WO1992001779A1 - Recipient de fermentation - Google Patents

Recipient de fermentation Download PDF

Info

Publication number
WO1992001779A1
WO1992001779A1 PCT/EP1991/001323 EP9101323W WO9201779A1 WO 1992001779 A1 WO1992001779 A1 WO 1992001779A1 EP 9101323 W EP9101323 W EP 9101323W WO 9201779 A1 WO9201779 A1 WO 9201779A1
Authority
WO
WIPO (PCT)
Prior art keywords
vessel
tank
fermentation
inlet
outlet
Prior art date
Application number
PCT/EP1991/001323
Other languages
English (en)
Inventor
Stanley John Pirt
Original Assignee
Pirtferm Limited
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 Pirtferm Limited filed Critical Pirtferm Limited
Publication of WO1992001779A1 publication Critical patent/WO1992001779A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/22—Activated sludge processes using circulation pipes
    • C02F3/223—Activated sludge processes using circulation pipes using "air-lift"
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/18—Flow directing inserts
    • C12M27/20—Baffles; Ribs; Ribbons; Auger vanes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/24—Recirculation of gas
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • This invention relates to fermentation vessels and to assemblies of such vessels.
  • fermentation vessels are designed to permit growth of microorganisms or other cells therein and to digest the substrate medium in which the cells are suspended.
  • continuous fermentation such vessels permit passage of medium containing the cells through the vessel, and continuous collection of the digested medium.
  • the vessel is elongated and the medium passes in plug flow or an approximation thereto, so that back mixing is minimised and at any point along the length of the vessel, the medium is essentially under batch fermentation conditions and undergoes the required fermentation in the time taken to traverse the length of the tank.
  • the present invention provides an apparatus and " method in which medium passing along an elongated fermentation vessel can be caused to move cyclically in a lateral direction to effect stirring while moving longitudinally in an approximation to plug flow.
  • a fermentation vessel comprising an elongated horizontal tank of narrow vertical cross-section having an inlet and an outlet longitudinally spaced therefrom, a substantially vertical panel being provided which divides the tank from the region of said inlet to the region of said outlet into two channels connected by gaps above and below said panel along its length and gas inlet means being situated at the bottom of the tank so that, in operation, influx of gas causes fermentation medium to flow transversely around the panel in the flow path defined by the two channels and the gaps above and below the panel while also moving longitudinally through the tank, means being provided to permit recycling of at least part of the effluent from the outlet back to the inlet.
  • the present system lends itself to scaling up while retaining suitable conditions for fermentation.
  • the tanks used in accordance with the invention will be about 3m in height and about 0.6m in breadth.
  • the tanks are advantageously U-shaped, so that their inlets and outlets are relatively close to each other and this facilitates such parallel assemblies.
  • a fermentation medium is introduced into the inlet of a fermentation vessel as claimed in claim 1 and passes to the outlet thereof while gas from the gas inlet means of said fermentation vessel causes the medium to move cyclically in the plane substantially perpendicular to the length of the fermentation vessel.
  • the tanks are provided with means for controlling their temperature, eg. heating and/or refrigeration means.
  • Figure 1 shows in perspective a straight fermentor module
  • Figure 2 shows an elevation of the outlet end of a module
  • Figure 3 shows an elevation of the inlet end of a module
  • Figure 4 shows a plan of the top of a straight module
  • Figure 5 shows a longitudinal elevation of a straight module
  • Figure 6 shows in perspective a U-shaped fermentor module
  • Figure 7 shows a plan of the top of a U-shaped fermentor module
  • Figure 8 shows in perspective and to scale U- shaped fermentor module; length from inlet to b 1, 10m; nominal volume 18m 3 ;
  • Figure 9 shows in perspective and to scale a multimodule fermentor consisting of five U-shaped modules assembled in two dimensions; length from inlet to bend, 10m; nomi al volume of each module, 18m 3 ;
  • Figure 10 shows in perspective and to scale a multimodule fermentor consisting of ten U-shaped modules assembled in three dimensions; length from inlet to bend, 10m; nominal volume of each module, 18m 3 ;
  • Figure 11 shows an exploded diagram in perspective of a U-shaped fermentor module
  • the straight fermentor module shown in Figure 1 consists of an elongated tank divided into two channels by the central panel 10 which has a gap both above and below it.
  • the gaps allow the liquid contents of the module to be cycled vertically around the central panel by means of an air or gas lift provided by means of gas sparger 11 situated on the upcomer side of the central panel.
  • the gas may be fed in at both ends of the sparger 11.
  • the top of the module is normally sealed by a lid
  • Temperature control is achieved by means of a heat exchange tube 20 connected to a heat exchanger 21.
  • the substrate stream 22 together with the recycled biomass 29 are fed into the module through the inlet 23. Plug flow of the culture occurs in the direction 33 as shown in Figures 1 and 4.
  • the culture exits through the outlet 24 at the base of the module.
  • the outlet 25 is an overflow weir connected to the effluent stream 26.
