WO2007129327A1 - Photobioréacteur destiné à cultiver et à recueillir une biomasse et son procédé - Google Patents

Photobioréacteur destiné à cultiver et à recueillir une biomasse et son procédé Download PDF

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WO2007129327A1
WO2007129327A1 PCT/IN2006/000407 IN2006000407W WO2007129327A1 WO 2007129327 A1 WO2007129327 A1 WO 2007129327A1 IN 2006000407 W IN2006000407 W IN 2006000407W WO 2007129327 A1 WO2007129327 A1 WO 2007129327A1
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culture medium
light
reactor
bio
coil
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PCT/IN2006/000407
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Abhishek Narain Singh
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Abhishek Narain Singh
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    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K35/00—Medicinal preparations containing materials or reaction products thereof with undetermined constitution
    • A61K35/66—Microorganisms or materials therefrom
    • A61K35/74—Bacteria
    • A61K35/748—Cyanobacteria, i.e. blue-green bacteria or blue-green algae, e.g. spirulina
    • 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
    • C12M21/02—Photobioreactors
    • 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
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/20—Degassing; Venting; Bubble traps
    • 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
    • C12M31/00—Means for providing, directing, scattering or concentrating light
    • C12M31/02—Means for providing, directing, scattering or concentrating light located outside the reactor
    • 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
    • C12M33/00—Means for introduction, transport, positioning, extraction, harvesting, peeling or sampling of biological material in or from the apparatus
    • 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

Definitions

  • This invention relates to a PhotoBioreactor for cultivation of Botryococcus braunii and a method for efficiently growing the microalgae. More particularly, the invention relates to a PhotoBioreactor and method for cutivation of biomass for producing hydrocarbon. The bioreactor and the method can be adapted to production of other microalgae including spirulina.
  • Botryococcus braunii is a highly rich renewable source of hydrocarbons.
  • the high cost of known microalgal culture systems relates to the need for light and the relatively slow growth rate of the algae.
  • the photobioreactors must be designed keeping in mind that light is needed continuously for microalgal cultures. Since the intensity of light decreases rapidly with the depth of the culture, the geometry of the reactor is equally important. Important concern is to reduce the costs of these systems further to make them economically competitive.
  • Bioreactor System design depends on organism property, media property and system kinetics.
  • the property of the organism is important because we need the organism to grow in the desired fashion so that the acclaimed metabolic route is followed to yield us the preponderance of desired product.
  • Factors such as Oxygen / Carbon Dioxide dependency play crucial role, hence the importance of the size of the bubble and the time it spends in the liquid column.
  • Cell damage is dependent on the strain used, the bubble size based on the nozzle because smaller nozzle, which produce smaller bubbles, are more detrimental.
  • a drawback of this system is that in horizontal cultivator systems, light penetrates the suspension only to 5 cm, leaving most of the algae in darkness. The top layer of algae requires only about 1/1 Oth the intensity of full sunlight to maximize growth, so the remaining sunlight is wasted.
  • James C. Ogbonna and Hideo Tanaka have developed a prototype photobioreactor consisting of four units built with 0.5-cm-thick transparent Pyrex glass for the- cultivation of C. pyrenoidosa. Each unit was equipped with a centrally fixed glass tube into which the light source was inserted. Transparent glass tubes were used as housings for the lamps, so the reactor was illuminated by simply inserting the lamps into the glass tubes (no mechanical fixing). Any light source could be used.
  • Either 4- W fluorescent or halogen lamps with controllable , light intensity were used as the illuminating system. Because the lamps are not mechanically fixed and can easily be replaced, the same reactor can be used for efficient cultivation of various cells by using a light source with controllable light intensity or by simply replacing the light source with one that gives the desired light intensity. For mixing, an impeller modified in shape is used so that it did not touch the glass housing unit during rotation.
  • United States Patent 5,614,378 discloses a photo bio reactor comprising a hollow, cylindrical irradiation chamber, wherein said chamber comprises a top sealed to a cylindrical side wall; a bottom sealed to said cylindrical side wall; said top, bottom and cylindrical side wall together enclosing a cylindrical space; a first cylindrical light irradiator disposed in said cylindrical space and attached only to said top; and a second cylindrical light irradiator disposed in said cylindrical space and attached only to said bottom; wherein all cylindrical light irradiators and said cylindrical side, wall are coaxial; the distance between said cylindrical side wall and cylindrical light irradiator closest to said side wall is within 1 mm to 20 cm, and v the distance between each adjacent cylindrical light irradiator is within 1 mm to 20 cm, for a time sufficient to produce said biologically-active compound, while irradiating said cells with said first light cylindrical irradiator and said second light cylindrical irradiator.
