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WO1998030710A1 - Reacteurs verticaux pour la bioconversion d'une matiere ligno-cellulosique - Google Patents

Reacteurs verticaux pour la bioconversion d'une matiere ligno-cellulosique Download PDF

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Publication number
WO1998030710A1
WO1998030710A1 PCT/US1998/000664 US9800664W WO9830710A1 WO 1998030710 A1 WO1998030710 A1 WO 1998030710A1 US 9800664 W US9800664 W US 9800664W WO 9830710 A1 WO9830710 A1 WO 9830710A1
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Prior art keywords
slurry
mixing
hydrolysis
section
mixer
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PCT/US1998/000664
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English (en)
Inventor
Quang A. Nguyen
Original Assignee
Nguyen Quang A
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
Priority claimed from US08/780,943 external-priority patent/US5733758A/en
Application filed by Nguyen Quang A filed Critical Nguyen Quang A
Priority to AU65331/98A priority Critical patent/AU6533198A/en
Publication of WO1998030710A1 publication Critical patent/WO1998030710A1/fr

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    • 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
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
    • 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
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/16—Solid state fermenters, e.g. for koji production
    • 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
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/18—Apparatus specially designed for the use of free, immobilized or carrier-bound enzymes
    • 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
    • C12M27/02—Stirrer or mobile mixing elements
    • 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
    • C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
    • C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
    • C12M41/22—Heat exchange systems, e.g. heat jackets or outer envelopes in contact with the bioreactor walls
    • 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
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/09—Means for pre-treatment of biological substances by enzymatic treatment
    • 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
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/06—Hydrolysis; Cell lysis; Extraction of intracellular or cell wall material
    • 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

