US20120276633A1 - Supplying treated exhaust gases for effecting growth of phototrophic biomass - Google Patents
Supplying treated exhaust gases for effecting growth of phototrophic biomass Download PDFInfo
- Publication number
- US20120276633A1 US20120276633A1 US13/095,490 US201113095490A US2012276633A1 US 20120276633 A1 US20120276633 A1 US 20120276633A1 US 201113095490 A US201113095490 A US 201113095490A US 2012276633 A1 US2012276633 A1 US 2012276633A1
- Authority
- US
- United States
- Prior art keywords
- carbon dioxide
- fraction
- rich
- separation
- reaction zone
- Prior art date
- Legal status (The legal status 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 status listed.)
- Abandoned
Links
Images
Classifications
-
- A—HUMAN NECESSITIES
- A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
- A01G—HORTICULTURE; CULTIVATION OF VEGETABLES, FLOWERS, RICE, FRUIT, VINES, HOPS OR SEAWEED; FORESTRY; WATERING
- A01G33/00—Cultivation of seaweed or algae
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K14/00—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
- C07K14/435—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans
- C07K14/46—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans from vertebrates
- C07K14/47—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans from vertebrates from mammals
- C07K14/4701—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans from vertebrates from mammals not used
- C07K14/472—Complement proteins, e.g. anaphylatoxin, C3a, C5a
-
- 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
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
-
- 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
- C12M43/00—Combinations of bioreactors or fermenters with other apparatus
- C12M43/04—Bioreactors or fermenters combined with combustion devices or plants, e.g. for carbon dioxide removal
-
- 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
- C12N1/12—Unicellular algae; Culture media therefor
-
- 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
- C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
- C12N5/04—Plant cells or tissues
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/59—Biological synthesis; Biological purification
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Zoology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Wood Science & Technology (AREA)
- Genetics & Genomics (AREA)
- Biotechnology (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Microbiology (AREA)
- General Engineering & Computer Science (AREA)
- Sustainable Development (AREA)
- Molecular Biology (AREA)
- Medicinal Chemistry (AREA)
- Cell Biology (AREA)
- Botany (AREA)
- Biophysics (AREA)
- Environmental Sciences (AREA)
- Combustion & Propulsion (AREA)
- Gastroenterology & Hepatology (AREA)
- Toxicology (AREA)
- Analytical Chemistry (AREA)
- Marine Sciences & Fisheries (AREA)
- Proteomics, Peptides & Aminoacids (AREA)
- Tropical Medicine & Parasitology (AREA)
- Virology (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
- Carbon And Carbon Compounds (AREA)
- Treating Waste Gases (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
There is provided a process for growing a phototrophic biomass in a reaction zone. The process includes treating an operative carbon dioxide supply-comprising gaseous material feed so as to effect production of a carbon dioxide-rich product material. The carbon dioxide concentration of the carbon dioxide-rich product material is greater than the carbon dioxide concentration of the operative carbon dioxide supply-comprising gaseous material feed. Production of at least a fraction of the operative carbon dioxide supply-comprising gaseous material feed is effected by a gaseous exhaust material producing process. At least a fraction of the carbon dioxide-rich product material is supplied to the reaction zone so as to effect growth of the phototrophic biomass by photosynthesis in the reaction zone.
Description
- The present disclosure relates to a process for growing biomass.
- The cultivation of phototrophic organisms has been widely practised for purposes of producing a fuel source. Exhaust gases from industrial processes have also been used to promote the growth of phototrophic organisms by supplying carbon dioxide for consumption by phototrophic organisms during photosynthesis. By providing exhaust gases for such purpose, environmental impact is reduced and, in parallel a potentially useful fuel source is produced. Challenges remain, however, to render this approach more economically attractive for incorporation within existing facilities.
- In one aspect, there is provided a process for growing a phototrophic biomass in a reaction zone. The process includes treating an operative carbon dioxide supply-comprising gaseous material feed so as to effect production of a carbon dioxide-rich product material. The carbon dioxide concentration of the carbon dioxide-rich product material is greater than the carbon dioxide concentration of the operative carbon dioxide supply-comprising gaseous material feed. Production of at least a fraction of the operative carbon dioxide supply-comprising gaseous material feed is effected by a gaseous exhaust material producing process. At least a fraction of the carbon dioxide-rich product material is supplied to the reaction zone so as to effect growth of the phototrophic biomass by photosynthesis in the reaction zone.
- The process of the preferred embodiments of the invention will now be described with the following accompanying drawings:
-
FIG. 1 is a process flow diagram of an embodiment of the process. -
FIG. 2 is a schematic illustration of a portion of a fluid passage of an embodiment of the process. - Reference throughout the specification to “some embodiments” means that a particular feature, structure, or characteristic described in connection with some embodiments are not necessarily referring to the same embodiments. Furthermore, the particular features, structure, or characteristics may be combined in any suitable manner with one another.
- Referring to
FIG. 1 , there is provided a process of growing a phototrophic biomass in areaction zone 10. Thereaction zone 10 includes a reaction mixture that is operative for effecting photosynthesis upon exposure to photosynthetically active light radiation. The reaction mixture includes phototrophic biomass material, carbon dioxide, and water. In some embodiments, the reaction zone includes phototrophic biomass and carbon dioxide disposed in an aqueous medium. Within thereaction zone 10, the phototrophic biomass is disposed in mass transfer communication with both of carbon dioxide and water. - “Phototrophic organism” is an organism capable of phototrophic growth in the aqueous medium upon receiving light energy, such as plant cells and micro-organisms. The phototrophic organism is unicellular or multicellular. In some embodiments, for example, the phototrophic organism is an organism which has been modified artificially or by gene manipulation. In some embodiments, for example, the phototrophic organism is an alga. In some embodiments, for example, the algae are microalgae.
- “Phototrophic biomass” is at least one phototrophic organism. In some embodiments, for example, the phototrophic biomass includes more than one species of phototrophic organisms.
- “
Reaction zone 10” defines a space within which the growing of the phototrophic biomass is effected. In some embodiments, for example, thereaction zone 10 is provided in aphotobioreactor 12. In some embodiments, for example, pressure within the reaction zone is atmospheric pressure. - “
Photobioreactor 12” is any structure, arrangement, land formation or area that provides a suitable environment for the growth of phototrophic biomass. Examples of specific structures which can be used is aphotobioreactor 12 by providing space for growth of phototrophic biomass using light energy include, without limitation, tanks, ponds, troughs, ditches, pools, pipes, tubes, canals, and channels. Such photobioreactors may be either open, closed, partially closed, covered, or partially covered. In some embodiments, for example, thephotobioreactor 12 is a pond, and the pond is open, in which case the pond is susceptible to uncontrolled receiving of materials and light energy from the immediate environments. In other embodiments, for example, thephotobioreactor 12 is a covered pond or a partially covered pond, in which case the receiving of materials from the immediate environment is at least partially interfered with. Thephotobioreactor 12 includes thereaction zone 10 which includes the reaction mixture. In some embodiments, thephotobioreactor 12 is configured to receive a supply of phototrophic reagents (and, in some of these embodiments, optionally, supplemental nutrients), and is also configured to effect discharge of phototrophic biomass which is grown within thereaction zone 10. In this respect, in some embodiments, thephotobioreactor 12 includes one or more inlets for receiving the supply of phototrophic reagents and supplemental nutrients, and also includes one or more outlets for effecting the recovery or harvesting of biomass which is grown within thereaction zone 10. In some embodiments, for example, one or more of the inlets are configured to be temporarily sealed for periodic or intermittent time intervals. In some embodiments, for example, one or more of the outlets are configured to be temporarily sealed or substantially sealed for periodic or intermittent time intervals. Thephotobioreactor 12 is configured to contain the reaction mixture which is operative for effecting photosynthesis upon exposure to photosynthetically active light radiation. Thephotobioreactor 12 is also configured so as to establish photosynthetically active light radiation (for example, a light of a wavelength between about 400-700 nm, which can be emitted by the sun or another light source) within thephotobioreactor 12 for exposing the phototrophic biomass. The exposing of the reaction mixture to the photosynthetically active light radiation effects photosynthesis and growth of the phototrophic biomass. In some embodiments, for example, the established light radiation is provided by anartificial light source 14 disposed within thephotobioreactor 12. For example, suitable artificial lights sources include submersible fiber optics or light guides, light-emitting diodes (“LEDs”), LED strips and fluorescent lights. Any LED strips known in the art can be adapted for use in thephotobioreactor 12. In the case of the submersible LEDs, in some embodiments, for example, energy sources include alternative energy sources, such as wind, photovoltaic cells, fuel cells, etc. to supply electricity to the LEDs. Fluorescent lights, external or internal to thephotobioreactor 12, can be used as a back-up system. In some embodiments, for example, the established light is derived from anatural light source 16 which has been transmitted from externally of thephotobioreactor 12 and through a transmission component. In some embodiments, for example, the transmission component is a portion of a containment structure of thephotobioreactor 12 which is at least partially transparent to the photosynthetically active light radiation, and which is configured to provide for transmission of such light to thereaction zone 10 for receiving by the phototrophic biomass. In some embodiments, for example, natural light is received by a solar collector, filtered with selective wavelength filters, and then transmitted to thereaction zone 10 with fiber optic material or with a light guide. In some embodiments, for example, both natural and artificial lights sources are provided for effecting establishment of the photosynthetically active light radiation within thephotobioreactor 12. - “Aqueous medium” is an environment that includes water. In some embodiments, for example, the aqueous medium also includes sufficient nutrients to facilitate viability and growth of the phototrophic biomass. In some embodiments, for example, supplemental nutrients may be included such as one of, or both of, NOX and SOX. Suitable aqueous media are discussed in detail in: Rogers, L. J. and Gallon J. R. “Biochemistry of the Algae and Cyanobacteria,” Clarendon Press Oxford, 1988; Burlew, John S. “Algal Culture: From Laboratory to Pilot Plant.” Carnegie Institution of Washington Publication 600. Washington, D.C., 1961 (hereinafter “Burlew 1961”); and Round, F. E. The Biology of the Algae. St Martin's Press, New York, 1965; each of which is incorporated herein by reference). A suitable supplemental nutrient composition, known as “Bold's Basal Medium”, is described in Bold, H. C. 1949, The morphology of Chlamydomonas chlamydogama sp. nov. Bull. Torrey Bot. Club. 76: 101-8 (see also Bischoff, H. W. and Bold, H. C. 1963. Phycological Studies IV Some soil algae from Enchanted Rock and related algal species, Univ. Texas Publ. 6318: 1-95, and Stein, J. (ED.) Handbook of Phycological Methods, Culture methods and growth measurements, Cambridge University Press, pp. 7-24).