  • This photo bioreactor may also be used in a method to fix carbon dioxide, to produce, e.g., fuels and/or chemical feed stocks.
  • the cultured cells are suitably, e.g., Botryococcus braunii.
  • United States Patent 4,952,511 (Radmer , August 28, 1990) teaches a photo bio reactor which comprising a tank for containing a liquid microbial culture; a high- intensity light source whose light is substantially entirely directed into a light compartment; said light compartment having at least one transparent wall extending into said tank; and said light compartment containing a tube of internally reflective prismatic sheet, said tube extending substantially from said light source to an end wall of said light compartment opposite said light source and said tube having transverse dimensions sufficient to substantially surround said light source, said tube further including a mirror at the end thereof opposite said light source oriented to reflect light back into said tube, wherein the light source, the tube and the mirror are arranged, so as to distribute light from said high-intensity light source substantially uniformly across the interior surface of the transparent wall of said light compartment.
  • United States Patent 5,137,828 (Robinson. , et al. August 11, 1992) teaches an apparatus comprising an upstanding substantially cylindrical support structure; a substantially transparent tube supported by the support structure and wound helically on the outside thereof so that, in use, the exterior of the wound tube is exposed to natural light, said tube containing at least living plant matter; a header tank at the top of the support structure, the upper end of the transparent tube being connected to the header tank; a pipe extending from the header tank to the bottom of the support structure, said pipe being connected to the lower end of the transparent tube; means for causing a synthesis mixture to flow under turbulent conditions through the tube, the header tank and the pipe; and means for withdrawing a biomass synthesis product from at least one of the header tank and the wound tube.
  • United States Patent 4,724,214 discloses an apparatus for photosynthesis comprising bath means containing a photosynthetic reaction bath, a plurality of tubular photoradiators arranged upright in said bath means in parallel array, upper support means and lower, support means in said bath means for supporting the upper and lower end portions respectively of said tubular photoradiators, said tubular photoradiators being spaced from one another so as to define a plurality of upright passages between said tubular photoradiators, said upper support means closing off the upper ends of said upright passages, said bath means having a lower chamber underlying said lower support means, said lower support means having a flow-through portion which provides communication between said chamber and a first plurality of upright passages and a stopped up portion which blocks communication between said chamber and a second .
  • United States Patent 4,676,956 (Mori June 30, 1987) teaches an apparatus for photo synthesis comprising a reaction bath means for causing a photosynthetic reaction therein, said reaction bath means comprising an inner transparent wall and an outer transparent wall surrounding and spaced from said inner transparent wall to define an annular space between the inner and the outer transparent walls, the inner and outer transparent walls being generally vertically disposed, and a light source positioned radially inwardly of the inner wall; a plurality of narrow tubular photoradiators arranged upright in said annular space parallel to each other, each of said photoradiators being constructed to radiate light which propagates therethrough; and a disc rotatable in a horizontal plane below the reaction bath means and disposed perpendicular to the photoradiators to eject jets of carbon dioxide-containing air into the annular space.
  • Japanese Patent JP7023767 provides a culture tank opened at one end provided with a fixing plate having plural holes to close the open end of the culture tank.
  • Plural protection tubes made of a transparent material and each having an insertion opening at one end and closed at the other end are fixed to the fixing plate parallel to each other by bonding the circumference of each hole to the outer circumference of the insertion opening.
  • the fixed tubes are put into the culture tank.
  • a rod light-source is removably inserted into each protection tube and a lid is applied to the fixing plate at the side opposite to the side holding the protection tubes.
  • the circumference of the opening of the culture tank 10 is detachably fixed to the circumference of the fixing plate in liquid-tight state with an engaging means to provide this photo- bioreactor.
  • Japanese Patent JP9009953 teaches a method to obtain a new Botryococcus braunii B race strain producing hydrocarbons mainly consisting of 30-33 C hydrocarbons and containing above a specific weight ratio of a 30C hydrocarbon to the total of hydrocarbons.
  • Planktons on the surface of Ippeki lake (Shizuoka prefecture) are collected by using a Kitahara type plankton net with 25 ⁇ m mesh. The prepared specimen is observed by a microscope and a colony of an alge of the genus Botryococcus is collected.
  • the colony is cultured in a test tube, a single colony of the alga of the genus Botryococcus is raked by a platinum wire while observing characteristic properties of the alga of the genus Botryococcus in a colony state, etc., by using a stereoscopic microscope and cultured in a float plate medium to give a new Botryococcus braunii B race strain which produces hydrocarbons consisting mainly of 3OC to 33C hydrocarbons and containing > 5wt.% 3OC hydrocarbon based on the total of hydrocarbons and is Botryococcus braunii SI-I strain.
