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WO2011117625A1 - Culture continue de bactéries anaérobies produisant un solvant - Google Patents

Culture continue de bactéries anaérobies produisant un solvant Download PDF

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Publication number
WO2011117625A1
WO2011117625A1 PCT/GB2011/050569 GB2011050569W WO2011117625A1 WO 2011117625 A1 WO2011117625 A1 WO 2011117625A1 GB 2011050569 W GB2011050569 W GB 2011050569W WO 2011117625 A1 WO2011117625 A1 WO 2011117625A1
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WIPO (PCT)
Prior art keywords
tube
microorganisms
flow
reactor
solvent
Prior art date
Application number
PCT/GB2011/050569
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English (en)
Inventor
Jeremy Cooper
Christopher Jonathan Dowle
Stephen Donegan
Michael K Theodorou
Bernd Van Houten
Gustavo VALENTE PEREZ
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Cpi Innovation Services Limited
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Publication date
Application filed by Cpi Innovation Services Limited filed Critical Cpi Innovation Services Limited
Publication of WO2011117625A1 publication Critical patent/WO2011117625A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/20—Bacteria; Culture media therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/006—Baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/185—Stationary reactors having moving elements inside of the pulsating type
    • 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
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • C12M23/06—Tubular
    • 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
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • 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
    • C12P7/065—Ethanol, i.e. non-beverage with microorganisms other than yeasts
    • 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
    • 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
    • C12P7/24—Preparation of oxygen-containing organic compounds containing a carbonyl group
    • C12P7/26—Ketones
    • C12P7/28—Acetone-containing products
    • 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