  • the effluent culture stream 26 passes into a separator 27 such as a hydrocyclone or sedimenter which concentrates the biomass and other solids into a sludge and separates the liquid which issues from the separator in the stream 28. Part of the biomass concentrate is recycled to the module in the stream 29 and excess sludge exits from the system in stream 30.
  • a separator 27 such as a hydrocyclone or sedimenter which concentrates the biomass and other solids into a sludge and separates the liquid which issues from the separator in the stream 28.
  • Part of the biomass concentrate is recycled to the module in the stream 29 and excess sludge exits from the system in stream 30.
  • the channels are bent round into the U-shape so that the outlet and inlet ends are juxtaposed and the length of the module is halved.
  • the outlet end and the feed end shown in Figures 2 and 3 respectively are identical to those used in the straight module.
  • the sparger 11 and the heat exchange tube 20 are continuous round the bend of the module.
  • the inner wall 34 which extends from the lid to the base has a gap at the bend in the module to permit the culture stream to turn.
  • the biomass recycle, gas sparger and heat exchange systems associated with the U- shaped module are similar to those shown for the straight module in Figure 1.
  • FIG. 8 The elongated form of the module and its relatively narrow cross section are illustrated in Figure 8 where, in outline, a U-shaped module is drawn to scale.
  • the height and width of the module are kept constant to conserve the essential geometry of the module.
  • the length of the module from end to end can be varied to alter the volume of the module as required.
  • the exploded diagram of a U-shaped module in Figure 11 shows the body section 32 separated from the ends of the module. Additional body sections may be inserted as required.
  • the module is fabricated of steel or other metal plate or plastic including glass fibre plastic or other suitable material. Struts 31 are inserted, as shown in Figures 6 and 7, or as required between the walls of the module to reinforce the structure and maintain its rigidity.
  • modules are connected in series with changes in the appropriate conditions, for example, of substrate and temperature from module to module in the series.
  • the first process is the aerobic activated sludge process for sewage purification.
  • the second process is the anaerobic fermentation of sugar to produce ethanol.
  • U-shaped fermentor modules of the type shown in Figures 6 and 8 may be used.
  • the module has a height of 3m and width of 0.6m so that the distance between the central panel and the wall is 0.15m.
  • the gap between the central panel and the base of the module is 0.15m.
  • the length from the feed end of the module to the bend is 10m.
  • the total volume of the module is about 18m 3 and the working culture volume is 15m 3 .
  • the module In the single stage activated sludge process the module is filled with sewage with a B.O.D. (biochemical oxygen demand) of about 250 mg l "1 .
  • the temperature of the sewage is set at 30°C.
  • the contents of the module are inoculated with activated sludge then aerated by means of the sparger.
  • the gas flow rate through the sparger is fixed between about 1.5 to 3.0m 3 min "1 to generate a liquid velocity in the downcomer and upcomer streams between about 1.5 to 3.0 cms "1 .
  • the vertical cycling keeps in suspension particles of matter present in the medium and forms a fluidised bed of the particles.
  • the aeration gas is either air or part recycled gas with air.
  • the dissolved oxygen concentration as measured by an oxygen electrode placed near the base of the downcomer channel is maintained at about 2mg l "1 by control of the rate of air flow through the inlet 19.
  • sewage together with recycled biomass sludge is continuously fed into the module through the inlet 23.
  • the temperature of this feed is adjusted to about 30°C before it enters into the module.
  • the feed rate of the sewage stream 22 is 72m 3 d '1 .
  • a hydrocyclone or other type of separator concentrates the biomass solids in the biomass recycle stream 29 to 50 kg dry matter m "3 and the flow rate of this stream 29 is adjusted to be 2.23m 3 d "1 .
  • Modules in series are added if additional stages of purification such as anaerobic digestion, nitrification, denitrification and phosphate removal are required.
  • the 18m 3 module after cleaning and disinfecting is charged with disinfected culture medium, 13.5m 3 .
  • the culture contains: glucose, 185g l "1 together with sources of B vitamins, nitrogen, such as ammonia or urea, phosphate, sulphate, magnesium, iron and trace elements as required to produce a yeast concentration of 20.9g dry weight l "1 .
  • the pH value of the medium is adjusted to pH 4.5. Before use the medium is pasteurized if necessary.
  • the temperature of the medium is adjusted to 30-35°C.
  • the inoculum of Saccharomyces uvaru is grown in the complete medium described above with 185g glucose l "1 .
  • the module is inoculated with 1.5m "3 of the inoculum culture which has just about reached its maximum gas production rate. Gas generation in the module is allowed to reach its peak then the effluent gas is recycled to the sparger at a rate of about 1.0m 3 min "1 . Complete culture medium is fed into the module through stream 22 at a flow rate of 1.0m 3 h "1 . A bleed of air at about 1.0m 3 min "1 into the sparger through the inlet 19 is required to avoid a sterol deficiency in the yeast.
  • biomass is concentrated to 150g dry weight l “1 in the biomass recycle stream 29, which is fed back to the module at a flow rate of 0.5m 3 h "1 .
  • the liquid effluent from the culture contains about 80g ethanol I “1 and the productivity of the culture is 5.4 kg ethanol m “3 h “1 .