  • Japanese Patent JP9234055 recites a method for efficiently culturing the strain of fine algae belonging to the genus Botryococcus braunii A race capable of producing a 33C hydrocarbon.
  • a hydrocarbon produced by the alga of this strain contains a 33C hydrocarbon.
  • a race is cultured under intermittently irradiating the strain with an artificial light preferably once daily for 5- 15 hours.
  • Japanese Patent JP9173050 teaches a method for efficiently culturing a microalgae belonging to green algae, which has ability to fix CO 2 by light energy and converts it into useful substances such as fuel comprises culturing microalgae (e.g.
  • Botryococcus braunii CCAP807/1, etc. belonging to such as Botryococcus, Chlorella, or Haematococcus, which belongs to green algae, while adding intermittently a disinfectant such as hypochlorous acid, hypochlorite, hydrogen peroxide and ozone to the culture medium intermittently each in a quantity of 0.01-200ppm so as to attain an effective quantity of the disinfectant in an open system under conditions of light illuminance and aeration of 0.05-5wm air containing CO 2 in concentration of 0.03- 30% at culturing temperature of 10-4 0 C for about 10 days.
  • a disinfectant such as hypochlorous acid, hypochlorite, hydrogen peroxide and ozone
  • a common CSTR type reactor which is externally illuminated by light source. This has a poor surface to volume value and since the illumination is from outside, a major part of light energy is wasted and inefficiently utilized.
  • a common lab scale reactor provides high light supply capacity and can be illuminated by both artificial and solar light. However, this has a poor surface to volume value and so a large number of light tubes would be required and thus would be energy consuming, a factor very detrimental for scale up.
  • a Flat Plate reactor derives the laminar concept from plants. If light energy has to be available continuously to the cells, a lamination of photobioreactor directed to the light source seems to be the best solution. Apart from the high surface/volume value offered in case of tubular reactors, plate-type reactors have some advantages with respect to compactness.
  • Recirculation of culture suspension can be obtained by airlift technology or by means of pump. Floating or submerging the tubes on or in a pool of water controlled temperature, oxygen degassing being guaranteed by flexible tube elements.
  • Biocoil is an arrangement of coiled polyethylene tubes of about 30-60 mm diameters around an open circular framework.
  • Helical tubular photobioreactor is advantageous because it allows a larger ratio of surface area to culture volume to receive illumination effectively, thereby reducing the self-shading phenomenon.
  • This reactor has a drawback that upscaling involves large area for a given biomass production.
  • the principle object of the present invention is to propose a photo bioreactor for efficiently growing the microalgae Botryococcus braunii with an enhanced growth rate than obtained by bioreactors known in the art.
  • Another object of the present invention is to propose a method efficiently growing the microalgae Botryococcus braunii with an enhanced growth rate than obtained by the methods known in the art.
  • Yet another object of the present invention is to propose a bioreactor and method which is simple and economical to implement.
  • a photo bio-reactor for cultivating and harvesting a bio-mass suitable for producing hydrocarbon comprising: (i) a helical tubular system having at least two substantially coaxial helical transparent autoclavable tubular coils for flow of a culture medium containing micro algae to be cultivated, said coils being at least a first coil and at least a last coil, each coil being hydraulically connected to its adjacent coaxial coil, said coils having annular spaces interposed between the adjacent coils and a space enclosed by the inner diameter of innermost coil, the first and the last coil each having a free end; (ii) a means of providing periods of light and darkness on each point alternately for predetermined time periods on the inner and outer surfaces of each of said coil; (iv) a de-gasser chamber having hydraulic connection with said free end of first coil for removing unwanted gases from said culture medium; (v) optionally, a stirrer provided in said de-gasser chamber for keeping the bio-mass in suspension in said culture medium
  • a method of cultivating and harvesting a bio-mass in a photo bio-reactor comprising the steps of: (a) circulating a culture medium containing a micro algae in said reactor at a predetermined flow rate; (b) providing alternately period of light and darkness for predetermined time periods on each point along the flow path of said circulating culture medium; (c) removing unwanted gases from said circulating culture medium; (d) controlling temperature of said culture medium between 25° and 36° C; (e) optionally, stirring said circulating culture medium to keep said micro algae id suspension; (f) injecting CO 2 and air into said circulating culture medium to ensure a predetermined gas flow rate; (g) providing continuous darkness for a predetermined time period on each point along the flow path of said circulating a culture medium; and (h) harvesting cultivated micro algae from said circulating culture medium.
  • Figure 1 shows the photobioreactor.
  • Figure 2. shows the cage around which the helical coil is wound.