- The process includes supplying the
reaction zone 10 with carbon dioxide derived from agaseous exhaust material 14 being discharged by a gaseous exhaustmaterial producing process 16. Thegaseous exhaust material 14 includes carbon dioxide, and the carbon dioxide of the gaseous exhaust material defines produced carbon dioxide. - In some embodiments, for example, the
gaseous exhaust material 14 includes a carbon dioxide concentration of at least two (2) volume % based on the total volume of thegaseous exhaust material 14. In some embodiments, for example, thegaseous exhaust material 14 includes a carbon dioxide concentration of at least four (4) volume % based on the total volume of thegaseous exhaust material 14. In some embodiments, for example, the gaseousexhaust material reaction 14 also includes one or more of N2, CO2, H2O, O2, NOx, SOx, CO, volatile organic compounds (such as those from unconsumed fuels) heavy metals, particulate matter, and ash. In some embodiments, for example, thegaseous exhaust material 14 includes 30 to 60 volume % N2, 5 to 25 volume % O2, 2 to 50 volume % CO2, and 0 to 30 volume % H2O, based on the total volume of thegaseous exhaust material 14. Other compounds may also be present, but usually in trace amounts (cumulatively, usually less than five (5) volume % based on the total volume of the gaseous exhaust material 14). - In some embodiments, for example, the
gaseous exhaust material 14 includes one or more other materials, other than carbon dioxide, that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Materials within the gaseous exhaust material which are beneficial to the growth of the phototrophic biomass within thereaction zone 10 include SOX, NOX, and NH3. - In some embodiments, for example, a
supplemental nutrient supply 18 is supplied to thereaction zone 10. In some embodiments, for example, thesupplemental nutrient supply 18 is effected by a pump, such as a dosing pump. In other embodiments, for example, thesupplemental nutrient supply 18 is supplied manually to thereaction zone 10. Nutrients within thereaction zone 10 are processed or consumed by the phototrophic biomass, and it is desirable, in some circumstances, to replenish the processed or consumed nutrients. A suitable nutrient composition is “Bold's Basal Medium”, and this is described in Bold, H. C. 1949, The morphology of Chlamydomonas chlamydogama sp. nov. Bull. Torrey Bot. Club. 76: 101-8 (see also Bischoff, H. W. and Bold, H. C. 1963, Phycological Studies IV Some soil algae from Enchanted Rock and related algal species, Univ. Texas Publ. 6318: 1-95, and Stein, J. (ED.) Handbook of Phycological Methods, Culture methods and growth measurements, Cambridge University Press, pp. 7-24). Thesupplemental nutrient supply 18 is supplied for supplementing the nutrients provided within the reaction zone, such as “Bold's Basal Medium”, or one or more dissolved components thereof. In this respect, in some embodiments, for example, thesupplemental nutrient supply 18 includes “Bold's Basal Medium”. In some embodiments for example, thesupplemental nutrient supply 18 includes one or more dissolved components of “Bold's Basal Medium”, such as NaNO3, CaCl2, MgSO4, KH2PO4, NaCl, or other ones of its constituent dissolved components. - In some of these embodiments, the rate of supply of the
supplemental nutrient supply 18 to thereaction zone 10 is controlled to align with a desired rate of growth of the phototrophic biomass in thereaction zone 10. In some embodiments, for example, regulation of nutrient addition is monitored by measuring any combination of pH, NO3 concentration, and conductivity in thereaction zone 10. - In some embodiments, for example, a supply of the supplemental
aqueous material supply 20 is effected to thereaction zone 10 so as to replenish water within thereaction zone 10 of thephotobioreactor 12. In some embodiments, for example, and as further described below, the supplementalaqueous material supply 20 effects the discharge of product from thephotobioreactor 12 by displacement. For example, the supplementalaqueous material supply 20 effects the discharge of product from thephotobioreactor 12 as an overflow. - In some embodiments, for example, the supplemental aqueous material is water or substantially water. In some embodiments, for example, the supplemental
aqueous material supply 20 includes at least one of: (a) aqueous material that has been condensed from the supplied exhausted carbon dioxide while the supplied exhausted carbon dioxide is being cooled before being supplied to the contactingzone 34, and (b) aqueous material that has been separated from a discharged phototrophic biomass-comprising product 202 (see below). In some embodiments, for example, the supplementalaqueous material supply 20 is derived from an independent source (i.e., a source other than the process), such as amunicipal water supply 203. - In some embodiments, for example, the supplemental
aqueous material supply 20 is supplied from a container that has collected aqueous material recovered from discharges from the process, such as: (a) aqueous material that has been condensed from the supplied exhausted carbon dioxide while the supplied exhausted carbon dioxide is being cooled before being supplied to the contacting zone, and (b) aqueous material that has been separated from a discharged phototrophic biomass-comprisingproduct 202. In some embodiments, for example, the container is in the form of a settling column 212 (see below). - In some embodiments, for example, the
supplemental nutrient supply 18 is mixed with the supplementalaqueous material 20 to provide a nutrient-enriched supplementalaqueous material supply 22, and the nutrient-enriched supplementalaqueous material supply 22 is supplied to thereaction zone 10. In some embodiments, for example, thesupplemental nutrient supply 18 is mixed with the supplementalaqueous material 20 within the container which has collected the discharged aqueous material. In some embodiments, for example, the supply of the nutrient-enriched supplementalaqueous material supply 18 is effected by a pump. - An operative carbon dioxide supply-comprising gaseous material feed is provided. The operative carbon dioxide supply-comprising gaseous material feed includes carbon dioxide and one or more other materials. The operative carbon dioxide supply-comprising gaseous material feed includes at least a fraction of the
gaseous exhaust material 14, and the at least a fraction of thegaseous exhaust material 14 of the operative carbon dioxide supply-comprising gaseous material feed defines supplied gaseous exhaust material. The carbon dioxide that is supplied to the operative carbon dioxide supply-comprising gaseous material feed from the gaseous exhaustmaterial producing process 16 defines supplied exhausted carbon dioxide. The supplied exhausted carbon dioxide is defined by at least a fraction of the produced carbon dioxide. The carbon dioxide of the operative carbon dioxide supply-comprising gaseous material feed includes supplied exhausted carbon dioxide. In some embodiments, for example, the carbon dioxide of the operative carbon dioxide supply-comprising gaseous material feed is defined by the supplied exhausted carbon dioxide. In some embodiments, for example, the operative carbon dioxide supply-comprising gaseous material feed is defined by supplied gaseous exhaust material. - In some embodiments, for example, the operative carbon dioxide supply-comprising gaseous material feed includes one or more other materials supplied from the
gaseous exhaust material 14, other than carbon dioxide, that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - The gaseous exhaust
material producing process 16 includes any process which effects production and discharge of thegaseous exhaust material 14. In some embodiments, for example, at least a fraction of thegaseous exhaust material 14 being discharged by the gaseous exhaustmaterial producing process 16 is supplied to thereaction zone 10. The at least a fraction of thegaseous exhaust material 14, being discharged by the gaseous exhaustmaterial producing process 16, and supplied to thereaction zone 10, includes carbon dioxide derived from the gaseous exhaustmaterial producing process 16. In some embodiments, for example, the gaseous exhaustmaterial producing process 16 is a combustion process. In some embodiments, for example, the combustion process is effected in a combustion facility. In some of these embodiments, for example, the combustion process effects combustion of a fossil fuel, such as coal, oil, or natural gas. For example, the combustion facility is any one of a fossil fuel-fired power plant, an industrial incineration facility, an industrial furnace, an industrial heater, or an internal combustion engine. In some embodiments, for example, the combustion facility is a cement kiln. - The operative carbon dioxide supply-comprising gaseous material feed is treated so as to effect production of a carbon dioxide-
rich product material 26. In some embodiments, the carbon dioxide-rich product material 26 is gaseous. The carbon dioxide of the carbon dioxide-rich product material 26 defines concentrated reaction zone supply carbon dioxide. The carbon dioxide concentration of the carbon dioxide-rich product material 26 is greater than the carbon dioxide concentration of the operative carbon dioxide supply-comprising gaseous material feed. The carbon dioxide-rich product material 26 includes at least a fraction of the supplied exhausted carbon dioxide, such that the concentrated reaction zone supply carbon dioxide includes at least a fraction of the supplied exhausted carbon dioxide. In some embodiments, the concentrated reaction zone supply carbon dioxide is defined by at least a fraction of the supplied exhausted carbon dioxide. As such, the carbon dioxide-rich product material 26 includes at least a fraction of the produced carbon dioxide, such that the concentrated reaction zone supply carbon dioxide includes at least a fraction of produced carbon dioxide. In some embodiments, the concentrated reaction zone supply carbon dioxide is defined by at least a fraction of the produced carbon dioxide. - In some embodiments, for example, the carbon dioxide-
rich product material 26 includes one or more other materials supplied from thegaseous exhaust material 14, other than carbon dioxide, that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - In some embodiments, the treating of the operative carbon dioxide supply-comprising gaseous material feed includes effecting separation, from a separation
process feed material 24, of a carbon dioxide-rich separation fraction 28. The separationprocess feed material 24 is defined by at least a fraction of the operative carbon dioxide supply-comprisinggaseous material feed 24. The carbon dioxide-rich product material 26 includes at least a fraction of the carbon dioxide-rich separation fraction 28. In some embodiments, for example, the carbon dioxide-rich separation fraction 28 is gaseous. The carbon dioxide of the carbon dioxide-rich separation fraction 28 includes at least a fraction of the supplied exhausted carbon dioxide, and, in some embodiments, for example, is defined by at least a fraction of the supplied exhausted carbon dioxide. As such, the carbon dioxide of the carbon dioxide-rich separation fraction 28 includes at least a fraction of the produced carbon dioxide, and, in some embodiments, for example, the carbon dioxide of the carbon dioxide-rich separation fraction 28 is defined by at least a fraction of the produced carbon dioxide. In some embodiments, for example, the carbon dioxide-rich separation fraction 28 includes one or more other materials supplied from thegaseous exhaust material 14, other than carbon dioxide, that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - In some embodiments, for example, the separation
process feed material 24 includes one or more other materials, other than carbon dioxide. In some embodiments, for example, the one or more other materials of the separationprocess feed material 24 are supplied from thegaseous exhaust material 14 and are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - The ratio of [moles of carbon dioxide within the carbon dioxide-rich separation fraction 28] to [moles of the one or more other materials of the separation
process feed material 24 within the carbon dioxide-rich separation fraction 28] is greater than the ratio of [moles of carbon dioxide within the separation process feed material 24] to [moles of the one or more other materials of the separationprocess feed material 24 within the separation process feed material 24]. In some embodiments, for example, the concentration of carbon dioxide within the carbon dioxide-rich fraction 28 is greater than the concentration of carbon dioxide within the separationprocess feed material 24. - The carbon dioxide-
rich product material 26 includes at least a fraction of the carbon dioxide of the carbon dioxide-rich separation fraction 28, such that the concentrated reaction zone supply carbon dioxide includes at least a fraction of the carbon dioxide of the carbon dioxide-rich separation fraction 28. In some embodiments, for example, the concentrated reaction zone supply carbon dioxide is defined by at least a fraction of the carbon dioxide of the carbon dioxide-rich separation fraction 28. - In some embodiments, for example, the effecting separation, from the separation process feed material, of a carbon dioxide-
rich separation fraction 28, includes contacting the separationprocess feed material 24 with an operative solvation (or dissolution)agent 30, so as to effect production of an intermediate operative carbon dioxide supply-comprisingmixture 32 including dissolved carbon dioxide. The contacting effects solvation (or dissolution) of at least a fraction of the supplied exhausted carbon dioxide within the operative solvation agent, and thereby effects production of the dissolved carbon dioxide. In some embodiments, for example, the contacting also effects solvation (or dissolution) of at least a fraction of the one or more other materials within the separationprocess feed material 24. In some embodiments, for example, the one or more other materials that are solvated (or dissolved) are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - The intermediate operative carbon dioxide supply-comprising
mixture 32 includes a carbon dioxide-comprising solution intermediate, wherein the carbon dioxide-comprising solution intermediate includes the dissolved carbon dioxide. The dissolved carbon dioxide includes at least a fraction of the supplied exhausted carbon dioxide, and, in some embodiments, is defined by at least a fraction of the supplied exhausted carbon dioxide. In this respect, the dissolved carbon dioxide includes at least a fraction of the produced carbon dioxide, and in some embodiments, is defined by at least a fraction of the produced carbon dioxide. In some embodiments, for example, the carbon dioxide-comprising solution intermediate also includes the one or more other materials supplied by the separationprocess feed material 24 that are solvated (or dissolved) and that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - It is understood that the contacting may also effect solvation (or dissolution) of at least a fraction of the one or more other materials of the separation
process feed material 24, but only to an extent that the above-described relationship of the ratio of [moles of carbon dioxide within the carbon dioxide-rich separation fraction 28] to [moles of the one or more other materials of the separationprocess feed material 24 within the carbon dioxide-rich separation fraction 28] and the ratio of [moles of carbon dioxide within the separation process feed material 24] to [moles of the one or more other materials of the separation process feed material within the separation process feed material 24] is maintained. - The contacting also effects production of a carbon dioxide-depleted gaseous intermediate, such that the intermediate operative carbon dioxide supply-comprising