  • Butanol (1-butanol), acetone, isopropanol (2-propanol) and ethanol are major products of several species of solvent- producing anaerobic Clostridia. These solvents are
  • butanol, isopropanol and ethanol can be used on their own or as additives in liquid transport fuels.
  • acetone is co-produced during the synthesis of phenol
  • butanol and isopropanol are synthesised commercially using petroleum (propylene) derivatives.
  • Ethanol is produced both synthetically, by the petrochemical and coal
  • Solvent fermentation was a major commercial operation for much of the early 20 th Century.
  • Different clostridial strains were isolated and maintained and the biomass feedstocks used for fermentations were initially based on potato and corn starch and latterly molasses.
  • petrochemical-based synthesis replaced industrial- scale bio-based fermentation by the mid-to latter part of the 20 th century.
  • the fact that these solvents were successfully produced from plant biomass serves to demonstrate that it is possible to change our petrochemical-based economy back to a bio-based economy, producing organic chemicals and liquid fuels from biomass-based feedstocks.
  • solvent fermentation is based on corn starch or molasses and undertaken in completely (or continuously) stirred tank reactor (CSTR) reactors (batch fermentors) with maximum volumes of just less than 500,000 gallons (2.3xl0 7 (Beesch, 1953) .
  • concentration of solvents produced is about 2.2% with an approximate 6:3 : 1 weight ratio of butanol : acetone : ethanol, representing a yield of 0.45 kg of solvent from 1.3 kg of corn starch (Beesch, 1953) .
  • Other substrates usually considered as wastes and presenting disposal problems/economic opportunities, have been used for solvent fermentation.
  • Solvent-producing bacteria can be characterised and split into four groups based upon their major fermentation end-products. These groups are (1) acetone but not butanol or isopropanol producers, (2) butanol and acetone producers, (3)
  • Solvent production is usually associated with a change in growing conditions and can be triggered by several
  • Solvent-producing Clostridia gradually lose their ability to produce solvent and/or sporulate when cells are kept in the vegetative state through serial transfer for prolonged periods of time. This degeneration is not entirely
  • Acetone, butanol and isopropanol are currently produced using synthetic processes, with petro-chemicals as the starting materials.
  • climate change and the need to develop sustainable production processes that are less or not at all dependent on petrochemicals has inspired renewed global interest in solvent fermentation and once again the process is operational and expanding in China.
  • fermentation research is increasing and topics for study include (a) the isolation and characterisation of more solvent-producing strains, (b) enzymology, genetics and regulation of solvent production, (c) metabolic engineering to manipulate pathways and produce better and more
  • This invention is concerned among other things with the culture and harvesting of anaerobic solvent-producing bacteria and their solventogenic fermentation end-products from a range of starch-, sugar- and fibre-containing substrates. What follows is a brief review of the prior art in this area. Continuous culture of microorganisms is considered superior to batch culture because continuous operation permits more effective use of the fermentation facility, allowing for better production economics, smaller vessel sizes, reduced industrial footprint and, generally, a more sustainable process. Since the early 1980' s, much effort has been devoted to understanding the parameters associated with solvent production and the development of continuous culture systems for solvent-producing bacteria. In
  • a two-stage continuous culture process involving a
  • metabolic fluctuations (metabolic oscillation) (Gapes et al . , 1996) making the process difficult to control and unsuitable for industrial-scale production.
  • the invention is directed to a process for the continuous production of solvent from solvent-producing Clostridia. It has been recognised that the original industrial
  • batch culture permits retention of non- dividing, solventogenic cells towards the end of their cell cycle and prior to the onset of sporulation. It is not possible to achieve this in a continuous culture because influent and effluent flows determine growth rate and ensure that cells are actively growing and thus maintained in a non-solventogenic state.
  • the invention is defined in claim 1 as a process, and in claim 8 as an apparatus.
  • One of the features in the continuous production process of the invention is to recognise that one needs to grow clostridial cells continuously, but in a series of
  • the process allows for the various stages of the typical growth and development cycle of the solvent-producing bacterium in batch culture and permits them to be segregated, not just in time in a batch culture but also in space by being located in particular regions of a tubular bio-reactor.
  • the underpinning and novel character of the invention is to enable the various cell cycle growth phases of the
  • microorganism including the non-dividing, solvent- producing phase associated with sporulation, to develop and co-exist within the tubular bioreactor in discrete plugs or batches as the culture moves continuously through the reactor.
  • Embodiments of the invention recognise and take advantage of the fact that OBR technology, when operated continuously and under plug-flow conditions, presents many control-point opportunities for optimising solvent production that are not available in a batch production process. These control points are concerned with regional temperature, pH and redox control and, through additions and removals, the precise control of media constituents. By taking advantage of these process control points, we are able to optimise the solventogenic process, making it more efficient and effective for solvent production in comparison to the conventional batch culture process.