  • Figure 3. shows the growth profile of B. braunii at 31 0 C
  • Figure 4. shows the hydrocarbon content profile of of B. braunii at 31 0 C
  • Figure 5. shows the growth profile of B. braunii at 27 0 C
  • Figure 6. shows the hydrocarbon content profile of of B. braunii at 27 0 C
  • photoautotrophic microbes to make use of solar energy for metabolism is dependent upon the effective surface area of the rays to which it is subjected, which reduces with increase in population.
  • the supply of photons is based on the surface area. Light gradient would always tend to occur due .to mutual shading of the cells and light absorption.
  • the light intensity in a photobioreactor decreases exponentially with the depth. Since the intensity of light decreases rapidly with the depth of the culture, the geometry of the reactor is equally important.
  • Helical tubular bioreactor facilitates temperature control and restricts contaminants because it is a closed bioreactor.
  • a modification may include introducing alternating dark and transparent section in the inner column to take into account of organism specific flashing light effect Its disadvantages include requirement of a large land area for a given volume.
  • Another aspect is that the system is suitable only for disperse culture suspension as pump action disperses cell clumps.
  • chlorophyll a in the range of 400-450 nm (between Violet and Blue) and around 680nm(Red), ⁇ -carotene 400-500 nm (Violet to Green), chlorophyll b (400-500nm). Further we also need to remember that energy delivered is inversely proportional to the wavelength, but the penetration is directly proportional to the wavelength.
  • Chlorophill a, Chlorophill b and ⁇ -carotene are light harvesting pigments which have their absorption wavelength maxima in the range 400nm-500nm and 620-680nm.
  • Type of Light source Some of the efficient light sources from the electric consumption and wavelength requirement point of view are Light Emitted diodes (LEDs), Fluorescent lights, and incandescent/halogen lamps. Fluorescent lamps are used most frequently for the cultivation of phototrophic organisms. The emission wavelength emitted from the mercury vapor can be converted to continuous radiation by modifying the composition of the fluorescent material, which allows for an optimum spectrum of photosynthesis. LEDs are one of the most efficient one in converting electricity to light with desired wavelength. However, if broader wavelength is required then combination of LEDs has to be used. We also need to keep into account the increase in wavelength due to absorption of rays as Heat energy.
  • LEDs Light Emitted diodes
  • Fluorescent lights are used most frequently for the cultivation of phototrophic organisms.
  • the emission wavelength emitted from the mercury vapor can be converted to continuous radiation by modifying the composition of the fluorescent material, which allows for an optimum spectrum of photosynthesis.
  • LEDs are one of the most efficient one in converting electricity to light with desired wavelength.
  • Ic compensation intensity
  • Is saturation intensity
  • the helical system bioreactors prove to be better than the stirred system.
  • This can be attributed to large dark volume characterized by cylindrical reactors. This dark volume can be taken care by inserting transparent pipes into the cylinder from the top through holes in the lid, holding fluorescent tubes, such that it can easily be removed during sterilization.
  • T-shaped multifunctional stirrer is used to agitate the suspension and to supply sterile air.
  • the denser is the culture of micro algae, the more problematic is the light penetration, and extremely limited. This restricts the commercial production to just flat plate photobioreactor and narrow bore tubular reactor. In spite of the efficient performance of thin channel flat plate types of photobioreactors, there is difficulty in scaling it up for production of significant quantities of product. This further limits our choice to tubular photobioreactor.
  • the major disadvantage of tubular reactors is that for the same amount of volume, the area required is much more in comparison to other reactors. Other possibilities comprise of bubble column and airlift reactors that are more compact than tubular devices and can be deployed if a certain loss of productivity is acceptable.
  • a PBR must have high productivity, large volume, low maintenance and building expenses, and flexibility and ease to control culture parameters.
  • Immobilized cell culture offers important advantages over free suspension in particular when the cells are slow growing. Extra-cellular products can be recovered continuously with ease. Since micro algae are shear sensitive, immobilization can protect cells against hydrodynamic shear forces. Immobilization by Calcium Alginate beads results in cells with enhanced chlorophyll content in attempt to capture more of the available light. Gel-entrapped cells are thus protected from photoinhibition, a condition in which intense irradiance actually causes a loss in photosynthetic performance. However, Alginate gel-immobilized cells have a lower growth rates and lower biomass production relative to free controls, possibly because immobilization can reduce availability of substrate to the cells. It is to be noted that Immobilized cells retain the ability to produce hydrocarbons, whose structure and relative abundance are not affected by immobilization.
  • PUF Polyurethane Foams
  • support matrices have broad range of porosity and mechanical strength.
  • the exposure to light to the cells drops down noticeably and so does the growth.
  • Cotton gauze - immobilized B. braunii cells show higher levels of hydrocarbon production, biomass growth, and photosynthetic activity when compared with cells immobilized in PUF.
