with different cooling temperatures. In addition, this opens up the possibility of selective condensation of still existing other accompanying substances, such as water or other volatile substances.
- condensation releases the condensation enthalpy.
- this thermal energy is transferred by means of heat exchangers to preceding and / or possible subsequent, energy-requiring method steps.
- these energy-demanding method steps are the preceding desorption of the ethanol and / or a possible subsequent rectification.
- the condensed ethanol obtained is further purified and concentrated.
- a typical concomitant of ethanol in the condensate is water.
- the removal of water and / or other impurities can be done by rectification.
- the temperature is kept just below the boiling point of the resulting condensate, so that the ethanol solution to be rectified is transferred to the rectification near the boiling point, thereby reducing the energy required for the rectification.
- the energy requirement of the rectification can be further reduced.
- the water obtained in the bottom of the rectification column can be recycled to the fermenter.
- the azeotrope is obtained between ethanol and water.
- suitable separation techniques such as the removal of water by means of a molecular sieve, or by the use of selective membrane techniques. It is also possible to shift the position of the azeotrope via the change in the pressure during the rectification.
- a further alternative embodiment of the method according to the invention provides for feeding the condensate obtained after desorption to pervaporation, so that absolute ethanol can be achieved.
- the carrier gas stream which is recovered by the condensation of the ethanol and other possible impurities, circulated, so that no or only a small external supply of carrier gas is necessary for the gas stripping in the fermenter.
- Figure 1a shows a possible embodiment of the method according to the invention.
- An inert carrier gas stream (1) is blown into the fermenter (2) for gas stripping.
- LCB is fermented to ethanol, with adjuvants (3) such as pH steep.
- the gas leaving the fermenter, which contains ethanol and other volatiles, is passed through an adsorption column (4) which selectively adsorbs the ethanol.
- an adsorption column (4) which selectively adsorbs the ethanol.
- two or more columns are connected in parallel and / or in series. A thermal exchange between the columns is achieved by internal heating coils.
- Part of the carrier gas stream is removed due to the carbon dioxide formed by fermentation (5).
- the temperature and / or the pressure within the columns (4) is changed.
- the carrier gas stream necessary for the discharge of the desorbed ethanol is adjusted accordingly via a heat exchanger (6) and / or throttles.
- the gas leaving the column during desorption is then condensed by means of compression and / or cooling (7).
- the thus regenerated carrier gas stream (8) is recycled.
- the condensate is further purified and concentrated by feeding it to a rectification column (9). At the bottom of the column, water is obtained (10), at the top of the column, the azeotrope between ethanol and water (11).
- FIG. 1b shows a further possible embodiment of the method according to the invention, in which case gas stripping takes place in an external gas stripping column (12) connected to the fermenter. Fermentation solution is fed to the external gas stripping column and the stripped solution is then returned to the fermenter. All further process steps are analogous to Figure 1a.
- Figure 4 shows the "turret configuration, in which three columns (A1-A3) for adsorption from the stripping gas from the fermenter (F) are connected in series.
- the columns A4 to A6 are connected in parallel.
- the column becomes A4 heated (a), the acid A5 desorbed (b) and the acid A6 cooled (c).
- column A3 enters the heating phase (a), A4 is desorbed (b) and A5 is cooled (c).
- the acids A6, A1 and A2 are then connected in series. After 6 cycle times, the same acid is desorbed again as at the beginning, so that one cycle is completed and a new one begins.
- the following method is furthermore particularly preferred:
- the ethanol concentration is preferably kept below 5% (w / v) by controlling the rate of inflow of the ethanol and C5 sugar-containing fermentation solution into the second fermenter and / or the gasification rate during gas stripping and / or the amount of adsorber be adjusted.
- the adsorber preferably contains zeolite.
- the heat released during the adsorption is used for the desorption.
- the fermentation, the gas stripping, the adsorption and desorption and the final cleaning are preferably thermally linked to one another, so that the energy costs for the purification of the end product ethanol are significantly reduced compared to conventional processes.
- Example 1- / n-s / fn-segregation of ethanol during fermentation
- Pachysolen tannophilus (DS Z, Braunschweig) was fermented with and without in situ separation of ethanol under otherwise identical conditions for 100 hours at 30 ° C.
- the fermentation medium consisted of 5 g / L Bacto TM Yeast Extract (Becton, Dickinson Co., France), 6.7 g / L 1x Difco Yeast Nitrogen Base w / o Amino Acids (Becton, Dickinson Co., France), to 350 mL H 2 0 dist.
- Pichia stipitis (DSMZ, Braunschweig, Germany) was fermented with and without in situ separation of ethanol under otherwise identical conditions for 95 hours at 30 ° C under microaerobic conditions.
- the fermentation medium was pretreated and hydrolyzed lignocellulosic substrate.
- Two 800 mL cultures each were prepared in 1, 4 L small fermenter.
- 56 g / l of glucose and 31 g / l of xylose were contained as the source of carbon dioxide. Fermented in batch mode.
- One of the two cultivations was performed without in situ stripping, the other with in situ stripping.
- the gas flow was adjusted to 1 vvm via a rotameter (Vöglin, Aesch, Switzerland). With the help of a membrane pump (KNF, Freiburg, Germany) and gas-tight hoses (VWR, Darmstadt, Germany), the gas flow was passed through a Glasrochie and then returned.