  • This invention relates to the field of ethanol production from lignocellulosic material.
  • Lignocellulosic materials such as wood, herbaceous material, agricultural residues, corn fiber, waste paper, pulp and paper mill residues, etc. can be used to produce ethanol.
  • production of ethanol from lignocellulosic material requires four major steps. These four steps are pretreatment, hydrolysis, fermentation and recovery.
  • pretreatment is also known as pre-hydrolysis.
  • the lignocellulosic material is heated to break down the lignin and carbohydrate structure, solubilize most of the hemicellulose and make the cellulose fraction accessible to cellulase enzymes. This heating is done either directly with steam or in slurry.
  • a catalyst may be added to the material to speed up the reactions. Catalysts suitable for this include strong acids, such as sulfuric acid and SO 2 or alkalis, such as sodium hydroxide.
  • the second step is hydrolysis, more specifically enzymatic hydrolysis.
  • enzymes are added to the pretreated material to convert the cellulose fraction to glucose. This is also known as saccharification and is generally done in stirred-tank reactors or ferment or s under controlled pH, temperature and mixing conditions.
  • the third step is fermentation of the sugars to ethanol.
  • the sugars, released from the material as a result of the pretreatment and enzymatic hydrolysis, are fermented to ethanol by a fermenting organism, such as yeast, for example.
  • the fermentation can also be carried out simultaneously with the enzymatic hydrolysis in the same vessels, again under controlled pH, temperature and mixing conditions.
  • the process is generally termed simultaneous saccharification and fermentation or SSF.
  • the fourth step is the recovery of the ethanol from the fermentation broth by distillation.
  • the enzymatic hydrolysis and fermentation processing steps have the following common requirements, particularly when the cellulosic material is in the form of a slurry.
  • the slurry is maintained at a set temperature for a predetermined time
  • Adequate mixing is required to ensure effective and uniform heat and mass transfers
  • overly vigorous mixing can damage and denature the enzymes and fermenting organisms due to high shear See Shear lnactivation of Cellulase of Trichoderma ressei by Reese and Ryu. Enzyme Microb Technol . July, 1980, Vol 2, p 239-240 and Effects of Agitation on Enzymatic Hydrolysis of Cellulose in a Stirred-Tank Reactor by Mukataka, Tada and Takahashi, Ferment Technol.
  • the enzymatic hydrolysis and SSF fermentors are continuous stirred tank reactors (CSTR) arranged in series or cascade.
  • CSTR continuous stirred tank reactors
  • the total volume of the CSTR can be very large because the enzyme hydrolysis process typically takes 4 to 5 days to complete in batch mode.
  • the residence time for a continuous cascade CSTR system is generally longer than in a batch mode to achieve the same degree of conversion because of back mixing of substrate.
  • the volumetric productivity of the continuous cascade CSTR system is higher than that of a batch system because of the excessively long time required to fill and unload large batch fermentors.
  • Other major drawbacks of CSTR include high mixing power requirements to maintain the undissolved solids in suspension and avoid dead space. Vigorous mixing and long residence time would likely denature the enzymes, and thus lead to more fresh enzyme to be added to the system to effectively hydrolyze the cellulose. All of the above factors result in high capital and operating costs.
  • Plug-flow reactors have been recognized as having higher volumetric productivity than CSTR systems. For enzyme hydrolysis reactors, higher productivity translates into smaller reactor volume, shorter residence time and therefore less damage and denaturation of enzyme. It has been estimated that 20 fermentors in a cascade CSTR system would be required to approach the productivity of a plug flow reactor. See Biochemical Engineering Fundamentals by Bailey and Ollis, 1977, McGraw Hill, New York, p. 535-538. A variety of plug-flow reactors in the form of tower bioreactors have been proposed to improve ethanol productivity; however, these designs are suitable only for processing liquid substrates and not for slurries containing high concentration of undissolved solids such as lignocellulosic materials.
  • liquid-processing tower bioreactors examples include: US Patent 4,654,308 to Safi, Rouleau, and Mayer.
  • This reference suggests a bioreactor with horizontal trays stacked in a vertical tower.
  • the inventors suggest that the bioreactor may be used to ferment ethanol from wastewater from a pulp or paper plant, or to produce methane from cheese plant waste.
  • the reactor of this reference is designed to handle aqueous solutions of sugars containing little undissolved solids.
  • the slurries containing high insoluble solids for which the reactors of the present invention are designed will likely plug up the trays of this type of bioreactor.
  • Wieczorek and Michalski describe a tower fluidized-bed bioreactor in Continuous Ethanol
  • the apparatus of the present invention comprises a tower bioreactor (hereinafter also referred to as tower or bioreactor) which is suitable for continuous enzymatic hydrolysis or SSF of pretreated lignocellulosic material in a near plug flow mode.
  • a tower bioreactor hereinafter also referred to as tower or bioreactor
  • the movement of liquid relative to undissolved solids is mainly concurrent.
  • Side-entry mixers are strategically located on the side of the tower bioreactors to ensure uniform heat and mass transfer, to prevent channeling where liquid bypasses solids, and to minimize shear that may denature and damage the enzymes and fermenting microorganisms. A small amount of back mixing takes place at or near the mixers, but most of the slurry moves forward in a near plug flow mode.