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  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Zoology (AREA)
  • Health & Medical Sciences (AREA)
  • Microbiology (AREA)
  • Genetics & Genomics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Biochemistry (AREA)
  • Sustainable Development (AREA)
  • Biotechnology (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)

Abstract

Cette invention décrit des récipients de fermentation, dont on peut augmenter la capacité, comprenant un réservoir horizontal allongé à section transversale verticale étroite qui comporte une entrée (23) et une sortie (24) longitudinalement espacée de celle-ci; un panneau pratiquement vertical (10) divise le réservoir, depuis la region de ladite entrée jusqu'à la région de ladite sortie en deux canaux reliés par des ouvertures situées au-dessus et au-dessous dudit panneau dans le sens de la longueur, et des moyens d'admission de gaz (11) se situent au fond du réservoir afin que, pendant le fonctionnement l'afflux de gaz provoque l'écoulement transversal du milieu de fermentation autour du panneau, sur le trajet d'écoulement défini par les deux canaux et par les ouvertures situées au-dessus et au-dessous du panneau, ainsi qu'également son déplacement longitudinal dans le réservoir; des moyens (29) permettent le recyclage d'au moins une partie de l'effluent depuis la sortie vers l'entrée; l'invention décrit des procédés de fermentation dans lesquels l'agitation s'effectue par déplacement cyclique du milieu contenu.
PCT/EP1991/001323 1990-07-16 1991-07-12 Recipient de fermentation WO1992001779A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB909015578A GB9015578D0 (en) 1990-07-16 1990-07-16 Fermentorbioreactor module
GB9015578.9 1990-07-16

Publications (1)

Publication Number Publication Date
WO1992001779A1 true WO1992001779A1 (fr) 1992-02-06

Family

ID=10679153

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1991/001323 WO1992001779A1 (fr) 1990-07-16 1991-07-12 Recipient de fermentation

Country Status (2)