  • the practicability of immobilized algal culture remains questionable unless the cells can be cultured in long-duration continuous culture and the hydrocarbons can be extracted continuously, say by doing some protein engineering for post-translational modification in the corresponding DNA sequence, or by selectively subjecting the beads to extracting solvent such that the hydrocarbon is extracted and the cell remains as it is inside the beads.
  • B. braunii has a disperse culture growth and growth into clump-form is not an advantage to the organism, rather causes reduction in the supply of oxygen to the inner cells.
  • Application of Tubular coiled reactor is advantageously is the best for the purpose.
  • High surface to volume value is desired for more or less equal distribution of light intensity.
  • Application of Tubular coiled reactor serves best for the purpose.
  • B. braunii dark strips of appropriate width are introduced at regular intervals, such that the order is not more than a second. For maximum utilization of energy, light is provided from inside and not from outside, such as inside the coiled helix in the Tubular coiled reactor.
  • Chlorophill b and ⁇ -carotene are light harvesting pigments which have their absorption wavelength maxima in the range 400nm-500nm and 620-680nm. Either single fluorescent light can be deployed covering the entire wavelength of 400- 700nm, or 2 LEDs can be made use of, one with the emission bandwidth of 400- 500nm and another with 600-700 nm as LEDs have a narrow bandwidth. The choice would be governed by comparative economics.
  • the Carbon-Dioxide percentage of 5% can be considered to be optimum for microalgae growth though the exact optimum value would be dependent on other factors such as the strain & temperature.
  • Tubular Helical PBR takes into account of most of the above considerations. The only demerit is the large land area required for scale up as for a given volume the coiled tube would be very long. The present invention nullifies this effect and thereby reduces the problem of large land area.
  • a peristaltic pump is provided it is not harmful for the shear- sensitive organism such as the B. Braunii. Usage of pump also reduces the chances of reverse flow. Additionally, the pump action also disperses cell clumps and thereby facilitates more of absorption of nutrients and light by individual cells. Care should be taken that pressure of the medium being pumped does not exceed the osmotolerance pressure which is 1 atmosphere (guage).
  • the present 'Flash Light Super Helical Photo Bio Reactor' takes care of the scalability issue of traditional helical photobioreactor and also introduces increase in the photosynthetic activity of the microalgae by Flash-Light effect.
  • a preferred embodiment of the bio-rector comprises a helical tubular system having at least two substantially coaxial helical transparent autoclavable tubular coils(l) for flow of a culture medium containing micro algae to be cultivated, each coil being hydraulically connected to its adjacent coaxial coil, said coils having annular spaces interposed between the adjacent coils and a space enclosed by the inner diameter of innermost coil, the first and the last coil each having a free end.
  • the number of coaxial coils may be 2 or 3 or more.
  • the end of each coil is hydraulically connected to the starting point of adj ascent coil.
  • the primary requirements of the tube forming superhelical structure is that it should be transparent and autoclavable. Further, it should be non-fragile and economical. One possibility was that of Glass.
  • the photostage of present invention comprises said transparent autoclavable tubular coils made from silicon polymer material.
  • the bio reactor has a means(2,3) of providing Flash-Light effect i.e. periods of light and darkness on each point alternately for predetermined time periods on the inner and outer surfaces of each of said coil.
  • means(3) for providing periods of light is a plurality of tubelights uniformally placed in the annular space between two adj ascent coils and the space enclosed by inner diameter of the innermost coil.
  • a plurality of light emitting diodes is used for this purpose.
  • An optic fiber coil may be used to provide solar illumination in another embodiment.
  • a combination of these means are used.
  • means(2) of providing period of darkness comprises a plurality of opaque strips or wires of predetermined width or diameter which obstruct the light from means of illumination falling on various points along the surface of the helical tubular coils and thus provide periods of light and darkness for the culture medium circulating in the helical tubular coils.
  • said alternating light and darkness time periods on each point along the flow path of said circulating culture medium are in the ratio 1:0.1 to 1: 0.2.
  • these coils are wound around a 'wire cage'(2) as illustrated in Figure 2, which would provide strips of shadow or less light intensity zone at regular intervals to result in alternating light and darkness time periods on each point along the flow path.
  • said means of providing periods of light and darkness comprises an electronic flashing device.
  • there is preferably a cycle comprising alternately continuous darkness time period of 8 hours after each period of 16 hours of said alternating light and darkness time periods.
  • the bio reactor has a de-gasser chamber(4) having hydraulic connection with said free end of the first coaxial coil for removing unwanted gases from said culture medium.
  • a stirrer(5) is provided in said de-gasser chamber for keeping the bio-mass in suspension in said culture medium.
  • the stirrer is a magnetic stirrer or a small air-lift reactor for suspending the culture.