  • a method for producing an anaerobic microbiological process, or a series of such processes in an oscillatory-flow reactor.
  • the reactor comprises a preferably generally horizontal tube with baffles along its length and sufficient in length to permit plug flow conditions to develop. Fluid material is introduced continuously, or continuously but in discrete batches, into the tube through a medium-influent port at the beginning of the tube, the fluid and feed comprising the following components: finely divided ( ⁇ 2 mm 2 )
  • microorganisms is supplied with each feed or fed
  • the clostridial cells are heat-treated (pasteurization) to kill vegetative cells and permit spore germination.
  • the cells can be recycled from the end of the reactor back to the beginning .
  • the major carbon source in the feed material can be, for instance, ground plant material such as potato waste or straw and/or soluble material such as starch or molasses. This can be fermented to give
  • microbial cells and fermentation end-products including volatile fatty acids, ethanol, acetone, butanol and
  • the fluid material and microorganisms pass through the column under plug flow at a speed that allows the anaerobic process (the clostridial growth cycle) to take place, usually a number of days, the fluid oscillating with respect to the baffles to ensure that particles and micro-organism are kept in suspension.
  • the grown microbial cells and solvent- containing, spent culture fluids are collected from an effluent collection port at the end of the column and a proportion of the collected residues (ca. 20-25%) is fed back through the inoculation port following pasteurisation.
  • the horizontal type of reactor can be held at a slight incline to permit bubbles of fermentation gas to pass out of the reactor via grooves cut in the top of the baffles and through a gas vent at the end of the tube (the end remote from the feed end) .
  • the apparatus allows the addition of material either at the inlet end, for instance at the beginning of the tube, or at any intermediate point in the tube. Microbial biomass and liquid and gaseous fermentation end-products can be removed at intermediate points in the tube or at the end of the tube (the end remote from the feed end) .
  • the apparatus also allows for effluent and micro-organism recycle and can include one or more separation devices in the recycle loop.
  • the motor that causes the oscillation of liquid in the tube is preferably connected to the tube by a downwardly
  • each loop of the reactor contains a microbial culture at a different phase of growth; given appropriate control of timing, temperature, feed and other conditions, the solventogenic phase dominates in the final loops of the reactor.
  • the piston that causes the oscillation of liquid in the tube is preferably close to the beginning of the reactor and housed in a gas-tight chamber. Oscillations are transmitted to the liquid regions of the reactor via the gas in each upper loop region. Oscillatory piston motion ceases, in order to coincide with each feed, thereby preventing ingress of fluid and feed to the piston housing.
  • Figure 1 shows an apparatus embodying the invention
  • Figure 2 shows a second embodiment
  • OBR oscillatory baffle reactor
  • Clostridium beijerinckii is a non-pathogenic saccharolytic, strictly anaerobic, mesophilic, motile, rod-shaped
  • bacterium with peritrichous flagella producing oval, sub- terminal spores The organism is mostly known for its production of the solvents acetone, butanol and ethanol (ABE) .
  • ABE ethanol
  • a number of products are produced including acetate, butyrate, hydrogen gas, carbon dioxide, acetone, butanol, ethanol, lactate, acetoin and acetyl methyl carbonyl .
  • the morphology of the cells changes over the growth cycle of the organism; at early exponential phase, the cells are long, filamentous and very motile. As the culture approaches the solventogenic stage, which corresponds with the stationary phase, cells shorten, become plumper and exhibit a lower level of motility.
  • Anaerobic technique focuses on removal and exclusion of oxygen during medium preparation and cultivation.
  • Media are generally boiled to reduce the oxygen concentration and subsequently cooled down whilst sparging with an anaerobic gas .e.g. oxygen-free nitrogen or carbon dioxide.
  • the medium is dispensed into cultivation vessels under an anaerobic gas phase.
  • reducing agents such as sodium sulphide, cysteine or ascorbic acid are commonly added.
  • Resazurin can be used as a redox indicator for a visual check of the redox state of the medium. Under pH neutral conditions this indicator changes from blue via pink to colourless when the medium is reduced to anaerobic conditions
  • Cultivation vessels are normally glass containers sealed with butyl rubber stoppers. These include serum bottles with crimp caps and Hungate tubes with screw caps. Larger fermentation equipment used for aerobic fermentations can be used, but special care must be given to tubing and seals. Only materials that have a low oxygen permeability should be used, these include butyl rubber, Tygon R-3603, Pharmed, Marprene . Silicon based tubing commonly supplied with fermentation equipment is not suitable. Fermentation vessels should be blanketed or sparged with an anaerobic gas. As the culture vessels and medium components are normally sealed, sterile syringes and hypodermic needles are used for transferring liquids and sampling across the seals .
  • SSM semi-synthetic medium
  • the medium contained a high glucose concentration (5 % w/v) .
  • the reactor was held at a temperature of 35 °C and the piston used to oscillate the inoculated culture medium back and forth through the baffles of the tubular reactor.
  • CSTR continuously stirred tank reactor
  • Table 1 Solvent production by Clostridium beijerinckii (strain NCIMB 8052) in an oscillatory baffle reactor (OBR) operated under anaerobic conditions.
  • FIG. 1 shows a horizontal tubular reactor 1 that can be used for the microbiological processes of the invention.
  • the reactor is an oscillating-flow or "OBR" (oscillatory baffle reactor) comprising a generally horizontal glass tube 3 of diameter 6 cm and of variable length depending on the process.