Country Link
GB (1) GB9015578D0 (fr)
WO (1) WO1992001779A1 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993022418A1 (fr) * 1992-04-28 1993-11-11 Pirtferm Limited Systeme de bioreacteur
FR2722206A1 (fr) * 1994-07-06 1996-01-12 Buehler Ag Fermenteur horizontal pour la fermentation de dechets biologiques
US5540839A (en) * 1991-08-30 1996-07-30 Pirtferm Limited Process for degrading organic matter
WO2001085902A1 (fr) * 2000-05-11 2001-11-15 GESELLSCHAFT FüR BIOTECHNOLOGISCHE FORSCHUNG MBH (GBF) Procede pour separer des cellules viables de suspensions cellulaires
WO2002100999A2 (fr) * 2001-06-08 2002-12-19 HöFer Bioreact GmbH Bioreacteur comportant au moins deux chambres de reaction
WO2003012196A3 (fr) * 2001-08-02 2003-12-11 Bradley A Saville Procede de recuperation pour biocatalyseurs immobilises
US7172691B2 (en) 2002-10-24 2007-02-06 Dunlop Eric H Method and system for removal of contaminants from aqueous solution
WO2017023638A1 (fr) * 2015-07-31 2017-02-09 Stadler Ernest L Fermenteur portatif horizontal multi-agité modulaire à usage unique pouvant être mis sous pression pour la culture de microorganismes

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2071591A (en) * 1935-12-02 1937-02-23 Albert L Tholin Sewage treatment
DE1064458B (de) * 1955-05-02 1959-09-03 Eugen Georg Stich Verfahren und Vorrichtung zur Belueftung von hefehaltigen Maischen
US3057785A (en) * 1959-10-15 1962-10-09 Distillers Co Yeast Ltd Fermentation vessel and process
EP0007168A1 (fr) * 1978-06-02 1980-01-23 Graham-Snider Energy Systems Procédé d'extraction de méthane et d'ammoniaque de résidus organiques
EP0112095A1 (fr) * 1982-12-07 1984-06-27 Simon-Hartley Limited Procédé et dispositif pour le traitement de liquides aqueux

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2071591A (en) * 1935-12-02 1937-02-23 Albert L Tholin Sewage treatment
DE1064458B (de) * 1955-05-02 1959-09-03 Eugen Georg Stich Verfahren und Vorrichtung zur Belueftung von hefehaltigen Maischen
US3057785A (en) * 1959-10-15 1962-10-09 Distillers Co Yeast Ltd Fermentation vessel and process
EP0007168A1 (fr) * 1978-06-02 1980-01-23 Graham-Snider Energy Systems Procédé d'extraction de méthane et d'ammoniaque de résidus organiques
EP0112095A1 (fr) * 1982-12-07 1984-06-27 Simon-Hartley Limited Procédé et dispositif pour le traitement de liquides aqueux

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5540839A (en) * 1991-08-30 1996-07-30 Pirtferm Limited Process for degrading organic matter
WO1993022418A1 (fr) * 1992-04-28 1993-11-11 Pirtferm Limited Systeme de bioreacteur
FR2722206A1 (fr) * 1994-07-06 1996-01-12 Buehler Ag Fermenteur horizontal pour la fermentation de dechets biologiques
BE1010988A3 (fr) * 1994-07-06 1999-03-02 Buehler Ag Fermenteur.
US6878545B2 (en) 2000-05-11 2005-04-12 Gesellschaft Fuer Biotechnologische Forschung Mbh (Gbf) Method for separating viable cells from cell suspensions
WO2001085902A1 (fr) * 2000-05-11 2001-11-15 GESELLSCHAFT FüR BIOTECHNOLOGISCHE FORSCHUNG MBH (GBF) Procede pour separer des cellules viables de suspensions cellulaires
WO2002100999A2 (fr) * 2001-06-08 2002-12-19 HöFer Bioreact GmbH Bioreacteur comportant au moins deux chambres de reaction
WO2002100999A3 (fr) * 2001-06-08 2003-12-18 Udo Hoelker Bioreacteur comportant au moins deux chambres de reaction
WO2003012196A3 (fr) * 2001-08-02 2003-12-11 Bradley A Saville Procede de recuperation pour biocatalyseurs immobilises
US7144716B2 (en) 2001-08-02 2006-12-05 Saville Bradley A Recovery method for immobilized biocatalysts
US7659099B2 (en) 2001-08-02 2010-02-09 Saville Bradley A Recovery method for immobilized biocatalysts
US7172691B2 (en) 2002-10-24 2007-02-06 Dunlop Eric H Method and system for removal of contaminants from aqueous solution
WO2017023638A1 (fr) * 2015-07-31 2017-02-09 Stadler Ernest L Fermenteur portatif horizontal multi-agité modulaire à usage unique pouvant être mis sous pression pour la culture de microorganismes

Also Published As

Publication number Publication date
GB9015578D0 (en) 1990-09-05

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