  • the side-entry mixers are used to generate an intermittent mixing regime inside the tower bioreactors. Although the mixers operate continuously, intermittent mixing is achieved when the slurry passes through alternating mixing zones and non-mixing zones inside the towers. Intermittent mixing achieves essentially the same rate of hydrolysis as continuous mixing, but at reduced overall mixing power consumption. Temperature control of the reaction is achieved by circulating heating or cooling fluid through the heat transfer jacket. For a lower viscosity slurry where the slurry can be readily pumped through heat exchangers, temperature control and mixing can be achieved by way of external heat exchange loops.
  • Fig 1 shows a schematic diagram of a typical tower bioreactor equipped with side-entry mixers for enzyme hydrolysis or fermentation of pretreated lignocellulosic material at high solid loading, which is defined herein as a feed stream containing greater than about 10 wt% total suspended solids
  • Fig 2 shows a schematic diagram of a typical tower bioreactor equipped with mixing and heat transfer loops for enzyme hydrolysis or fermentation of pretreated lignocellulosic material at medium solid loading, which is defined as a feed stream containing about 5-10 wt% total suspended solids
  • Fig 3 shows a schematic diagram of a typical tower bioreactor equipped with mixing and heat transfer loops for enzyme hydrolysis or fermentation of pretreated lignocellulosic material at low solid loading, which is defined as a feed stream containing less than about 5 wt% total suspended solids
  • Fig 4 shows a schematic diagram of a typical four-stage bioreactor system for enzymatic hydrolysis or SSF of pretreated lignocellulosic material
  • the system consists of high-, medium-, and low-solid tower bioreactors connected in series Depending on the throughput and size of the bioreactors, each stage can have one, two or more bioreactors connected in parallel
  • Fig 5 is a graph illustrating the effect of mixing on enzymatic hydrolysis of alpha cellulose Detailed Description of Embodiments of the Invention
  • the tower bioreactor design is arbitrarily divided into three categories high-solids having greater than about 10 wt% undissolved solid concentration, medium-solids having between about 5 wt% and 10 wt% undissolved solid concentration and low-solids, having less than about 5 wt% undissolved solid concentration Exemplary designs for these configurations are shown in Figs.
  • Fig. 1 shows a typical high-solids tower bioreactor which is suitable for use at the beginning of the enzymatic hydrolysis or SSF process where approximately less than 50% of the cellulose is hydrolyzed to glucose upon leaving the bioreactor.
  • this high-solids bioreactor can be used in the first stage in a four-stage tower bioreactor system in series with a total residence time of four days (see Fig. 4).
  • Fig. 1 shows the slurry feed coming into the bottom of the bioreactor for upward directional flow.
  • the inlet can also be at the top of the bioreactor, in which case the slurry flow is in the downward direction, but for purposes of this description an upward flow will be described.
  • the description of the operation of the tower bioreactor using a downward directional flow will be obvious to the skilled artisan by reversing the sequence of the upward directional flow description.
  • the bioreactor may have more mixing zones as shown.
  • the volume of each bioreactor can be as large as 2 million liters.
  • the hydraulic retention time in each bioreactor can be up to 24 hours.
  • the height-to-diameter ratio can vary between about 3 and 10 but is preferably kept between about 4 and 5 to limit the height of large bioreactors. Too low a height- to-diameter ratio may cause ineffective mixing or back mixing. For example, for a 2 million-liter bioreactor, the height could be about 40 meters and the inside diameter could be approximately 8 meters. For a 1 million-liter bioreactor, the height could be about 30 meters and the diameter could be about 6.6 meters.
  • the slurry of pretreated lignocellulosic material is pumped through line 1 into mixer 3 where enzymes and nutrients are also added through line 2 and blended with the slurry.
  • the solids loading of the slurry entering the mixer vary between about 10 to 25 wt%, more preferably between about 15-20 wt%.
  • the mixer ensures enzyme and nutrients are uniformly distributed throughout the slurry.
  • the residence time in the mixer is typically less than about 10 minutes.
  • the mixer also serves as a pump that pushes the slurry into the bottom of tower bioreactor 4 and conveys the slurry through the tower.
  • the tower bioreactor is equipped with heat transfer jackets 5, 6, 10, 15 and 19, through which heat transfer fluid can be circulated to control the temperature inside the tower bioreactor
  • the heat transfer jackets are divided into zones such that the temperature in each zone can be controlled independently This feature provides an option to create a temperature gradient along the height of the bioreactor
  • most fungal cellulase enzymes hydrolyze cellulose most effectively between about 45° and 50°C, however most ethanol fermenting organisms such as brewer yeast are most effective between 30°C and 34°C
  • most SSF processes use temperatures in the 35-38°C range
  • the temperature gradient capabilities of the present invention allow for optimization of enzymatic hydrolysis and fermentation by allowing each of these processes to take place at or near their optimal temperatures
  • the inlet of the bioreactor is operated at about 40-50°C, or within the optimal temperature range for the cellulase enzymes used, to maximize the hydrolysis rate
  • the fermenting organism is not introduced at this high- temperature zone
  • the mixing intervals must be adjusted according to the viscosity of the slurry, the degree of mixing (or mixing powers), the types of mixers used and the heat transfer required Since the position of the mixers or mixing loops on tower bioreactors can not be readily changed during operation, the size of the mixing zone and the mixing intensity in the zones can be varied by changing the speed of the mixer or the impeller design Lower intensity mixing occurs between mixing zones due to movement of the slurry conveyed by the mixer 3 There are also transition areas immediately above and below each mixing zone where intermediate intensity mixing occurs.