  • the de-gasser chamber has hydraulic connection with a heat exchanger( ⁇ ) for controlling temperature of said culture medium preferably between 25° C and 36° C.
  • the heat exchanger may comprise a water bath for heating and/ or a chilling unit for cooling.
  • the water bath may comprise copper coils for flow of said culture medium, fitted inside a container for water circulation.
  • the bio reactor has a means(7) for causing flow of said culture medium in said coils without said means coming into direct contact with said medium.
  • this means is a perislatic pump(7), which acts on the outer surface of the tube to cause pumping of the culture medium without coming in contact with the medium.
  • a gas injection means(8) is connected to said de-gasser chamber of the bio reactor on one end and said free end of last coil on the other end.
  • the gas injection means may be a Y-shaped junction(8) having two inlet arms and one outlet arm with said outlet arm connected to said free end of last coil and said two inlet arms connected to a CO 2 source and an air source respectively.
  • the flow of the air plus carbon-dioxide and the pump together are kept such that the relative superficial velocity of the gas with respect to the liquid does riot exceed the value 0.085 m/s.
  • We can obtain such value by taking air flow rate to be ⁇ 0.170 m/s and the pump flow rate to be 0.085 m/s.
  • flow rate of said circulating culture medium is from .085 m/s to 0.10 m/s and said gas flow rate is between 0.170 m/s to 0.200 m/s.
  • a preferred method of cultivating and harvesting a bio-mass in the photo bio-reactor of present invention comprises the steps of: (a) circulating a culture medium containing a micro algae in said reactor at a predetermined flow rate;
  • the micro algae used is Botryococcus braunii.
  • the method may also be adapted for cultivating and harvesting spirulina or any other algae.
  • the modified Chu-13 medium is used to culture B: braunii. This medium has the following composition (Kgm "3 ) at four-fold normal strength:
  • Colony size increase with increased light intensity initially when the cell concentration is low and sufficient light for photosynthesis was available. As the cell concentration increase, the average light intensity within the photobioreactor decreased because of mutual shading, and thus the production rates of extracellular polysaccharides and hydrocarbons decrease with decreasing average light intensity.
  • the equilibrium colony size is determined by a dynamic balance between the mechanical strength of colonies and the hydrodynamics stress due to turbulence in the reactors.
  • the pH of the culture medium is generally adjusted to between 7.4 and 7.6 before inoculation. A regular increase in pH is observed during active growth followed by a slight decline later. The increase in pH is partly due to the consumption of dissolved CO2 for photosynthesis. Similar changes in pH are observed in CO 2 enriched culture during exponential growth.
  • the pH is adjusted to 7.5 before sterilization.
  • Optimum temperature for growth is 25- 30°C.
  • Reviews of the different techniques available have concluded that centrifugation is possibly the most reliable technique and only slightly more expensive than other techniques.
  • the goal of microalgal biotechnology efforts to recover a high value product from the microalgal biomass needs to be separated from the biomass.
  • the microalgal cells may need to be physically disrupted. Both ball mills and high pressure homogenisers have been used successfully to disrupt microalgal cells to enhance recovery.
  • Microalgal mass can be dehydrated in spray dryers, drum dryers, freeze dryers and sun dryers. In the case of Heat sensitive compounds commercial producers have developed technologies that limit exposure to conditions known to cause degradation.
  • biomass may not need to be dehydrated, and the extraction and fractionation can be carried out on the wet biomass. Further downstream processing may be needed to isolate the active compound depending on the intended final product.
  • NIES- N-836 B. braunii, sourced from Japan (NIES culture collection centre) was obtained from Central Food Technological Research Institute, Mysore, India and was used for evaluation of the performace of the reactor and other studies.
  • a wire strip is intermittently interposed between light source and tube.
  • the wire strip has a thickness of 0.3 cm.
  • Example 2 The Biomass estimation is carried out by the following steps: 1. 25ml. medium is harvested. 2. Take eppendorf and pre- weigh it.
  • the weight of hydrocarbons is calculated by the difference in the weight of vial.
  • the doubling time for biomass growth rate in the exponential phase is found to be nearly 8-9 days at 27 0 C and 14-15 days at 31 0 C as shown in the Figure 5 and 3 respectively.
  • the hydrocarbon accumulation was found to be growth associated and comprised 50-55% of the cell mass as shown in Figures 4 and 6.