- the glass column was with 535 g of zeolite granules (ZSM-5; Süd-Chemie AG, Germany).
- zeolite granules ZSM-5; Süd-Chemie AG, Germany.
- the ethanol content was quantified by gas chromatography (Trace GC, ThermoFisher, Germany) and the sugars by HPLC (Dionex, USA).
- the weight gain of the zeolite and the water content of the adsorbed mixture were determined by Karl Fischer titration (Schott Instruments, Germany).
- Karl Fischer titration Schott Instruments, Germany.
- Example 1 B A sequential fermentation was carried out, with first fermentation of the glucose anaerobically in batch mode with Saccharomyces cerevisiae (DSMZ, Braunschweig, Germany) without in situ Gas stripping was performed.
- the solution used contained 63 g / L glucose and 32 g / L xylose. Fermented in batch mode.
- the resulting xylose- and ethanol-containing substrate was fermented with / ns / fu-separation of ethanol under microaerobic conditions in the batch with Pachysolen tannophiius (DSMZ, Braunschweig, Germany) for 114 hours at 30 ° C.
- Example 1 B All conditions in this experiment were identical to Example 1 B.
- Pachysolen tannophilus (DSMZ, Braunschweig, Germany) for 113 hours at 40 ° C fermented.
- the start volume was 300 mL.
- the result of the experiment is shown in Figure 5.
- the analysis values of the fermentation broths show that the ethanol concentration in the fed-batch mode at 40 ° C can be kept below 1.5% and the simultaneous conversion of both the C6 and C5 sugars with the combination of fed-batch operation and In situ gas stripping was made possible.
- Example 2 Concentration of a 7.5% (w / v) ethanol-water solution by gas stripping, adsorption, desorption and condensation
- the temperature was linearly increased to 150 ° C within 90 minutes by means of the heating coils and over the column wall.
- the desorbed ethanol was condensed in a cold trap at -20 ° C.
- the absolute pressure was 800 mbar for adsorption and desorption.
- the carrier gas stream was circulated.
- Mass balance were therefore calculated the adsorbed amounts of ethanol and water and thus determined the following ethanol mass fractions of the adsorbed mixture:
- Activated carbon 49.8% (w / w) It turns out, therefore, that the use of a zeolite has clear advantages over activated carbon, since the adsorption of zeolites proceeds much more selectively. This is a decisive advantage in terms of energy costs for the subsequent thermal purification.
- activated carbon With activated carbon, the technical effect of the present application can not be achieved because activated carbon binds significantly more water than zeolite.
- the key advantage of zeolite over activated carbon is therefore the higher selectivity, i. Zeolite preferably binds ethanol and only a little water. This simplifies the subsequent purification of the desorbed ethanol (less mass must be desorbed, the rectification column is smaller and the energy costs are drastically reduced).
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EP10785092.7A EP2510101B1 (de) | 2009-12-08 | 2010-12-08 | Verfahren zur gewinnung von ethanol während einer fermentation |
PL10785092T PL2510101T3 (pl) | 2009-12-08 | 2010-12-08 | Sposób odzyskiwania etanolu podczas fermentacji |
ES10785092.7T ES2648245T3 (es) | 2009-12-08 | 2010-12-08 | Procedimiento para la producción de etanol durante una fermentación |
MX2012006592A MX2012006592A (es) | 2009-12-08 | 2010-12-08 | Un procedimiento para la obtención de etanol durante la fermentacion. |
CN2010800636214A CN102791868A (zh) | 2009-12-08 | 2010-12-08 | 在发酵过程中获得乙醇的方法 |
AP2012006354A AP3405A (en) | 2009-12-08 | 2010-12-08 | Method for obtaining ethanol during fermentation |
US13/514,510 US9637434B2 (en) | 2009-12-08 | 2010-12-08 | Method for obtaining ethanol during fermentation |
BR112012013917A BR112012013917B1 (pt) | 2009-12-08 | 2010-12-08 | um método para obtenção de etanol durante a fermentação |
AU2010329971A AU2010329971B2 (en) | 2009-12-08 | 2010-12-08 | Method for obtaining ethanol during fermentation |
CA2783682A CA2783682C (en) | 2009-12-08 | 2010-12-08 | Method for obtaining ethanol during fermentation |
RU2012128497/10A RU2529371C2 (ru) | 2009-12-08 | 2010-12-08 | Способ получения этанола в процессе ферментации |
UAA201208335A UA105823C2 (uk) | 2009-12-08 | 2010-12-08 | Спосіб одержання етанолу в процесі ферментації |
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DK2333092T3 (da) | 2009-12-08 | 2013-01-07 | Sued Chemie Ip Gmbh & Co Kg | Fremgangsmåde til indvinding af ethanol under en fermentering |
DE102011104006A1 (de) * | 2010-12-10 | 2012-06-14 | Süd-Chemie AG | Granulierte Zeolithe mit hoher Adsorptionskapazität zur Adsorption von organischen Molekülen |
JPWO2016067677A1 (ja) | 2014-10-30 | 2017-08-17 | 三菱化学株式会社 | 高濃度アルコールの製造方法 |
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