mixture 32 includes the carbon dioxide-depleted gaseous intermediate. The carbon dioxide-depleted gaseous intermediate includes a fraction of the separationprocess feed material 24. The ratio of [moles of carbon dioxide within the separation process feed material 24] to [moles of the other one or more materials of the separationprocess feed material 24 within the separation process feed material feed 24] is greater than the ratio of [moles of carbon dioxide within the carbon dioxide-depleted gaseous intermediate] to [moles of the other one or more materials of the separationprocess feed material 24 within the carbon dioxide-depleted gaseous intermediate]. - In some embodiments, for example, the contacting of the separation
process feed material 24 with an operative solvation (or dissolution)agent 26 effects solvation (or dissolution) of a fraction of the separationprocess feed material 24 such that a material depleted operative carbon dioxide supply-comprising gaseous material feed is provided, and the material depleted operative carbon dioxide supply-comprising gaseous material feed includes, and, in some embodiments, is defined by, the carbon dioxide-depleted gaseous intermediate. - In some embodiments, for example, the one or more other materials of the separation
process feed material 24 includes at least one relatively less soluble material. Relative to carbon dioxide, each one of the at least one relatively less soluble material is less soluble within the operative solvation (or dissolution) agent, when the operative solvation (or dissolution) agent is disposed within the contacting zone. Examples of the relatively less soluble material include N2, O2, and CO. - In some embodiments, for example, the contacting is effected in a contacting
zone 34. - In some embodiments, for example, the operative solvation (or dissolution)
agent 30 is aqueous material. In some embodiments, for example, the operative solvation (or dissolution)agent 30 is water or substantially water, and the contacting is effected in a contactingzone 34 including a pressure of between 10 psia and 25 psia and a temperature of between two (2) degrees Celsius and four (4) degrees Celsius. In some embodiments, for example, the pressure is atmospheric and the temperature is three (3) degrees Celsius. - In some embodiments, for example, the operative solvation (or dissolution)
agent 30 is provided within the contactingzone 34 in the form of a mist by supplying the operative solvation (or dissolution)agent 34 to the contactingzone 34 through aspray nozzle 36. In some embodiments, for example, thespray nozzle 36 includes a plurality of substantially uniformly spaced-apart nozzles to maximize volumetric exchange of gas into the water droplets. Providing the operative solvation (or dissolution)agent 30 in the form of a mist increases the contact surface area between the operative solvation (or dissolution)agent 30 and the separationprocess feed material 24 being contacted. In some embodiments, for example, the operative solvation (or dissolution) agent discharging from thespray nozzle 36 includes a droplet size of between 10 and 2000 microns. In some embodiments, the operative solvation (or dissolution)agent 30 is discharged through thespray nozzle 36 at a temperature of between two (2) degrees Celsius and four (4) degrees Celsius. In some embodiments, for example, the temperature of the discharged operative solvation (or dissolution) agent is three (3) degrees Celsius. - In some embodiments, for example, the contacting
zone 34 is provided within a contactingtank 38. In some embodiments, for example, the contactingtank 38 contains a contactingzone liquid material 40 disposed within the contacting zone. In some embodiments, for example, the contactingzone liquid material 40 includes a vertical extent of between one (1) foot and five (5) feet. In some embodiments, for example, the contactingzone liquid material 40 is disposed at the bottom of the contactingtank 38. The contactingzone liquid material 40 includes the operative solvation (or dissolution)agent 30. In some embodiments, for example, the contactingzone liquid material 40 includes at least a fraction of the operative solvation (or dissolution)agent 30 that has been introduced to the contactingzone 34 through thespray nozzle 36. In some of these embodiments, for example, the contactingzone liquid material 40 includes at least a fraction of the operative solvation (or dissolution)agent 30 that has been introduced to the contactingzone 34 through thespray nozzle 36 and has collected at the bottom of the contactingzone tank 38. In some embodiments, for example, the contactingzone liquid material 40 includes at least a fraction of the carbon dioxide-comprising solution intermediate. In some of these embodiments, for example, the contactingzone liquid material 40 includes carbon dioxide-comprising solution intermediate that has collected at the bottom of the contactingzone tank 38. Theseparation feed material 24 is flowed through the contactingzone liquid material 40 upon its introduction to the contactingzone 34. In some embodiments, for example, theseparation feed material 24 is introduced to the contactingzone liquid material 40 through a sparger. - Separation of a carbon dioxide-comprising
liquid solution product 42 is effected from the intermediate operative carbon dioxide supply-comprisingmixture 32. The carbon dioxide-comprisingliquid solution product 42 includes at least a fraction of the carbon dioxide-comprising solution intermediate, and, in some embodiments, is defined by at least a fraction of the carbon dioxide-comprising solution intermediate, such that the carbon dioxide-comprisingliquid solution product 42 includes at least a fraction of the supplied exhausted carbon dioxide, and, in this respect, includes at least a fraction of the produced carbon dioxide. In this respect, the carbon dioxide of the carbon dioxide-comprisingliquid solution product 42 includes at least a fraction of the supplied exhausted carbon dioxide, and, in some embodiments, is defined by at least a fraction of the supplied exhausted carbon dioxide. Also in this respect, the carbon dioxide of the carbon dioxide-comprisingliquid solution product 42 includes at least a fraction of the produced carbon dioxide, and, in some embodiments, is defined by at least a fraction of the produced carbon dioxide. - In some embodiments, for example, the carbon dioxide-comprising
liquid solution product 42 includes the one or more other materials supplied by the separationprocess feed material 24 that are solvated (or dissolved) within the contactingzone 34 and that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - In some embodiments, for example, the carbon dioxide-comprising
liquid solution product 42 includes dissolved carbon dioxide and at least one of SOx and NOx. - In some embodiments, for example, the separation of the carbon dioxide-comprising
liquid solution product 42 from the intermediate operative carbon dioxide supply-comprisingmixture 32 includes separation by gravity separation. In some embodiments, for example, the separation is effected in the contactingzone 34. - In some embodiments, for example, the separation of the carbon dioxide-comprising
liquid solution product 42 from the intermediate operative carbon dioxide supply-comprisingmixture 32 effects separation of a gaseous contacting operation by-product 44 from the carbon dioxide-comprisingliquid solution product 42. The gaseous contacting operation by-product 44 includes at least a fraction of the carbon dioxide-depleted gaseous intermediate, and, in some embodiments, for example, is defined by at least a fraction of the carbon dioxide-depleted gaseous intermediate. - In some embodiments, for example, in parallel with the separation of the carbon dioxide-comprising
liquid solution product 42 from the intermediate operative carbon dioxide supply-comprisingmixture 32, depletion of the carbon dioxide, and, in some embodiments, of one or more other materials, from within the intermediate operative carbon dioxide supply-comprisingmixture 32 is effected, such that separation of a material depleted intermediate operative carbon dioxide supply-comprising mixture from the carbon dioxide-comprisingliquid solution product 42 is effected, wherein the material depleted intermediate operative carbon dioxide supply-comprising mixture includes the gaseous contacting operation by-product 44. In some embodiments, for example, the material depleted intermediate operative carbon dioxide supply-comprising mixture is defined by the gaseous contacting operation by-product 44. - In some embodiments, for example, the gaseous contacting operation by-
product 44 includes N2, O2, and CO. In some embodiments, for example, the gaseous contacting operation by-product 44 is discharged from the contacting tank as anexhaust 441. - In some embodiments, for example, the supplied gaseous exhaust material, either by itself or as part of the separation
process feed material 24, is cooled prior to the separation of a carbon dioxide-rich separation fraction 28 from the separationprocess feed material 24. In some embodiments, for example, the supplied gaseous exhaust material is cooled prior to supply to the contactingzone 34 so as to facilitate the solvation (or the dissolution) of the carbon dioxide. In some embodiments, for example, the cooling of the supplied gaseous exhaust material facilitates the provision of a material supply to thereaction zone 10 with a temperature that is suitable for the growth of the phototrophic biomass. In some embodiments, for example, the supplied gaseous exhaust material is disposed at a temperature of between 110 degrees Celsius and 150 degrees Celsius. In some embodiments, for example, the temperature of the supplied gaseous exhaust material is about 132 degrees Celsius. In some embodiments, the temperature at which the supplied gaseous exhaust material is disposed is much higher than this, and, in some embodiments, such as thegaseous exhaust material 14 from a steel mill, the temperature can be as high as 500 degrees Celsius. In some embodiments, for example, the cooling is effected so as to facilitate the solvation (or the dissolution) of the carbon dioxide. In some embodiments, for example, the supplied gaseous exhaust material is cooled to 50 degrees Celsius or less (in some embodiments, for example, this depends on the dew point of the water vapour within the supplied gaseous exhaust material). In some of these embodiments, in effecting the cooling of the supplied gaseous exhaust material, at least a fraction of any water vapour of the supplied gaseous exhaust material is condensed in a heat exchanger 46 (such as a condenser) and separated from the supplied gaseous exhaust material as anaqueous material 201. In some embodiments, the resultingaqueous material 201 is re-used in the process. In some embodiments, for example, the resultingaqueous material 201 is re-used as supplementalaqueous material supply 20. In some embodiments, for example, the aqueous material is supplied to the settling column 212 (described below). In some embodiments, the condensing effects heat transfer from the supplied gaseous exhaust material to aheat transfer medium 68, thereby raising the temperature of theheat transfer medium 48 to produce a heatedheat transfer medium 48, and the heatedheat transfer medium 48 is then supplied (for example, flowed) to a dryer 50 (discussed below), and heat transfer is effected from the heatedheat transfer medium 48 to a phototrophic biomass-rich intermediate product that has been derived from a discharge from the photobioreactor to effect drying of the phototrophic biomass-rich intermediate product and thereby effect production of the finalreaction zone product 52. In some embodiments, for example, after being discharged from thedryer 50, theheat transfer medium 48 is recirculated to theheat exchanger 46. Examples of a suitableheat transfer medium 48 include thermal oil and glycol solution. - Release of a gaseous carbon dioxide-rich intermediate from a carbon dioxide-comprising liquid solution feed 42A is effected. The carbon dioxide-comprising liquid solution feed 42A includes at least a fraction of the carbon dioxide-comprising
liquid solution product 42. In some embodiments, the carbon dioxide-comprising liquid solution feed 42A is defined by at least a fraction of the carbon dioxide-comprising liquid solution product. The gaseous carbon dioxide-rich intermediate includes at least a fraction of the dissolved carbon dioxide of the carbon dioxide-comprising liquid solution feed 42A. In some embodiments, for example, carbon dioxide of the gaseous carbon dioxide-rich intermediate is defined by at least a fraction of the dissolved carbon dioxide of the carbon dioxide-comprising liquid solution feed 42A. In this respect, the carbon dioxide of the gaseous carbon dioxide-rich intermediate includes at least a fraction of the supplied exhausted carbon dioxide, and, in some embodiments, is defined by at least a fraction of the supplied exhausted carbon dioxide. Also in this respect, the carbon dioxide of the gaseous carbon dioxide-rich intermediate includes at least a fraction of the produced carbon dioxide, and, in some embodiments, is defined by at least a fraction of the produced carbon dioxide. - In some embodiments, for example, the carbon dioxide-comprising liquid solution feed 42A includes the one or more other materials supplied by the separation
process feed material 24 that are solvated (or dissolved) and included within the carbon dioxide-comprisingliquid solution product 42, and that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. In this respect, in some embodiments, for example, the effected release of the gaseous carbon dioxide-rich intermediate from a carbon dioxide-comprising liquid solution feed 42A includes release of these one or more other materials. - In some embodiments, for example, the release is effected by effecting a decrease in the solubility of carbon dioxide within the carbon dioxide-comprising liquid solution feed 42A. By effecting the decrease in solubility of the carbon dioxide within the carbon dioxide-comprising liquid solution feed 42A, carbon dioxide, and, in some embodiments, one or more other materials dissolved within the carbon dioxide-comprising liquid solution feed 42A, become released from each of their respective dissolved relationships or associations from within the carbon dioxide-comprising liquid solution feed 42A. In some cases, this release, for each of these materials is characterized as “effervescence” or “coming out of solution”.
- In some embodiments, for example, the decrease in the solubility of carbon dioxide within the carbon dioxide-comprising liquid solution feed 42A is effected by effecting an increase in the temperature of the carbon dioxide-comprising liquid solution feed 42A. In some embodiments, for example, the decrease in the solubility of carbon dioxide within the carbon dioxide-comprising liquid solution feed 42A is effected by effecting a decrease in the pressure of the carbon dioxide-comprising liquid solution feed 42A.
- In some embodiments, for example, the release of the gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed 42A effects formation of a carbon dioxide-lean liquid intermediate, such that a carbon dioxide-comprising
mixture 54 is provided including the gaseous carbon dioxide-rich intermediate and the carbon dioxide-lean liquid intermediate. - In some embodiments, for example, in parallel with the release of the gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed 42A, depletion of the carbon dioxide, and, in some embodiments, of one or more materials, from the carbon dioxide-comprising liquid solution feed 42A is effected, such that formation of a material depleted carbon dioxide-comprising liquid solution feed 42A is effected, wherein the material depleted carbon dioxide-comprising liquid solution feed 42A includes the carbon dioxide-lean liquid intermediate. In some embodiments, for example, the material depleted carbon dioxide-comprising liquid solution product defines the carbon dioxide-lean liquid intermediate.