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Abstract

L'objet de la présente invention consiste à satisfaire le besoin de longue date d'obtenir des photobioréacteurs à l'échelle du laboratoire et la culture massive d'organismes photosynthétiques, tels que la spiruline et de nombreuses autres micro-algues. Le photobioréacteur est constitué d'un système de spires tubulaires hélicoïdales, coaxiales, transparentes (1), résistant à l'autoclave, destinées à l'écoulement d'un milieu de culture contenant des micro-algues à cultiver. Les espaces annulaires entre les spires adjacentes et l'espace délimité par la spire la plus interne sont pourvus d'éléments (3) permettant de créer des périodes alternées prédéterminées de lumière et d'obscurité sur les surfaces interne et externe de chacune desdites spires, en vue d'une régulation de la température du milieu et d'une amélioration de la performance photosynthétique. Les spires tubulaires présentent un rapport surface active-volume élevé qui permet une dissolution considérable du dioxyde de carbone gazeux injecté dans les milieux. L'organisme utilisé pour la culture d'une biomasse appropriée pour la production d'hydrocarbure est la micro-algue bleu-vert appelée Botryococcus braunii.
PCT/IN2006/000407 2006-05-08 2006-10-13 Photobioréacteur destiné à cultiver et à recueillir une biomasse et son procédé WO2007129327A1 (fr)

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KR100884938B1 (ko) 2008-09-25 2009-02-23 이영환 미생물 복합 배양장치
WO2010048525A3 (fr) * 2008-10-24 2010-06-17 Bioprocessh20 Llc Systèmes, appareils et méthodes de culture de micro-organismes et d’atténuation de gaz
WO2011015653A2 (fr) 2009-08-07 2011-02-10 Wacker Chemie Ag Bioréacteur en matériaux siliconiques
DE102009045851A1 (de) 2009-10-20 2011-04-21 Wacker Chemie Ag Schlauch-Photobioreaktor
WO2012035027A1 (fr) 2010-09-13 2012-03-22 Universite De Nantes Dispositif de controle de la temperature d'un photobioreacteur solaire a eclairage direct
DE102010043587A1 (de) * 2010-11-08 2012-05-10 Christoph Peppmeier Zuchtvorrichtung für phototrophe Kulturen, sowie Verfahren zu deren Steuerung
US8476067B2 (en) 2007-02-06 2013-07-02 Phyco2 Llc Photobioreactor and method for processing polluted air
KR101287384B1 (ko) 2013-04-17 2013-07-23 이수연 Led 광파장의 혼합을 이용한 미세조류의 성장 및 지질함량 향상 방법
US20130302869A1 (en) * 2010-11-15 2013-11-14 Cornell University Optofluidic photobioreactor apparatus, method, and applications
US8809037B2 (en) 2008-10-24 2014-08-19 Bioprocessh20 Llc Systems, apparatuses and methods for treating wastewater
WO2014133793A1 (fr) 2013-02-26 2014-09-04 Heliae Development, Llc Bioréacteur tubulaire modulaire
US9200248B2 (en) 2009-08-07 2015-12-01 Wacker Chemie Ag Bioreactor comprising a silicone coating
WO2016090090A1 (fr) * 2014-12-05 2016-06-09 Kohane Technologies, Llc Système de puissance bioénergétique
WO2020055719A1 (fr) * 2018-09-10 2020-03-19 Saudi Arabian Oil Company Procédé et système de traitement d'eaux usées sanitaires dans un tube spiralé emboîté
FR3089521A1 (fr) 2018-12-10 2020-06-12 Commissariat A L'energie Atomique Et Aux Energies Alternatives photobioréacteur
CN112813113A (zh) * 2020-12-30 2021-05-18 兴源环境科技股份有限公司 一种畜禽粪污增效生产生物油的方法
WO2022175984A1 (fr) * 2021-02-19 2022-08-25 Greengroves Bahrain Wll Réacteur algal à décarbonisation automatisée
EP4385614A1 (fr) * 2022-12-15 2024-06-19 Samsung Electronics Co., Ltd. Dispositif de surveillance optique

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EP0402496A1 (fr) * 1989-06-13 1990-12-19 Institut für Getreideverarbeitung GmbH Installation pour la culture de microorganismes autotrophes
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US8476067B2 (en) 2007-02-06 2013-07-02 Phyco2 Llc Photobioreactor and method for processing polluted air
KR100884938B1 (ko) 2008-09-25 2009-02-23 이영환 미생물 복합 배양장치
JP2012506700A (ja) * 2008-10-24 2012-03-22 バイオプロセス エイチツーオー・エルエルシー 微生物を培養しガスを軽減するためのシステム、装置、および方法