  • each mixing zone may contain one or more agitators.
  • the objective is to achieve complete suspension and motion of the solid particles or blending of the slurry in the mixing zone.
  • the agitator blades can be of various configurations such as marine impellers, turbines, helicals or anchor impellers, for example. Helical and anchor impellers are referred because, generally, they require less power and generate less shear than other impeller design.
  • first and second hydrolysis sections 4 and 9 where the heat transfer jacket 5 maintains the temperature of the slurry at about 45 °C
  • the partly digested slurry enters mixing zone 14 where yeast or other fermenting organism is added through line 11.
  • mixing zone 14 There may be more than one mixing zone in the hydrolysis zones, as shown in Figure 1.
  • the temperature of the slurry is gradually lowered from about 15 45°C at the inlet of the tower bioreactor to about 37°C (or near the optimal temperature for the SSF process) in mixing zone 14.
  • Recycled enzyme and fermentation organisms from the last stage of the SSF system are also introduced into this zone through line 12.
  • Above second hydrolysis section 9 is the SSF section 16, where hydrolysis and fermentation take place simultaneously.
  • the interval between mixing zones in the SSF sections vary between 3 hours and 5 hours depending on the viscosity of the slurry. The higher the viscosity, the shorter the intervals between mixing zones. The viscosity decreases as the slurry passes through the sequential stages of the system. This is depicted in Figure 4, which shows a 4-stage system.
  • the partly hydrolyzed slurry is withdrawn at the top of the tower bioreactor through line 25 22 and pumped to the next bioreactor in series (i.e., in stage 2).
  • An auger can be installed at the tower outlet to facilitate the withdrawal of the slurry through line 22.
  • a level controller is used to establish a level 21 in the bioreactor. Carbon dioxide generated during fermentation, entrained air and other gases are collected in the tower overhead space 20. The gases are vented out of the bioreactor by way of ethanol condenser 23 and line 24.
  • Fig. 2 shows a typical tower bioreactor for a slurry having medium suspended solid concentration. These bioreactors are suitable for use in series after the high-solids bioreactors, i.e., in the intermediate stages of the enzymatic hydrolysis or SSF process As depicted in Fig 4, the intermediate stages, namely the second stage or tower 68 and third stage or tower 69, consist of one or more pairs of bioreactors connected in series Returning to Fig 2, partly digested slurry is pumped from the exit of the high-solids bioreactor into the inlet of the medium- solids bioreactor 26 through line 25 For a downflow tower bioreactor, the inlet would be at the top However, for consistency of description, an upward flow is described As the slurry moves up the tower bioreactor, temperature control is achieved by way of heat transfer jackets 27, 31, 35 and 39 Depending on the viscosity of the slurry, mixing can be done by mixing loops 30, 34 and 38 instead of agitators Medium-solids bioreactors
  • the partly hydrolyzed slurry is withdrawn at the top of the tower bioreactor through line 42 and pumped to the next bioreactor in series, either in the third stage or fourth stage
  • a level controller is used to establish a level 40 in the tower bioreactor.
  • Carbon dioxide generated during fermentation and entrained air and other gases are collected in the tower bioreactor overhead space 41
  • the gases are vented out of the bioreactor by way of ethanol condenser 43 and line 44 Low-solids tower bioreactors
  • Fig. 3 shows a schematic diagram of a bioreactor for slurry having low solids concentration
  • this bioreactor is equipped with a solid settler to facilitate the separation of cells of yeast or other fermenting microorganism from residual insoluble solids
  • This low-solids tower bioreactor is suitable for use in series after the medium-solids bioreactors, i.e , in the final stage of the enzymatic hydrolysis or SSF process
  • the low-solids bioreactors have similar design and operation as the medium-solids bioreactors, i.e., mixing loops are used, but the interval between mixing loops is increased to 6 to 10 hours
  • Slurry exiting from a medium-solids tower bioreactor is pumped into the low-solids reactor 46 through line 45
  • the low-solids tower bioreactors are equipped with heat transfer jackets 47, 51, 55 and 59, mixing loops 50, 54 and 58, mixing pumps 48, 52, and 56, and external heat exchangers 49, 53 and 57
  • these low-solids bioreactors are equipped with a solid settler 60 at the top of the settling zone 61 to separate the enzymes and cells of fermenting organisms from residual insoluble solids for recycling back to the high solids or first stage bioreactors
  • An example of solid settler 60 is inclined plates
  • the slurry is retained in settling zone 61 for up to about 6 hours to ensure sufficient time for the residual solids to separate from the microbial cells
  • the fermentation broth is withdrawn from the bioreactor by line 62 at the bottom of the solid settler
  • the broth is forwarded to the ethanol recovery system (not shown)
  • the recycled cells and enzyme stream is withdrawn at
  • Fig 5 is a graphical representation showing results of experiments conducted to demonstrate intermittent mixing compared with continuous mixing
  • 250 mL of 10 wt% cellulose slurry was placed in 500 mL Erlenmeyer flasks at the beginning of the hydrolysis
  • Cellulase enzymes were added to the flasks using a loading of 25 filter paper unit per gram of cellulose (FPU/g cellulose)
  • the flasks were prepared in duplicate, and were placed in orbital shakers set at 45°C and predetermined speeds Small samples were withdrawn from the flasks as needed for determination of glucose released by the enzymatic hydrolysis. Before a sample was withdrawn, the contents of the flask were mixed thoroughly to ensure uniformity.