- A gaseous carbon dioxide-
rich recovery product 56 is separated from the carbon dioxide-comprisingmixture 54. The gaseous carbon dioxide-rich recovery product 56 includes at least a fraction of the gaseous carbon dioxide-rich intermediate, and, in some embodiments, is defined by at least a fraction of the gaseous carbon dioxide-rich intermediate, such that the gaseous carbon dioxide-rich recovery product 56 includes at least a fraction of the supplied exhausted carbon dioxide, and, in this respect, includes at least a fraction of the produced carbon dioxide. In this respect, the carbon dioxide of the gaseous carbon dioxide-rich recovery product 56 includes at least a fraction of the supplied exhausted carbon dioxide, and, in some embodiments, is defined by at least a fraction of the supplied exhausted carbon dioxide. Also in this respect, the carbon dioxide of the gaseous carbon dioxide-rich recovery product 56 includes at least a fraction of the produced carbon dioxide, and, in some embodiments, is defined by at least a fraction of the produced carbon dioxide. - In some embodiments, for example, the gaseous carbon dioxide-
rich recovery product 56 includes the one or more other materials supplied by the separationprocess feed material 24 that are solvated (or dissolved) and then supplied within the carbon dioxide-comprising liquid solution feed 42A, and that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - In some embodiments, for example, the gaseous carbon dioxide-rich recovery product also includes at least one of SOx and NOx In some embodiments, for example, the concentration of carbon dioxide within the carbon dioxide-
rich recovery product 56 is at least 90 volume % based on the total volume of theproduct 56. In some embodiments, for example, the gaseous carbon dioxide-rich recovery product 56 is substantially pure carbon dioxide. - In some embodiments, for example, the separation of the gaseous carbon dioxide-
rich recovery product 56 from the carbon dioxide-comprisingmixture 54 includes separation by gravity separation. In some embodiments, for example, the separation is effected in the contacting zone. - In some embodiments, for example, the separation of the gaseous carbon dioxide-
rich recovery product 56 from the carbon dioxide-comprisingmixture 54 effects separation of a carbon dioxide-leanliquid product 58 from the gaseous carbon dioxide-rich recovery product 56. The carbon dioxide-leanliquid product 58 includes at least a fraction of the carbon dioxide-lean liquid intermediate, and, in some embodiments, for example, is defined by at least a fraction of the carbon dioxide-lean liquid intermediate. - In some embodiments, for example, in parallel with the separation of the gaseous carbon dioxide-
rich recovery product 56 from the carbon dioxide-comprisingmixture 54, depletion of the carbon dioxide, and, in some embodiments, of one or more materials, from the carbon dioxide-comprisingmixture 54 is effected, such that separation of a material depleted carbon dioxide-comprising mixture from the gaseous carbon dioxide-rich recovery product 56 is effected, wherein the material depleted carbon dioxide-comprising mixture includes the carbon dioxide-leanliquid product 58. In some embodiments, for example, the material depleted carbon dioxide-comprising mixture is defined by the carbon dioxide-leanliquid product 58. - In some embodiments, for example, the carbon dioxide-lean
liquid product 58 includes carbon dioxide, and in some of these embodiments, also includes SOx and NOx, but, for each of these, in much smaller concentrations than their corresponding concentrations in the carbon dioxide-rich recovery product 56. - The carbon dioxide-
rich separation fraction 28 includes at least a fraction of the gaseous carbon dioxide-rich recovery product 56. In some embodiments, for example the carbon dioxide-rich separation fraction 28 is defined by at least a fraction of the gaseous carbon dioxide-rich recovery product 56. In this respect, as a corollary, the carbon dioxide-rich separation fraction 28 includes at least a fraction of the supplied exhausted carbon dioxide, and, in this respect, includes at least a fraction of the produced carbon dioxide. Also in this respect, as a corollary, the carbon dioxide of the carbon dioxide-rich separation 28 includes at least a fraction of the supplied exhausted carbon dioxide, and, in some embodiments, is defined by at least a fraction of the supplied exhausted carbon dioxide. Also in this respect, as a corollary, the carbon dioxide of the carbon dioxide-rich separation 28 includes at least a fraction of the produced carbon dioxide, and, in some embodiments, is defined by at least a fraction of the produced carbon dioxide. - In some embodiments, for example, the carbon dioxide-
rich separation fraction 28 includes the one or more other materials supplied by the separationprocess feed material 24 that are solvated (or dissolved), then supplied within the carbon dioxide-comprising liquid solution feed 42A, and then provided within the gaseous carbon dioxide-rich recovery product 56, and that are beneficial to the growth of the phototrophic biomass within thereaction zone 10. Examples of such materials include SOX, NOX, and NH3. - In some embodiments, for example, the carbon dioxide-comprising liquid solution feed 42A is supplied to a carbon
dioxide recovery zone 60, wherein the above-described release of the gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed 42A is effected in the carbondioxide recovery zone 60. - In some embodiments, for example, the temperature within the carbon
dioxide recovery zone 60 is higher than the temperature of the contactingzone 34, so as to effect the release of the gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed 42A. In this respect, in some embodiments, for example, the temperature within the carbondioxide recovery zone 60 is higher than the temperature within the contactingzone 34 by at least 15 degrees Celsius. In some embodiments, for example, this temperature difference is at least 20 degrees Celsius. In some embodiments, for example, this temperature difference is at least 25 degrees Celsius. In some embodiments, for example, this temperature difference is at least 30 degrees Celsius. In this respect, in those embodiments, where the operative solvation (or dissolution) agent is an aqueous material, the temperature within the carbon dioxide recovery zone is at least 17 degrees Celsius. - It is understood that the temperature within the carbon
dioxide recovery zone 60 is dependent on the temperature within the contactingzone 34, as well as on the composition of theseparation fraction 24 to be recovered. The extent of the temperature spread between the carbondioxide recovery zone 60 and the contactingzone 34 is dictated by the solubility characteristics of the materials within theseparation fraction 24 to be recovered. In order to effect the desired solvation (or dissolution) of materials within the contactingzone 34, and then effect the desired release (or effervescence) of those same materials within the carbondioxide recovery zone 60, for each of these materials, the solubility of the material within the solvent provided in the carbondioxide recovery zone 60 must be sufficiently lower than the solubility of the same material within the solvent provided in the contactingzone 34 such that meaningful recovery of such material from the separationprocess feed material 24 is effected. - In some embodiments, for example, the pressure of the carbon
dioxide recovery zone 60 is lower than the pressure of the contactingzone 34. This also effects the release of the gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed 42A. In some embodiments, for example, a vacuum is generated within the recovery zone so as to effect the release. - In some embodiments, for example, the carbon dioxide-comprising liquid solution feed 42A is supplied to a carbon
dioxide recovery zone 60 as a flow. In some embodiments, for example, the flow of the carbon dioxide-comprising liquid solution feed 42A is effected by a prime mover, such as a pump. In some embodiments, for example, flow of the carbon dioxide-comprising liquid solution feed 42A from the contactingzone 34 to the carbondioxide recovery zone 60 is effected by gravity. In some embodiments, for example, the carbon dioxide-comprising liquid solution feed 42A from the contactingzone 34 to the carbondioxide recovery zone 60 is effected by a prime mover, such as a pump, whose suction is disposed in fluid communication with the carbondioxide recovery zone 60. - In some embodiments, for example, a
heat exchanger 64 is disposed in thermal communication with the carbondioxide recovery zone 60 to effect an increase in the temperature of the carbon dioxide-comprising liquid solution feed 42A, and thereby effect a decrease in solubility of the carbon dioxide within the carbon dioxide-comprising liquid solution feed 42A. In some embodiments, for example, the carbondioxide recovery zone 60 is disposed in a carbon dioxide recovery tank 66, and theheat exchanger 64 is mounted in thermal communication with the external surface of the carbon dioxide recovery tank 66. - In some embodiments, for example, the separation of the gaseous carbon dioxide-
rich recovery product 56 from the carbon dioxide-comprisingmixture 54 is effected in the carbondioxide recovery zone 60. - In some embodiments, for example, the carbon dioxide recovery tank 66 contains a carbon dioxide recovery
zone liquid material 68 disposed within the carbondioxide recovery zone 60, and also includes aheadspace 70 disposed above the carbon dioxide recovery zone liquid material for collecting the gaseous carbon dioxide-rich recovery product 56. In some embodiments, for example, the carbon dioxide recoveryzone liquid material 68 includes a vertical extent of at least three (3) feet. In some embodiments, for example, the vertical extent is at least ten (10) feet. In some embodiments, for example, this vertical extent is between ten (10) and twenty (20) feet. In some embodiments, for example, sufficient volume of carbon dioxide recoveryzone liquid material 68 is provided, and co-operates with a disposition of the outlet for discharging theliquid material 68, such that sufficient residence time is provided within the carbondioxide recovery zone 60 for effecting the desired release and separation of carbon dioxide from theliquid material 68 prior to discharge of theliquid material 68 from the carbondioxide recovery zone 60. The carbon dioxide recoveryzone liquid material 68 includes the material depleted carbon dioxide-comprising liquid solution product. In some embodiments, for example, the carbon dioxide recoveryzone liquid material 68 includes a fraction of the carbon dioxide-comprising liquid solution feed 42A from which carbon dioxide, and, in some embodiments, one or more other materials, have not been separated. In some embodiments, for example, the carbon dioxide-comprising liquid solution feed 42A is supplied to the carbondioxide recovery zone 60 by introduction into a lower portion of the carbon dioxide recoveryzone liquid material 68, and is heated by heat that is thermally communicated to the carbon dioxide recoveryzone liquid material 68 from in and around the lower portion of the carbon dioxide recoveryzone liquid material 68. - In some embodiments, for example, the gaseous carbon dioxide-
rich recovery product 58 is discharged from the carbon dioxide recovery tank 66. In some embodiments, for example, the discharge of the gaseous carbon dioxide-rich recovery product 66 from theheadspace 70 of the carbon dioxide recovery tank 66 is effected with a vacuum. In some embodiments, for example, a vacuum generated is such that the pressure within the headspace is between 10 and 14.7 psia, and is also lower than the pressure in the contactingzone 34. In some embodiments, for example, the vacuum is generated by a prime mover or eductor that is fluidly coupled to the headspace for effecting supply of at least a fraction of the gaseous carbon dioxide-rich recovery product 58 to thereaction zone 10 from the carbon dioxide recovery tank 66. - In some embodiments, for example, the carbon dioxide recovery
zone liquid material 68 is discharged from the carbondioxide recovery zone 60. In some embodiments, the carbon dioxide recoveryzone liquid material 68 is discharged from the carbondioxide recovery zone 60 through an outlet of the carbon dioxide recovery tank 66 disposed proximate to the upper level of the carbon dioxide recoveryzone liquid material 68 within the carbon dioxide recovery tank 66. In some embodiments, for example, the outlet is vertically displaced from the upper level ofliquid material 68 no further than 25% of the vertical extent of the liquid material disposed within therecovery zone 60. In some embodiments, for example, the outlet is vertically displaced from the upper level ofliquid material 68 no further than 15% of the vertical extent of the liquid material disposed within therecovery zone 60. In some embodiments, for example, the outlet is vertically displaced from the upper level ofliquid material 68 no further than 10% of the vertical extent of the liquid material disposed within therecovery zone 60. Amongst other things, this mitigates against short-circuiting of therecovery zone 60 by the material supplied by the carbon dioxide-comprising liquid solution feed 42A, which would effectively reduce the residence time of this supplied material within the carbondioxide recovery zone 60, and thereby decreases the proportion of carbon dioxide that undergoes the above-described release from solution and becomes separated from theliquid material 68 before being discharged from the outlet of the tank 66. As well, in some embodiments, for example, theliquid material 68 disposed closer to the upper level is warmer than the liquid material disposed closer to the bottom of therecovery zone 60, and carbon dioxide is less likely to be in solution in theliquid material 68 disposed closer to the upper level relative to the liquid material disposed closer to the bottom of therecovery zone 60, thereby further reinforcing the desirability of having the discharge effected closer to the upper level of theliquid material 68 within the tank 66. In some embodiment, for example, the discharged carbon dioxide recoveryzone liquid material 68 is recycled to provide at least a fraction of the operative solvation (or dissolution)agent 30 to the contactingzone 34. In some embodiments, prior to being introduced into the contactingzone 34, the discharged carbon dioxide recoveryzone liquid material 68 is cooled so as to effect a reduction in temperature of the discharged carbon dioxide recoveryzone liquid material 68 and thereby render it suitable for use as at least a fraction of the operative solvation (or dissolution)agent 30 being supplied to the contactingzone 34. In this respect, in some embodiments, for example, the discharged carbon dioxide recoveryzone liquid material 68 is flowed through achiller 72 for effecting the reduction in temperature. - In some embodiments, for example, when the carbon dioxide recovery tank 66 is of a relatively wider dimension, the disposition of the outlet relative to the upper level of
liquid material 68 is not as critical, so long as the carbon dioxide-comprising liquid solution feed 42A is supplied to the carbon dioxide recovery tank 66 through an inlet that is disposed substantially opposite relative to the outlet, as sufficient residence time is more likely to be realized in such a configuration. - In some embodiments, for example, the