  • the reactor has an inlet end 5 and outlet end 7; the tube in fact rises slightly from inlet to outlet to prevent accumulation of gas.
  • Various connections are made, such that feed held in the feed reservoir 21 is pumped 37 and can enter at the feed inlet 2.
  • Microorganisms enter directly at inlet point 23 or via the pump recycle/separation route 27. There is a gas outlet 29 located at the outlet end 7.
  • baffles 11 Inside the tubular reactor 3 is a series of axially spaced baffles 11.
  • the baffles are in the form of rings or washers, constituted by stainless-steel plates with an outside diameter just fitting inside the tube, say 5.5 cm, having a central circular aperture of about half this, say 2.5-3 cm.
  • the baffles are regularly spaced along the tube over most of its length between inlet and outlet, at intervals comparable to their diameter, say every 5-7 cm. They are mounted on metal rods 13 extending the length of the tube and fixed in a suitable manner. They have small grooves or slits (not shown) at their uppermost point to allow small gas bubbles to pass through.
  • a further pump 41 is fitted.
  • This pump is designed to cause the liquid in the tube to oscillate backwards and forwards.
  • the outlet end must be at atmospheric pressure, even if sealed.
  • valves are in place to ensure that no backwash occurs in the feed circuits.
  • liquid in the vicinity of the baffles 11 is well mixed locally.
  • the tube is surrounded by one or more thermal jackets 31 to maintain a prescribed temperature in the tube, or in certain sections of the tube. Care is taken to exclude air from the reactor, by having non-return valves at all suitable points.
  • Various measuring devices 13a, b are connected to the reactor to record (for example)
  • nutrient is prepared 25 and supplied to the reactor from the feed reservoir 21 through the entry point 2 at a given, low, feed rate, continuously or
  • the reactor is inoculated with a culture of Clostridium acetobutylicum through the inlet port 23, and recycle loop 27, topped up as required.
  • the pump 41 is operated so that the liquid oscillates back and forth at a frequency of about 1 Hz and an amplitude of a small fraction of the baffle spacing, say about 1 cm. Again, this is compatible with plug flow since the mixing is only over a length of a few centimetres, a small fraction of the length of the tube, during the time it takes a volume of liquid to travel from one end of the tube to the other, which would typically be of the order of a few days .
  • the baffles can be moved backwards and forwards, relative to the tube, to generate the mixing.
  • the flow rate is chosen so that the bacterium completes its life cycle from heat- treatment to the onset of sporulation in the time it takes to travel through the tube.
  • the organisms are thus
  • microorganisms that exit can be "re-primed” by heating and then re-introduced.
  • FIG. 2 shows a second embodiment using a vertical loop reactor 1 with four loops that can be used for the microbiological processes of the invention.
  • the reactor is an oscillating-flow or "COB" (continually oscillating baffle) reactor comprising a glass tube 3 of diameter 6 mm and total length of 4000 mm.
  • the tube is of serpentine form in a vertical plane, consisting of vertical straight portions 34 connected by top U-portions 35 and bottom U- portions 33.
  • the reactor has an inlet end 5 and outlet end 7. Various connections are made, such as liquid and feed inlet 23, microorganism feed 21, effluent outlet 24. There is a gas release valve 29 associated with each upper loop 35 and linked to a gas levelling device 43.
  • baffles 11 Inside the tube 3 is a series of axially spaced baffles 11.
  • the baffles are again in the form of stainless-steel rings or aperture plates with an outside diameter just fitting inside the tube, say 5.5 cm, an a central circular aperture of about 2.5 - 3 cm.
  • the baffles are regularly spaced along the tube over all of its length between inlet and outlet, except for the gas-filled U-shaped regions at the top of the loops. Where baffles are present, they are located at intervals comparable to their diameter, about every 5 cm. They are mounted on metal rods extending the height of each vertical portion 34 and along each lower U- portion 33, and are fixed in a suitable manner.
  • a piston housing and pump 41 At the inlet end 5 a piston housing and pump 41 is fitted. The piston is located in a gas-filled or non-mixing liquid filled chamber and driven by the pump so as to cause the liquid in the first loop to oscillate backwards and
  • the inlet to the reactor also contains an inoculation port 36, associated with an effluent recycle loop, and a x ram-rod-like' feeding mechanism 37 which introduces liquid, feed and microorganisms to the reactor at discrete time intervals and in appropriate amounts to ensure
  • Each vertical section 34 of the tubular reactor is
  • a valve system 43 maintains the level of liquid in each loop, with a gas pocket in the upper U-portion.
  • nutrients and microorganisms are supplied through the inlets 21 and 23 at a given, low, feed rate, intermittently.
  • the rate is such as to lead to an
  • the reactor is inoculated with a culture of solventogenic Clostridium acetobutylicum through the inlet port 23, and is topped up as required through the recycle loop 36.
  • the associated with the feeding mechanism is operated to push each loop of liquid into the next section of the reactor.
  • the last loop exits and the solvents are extracted.
  • the time taken for a volume of liquid to travel from one end of the tube to the other can be made to vary according to inoculum and feeding conditions.
  • the flow rate is chosen so that the bacterium completes its life cycle from heat-treatment to the onset of sporulation in the time it takes to travel through the tube (4-9 days) .
  • the organisms are thus producing their maximum output of process chemicals just at the desired point.
  • the microorganisms that exit can be "re-primed” by heating and then re-introduced via the recycle loop 36 and feeding port 23.

