WO1985002864A1 - Procede de production d'ethanol - Google Patents

Procede de production d'ethanol Download PDF

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Publication number
WO1985002864A1
WO1985002864A1 PCT/SE1984/000439 SE8400439W WO8502864A1 WO 1985002864 A1 WO1985002864 A1 WO 1985002864A1 SE 8400439 W SE8400439 W SE 8400439W WO 8502864 A1 WO8502864 A1 WO 8502864A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
fermentor
yeast
liquid
gas
Prior art date
Application number
PCT/SE1984/000439
Other languages
English (en)
Inventor
Anders Hofstedt
Original Assignee
Ac Biotechnics Ab
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Ac Biotechnics Ab filed Critical Ac Biotechnics Ab
Publication of WO1985002864A1 publication Critical patent/WO1985002864A1/fr

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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
    • 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 present invention relates to a process for the production of ethanol through continuous fermentation of a carbohydrate containing substrate in a fermentor during simultaneous recovering of carbon dioxide of a purity exceeding 95 % by volume, in which process a high yeast concentration is maintained in the fermentor by retaining the yeast in a circuit comprising the fermentor and a separation step, in which a stream of fermentation liquor from the fermentor is divided into a yeast impoverished stream which is fed to an ethanol recovering step, and a yeast enriched stream, which is returned to the fermentor, and further by adding to the fermentation liquor in said circuit an oxygen containing gas for achieving ja growth of yeast that balances the yeast losses in the circuit.
  • the object of the present invention is to achieve the supply of oxygen required for the yeast growth in the fermentation process concerned so that the carbon dioxide discharged from the fermentor has a purity exceeding 95 % by volume and so that the additional operation costs and plant costs required for this purpose will be considerably lower than the value of the produced carbon dioxide.
  • this object has been reached in a process of the kind introductively mentioned, which process is primarily characterized in that a liquid stream from the fermentor is atomized in an oxygen containing gas stream, whereafter the liquid phase is separated from the gas stream and returned to the fermentor.
  • the oxygenation of the fermentation liquor occurs by dispersing the fermentation liquor in the gas phase in contrast of conventional technique according to which the gas is dispersed in the form of bubbles in the liquid phase.
  • this modification has proved to give a much larger effect on the oxygen assimilation and therefore also to require a considerably smaller liquid flow than could be expected from known values of the oxygen solubility.
  • a probable explanation herefore is that the dispersing of the liquid phase not only facilitates that equilibrium with respect to dissolved oxygen in the liquid is reached, but also drastically reduces the oxygen diffusion distance into the yeast cells, thereby enabling the yeast cells to assimilate a substancial part of the available oxygen during its transport through a gas-liquid contact zone.
  • Oxygenation tests carried out according to the invention have shown that as much as 60 - 80 % of the total oxygen absorbed by the liquid has been assimilated by the yeast cells. In all circumstances the recirculation flow of fermentation liquor can now according to the invention be reduced so that the operation costs and plant costs associated with oxygen supply outside the fermentor can be restricted well below the value of the carbon dioxide produced in the fermentor.
  • the stream enriched in yeast cells from the yeast separation step is primarily used for the oxygenation step. If an additional flow of fermentation liquor is required for achieving sufficient yeast growth in the circulation loop, a further stream of fermentation liquor is discharged from the fermentor and supplied to the gas-liquid contact step. This stream should prior to introduction into the oxygenation step be screened from particles in a screening step.
  • the same screening equipment can suitably be used for the stream of fermentation liquor recirculated to the gas-liquid contact step.
  • oxygen containing gas either air or oxygen gas can be used. Since the gas supplied to the gas-liquid contact step is separated from fermentation liquor before it is returned to the fermentor, the nitrogen in the air does not cause any disadvantage, left out that the required apparatus volume increases in inverse proportion to the oxygen concentration of the gas used. The profitability of using oxygen gas is thus determined by the cost for available oxygen gas and the reduction in plant costs due to reduced apparatus volume.
  • oxygen gas can however be optimal to first disperse the liquid stream to be oxygenated in an air stream, since a part of the oxygen containing gas can be considered as consumed for driving off the carbon dioxide contained in the fermentation liquor.