chiller 72 is thermally coupled to theheat exchanger 64 with a heat transfer loop that is based on a refrigeration circuit (commercially available) that extracts heat from the relatively warmer discharged carbon dioxide recoveryzone liquid material 68 flowing through the chiller to reduce its temperature (for example, to three (3) degrees Celsius) to maximize the solubility equilibrium of the soluble gases in the separationprocess feed material 24. The heat extracted from the discharged carbon dioxide recoveryzone liquid material 68 is returned to thecarbon dioxide recovery 60, to have the inverse effect and allow the dissolved gases in the carbon dioxide-comprising liquid solution feed 42A to escape into theheadspace 70 by increasing the temperature of the carbon dioxide-comprising liquid solution feed 42A, and thereby decreasing the solubility of the gases that have been previously solvated (or dissolved). - At least a fraction of the carbon dioxide-
rich product material 26 is supplied to thereaction zone 10 as a carbon dioxide-rich product material supply. The reactionzone feed material 80, being introduced to the reaction zone, includes the carbon dioxide-rich product material supply. In this respect, the reactionzone feed material 80 includes at least a fraction of the carbon dioxide-rich product material 26. In some embodiments, for example, the reactionzone feed material 80 is defined by at least a fraction of the carbon dioxide-rich product material 26. In this respect, as a corollary, the reaction zone feed material includes carbon dioxide of the carbon dioxide-rich product material 26. As such, the reactionzone feed material 80 includes at least a fraction of the supplied exhausted carbon dioxide, and, in this respect, includes at least a fraction of the produced carbon dioxide. As a further corollary, the carbon dioxide of the reaction zone feed material includes at least a fraction of the supplied exhausted carbon dioxide, and, in this respect, includes at least a fraction of the produced carbon dioxide. In some embodiments, for example, the carbon dioxide of this reactionzone feed material 80 is defined by at least a fraction of the supplied exhausted carbon dioxide, and, in this respect, is defined by the produced carbon dioxide. - In some of these embodiments, for example, introduction of the reaction
zone feed material 80 to thereaction zone 10 is effected while thegaseous exhaust material 14 is being discharged by the gaseous exhaustmaterial producing process 16. - In some embodiments, for example, the pressure of the carbon dioxide-rich product material supply is increased before being supplied to the
reaction zone 10. In some embodiments, for example, the pressure increase is at least partially effected by aprime mover 76. For those embodiments where the carbon dioxide-richproduct material supply 26 is disposed within a liquid-comprising material, a suitableprime mover 76 is, for example, a pump. For those embodiments where the carbon dioxide-rich product material supply is disposed within a gaseous material, suitableprime movers 76 include, for example, blowers, compressors, and air pumps. In other embodiments, for example, the pressure increase is effected by a jet pump or eductor. - With respect to such embodiments, where the pressure increase is effected by a jet pump or eductor, in some of these embodiments, for example, the carbon dioxide-rich product material supply is supplied to the jet pump or eductor and pressure energy is transferred to the reaction zone carbon dioxide feed material from another flowing fluid (the “motive fluid flow”) using the venturi effect to effect a pressure increase in the carbon dioxide-rich product material supply. In this respect, in some embodiments, for example, and referring to
FIG. 2 , amotive fluid flow 100 is provided, wherein material of themotive fluid flow 100 includes a motive fluid pressure PM1. In this respect also, a lower pressure state reaction zone feed-comprisingmaterial 300 is provided including a pressure PE, wherein the lower pressure state reaction zonefeed comprising material 300 includes the carbon dioxide-rich product material supply. In some embodiments, the lower pressure state reaction zone feed-comprising material is defined by the carbon dioxide-rich product material supply. PM1 of the motive fluid flow is greater than PE of the lower pressure state reaction zone feed-comprising material. Pressure of themotive fluid flow 100 is reduced from PM1 to PM2, such that Pm2 is less than PE, by flowing themotive fluid flow 100 from an upstreamfluid passage portion 102 to an intermediate downstreamfluid passage portion 104. The intermediate downstreamfluid passage portion 104 is characterized by a smaller cross-sectional area relative to the upstreamfluid passage portion 102. By flowing the motive fluid flow from the upstreamfluid passage portion 102 to the intermediate downstreamfluid passage portion 104, static pressure energy is converted to kinetic energy. When the pressure of themotive fluid flow 100 has becomes reduced to PM2, fluid communication between themotive fluid flow 100 and the lower pressure state reaction zone feed-comprisingmaterial 300 is effected such that the lower pressure state reaction zone feed-comprisingmaterial 300 is induced to mix with themotive fluid flow 100 in the intermediate downstreamfluid passage portion 104, in response to the pressure differential between the lower pressure state reaction zone feed-comprisingmaterial 300 and themotive fluid flow 100, to produce an intermediate reaction zone feed-comprisingmaterial 302 which includes the carbon dioxide-rich product material supply. Pressure of the intermediate reaction zone feed-comprisingmaterial 302, which includes the carbon dioxide-rich product material supply, is increased to PM3, such that the pressure of the carbon dioxide-rich product material supply is also increased to PM3. PM3 is greater than PE and is also sufficient to effect supply of the carbon dioxide-rich product material supply to thereaction zone 10 and, upon supply of the carbon dioxide-rich product material supply to thereaction zone 10 as at least a fraction of the reactionzone feed material 80, effect flow of the carbon dioxide-rich product material supply through a vertical extent of reaction mixture within thereaction zone 10 of at least a seventy (70) inches. In some embodiments, for example, PM3 is greater than PE and is also sufficient to effect supply of the carbon dioxide-rich product material supply to thereaction zone 10 and, upon supply of the carbon dioxide-rich product material supply to thereaction zone 10, effect flow of the carbon dioxide-rich product material supply through a vertical extent of reaction mixture within thereaction zone 10 of at least 10 feet. In some embodiments, for example, PM3 is greater than PE and is also sufficient to effect supply of the carbon dioxide-rich product material supply to thereaction zone 10 and, upon supply of the carbon dioxide-rich product material supply to thereaction zone 10, effect flow of the carbon dioxide-rich product material supply through a vertical extent of reaction mixture within thereaction zone 10 of at least 20 feet. In some embodiments, for example, PM3 is greater than PE and is also sufficient to effect supply of the carbon dioxide-rich product material supply to thereaction zone 10 and, upon supply of the carbon dioxide-rich product material supply to thereaction zone 10, effect flow of the carbon dioxide-rich product material supply through a vertical extent of reaction mixture within thereaction zone 10 of at least 30 feet. In any of these embodiments, the pressure increase is designed to overcome the fluid head within thereaction zone 10. The pressure increase is effected by flowing the intermediate reaction zone feed-comprisingmaterial 302 from the intermediate downstreamfluid passage portion 104 to a “kinetic energy to static pressure energy conversion” downstreamfluid passage portion 106. The cross-sectional area of the “kinetic energy to static pressure energy conversion” downstreamfluid passage portion 106 is greater than the cross-sectional area of the intermediate downstreamfluid passage portion 104, such that kinetic energy of the intermediate reaction zone feed-comprisingmaterial 302 disposed in the intermediate downstreamfluid passage portion 104 is converted into static pressure energy when the intermediate reaction zone feed-comprisingmaterial 302 becomes disposed in the “kinetic energy to static pressure energy conversion” downstreamfluid passage portion 106 by virtue of the fact that the intermediate reaction zone feed-comprisingmaterial 302 has become flowed to a fluid passage portion with a larger cross-sectional area. In some embodiments, for example, a converging nozzle portion of a fluid passage defines the upstreamfluid passage portion 102 and a diverging nozzle portion of the fluid passage defines the “kinetic energy to static pressure energy conversion” downstreamfluid passage portion 106, and the intermediate downstreamfluid passage portion 104 is disposed intermediate of the converging and diverging nozzle portions. In some embodiments, for example, the combination of the upstreamfluid passage portion 102 and the “kinetic energy to static pressure energy conversion” downstreamfluid passage portion 106 is defined by a venture nozzle. In some embodiments, for example, the combination of the upstreamfluid passage portion 102 and the “kinetic energy to static pressure energy conversion” downstreamfluid passage portion 106 is disposed within an eductor or jet pump. In some of these embodiments, for example, the motive fluid flow includes liquid aqueous material and, in this respect, the intermediate reaction zone feed-comprisingmaterial 302 includes a combination of liquid and gaseous material, and includes the carbon dioxide-rich product material supply. In this respect, in some embodiments, for example, the intermediate reaction zone feed-comprisingmaterial 302 includes a dispersion of a gaseous material within a liquid material, wherein the dispersion of a gaseous material includes the carbon dioxide-rich product material supply. Alternatively, in some of these embodiments, for example, the motive fluid flow is another gaseous flow, such as an air flow, and the intermediate reaction zone feed-comprisingmaterial 302 is gaseous. After pressure of the intermediate reaction zone feed-comprising material has been increased to PM3, the supply of the carbon dioxide-rich product material by the intermediate reaction zone feed-comprisingmaterial 302 to the reactionzone feed material 80 is effected. - The reaction mixture disposed in the
reaction zone 10 is exposed to photosynthetically active light radiation so as to effect photosynthesis. The photosynthesis effects growth of the phototrophic biomass. - In some embodiments, for example, the light radiation is characterized by a wavelength of between 400-700 nm. In some embodiments, for example, the light radiation is in the form of natural sunlight. In some embodiments, for example, the light radiation is provided by an artificial light source. In some embodiments, for example, light radiation includes natural sunlight and artificial light.
- In some embodiments, for example, the intensity of the provided light is controlled so as to align with the desired growth rate of the phototrophic biomass in the
reaction zone 10. In some embodiments, regulation of the intensity of the provided light is based on measurements of the growth rate of the phototrophic biomass in thereaction zone 10. In some embodiments, regulation of the intensity of the provided light is based on the molar rate of supply of carbon dioxide to the reactionzone feed material 80. - In some embodiments, for example, the light is provided at pre-determined wavelengths, depending on the conditions of the
reaction zone 10. Having said that, generally, the light is provided in a blue light source to red light source ratio of 1:4. This ratio varies depending on the phototrophic organism being used. As well, this ratio may vary when attempting to simulate daily cycles. For example, to simulate dawn or dusk, more red light is provided, and to simulate mid-day condition, more blue light is provided. Further, this ratio may be varied to simulate artificial recovery cycles by providing more blue light. - It has been found that blue light stimulates algae cells to rebuild internal structures that may become damaged after a period of significant growth, while red light promotes algae growth. Also, it has been found that omitting green light from the spectrum allows algae to continue growing in the
reaction zone 10 even beyond what has previously been identified as its “saturation point” in water, so long as sufficient carbon dioxide and, in some embodiments, other nutrients, are supplied. - With respect to artificial light sources, for example, a suitable artificial
light source 14 includes submersible fiber optics, light-emitting diodes, LED strips and fluorescent lights. Any LED strips known in the art can be adapted for use in the process. In the case of the submersible LEDs, the design includes the use of solar powered batteries to supply the electricity. In the case of the submersible LEDs, in some embodiments, for example, energy sources include alternative energy sources, such as wind, photovoltaic cells, fuel cells, etc. to supply electricity to the LEDs. - With respect to those embodiments where the
reaction zone 10 is disposed in aphotobioreactor 12 which includes a tank, in some of these embodiments, for example, the light energy is provided from a combination of sources, as follows. Naturallight source 16 in the form of solar light is captured though solar collectors and filtered with custom mirrors that effect the provision of light of desired wavelengths to thereaction zone 10. The filtered light from the solar collectors is then transmitted through light guides or fiber optic materials into thephotobioreactor 12, where it becomes dispersed within thereaction zone 10. In some embodiments, in addition to solar light, the light tubes in thephotobioreactor 12 contains high power LED arrays that can provide light at specific wavelengths to either complement solar light, as necessary, or to provide all of the necessary light to thereaction zone 10 during periods of darkness (for example, at night). In some embodiments, with respect to the light guides, for example, a transparent heat transfer medium (such as a glycol solution) is circulated through light guides within thephotobioreactor 12 so as to regulate the temperature in the light guides and, in some circumstances, provide for the controlled dissipation of heat from the light guides and into thereaction zone 10. In some embodiments, for example, the LED power requirements can be predicted and, therefore, controlled, based on trends observed with respect to thegaseous exhaust material 18, as these observed trends assist in predicting future growth rate of the phototrophic biomass. - In some embodiments, the exposing of the reaction mixture to photosynthetically active light radiation is effected while the supplying of the reaction zone carbon dioxide feed material is being effected.
- In some embodiments, for example, the growth rate of the phototrophic biomass is dictated by the available reaction zone carbon dioxide supply material. In turn, this defines the nutrient, water, and light intensity requirements to maximize phototrophic biomass growth rate. In some embodiments, for example, a controller, e.g. a computer-implemented system, is provided to be used to monitor and control the operation of the various components of the process disclosed herein, including lights, valves, sensors, blowers, fans, dampers, pumps, etc.