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Abstract

L'invention concerne un appareil permettant l'hydrolyse enzymatique et la fermentation d'une matière ligno-cellulosique prétraitée, l'appareil étant en forme de bioréacteur vertical, doté de mélangeurs pour effectuer un mélange intermittent de la matière. Il est important d'effectuer un mélange précis de la matière pour satisfaire aux demandes effectives de transfert de chaleur et de matière, sans endommager ou dénaturer les enzymes ou les micro-organismes en fermentation. La matière prétraitée, généralement sous forme de coulis, est pompée dans le bioréacteur, vers le haut, ou vers le bas, et est périodiquement mélangée, à mesure qu'elle passe dans les zones de mélange où se situent les mélangeurs. Pour obtenir un coulis léger, on peut effectuer un mélange alterné au moyen d'une boucle de pompage servant également de dispositif de transfert de chaleur. Un transfert de chaleur supplémentaire s'effectue dans les enveloppes de transfert de chaleur du réacteur.
PCT/US1998/000664 1997-01-10 1998-01-09 Reacteurs verticaux pour la bioconversion d'une matiere ligno-cellulosique WO1998030710A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU65331/98A AU6533198A (en) 1997-01-10 1998-01-09 Tower reactors for bioconversion of lignocellulosic material

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US08/780,943 US5733758A (en) 1997-01-10 1997-01-10 Tower reactors for bioconversion of lignocellulosic material
US08/780,943 1997-01-10
US08/878,037 US5888806A (en) 1997-01-10 1997-06-18 Tower reactors for bioconversion of lignocellulosic material
US08/878,037 1997-06-18