  • oxygen gas can thereafter be supplied.
  • the gas-liquid contact apparatus required for the process according to the invention can be arbitrarily selected among known equipment for dispersing liquid in a gas phase.
  • the oxygenation is carried out in a packed column, to which fermentation liquor is supplied in the top and streams downwards by gravity through the packing in counter-current with oxygen or air introduced at the bottom of the column.
  • the oxygenated fermentation liquor is collected on the bottom of the column and returned to the fermentor.
  • Fig. 1 is a flow sheet of the part of a continuous ethanol fermentation process of interest for the invention
  • Fig. 2 shows an alternative embodiment of the gas-liquid contact step of the process shown in Fig. 1.
  • a fermentor 1 is continuously supplied with a hydrocarbon containing substrate through a line 2. Carbon dioxide produced in the fermentor is continuously discharged from a gas outlet 3, and a stream of fermentation liquor is continuously discharged through a line 4 from the bottom of the fermentor. Stream 4 is supplied to a screening device 5. From the screening device a stream 6 enriched in solid material is discharged, and a part
  • the liquid stream 7 which passes through the screening device 5 is divided into a stream 8, which is led directly to a packed column 9 for oxygenation, and a stream 10 which is supplied to a centrifugal separation step 11.
  • the stream 10 is divided into a yeast enriched stream 12, which together with the stream 8 is fed into the packed column 9, and a yeast impoverished stream 13, which is led to a distillation unit (not shown) for recovering of ethanol.
  • the stream 13 is so dimensioned that the ethanol content in the fermentor 1 is maintained at a desired value in the range 3-7 % by weight.
  • the stream of fermentation liquid 8 and the yeast enriched stream 12 is introduced in the top of the packed column 9 and flows by gravity downwards in the column through a packing of filler bodies 14 in counter-current with air or oxygen gas supplied through a gas inlet 15 in the lower part of the column.
  • the downward streaming liquid is dispersed in the upward streaming gas phase, whereby the dispersed liquid elements offer a large surface for oxygen absorbtion.
  • Unabsorbed gas and carbon dioxide driven off from the liquid stream is discharged in the top of the column through a gas outlet 16, while the downward streaming liquid Is collected in a collecting zone 17 in the bottom of the column, wherefrom it is returned to the fermentor through line 18.
  • the gas liquid contacting apparatus shown in Fig. 2 consists as in Fig. 1 of a packed column 20.
  • the liquid stream 21 supplied in the top of the column for oxygenation is dispersed in a first gas-liquid contact zone 22, consisting of an upper part of a packing of filler bodies, where the dispersed liquid meets an upwards streaming air stream, which is fed into the column at an intermediate level through line 23.
  • a second contact zone 24, constituting the lower part of the packning the downwards streaming liquid dispersion then meets an oxygen gas stream, which is fed into the lower part of the column through line 25.
  • From a collecting zone 26 in the bottom of the column fermentation liquid is returned to the fermentor through line 27.
  • a fermentor with a liquid volume of 2.8 m continuous fermentation of a hydrolysed wheat substrate was carried out.
  • the substrate was supplied through line 2 in a fermentation plant of the kind schematically shown in Fig. 1.
  • the yeast species used was Saccaromyces Serevisiae.
  • From the fermentor a stream of fermentation liquid was discharged, and the stream was dimensioned so that a sufficient liquid stream remained after screening through a bow sieve 5 to discharge from the separation step 11 about 23 kg/h ethanol with the yeast-free stream 13 to a distillation unit and so that the yeast concentrate stream 12 together with the remaining partial stream 8, which is recirculated directly to the packed column 9, was 1.92 m /h.
  • a part of the sieve reject 6 is returned through 6a to the fermentor, while the remaining part 6b is washed in a further screening step (not shown) with recirculated stillage from the distillation unit to reduce yeast losses.
  • the sieve reject obtained thereby was supplied to the stripping unit of the distillation plant and the liquid stream freed from solid material was returned to the fermentor.
  • the united streams 8 and 12 were discharged in the top of a packed column having a diameter of 200 mm and containing a 2.5 m packing of intalox plastic saddles. At the lower part of the packing an oxygen gas stream of 0.74 m /h was introduced. The gas flow leaving the column was measured and analysed with respect of oxygen and carbon dioxide. The following test data were obtained:

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  • Organic Chemistry (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Zoology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Biotechnology (AREA)
  • Health & Medical Sciences (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)

Abstract

Procédé de production d'éthanol par fermentation continue d'un substrat contenant de l'hydrate de carbone en présence d'une levure dans une cuve de fermentation (1) pendant la récupération simultanée d'anhydride carbonique de grande pureté, plus spécifiquement d'une pureté dépassant 95% par volume. On maintient une forte concentration de levure dans la cuve de fermentation en maintenant la levure dans un circuit comportant la cuve de fermentation (1) et une étape de séparation (11) où un écoulement (10) de liqueur de fermentation provenant de la cuve de fermentation est divisé en un écoulement appauvri en levure (13), amené à une étape de récupération d'éthanol, et un écoulement enrichi en levure (12), retourné à la cuve de fermentation, puis par l'addition à la liqueur de fermentation dans ledit circuit d'un gaz contenant de l'oxygène pour permettre une croissance de la levure équilibrant les pertes en levure dans le circuit. La caractéristique du présent procédé est qu'un écoulement liquide (8, 12) déchargé de la cuve de fermentation (1) est atomisé dans un écoulement de gaz contenant de l'oxygène, après quoi la phase liquide est séparée de l'écoulement gazeux et retournée à la cuve de fermentation.
PCT/SE1984/000439 1983-12-27 1984-12-20 Procede de production d'ethanol WO1985002864A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8307166-2 1983-12-27
SE8307166A SE440793B (sv) 1983-12-27 1983-12-27 Forfarande for framstellning av etanol

Publications (1)

Publication Number Publication Date
WO1985002864A1 true WO1985002864A1 (fr) 1985-07-04

Family

ID=20353891

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SE1984/000439 WO1985002864A1 (fr) 1983-12-27 1984-12-20 Procede de production d'ethanol

Country Status (3)

Country Link
EP (1) EP0194263A1 (fr)
SE (1) SE440793B (fr)
WO (1) WO1985002864A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007038833A1 (fr) * 2005-10-03 2007-04-12 Agritechnology Pty Ltd Procede de fermentation d’ethanol et produits issus de ce procede
AU2006299737B2 (en) * 2005-10-03 2011-05-26 3g9 Group Pty Ltd of Queensland Ethanol fermentation process and products

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111187717A (zh) * 2019-07-17 2020-05-22 山东科技大学 糠醛渣强制循环高固气提发酵生产燃料乙醇装置

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2062003A (en) * 1979-09-21 1981-05-20 Uhde Gmbh Process for producing alcohol and yeast by continuous fermentation

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2062003A (en) * 1979-09-21 1981-05-20 Uhde Gmbh Process for producing alcohol and yeast by continuous fermentation

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007038833A1 (fr) * 2005-10-03 2007-04-12 Agritechnology Pty Ltd Procede de fermentation d’ethanol et produits issus de ce procede
AU2006299737B2 (en) * 2005-10-03 2011-05-26 3g9 Group Pty Ltd of Queensland Ethanol fermentation process and products
US8158396B2 (en) 2005-10-03 2012-04-17 Alternative Fuels Corporation Pty Ltd Ethanol fermentation process and products

Also Published As

Publication number Publication date
EP0194263A1 (fr) 1986-09-17
SE8307166L (sv) 1985-06-28
SE8307166D0 (sv) 1983-12-27
SE440793B (sv) 1985-08-19

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