- Reaction zone product is discharged from the reaction zone. The reaction zone product includes phototrophic biomass-comprising
product 58. In some embodiments, for example, the phototrophic biomass-comprisingproduct 58 includes at least a fraction of the contents of thereaction zone 10. In this respect, the discharge of the reaction zone product effects harvesting of thephototrophic biomass 202. In some embodiments, for example, the reaction zone product also includes a reaction zonegaseous effluent product 204 that is discharged within theexhaust 441. - In some embodiments, for example, the harvesting of the phototrophic biomass is effected by discharging the
phototrophic biomass 58 from the reaction zone. - In some embodiments, for example, the discharging of the
phototrophic biomass 58 from thereaction zone 10 is effected by displacement. In some of these embodiments, for example, the displacement is effected by supply supplementalaqueous material supply 20 to thereaction zone 10. In some of these embodiments, for example, the displacement is an overflow. In some embodiments, for example, the discharging of thephototrophic biomass 58 from thereaction zone 10 is effected by gravity. In some embodiments, for example, the discharging of thephototrophic biomass 58 from thereaction zone 10 is effected by a prime mover that is fluidly coupled to thereaction zone 10. - In some embodiments, for example, the discharge of the phototrophic biomass-comprising
product 202 is effected through an outlet extending from the reaction mixture within thereaction zone 10 at a vertical level of the reaction mixture that defines less than 50% of the vertical extent of the reaction mixture within thereaction zone 10. In some embodiments, for example, the outlet extends from the reaction mixture within the reaction zone at a vertical level of the reaction mixture that defines less than 25% of the vertical extent of the reaction mixture within thereaction zone 10. In some embodiments, for example, the outlet extends from the reaction mixture within the reaction zone at a vertical level of the reaction mixture that defines less than 10% of the vertical extent of the reaction mixture within thereaction zone 10. In some embodiments, for example, the outlet extends from the reaction mixture within the reaction zone at a vertical level of the reaction mixture that defines less than 5% of the vertical extent of the reaction mixture within thereaction zone 10. In some embodiments, for example, the outlet extends from the vertically lowermost portion of the reaction mixture within thereaction zone 10. In some of these embodiments, for example, the discharging of the phototrophic biomass-comprisingproduct 202 is effected by gravity. In some of these embodiments, for example, a prime mover, such as a pump, is fluidly coupled to the outlet to effect the discharge of thephototrophic biomass product 202 from thereaction zone 10. In some embodiments, for example, a rotary air lock valve (which also functions as a prime mover) is disposed at the outlet to effect the discharge of thephototrophic biomass product 202 from thereaction zone 10. - In some embodiments, for example, the molar rate of discharge of the
product 202 is controlled through the molar rate of supply of supplemental aqueous material supply, which influences the displacement from thephotobioreactor 12 of the phototrophic biomass-comprisingproduct 202 from an outlet of thephotobioreactor 12. For example, an overflow of an upper portion of phototrophic biomass suspension in thereaction zone 10 from the photobioreactor 12 (for example, the phototrophic biomass is discharged through an overflow port of the photobioreactor 12) is effected by this displacement to provide the phototrophic biomass-comprisingproduct 202. In some embodiments, for example, the discharging of theproduct 202 is controlled with a prime mover (such as a pump) fluidly coupled to an outlet of thephotobioreactor 12. - The phototrophic biomass-comprising
product 202 includes water. In some embodiments, for example, the phototrophic biomass-comprisingproduct 202 is supplied to a separator system for effecting removal of at least a fraction of the water from the phototrophic biomass-comprisingproduct 202 to effect production of an intermediate concentrated phototrophic biomass-comprising product (e.g., 208) and a recovered aqueous material 210 (generally, water). In some embodiments, the recoveredaqueous material 210 re-used by the process. - In some embodiments, for example, the separator system includes a
settling column 212, adecanter 214, and adryer 50. - In some embodiments, for example, the discharged phototrophic biomass-comprising product is supplied to the
settling column 212 under a motive force, such as that supplied by a pump. In some embodiments, for example,flocculant 216 is added so as to facilitate settling of the phototrophic biomass within thesettling column 212. In some embodiments, for example, the molar rate of supply of flocculant to the phototrophic biomass-comprising product is modulated based on the molar rate of supply of the phototrophic biomass of the phototrophic biomass-comprising product 202 (which, for example, can be determined by sensing molar concentration of phototrophic biomass within the phototrophic biomass-comprisingproduct 202 in combination with the detection of the molar rate of flow of the phototrophic biomass-comprisingproduct 202 being supplied to the settling column 212) to thesettling column 212. In some embodiments,aqueous material 201, which has condensed from theheat exchanger 46, as well as the aqueous material 2141 which has been separated from the decanter 214 (see below), is also supplied to thesettling column 212 so as to effect their re-use as the supplementalaqueous material supply 20. In some embodiments, for example, liquid level is controlled within the settling column so as to provide sufficient residence time to effect the desired settling of a phototrophic biomass-rich firstintermediate product 208. In this respect, in some embodiments, for example, upon determination that a detected liquid level in thesettling column 201 is below a predetermined minimum liquid level, water from a municipal water supply is supplied to the settling column to effect an increase to the liquid level, such as by effecting opening of avalve 213. Separation of the phototrophic biomass-rich firstintermediate product 208 from an aqueous liquidoverhead product 210 is effected by gravity settling in the settling column. In some embodiments, for example, the aqueous liquidoverhead product 210 is returned to thephotobioreactor 12 as the supplementalaqueous material supply 20 for re-use. In some embodiments, for example, the supplemental nutrient supply is added to the supplementalaqueous material supply 20 prior to supply to the photobioreactor. In some embodiments, for example, the molar rate of supply of the supplementalaqueous material supply 20 to thephotobioreactor 12 is modulated based on a detected molar rate of flow of the carbon dioxide-rich product material 26 to thereaction zone 10. - In some embodiments, for example, a level sensor is provided to detect the level of the reaction mixture within the
reaction zone 10, and transmit a signal representative of the detected level to a controller. The controller compares the received signal to a predetermined level value. If the received signal is less than the predetermined level value, the controller responds by effecting initiation of supply, or an increase to the molar rate of supply, of the supplementalaqueous material supply 20 to thereaction zone 10, such as by opening (in the case of initiation of supply), or increasing the opening (in the case of increasing the molar rate of supply), of a valve configured to interfere with the supply of the supplementalaqueous material supply 20 to thereaction zone 10. If the received signal is greater than the predetermined level value, the controller responds by effecting a decrease to the molar rate of supply, or termination of supply, of the supplementalaqueous material supply 20 to thereaction zone 10, such as by decreasing the opening of (in the case of decreasing the molar rate of supply), or closing the valve (in the case of terminating the supply) that is configured to interfere with the supply of the supplementalaqueous material supply 20 to thereaction zone 10. In some embodiments, for example, by regulating the supplying of the supplementalaqueous material supply 20 to thereaction zone 10 so as to effect the maintaining of a desired level within thereaction zone 10, make-up water is supplied to thereaction zone 10 to replace water that is discharged with the phototrophic biomass-comprisingproduct 202 with a view to maintaining steady state conditions within thereaction zone 10. - In some embodiments, for example, while growth of the phototrophic biomass is being effected within the reaction mixture disposed within the
reaction zone 10 and exposed to the photosynthetically active light radiation, discharge of the phototrophic biomass from thereaction zone 10 is effected at a molar rate of discharge that is equivalent to, or substantially equivalent to, a predetermined molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. The growth of the phototrophic biomass includes growth effected by photosynthesis. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is at least 90% of the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass within thereaction zone 10 is at least 95% of the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is at least 99% of the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is equivalent to the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the discharging of thephototrophic biomass 58 from thereaction zone 10 is effected by displacement. In some of these embodiments, for example, the displacement is effected by supplying supplementalaqueous material supply 20 to thereaction zone 10. In some of these embodiments, for example, the displacement is an overflow. In some embodiments, for example, the discharging of thephototrophic biomass 58 from thereaction zone 10 is effected by gravity. In some embodiments, for example, the discharging of thephototrophic biomass 58 from thereaction zone 10 is effected by a prime mover that is fluidly coupled to thereaction zone 10. - In some embodiments, for example, while growth of the phototrophic biomass is being effected within the reaction mixture disposed within the
reaction zone 10 and exposed to the photosynthetically active light radiation, the molar rate of discharge of the phototrophic biomass from thereaction zone 10 is modulated in response to detection of a difference between a phototrophic biomass growth indicator, detected from within thereaction zone 10, and a predetermined phototrophic biomass growth indicator value. The predetermined phototrophic biomass growth indicator value is correlated with a predetermined molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is based on the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is at least 90% of the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is at least 95% of the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass within the reaction mixture is at least 99% of the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass is equivalent to the maximum molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. In some embodiments, for example, the phototrophic biomass growth indicator is a molar concentration of phototrophic biomass. In some embodiments, for example, the predetermined molar rate of growth of phototrophic biomass, with which the predetermined phototrophic biomass growth indicator value is correlated, is based upon a rate of increase in molar concentration of phototrophic biomass within thereaction zone 10 effected by growth of the phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation. - In some embodiments, for example, while the modulating of the molar rate of discharge of the phototrophic biomass from the
reaction zone 10 is being effected, the volume of the reaction mixture disposed within the reaction zone is maintained constant or substantially constant for a time period of at least one (1) hour. In some embodiments, for example, the time period is at least six (6) hours. In some embodiments, for example, the time period is at least 24 hours. In some embodiments, for example, the time period is at least seven (7) days. In some embodiments, for example, while the modulating is being effected, the volume of the reaction mixture disposed within the reaction zone is maintained constant or substantially constant for the a period of time such that the predetermined phototrophic biomass growth indicator value, as well as the predetermined molar rate of growth of phototrophic biomass, is maintained constant or substantially constant during this period, with a view to optimizing economic efficiency of the process. - In some embodiments, for example, while the modulating of the molar rate of discharge of the phototrophic biomass from the
reaction zone 10 is being effected, the process further includes modulating the molar rate of supply of the supplemental nutrient supply to the reaction zone in response to the detection of a difference between a detected molar concentration of one or more nutrients (e.g., NO3) within thereaction zone 10 and a corresponding predetermined target molar concentration value. In some embodiments, for example, the molar rate of supply of the supplemental nutrient supply to thereaction zone 10 is modulated in response to a detected change in the molar rate of supply of the carbon dioxide-rich product material 26 to thereaction zone 10. - In some embodiments, for example, while the modulating of the molar rate of discharge of the phototrophic biomass from the
reaction zone 10 is being effected, the process further includes modulating the molar rate of supply of the carbon dioxide-rich product material 26 to thereaction zone 10 based on at least one carbon dioxide processing capacity indicator. In some embodiments, for example, the detection of at least one of the at least one carbon dioxide processing capacity indicator is effected in thereaction zone 10. The carbon dioxide processing capacity indicator which is detected is any characteristic that is representative of the capacity of thereaction zone 10 for receiving carbon dioxide and having at least a fraction of the received carbon dioxide converted in a photosynthesis reaction effected by phototrophic biomass disposed within the reaction zone. In some embodiments, for example, the carbon dioxide processing capacity indicator is a pH within thereaction zone 10. In some embodiments, for example, the carbon dioxide processing capacity indicator is a phototrophic biomass molar concentration within thereaction zone 10. - In some embodiments, for example, while the modulating of the molar rate of discharge of the phototrophic biomass from the
reaction zone 10 is being effected, the process further includes modulating the intensity of the photosynthetically active light radiation to which the reaction mixture is exposed to, in response to a detected change in the molar rate at which the carbon dioxide-rich product material 26 is being supplied to thereaction zone 10. - In some embodiments, for example, and as described above, the discharge of the phototrophic biomass from the
reaction zone 10 is effected by a prime mover, such as a pump. In this respect, in some embodiments, for example, the modulating of the molar rate of discharge of the phototrophic biomass from the reaction zone includes: - (i) modulating the power supplied to the prime mover effecting the discharge of the phototrophic biomass from the
reaction zone 10 in response to detection of a difference between a detected phototrophic biomass growth indicator, within the reaction mixture disposed within the reaction zone, and a predetermined phototrophic biomass growth indicator value, wherein the predetermined phototrophic biomass growth indicator target value is correlated with a predetermined molar rate of growth of phototrophic biomass within the reaction mixture which is disposed within thereaction zone 10 and is being exposed to the photosynthetically active light radiation, and; - (ii) while the modulating of the power supplied to the prime mover is being effected, modulating the molar rate of supply of the supplemental
aqueous material supply 20 to thereaction zone 10 in response to detection of a difference between a detected indication of volume of reaction mixture within the reaction zone and a predetermined reaction mixture volume indication value, wherein the predetermined reaction mixture volume indication value is representative of a volume of reaction mixture within thereaction zone 10 within which growth of the phototrophic biomass is effected within the reaction mixture at the predetermined molar rate of growth of phototrophic biomass while the phototrophic biomass growth indicator, within the reaction mixture, is disposed at the predetermined phototrophic biomass growth indicator target value. - In some of these embodiments, for example, the predetermined molar rate of growth of the phototrophic biomass is based upon the maximum molar rate of growth of the phototrophic biomass within the reaction mixture which is disposed within the
reaction zone 10 and is being exposed to the photosynthetically active light radiation, as described above. - In some embodiments, for example, the phototrophic biomass growth indicator is a molar concentration of phototrophic biomass.
- In some embodiments, for example, the indication of volume of reaction mixture within the reaction zone 10 (or, simply, the “reaction mixture volume indication”) is an upper liquid level of the reaction mixture within the
reaction zone 10. In some embodiments, for example, this upper liquid level is detected with a level sensor, as described above. - The phototrophic biomass-rich first
intermediate product 208 is supplied to thedecanter 214 to further effect dewatering of the phototrophic biomass and effect separation from the phototrophic biomass-rich firstintermediate product 208 of a phototrophic biomass-rich secondintermediate product 218 andaqueous product 2181. In some embodiments, for example, the supply of the phototrophic biomass-rich firstintermediate product 208 to thedecanter 214 is modulated based on the detected concentration of phototrophic biomass within the phototrophic biomass-rich firstintermediate product 208. In such embodiments, the phototrophic biomass-rich firstintermediate product 208 is supplied to thedecanter 214 when the concentration of phototrophic biomass within the phototrophic biomass-rich firstintermediate product 208 is above a predetermined concentration. In some embodiments, for example, the supply of theproduct 208 to thedecanter 214 is controlled by avalve 215 that responds to a signal from a controller upon the determination of a deviation of the detected phototrophic biomass concentration within the phototrophic biomass-rich first intermediate product from a predetermined value. In some embodiments, for example, the motor speed of the decanter is controlled by a variable frequency drive, also in response to a signal from a controller upon the determination of a deviation of the detected phototrophic biomass concentration within the phototrophic biomass-rich first intermediate product from a predetermined value. Thedecanter 214 effects separation of theaqueous product 2181 and the phototrophic biomass-rich secondintermediate product 218 from the phototrophic biomass-rich firstintermediate product 214. Theaqueous product 2181 is supplied to thesettling column 212. The phototrophic biomass-rich secondintermediate product 218 is discharged from thedecanter 214 and supplied to thedryer 50 which supplies heat to the phototrophic biomass-rich secondintermediate product 218 to effect evaporation of at least a fraction of the water of the phototrophic biomass-rich secondintermediate product 218, and thereby effect production of a final phototrophic biomass-comprising product. As discussed above, in some embodiments, the heat supplied to the intermediate concentrated phototrophic biomass-comprisingproduct 218 is provided by a heat transfer medium which has been used to effect the cooling of the supplied exhaust gas prior to supply of the supplied exhaust gas to the contacting zone. By effecting such cooling, heat is transferred from the supplied exhaust gas to the heat transfer medium, thereby raising the temperature of the heat transfer medium. In such embodiments, the heat requirement to effect evaporation of water from the phototrophic biomass-rich second intermediate product is not significant, thereby rendering it feasible to use the heated heat transfer medium as a source of heat to effect the drying of the phototrophic biomass-rich second intermediate product. After heating the phototrophic biomass-rich second intermediate product, the heat transfer medium, having lost some energy and becoming disposed at a lower temperature, is recirculated to the heat exchanger to effect cooling of the supplied exhaust gas. The heating requirements of thedryer 50 is based upon the rate of supply of the phototrophic biomass-rich second intermediate product to thedryer 50. Cooling requirements (of the heat exchanger) and heating requirements (of the dryer 50) are adjusted by the controller to balance the two operations by monitoring flow rates and temperatures of each of the supplied exhaust gas and the rate of production of theproduct 202 through discharging of theproduct 202 from thephotobioreactor 12. - While this invention has been described with reference to illustrative embodiments and examples, the description is not intended to be construed in a limiting sense. Thus, various modifications of the illustrative embodiments, as well as other embodiments of the invention, will be apparent to persons skilled in the art upon reference to this description. It is therefore contemplated that the appended claims will cover any such modifications or embodiments. Further, all of the claims are hereby incorporated by reference into the description of the preferred embodiments.