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003012196A3 (fr) * 2001-08-02 2003-12-11 Bradley A Saville Procede de recuperation pour biocatalyseurs immobilises
WO2006056838A1 (fr) * 2004-11-29 2006-06-01 Elsam Engineering A/S Hydrolyse enzymatique de biomasses ayant une teneur en matieres seches elevee
WO2012051523A1 (fr) * 2010-10-15 2012-04-19 Andritz Technology And Asset Management Gmbh Réacteur à enzymes à haute teneur en solides ou mélangeur d'enzymes à haute teneur en solides et procédé associé
WO2012072883A1 (fr) * 2010-12-01 2012-06-07 Chempolis Oy Traitement par hydrolyse
FR2991691A1 (fr) * 2012-06-08 2013-12-13 Toulouse Inst Nat Polytech Procede de traitement enzymatique d'une matiere ligno-cellulosique solide
CN107513497A (zh) * 2017-10-10 2017-12-26 杭州同孚环保科技有限公司 一种多段式仿生反应器温控系统

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US4654308A (en) * 1985-06-19 1987-03-31 La Corporation De L'ecole Polytechnique Bioreactor
US5141861A (en) * 1983-11-03 1992-08-25 Bio Process Innovation, Inc. Method of use of a multi-stage reactor-separator with simultaneous product separation
US5348871A (en) * 1992-05-15 1994-09-20 Martin Marietta Energy Systems, Inc. Process for converting cellulosic materials into fuels and chemicals
US5424417A (en) * 1993-09-24 1995-06-13 Midwest Research Institute Prehydrolysis of lignocellulose

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5141861A (en) * 1983-11-03 1992-08-25 Bio Process Innovation, Inc. Method of use of a multi-stage reactor-separator with simultaneous product separation
US4654308A (en) * 1985-06-19 1987-03-31 La Corporation De L'ecole Polytechnique Bioreactor
US5348871A (en) * 1992-05-15 1994-09-20 Martin Marietta Energy Systems, Inc. Process for converting cellulosic materials into fuels and chemicals
US5424417A (en) * 1993-09-24 1995-06-13 Midwest Research Institute Prehydrolysis of lignocellulose

Cited By (16)

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WO2006056838A1 (fr) * 2004-11-29 2006-06-01 Elsam Engineering A/S Hydrolyse enzymatique de biomasses ayant une teneur en matieres seches elevee
US7598069B2 (en) 2004-11-29 2009-10-06 Inbicon A/S Enzymatic hydrolysis of biomasses having a high dry matter (DM) content
EP2154236A1 (fr) * 2004-11-29 2010-02-17 Inbicon A/S Hydrolyse enzymatique de biomasses ayant une teneur en matières sèches élevée
US7842490B2 (en) 2004-11-29 2010-11-30 Inbicon A/S Enzymatic hydrolysis of biomasses having a high dry matter (DM) content
EA014759B1 (ru) * 2004-11-29 2011-02-28 Инбикон А/С Ферментативный гидролиз биомасс, имеющих высокое содержание сухого вещества
WO2012051523A1 (fr) * 2010-10-15 2012-04-19 Andritz Technology And Asset Management Gmbh Réacteur à enzymes à haute teneur en solides ou mélangeur d'enzymes à haute teneur en solides et procédé associé
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JP2013539658A (ja) * 2010-10-15 2013-10-28 アンドリッツ・テクノロジー・アンド・アセット・マネージメント・ゲゼルシャフト・ミット・ベシュレンクテル・ハフツング 高濃度固体酵素反応器または混合器および方法
CN103201375B (zh) * 2010-10-15 2015-10-07 安德里兹技术资产管理有限公司 高固体酶反应器或混合器及方法
US9422518B2 (en) 2010-10-15 2016-08-23 Andritz Inc. High solids enzyme reactor or mixer and method
WO2012072883A1 (fr) * 2010-12-01 2012-06-07 Chempolis Oy Traitement par hydrolyse
FR2991691A1 (fr) * 2012-06-08 2013-12-13 Toulouse Inst Nat Polytech Procede de traitement enzymatique d'une matiere ligno-cellulosique solide
CN107513497A (zh) * 2017-10-10 2017-12-26 杭州同孚环保科技有限公司 一种多段式仿生反应器温控系统

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