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Abstract

L'invention concerne un procédé de culture continu de micro-organismes ayant un cycle de vie incluant un point de départ et un point de production qui est effectué dans un réacteur tubulaire à écoulement oscillant sur une base continue ou semi-continue. Les micro-organismes - de préférence des clostridies produisant un solvant - et l'alimentation sont introduits en 23 et 21 dans le réacteur tubulaire 1 à une extrémité dans un milieu liquide qui est amené à s'écouler à l'autre extrémité. Le tube est suff: samment long pour permettre essentiellement l'écoulement continu sur toute sa longueur, et le débit est déterminé de telle manière que les micro-organismes atteignent leur point de production sensiblement à l'extrémité de sortie du réacteur. Les solvants peuvent ensuite être extraits et les micro-organismes retournent à leur point de départ.
PCT/GB2011/050569 2010-03-22 2011-03-22 Culture continue de bactéries anaérobies produisant un solvant WO2011117625A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GBGB1004663.9A GB201004663D0 (en) 2010-03-22 2010-03-22 Continuous culture of anaerobic solvent-producing bacteria
GB1004663.9 2010-03-22

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WO2011117625A1 true WO2011117625A1 (fr) 2011-09-29

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014068013A3 (fr) * 2012-10-30 2014-08-07 Ashe Morris Ltd Réacteur à écoulement présentant un trajet d'écoulement prolongé
WO2014068011A3 (fr) * 2012-10-30 2014-08-07 Ashe Morris Ltd Réacteur à écoulement perfectionné
CN107603875A (zh) * 2017-10-30 2018-01-19 乐山晟嘉电气股份有限公司 一种智能生物菌培养机及培养方法

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GB191504845A (en) 1915-03-29 1919-03-06 Charles Weizmann Improvements in the Bacterial Fermentation of Carbohydrates and in Bacterial Cultures for the same.
GB424135A (en) 1933-08-15 1935-02-15 Henry Dreyfus Production of organic compounds by fermentation
GB480770A (en) 1936-05-23 1938-02-23 William Arthur Burton Improvements in or relating to fermentation processes
US4568643A (en) 1981-08-03 1986-02-04 Sidney Levy Continuous process for producing n-butanol employing anaerobic fermentation
GB2423525A (en) * 2005-02-26 2006-08-30 Gareth King Photobioreactor solvent extraction process unit
WO2008033573A2 (fr) * 2006-09-13 2008-03-20 Petroalgae, Llc Système de croissance microbienne tubulaire
WO2009074806A2 (fr) 2007-12-11 2009-06-18 Cpi Innovation Services Limited Processus anaérobie

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Publication number Priority date Publication date Assignee Title
GB191504845A (en) 1915-03-29 1919-03-06 Charles Weizmann Improvements in the Bacterial Fermentation of Carbohydrates and in Bacterial Cultures for the same.
GB424135A (en) 1933-08-15 1935-02-15 Henry Dreyfus Production of organic compounds by fermentation
GB480770A (en) 1936-05-23 1938-02-23 William Arthur Burton Improvements in or relating to fermentation processes
US4568643A (en) 1981-08-03 1986-02-04 Sidney Levy Continuous process for producing n-butanol employing anaerobic fermentation
GB2423525A (en) * 2005-02-26 2006-08-30 Gareth King Photobioreactor solvent extraction process unit
WO2008033573A2 (fr) * 2006-09-13 2008-03-20 Petroalgae, Llc Système de croissance microbienne tubulaire
WO2009074806A2 (fr) 2007-12-11 2009-06-18 Cpi Innovation Services Limited Processus anaérobie

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WO2014068013A3 (fr) * 2012-10-30 2014-08-07 Ashe Morris Ltd Réacteur à écoulement présentant un trajet d'écoulement prolongé
WO2014068011A3 (fr) * 2012-10-30 2014-08-07 Ashe Morris Ltd Réacteur à écoulement perfectionné
US10632449B2 (en) 2012-10-30 2020-04-28 Ashe Morris Ltd. Method of mixing using an improved flow reactor
CN107603875A (zh) * 2017-10-30 2018-01-19 乐山晟嘉电气股份有限公司 一种智能生物菌培养机及培养方法

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