Claims (21)
1. A process for growing a phototrophic biomass in a reaction zone comprising:
treating an operative carbon dioxide supply-comprising gaseous material feed so as to effect production of a carbon dioxide-rich product material wherein the carbon dioxide concentration of the carbon dioxide-rich product material is greater than the carbon dioxide concentration of the operative carbon dioxide supply-comprising gaseous material feed, wherein production of at least a fraction of the operative carbon dioxide supply-comprising gaseous material feed is effected by a gaseous exhaust material producing process; and
supplying at least a fraction of the carbon dioxide-rich product material to the reaction zone so as to effect growth of the phototrophic biomass by photosynthesis in the reaction zone.
2. The process of claim 1 , wherein the treating of the operative carbon dioxide supply-comprising gaseous material feed includes effecting separation, from a separation process feed material, of a carbon dioxide-rich separation fraction;
wherein the separation process feed material is defined by at least a fraction of the operative carbon dioxide supply-comprising gaseous material feed; and
wherein the carbon dioxide-rich product material includes the carbon dioxide-rich separation fraction.
3. The process of claim 2 , wherein the ratio of [moles of carbon dioxide within the carbon dioxide-rich separation fraction] to [moles of the one or more other materials of the separation process feed material within the carbon dioxide-rich separation fraction] is greater than the ratio of [moles of carbon dioxide within the separation process feed material] to [moles of the one or more other materials of the separation process feed material within the separation process feed material].
4. The process of claim 3 , wherein the effecting separation, from a separation process feed material, of a carbon dioxide-rich separation fraction, includes:
effecting dissolution of at least a fraction of the carbon dioxide of the separation process feed material so as to effect production of a carbon dioxide-comprising liquid solution product including dissolved carbon dioxide;
effecting release of a gaseous carbon dioxide-rich intermediate from a carbon dioxide-comprising liquid solution product feed such that a carbon dioxide-comprising mixture is provided including the gaseous carbon dioxide-rich intermediate, wherein the carbon dioxide-comprising liquid solution feed includes at least a fraction of the carbon dioxide-comprising liquid solution product, wherein the gaseous carbon dioxide-rich intermediate includes at least a fraction of the dissolved carbon dioxide of the carbon dioxide-comprising liquid solution product; and
separating a gaseous carbon dioxide-rich recovery product from the gaseous carbon dioxide-rich intermediate, wherein the carbon dioxide separation fraction includes at least a fraction of the gaseous carbon dioxide-rich recovery product.
5. The process of claim 4 , wherein the effecting release of a gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed includes effecting release of at least a fraction of the dissolved carbon dioxide from the carbon dioxide-comprising liquid solution feed.
6. The process of claim 5 , wherein the effecting release of at least a fraction of the dissolved carbon dioxide from the carbon dioxide-comprising liquid solution feed includes effecting an increase in temperature of the carbon dioxide-comprising liquid solution feed.
7. The process of claim 4 , wherein the effecting dissolution includes effecting dissolution by contacting the separation process feed material with an operative dissolution agent within a contacting zone.
8. The process of claim 7 , wherein the one or more other materials of the separation process feed material includes at least one relatively less soluble material, wherein, relative to carbon dioxide, each one of the at least one relatively less soluble material is less soluble within the operative dissolution agent, when the operative dissolution agent is disposed within the contacting zone.
9. The process of claim 8 , wherein the at least one relatively less soluble material includes at least one of N2, O2, and CO.
10. The process of claim 8 , wherein the contacting effects production of an intermediate operative carbon dioxide supply-comprising mixture including a carbon dioxide-comprising solution intermediate, wherein the carbon dioxide-comprising solution intermediate includes dissolved carbon dioxide.
11. The process of claim 10 , further comprising effecting separation of the carbon dioxide-comprising liquid solution product from the intermediate operative carbon dioxide supply-comprising mixture, wherein the carbon dioxide-comprising liquid solution product includes at least a fraction of the carbon dioxide-comprising solution intermediate.
12. The process of claim 11 , wherein the effecting separation of the carbon dioxide-comprising liquid solution product from the intermediate operative carbon dioxide supply-comprising mixture includes separation effected by gravity separation.
13. The process of claim 11 , wherein each one of (i) the dissolution of at least a fraction of the carbon dioxide of the separation process feed material, and (ii) the separation of the carbon dioxide-comprising liquid solution product from the intermediate operative carbon dioxide supply-comprising mixture, is effected in a contacting zone.
14. The process of claim 13 , wherein the carbon dioxide-comprising liquid solution feed is supplied to a carbon dioxide recovery zone to effect the release of a gaseous carbon dioxide-rich intermediate from the carbon dioxide-comprising liquid solution feed within the carbon dioxide recovery zone; and
wherein the temperature of the contacting zone is lower than the temperature of the carbon dioxide recovery zone.
15. The process of claim 14 , wherein at least a fraction of the operative dissolution agent is supplied to the contacting zone in the form of a mist.
16. The process of claim 1 , wherein the concentration of carbon dioxide within the separation process feed material is at least two volume % based on the total volume of the separation process feed material.
17. The process of claim 4 , wherein at least a fraction of the carbon dioxide-rich separation fraction is flowed through an eductor prior to being supplied to the reaction zone.
18. The process of claim 4 , wherein at least a fraction of the carbon dioxide-rich separation fraction is supplied to the reaction zone with a prime mover.
19. The process of claim 1 , wherein at least a fraction of the fraction of the carbon dioxide-rich product material being supplied to the reaction zone is flowed through an eductor prior to being supplied to the reaction zone.
20. The process of claim 4 , wherein the separation process feed material further includes at least one of SOX, NOX, and NH3.
21. The process of claim 20 , wherein the at least one of SOX, NOX, and NH3 is supplied by the gaseous exhaust material.
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/095,490 US20120276633A1 (en) | 2011-04-27 | 2011-04-27 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
TW101114893A TW201243045A (en) | 2011-04-27 | 2012-04-26 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
EP12776555.0A EP2702134B1 (en) | 2011-04-27 | 2012-04-27 | Process using exhaust gases for effecting growth of phototrophic biomass |
CN201280031706.3A CN103946368A (en) | 2011-04-27 | 2012-04-27 | Process using exhaust gases for effecting growth of phototrophic biomass |
CA2834279A CA2834279C (en) | 2011-04-27 | 2012-04-27 | Process using exhaust gases for effecting growth of phototrophic biomass |
AU2012248080A AU2012248080A1 (en) | 2011-04-27 | 2012-04-27 | Process using exhaust gases for effecting growth of phototrophic biomass |
PCT/CA2012/000403 WO2012145835A1 (en) | 2011-04-27 | 2012-04-27 | Process using exhaust gases for effecting growth of phototrophic biomass |
US14/991,563 US11124751B2 (en) | 2011-04-27 | 2016-01-08 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/095,490 US20120276633A1 (en) | 2011-04-27 | 2011-04-27 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US14/991,563 Continuation US11124751B2 (en) | 2011-04-27 | 2016-01-08 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
Publications (1)
Publication Number | Publication Date |
---|---|
US20120276633A1 true US20120276633A1 (en) | 2012-11-01 |
Family
ID=47068183
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/095,490 Abandoned US20120276633A1 (en) | 2011-04-27 | 2011-04-27 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
US14/991,563 Active 2031-08-18 US11124751B2 (en) | 2011-04-27 | 2016-01-08 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US14/991,563 Active 2031-08-18 US11124751B2 (en) | 2011-04-27 | 2016-01-08 | Supplying treated exhaust gases for effecting growth of phototrophic biomass |
Country Status (7)
Country | Link |
---|---|
US (2) | US20120276633A1 (en) |
EP (1) | EP2702134B1 (en) |
CN (1) | CN103946368A (en) |
AU (1) | AU2012248080A1 (en) |
CA (1) | CA2834279C (en) |
TW (1) | TW201243045A (en) |
WO (1) | WO2012145835A1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20140242681A1 (en) * | 2013-02-28 | 2014-08-28 | Julian Fiorentino | Photobioreactor |
US20150007495A1 (en) * | 2013-07-08 | 2015-01-08 | Electric Energy Express Corporation | Autonomously controlled greenhouse cultivation system |
US9534261B2 (en) | 2012-10-24 | 2017-01-03 | Pond Biofuels Inc. | Recovering off-gas from photobioreactor |
US11512278B2 (en) | 2010-05-20 | 2022-11-29 | Pond Technologies Inc. | Biomass production |
US11612118B2 (en) | 2010-05-20 | 2023-03-28 | Pond Technologies Inc. | Biomass production |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20140199639A1 (en) * | 2013-01-17 | 2014-07-17 | Pond Biofuels Inc. | Process for Managing Photobioreactor Exhaust |
CN107306700B (en) * | 2017-08-22 | 2022-08-19 | 阳光富碳农业科技(天津)有限公司 | Method for increasing carbon dioxide application by using agricultural water and device used in method |
CN111437716B (en) * | 2020-04-03 | 2021-11-26 | 北京航空航天大学 | Microalgae carbon sequestration method based on natural environment regulation |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20090047722A1 (en) * | 2005-12-09 | 2009-02-19 | Bionavitas, Inc. | Systems, devices, and methods for biomass production |
US20090087898A1 (en) * | 2007-09-06 | 2009-04-02 | Clearvalue, Inc. | Methods, processes and apparatus of sequestering and environmentally coverting oxide(s) of carbon and nitrogen |
US20100021361A1 (en) * | 2008-07-23 | 2010-01-28 | Spencer Dwain F | Methods and systems for selectively separating co2 from a multi-component gaseous stream |
US8262776B2 (en) * | 2006-10-13 | 2012-09-11 | General Atomics | Photosynthetic carbon dioxide sequestration and pollution abatement |
Family Cites Families (433)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2732663A (en) | 1956-01-31 | System for photosynthesis | ||
US2732661A (en) | 1956-01-31 | Composition of chlorella | ||
US2658310A (en) | 1950-12-22 | 1953-11-10 | Carnegie Inst Of Washington | Apparatus and process for the production of photosynthetic microorganisms, particularly algae |
US2715795A (en) | 1954-06-22 | 1955-08-23 | Basic Res Corp | Microorganism culture method and apparatus |
US2815607A (en) | 1954-11-26 | 1957-12-10 | William E Beatty | Process and apparatus for the culture of photo-synthetic micro-organisms and macro-organisms, particularly algae |
US2854792A (en) | 1956-09-20 | 1958-10-07 | Ionics | Method and apparatus for propagating algae culture |
US3224143A (en) | 1962-04-17 | 1965-12-21 | Aerojet General Co | Apparatus and method for growing algae to recover oxygen |
US3243918A (en) | 1963-03-13 | 1966-04-05 | Robert A Erkins | Method for propagating photosynthetic microorganisms |
US3403471A (en) | 1965-02-18 | 1968-10-01 | Inst Francais Du Petrole | Method of culturing algae in an artificial medium |
US3303608A (en) | 1965-09-02 | 1967-02-14 | Patrick J Hannan | Oxygen production by photosynthesis of algae under pressure |
US3504185A (en) | 1968-05-09 | 1970-03-31 | Univ Syracuse Res Corp | Apparatus for measuring and controlling cell population density in a liquid medium |
FR1594564A (en) | 1968-07-05 | 1970-06-08 | ||
US3712025A (en) | 1970-03-30 | 1973-01-23 | R Wallace | Continuous electromigration process for removal of gaseous contaminants from the atmosphere and apparatus |
US3855121A (en) | 1971-11-01 | 1974-12-17 | A Gough | Biochemical process |
US3763824A (en) | 1971-11-30 | 1973-10-09 | Minnesota Mining & Mfg | System for growing aquatic organisms |
JPS564233B2 (en) | 1973-03-30 | 1981-01-29 | ||