WO2010048525A3 (fr) * 2008-10-24 2010-06-17 Bioprocessh20 Llc Systèmes, appareils et méthodes de culture de micro-organismes et d’atténuation de gaz
JP2013138676A (ja) * 2008-10-24 2013-07-18 Bioprocessh2O Llc 微生物を培養しガスを軽減するためのシステム、装置、および方法
CN102257125B (zh) * 2008-10-24 2015-06-17 生物进程H2O有限责任公司 用于培养微生物和减缓气体的系统、设备和方法
US8809037B2 (en) 2008-10-24 2014-08-19 Bioprocessh20 Llc Systems, apparatuses and methods for treating wastewater
AU2009308283B2 (en) * 2008-10-24 2014-07-17 Bioprocessh20 Llc Systems, apparatuses and methods for cultivating microorganisms and mitigation of gases
DE102009028339A1 (de) * 2009-08-07 2011-02-24 Wacker Chemie Ag Bioreaktor aus Siliconmaterialien
EP2462218B1 (fr) * 2009-08-07 2013-12-25 Wacker Chemie AG Boiréacteur en matériaux siliconés
US9200248B2 (en) 2009-08-07 2015-12-01 Wacker Chemie Ag Bioreactor comprising a silicone coating
US9200247B2 (en) 2009-08-07 2015-12-01 Wacker Chemie Ag Bioreactor consisting of silicone materials
WO2011015653A2 (fr) 2009-08-07 2011-02-10 Wacker Chemie Ag Bioréacteur en matériaux siliconiques
CN106367322B (zh) * 2009-10-20 2019-06-25 瓦克化学股份公司 管式光生物反应器
CN102575211A (zh) * 2009-10-20 2012-07-11 瓦克化学股份公司 管式光生物反应器
US8586344B2 (en) 2009-10-20 2013-11-19 Wacker Chemie Ag Tubular photobioreactor
WO2011048108A3 (fr) * 2009-10-20 2011-06-30 Wacker Chemie Ag Photo-bioréacteur à flexibles
CN106367322A (zh) * 2009-10-20 2017-02-01 瓦克化学股份公司 管式光生物反应器
WO2011048108A2 (fr) 2009-10-20 2011-04-28 Wacker Chemie Ag Photo-bioréacteur à flexibles
DE102009045851A1 (de) 2009-10-20 2011-04-21 Wacker Chemie Ag Schlauch-Photobioreaktor
WO2012035027A1 (fr) 2010-09-13 2012-03-22 Universite De Nantes Dispositif de controle de la temperature d'un photobioreacteur solaire a eclairage direct
DE102010043587B4 (de) * 2010-11-08 2012-06-14 Christoph Peppmeier Zuchtvorrichtung für phototrophe Kulturen, sowie Verfahren zu deren Steuerung
DE102010043587A1 (de) * 2010-11-08 2012-05-10 Christoph Peppmeier Zuchtvorrichtung für phototrophe Kulturen, sowie Verfahren zu deren Steuerung
US10604733B2 (en) 2010-11-15 2020-03-31 Cornell University Optofluidic photobioreactor apparatus, method, and applications
US9518248B2 (en) * 2010-11-15 2016-12-13 Cornell University Optofluidic photobioreactor apparatus, method, and applications
US20130302869A1 (en) * 2010-11-15 2013-11-14 Cornell University Optofluidic photobioreactor apparatus, method, and applications
US11186812B2 (en) 2010-11-15 2021-11-30 Cornell University Optofluidic photobioreactor apparatus, method, and applications
WO2014133793A1 (fr) 2013-02-26 2014-09-04 Heliae Development, Llc Bioréacteur tubulaire modulaire
US10053659B2 (en) 2013-02-26 2018-08-21 Heliae Development Llc Modular tubular bioreactor
US10876087B2 (en) 2013-02-26 2020-12-29 Heliae Development Llc Modular tubular bioreactor
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US10673087B2 (en) 2014-12-05 2020-06-02 Kohane Technologies, Llc Bio-energy power system
WO2016090090A1 (fr) * 2014-12-05 2016-06-09 Kohane Technologies, Llc Système de puissance bioénergétique
US10899644B2 (en) 2018-09-10 2021-01-26 Saudi Arabian Oil Company Sanitizing wastewater
WO2020055719A1 (fr) * 2018-09-10 2020-03-19 Saudi Arabian Oil Company Procédé et système de traitement d'eaux usées sanitaires dans un tube spiralé emboîté
FR3089521A1 (fr) 2018-12-10 2020-06-12 Commissariat A L'energie Atomique Et Aux Energies Alternatives photobioréacteur
EP3666879A1 (fr) 2018-12-10 2020-06-17 Commissariat à l'Energie Atomique et aux Energies Alternatives Photobioreacteur
CN112813113A (zh) * 2020-12-30 2021-05-18 兴源环境科技股份有限公司 一种畜禽粪污增效生产生物油的方法
WO2022175984A1 (fr) * 2021-02-19 2022-08-25 Greengroves Bahrain Wll Réacteur algal à décarbonisation automatisée
EP4385614A1 (fr) * 2022-12-15 2024-06-19 Samsung Electronics Co., Ltd. Dispositif de surveillance optique

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