US4116778A (en) | 1974-01-10 | 1978-09-26 | Viktor Vasilievich Belousov | Plant for continuous cultivation of microorganisms |
US3986297A (en) | 1974-06-24 | 1976-10-19 | Shoji Ichimura | Photosynthesis reactor tank assembly |
IL46022A (en) | 1974-11-08 | 1977-06-30 | Dor I | Process for promotion of algae growth in a sewage medium |
US3959923A (en) | 1974-12-04 | 1976-06-01 | Erno Raumfahrttechnik Gmbh | Equipment for growing algae |
DE2556290C3 (en) | 1975-12-13 | 1979-05-23 | Gesellschaft Fuer Strahlen- Und Umweltforschung Mbh, 8000 Muenchen | Optimal supply of autotrophic organisms |
US4078331A (en) | 1976-04-28 | 1978-03-14 | Mobil Oil Corporation | Process and culture composition for growth of alga and synthesis of biopolymer |
US4087936A (en) | 1976-12-13 | 1978-05-09 | Mobil Oil Corporation | Process for production of alga biopolymer and biomass |
US4525031A (en) | 1978-06-07 | 1985-06-25 | Kei Mori | Solar light energy and electric lighting system and solar and electric light lamps used therein |
JPS5561736A (en) | 1978-10-28 | 1980-05-09 | Nippon Carbide Kogyo Kk | Laver breeding method and material |
US4253271A (en) | 1978-12-28 | 1981-03-03 | Battelle Memorial Institute | Mass algal culture system |
US4297000A (en) | 1979-01-11 | 1981-10-27 | Fries James E | Solar lighting system |
IL57712A (en) | 1979-07-03 | 1984-02-29 | Yissum Res Dev Co | Cultivation of halophilic algae of the dunaliella species for the production of fuel-like product |
US4267038A (en) | 1979-11-20 | 1981-05-12 | Thompson Worthington J | Controlled natural purification system for advanced wastewater treatment and protein conversion and recovery |
US4438591A (en) | 1980-02-04 | 1984-03-27 | The University Of Arizona Foundation | Algal cell growth, modification and harvesting |
US4324068A (en) | 1980-03-03 | 1982-04-13 | Sax Zzyzx, Ltd. | Production of algae |
FR2505359B1 (en) | 1981-05-08 | 1985-07-05 | Air Liquide | METHOD AND PLANT FOR MANUFACTURING MICROORGANISMS |
US4900678A (en) | 1981-12-03 | 1990-02-13 | Kei Mori | Apparatus for photosynthesis |
JPS5898081A (en) | 1981-12-03 | 1983-06-10 | Takashi Mori | Photosynthetic apparatus |
US4383039A (en) | 1981-12-10 | 1983-05-10 | Ethyl Corporation | L-Proline production from algae |
EP0084325B1 (en) | 1982-01-16 | 1988-04-20 | Kei Mori | Apparatus for photosynthesis |
US4398926A (en) | 1982-04-23 | 1983-08-16 | Union Carbide Corporation | Enhanced hydrogen recovery from low purity gas streams |
US4417415A (en) | 1982-04-26 | 1983-11-29 | Battelle Development Corporation | Process for culturing a microalga, and extracting a polysaccharide therefrom |
US4442211A (en) | 1982-06-16 | 1984-04-10 | The United States Of America As Represented By The United States Department Of Energy | Method for producing hydrogen and oxygen by use of algae |
US4473970A (en) | 1982-07-21 | 1984-10-02 | Hills Christopher B | Method for growing a biomass in a closed tubular system |
EP0112556B1 (en) | 1982-12-24 | 1988-04-06 | Kei Mori | Apparatus for photosynthesis |
US4681612A (en) | 1984-05-31 | 1987-07-21 | Koch Process Systems, Inc. | Process for the separation of landfill gas |
US4539625A (en) | 1984-07-31 | 1985-09-03 | Dhr, Incorporated | Lighting system combining daylight concentrators and an artificial source |
US4595405A (en) | 1984-12-21 | 1986-06-17 | Air Products And Chemicals, Inc. | Process for the generation of gaseous and/or liquid nitrogen |
US4851339A (en) | 1986-04-01 | 1989-07-25 | Hills Christopher B | Extraction of anti-mutagenic pigments from algae and vegetables |
US4889812A (en) | 1986-05-12 | 1989-12-26 | C. D. Medical, Inc. | Bioreactor apparatus |
JPS6312274A (en) | 1986-07-03 | 1988-01-19 | Takashi Mori | Bioreactor |
US5081036A (en) | 1987-01-23 | 1992-01-14 | Hoffmann-La Roche Inc. | Method and apparatus for cell culture |
US4939087A (en) | 1987-05-12 | 1990-07-03 | Washington State University Research Foundation, Inc. | Method for continuous centrifugal bioprocessing |
US4869017A (en) | 1987-05-29 | 1989-09-26 | Harbor Branch Oceanographic Institution, Inc. | Macroalgae culture methods |
US4952511A (en) | 1987-06-11 | 1990-08-28 | Martek Corporation | Photobioreactor |
US5216976A (en) | 1987-10-23 | 1993-06-08 | Marinkovich Vincent S | Method and apparatus for high-intensity controlled environment aquaculture |
US4781843A (en) | 1987-12-11 | 1988-11-01 | Dubois Chemicals, Inc. | Chemical treatment for algae control in open water systems |
DE3802031A1 (en) | 1988-01-25 | 1989-07-27 | Hoechst Ag | MULTILAYERED RECORDING MATERIAL FOR OPTICAL INFORMATION |
US5104803A (en) | 1988-03-03 | 1992-04-14 | Martek Corporation | Photobioreactor |
US4958460A (en) | 1988-05-09 | 1990-09-25 | Algae Farms | Method of growing and harvesting microorganisms |
US5334497A (en) | 1988-12-13 | 1994-08-02 | Hideki Inaba | Method of feeding a substrate into tubular bioreactor |
US5040486A (en) | 1988-12-20 | 1991-08-20 | Korea Advanced Institute Of Science & Technology | Symbiotic production method for microalgae and fishes |
US5541056A (en) | 1989-10-10 | 1996-07-30 | Aquasearch, Inc. | Method of control of microorganism growth process |
US5882849A (en) | 1989-10-10 | 1999-03-16 | Aquasearch, Inc. | Method of control of Haematococcus spp, growth process |
US5151347A (en) | 1989-11-27 | 1992-09-29 | Martek Corporation | Closed photobioreactor and method of use |
US5407957A (en) | 1990-02-13 | 1995-04-18 | Martek Corporation | Production of docosahexaenoic acid by dinoflagellates |
US5656421A (en) | 1990-02-15 | 1997-08-12 | Unisyn Technologies, Inc. | Multi-bioreactor hollow fiber cell propagation system and method |
JP3065348B2 (en) | 1990-05-15 | 2000-07-17 | ズィーゲン インコーポレイテッド | High productivity continuous fermentation of carotenoid producing microorganisms |
JP3076586B2 (en) | 1990-05-16 | 2000-08-14 | 三井化学株式会社 | Non-yellowing molding resin and method for producing the same |
US5614378A (en) | 1990-06-28 | 1997-03-25 | The Regents Of The University Of Michigan | Photobioreactors and closed ecological life support systems and artifificial lungs containing the same |
US4995377A (en) | 1990-06-29 | 1991-02-26 | Eiden Glenn E | Dual axis solar collector assembly |
DE4037325A1 (en) | 1990-11-23 | 1992-05-27 | Karl Mueller U Co Kg | METHOD FOR GENERATING CELL MASS AND / OR FERMENTATION PRODUCTS UNDER STERILE CONDITIONS, AND DEVICE FOR IMPLEMENTING THE METHOD |
BE1008008A3 (en) | 1990-11-30 | 1995-12-12 | Ajinomoto Kk | Method and apparatus for adjusting the concentration of carbon source in aerobic culture microorganism. |
US5206173A (en) | 1991-06-05 | 1993-04-27 | Bedminster Bioconversion Corporation | Air hood |
US5330915A (en) | 1991-10-18 | 1994-07-19 | Endotronics, Inc. | Pressure control system for a bioreactor |
US5573669A (en) | 1992-06-02 | 1996-11-12 | Jensen; Kyle R. | Method and system for water purification by culturing and harvesting attached algal communities |
IL102189A (en) | 1992-06-12 | 1995-07-31 | Univ Ben Gurion | Microorganism growth apparatus |
FR2698350B1 (en) | 1992-11-23 | 1994-12-23 | Commissariat Energie Atomique | Device for purifying a liquid effluent loaded with pollutants and method for purifying this effluent. |
US5424209A (en) | 1993-03-19 | 1995-06-13 | Kearney; George P. | Automated cell culture and testing system |
US5552058A (en) | 1993-09-03 | 1996-09-03 | Advanced Waste Reduction | Cooling tower water treatment method |
EP0645456B1 (en) | 1993-09-27 | 2001-04-25 | Mitsubishi Jukogyo Kabushiki Kaisha | Process and system for the production of ethanol from microalgae |
US5565108A (en) | 1993-11-01 | 1996-10-15 | Dimesky; Robert S. | System for the control and retardation of the growth of algae |
US5534404A (en) | 1993-12-10 | 1996-07-09 | Cytotherapeutics, Inc. | Glucose responsive insulin secreting β-cell lines and method for producing same |
US5958761A (en) | 1994-01-12 | 1999-09-28 | Yeda Research And Developement Co. Ltd. | Bioreactor and system for improved productivity of photosynthetic algae |
US5358858A (en) | 1994-03-17 | 1994-10-25 | National Science Council | Process for preparing phycoerythrin from bangia atropurpurea and porphyra angusta |
ZA954157B (en) | 1994-05-27 | 1996-04-15 | Seec Inc | Method for recycling carbon dioxide for enhancing plant growth |
US5558984A (en) | 1994-06-03 | 1996-09-24 | Clemson University | Automated system and process for heterotrophic growth of plant tissue |
US5462666A (en) | 1994-09-28 | 1995-10-31 | Rjjb & G, Inc. | Treatment of nutrient-rich water |
US5851398A (en) | 1994-11-08 | 1998-12-22 | Aquatic Bioenhancement Systems, Inc. | Algal turf water purification method |
AUPN060095A0 (en) | 1995-01-13 | 1995-02-09 | Enviro Research Pty Ltd | Apparatus for biomass production |
US5843762A (en) | 1995-03-02 | 1998-12-01 | Desert Energy Research, Inc. | Method for the high yield, agricultural production of enteromorpha clathrata |
FR2734173B1 (en) | 1995-05-19 | 1997-08-01 | Rhone Poulenc Chimie | REACTOR FOR IMPLEMENTING CHEMICAL REACTIONS INVOLVING BIOMASS |
US5686299A (en) | 1995-05-23 | 1997-11-11 | Lockheed Idaho Technologies Company | Method and apparatus for determining nutrient stimulation of biological processes |
US6238908B1 (en) | 1995-06-07 | 2001-05-29 | Aastrom Biosciences, Inc. | Apparatus and method for maintaining and growth biological cells |
DE19522429A1 (en) | 1995-06-21 | 1997-01-02 | Thomas Lorenz | Arrangement for the treatment of gases containing carbon dioxide |
AU7430296A (en) | 1995-10-26 | 1997-05-15 | Purepulse Technologies, Inc. | Improved deactivation of organisms using high-intensity pulsed polychromatic light |
IL116995A (en) | 1996-02-01 | 2000-08-31 | Univ Ben Gurion | Procedure for large-scale production of astaxanthin from haematococcus |
US5659977A (en) | 1996-04-29 | 1997-08-26 | Cyanotech Corporation | Integrated microalgae production and electricity cogeneration |
DE19629433A1 (en) | 1996-07-22 | 1998-01-29 | Hoechst Ag | Preparation containing omega-3 fatty acids from microorganisms as a prophylactic or therapeutic agent against parasitic diseases in animals |
US5744041A (en) | 1996-09-19 | 1998-04-28 | Grove; John E. | Biological treatment process |
US5906750A (en) | 1996-09-26 | 1999-05-25 | Haase; Richard Alan | Method for dewatering of sludge |
US5846435A (en) | 1996-09-26 | 1998-12-08 | Haase; Richard Alan | Method for dewatering of sludge |
US6673592B1 (en) | 1996-10-21 | 2004-01-06 | Jaw-Kai Wang | Continuous cultivation of microorganisms in large open tanks in sunlight |
CZ326696A3 (en) | 1996-11-06 | 1998-05-13 | Mikrobiologický Ústav Av Čr | Process of external thin-layer cultivation of algae and blue-green algae and a bioreactor for making the same |
WO1998028404A1 (en) | 1996-12-20 | 1998-07-02 | Eastman Chemical Company | Method for deep bed filtration of microalgae |
US5776349A (en) | 1996-12-20 | 1998-07-07 | Eastman Chemical Company | Method for dewatering microalgae with a jameson cell |
US6000551A (en) | 1996-12-20 | 1999-12-14 | Eastman Chemical Company | Method for rupturing microalgae cells |
US5951875A (en) | 1996-12-20 | 1999-09-14 | Eastman Chemical Company | Adsorptive bubble separation methods and systems for dewatering suspensions of microalgae and extracting components therefrom |
US5910254A (en) | 1996-12-20 | 1999-06-08 | Eastman Chemical Company | Method for dewatering microalgae with a bubble column |
AU5695598A (en) | 1996-12-20 | 1998-07-17 | Eastman Chemical Company | Method for cross flow microfiltration of microalgae in the absence of flocculating agents |
US5871952A (en) | 1997-04-14 | 1999-02-16 | Midwest Research Institute | Process for selection of Oxygen-tolerant algal mutants that produce H2 |
SE509852C2 (en) | 1997-07-02 | 1999-03-15 | Marzena Belina Grodzka | Harvesting device for algae |
AU732808B2 (en) | 1997-08-25 | 2001-05-03 | Water Research Commission | Treatment of water |
JP3112439B2 (en) | 1997-09-16 | 2000-11-27 | 株式会社スピルリナ研究所 | Method for producing algae and apparatus for producing the same |
US6120690A (en) | 1997-09-16 | 2000-09-19 | Haase; Richard Alan | Clarification of water and wastewater |
GB9719965D0 (en) | 1997-09-19 | 1997-11-19 | Biotechna Environmental Intern | Modified bioreactor |
JP3950526B2 (en) | 1997-10-17 | 2007-08-01 | 次郎 近藤 | Photosynthesis culture apparatus and collective photosynthesis culture apparatus |
JPH11226351A (en) | 1998-02-12 | 1999-08-24 | Spirulina Kenkyusho:Kk | Production of cleaned air and apparatus for cleaning air |
ES2251183T3 (en) | 1998-03-31 | 2006-04-16 | Bioreal, Inc. | MICROALGAS CULTURE DEVICE. |
US6128135A (en) | 1998-05-01 | 2000-10-03 | Synertech Systems Corporation | Three-reflection collection system for solar and lunar radiant energy |
JP4084883B2 (en) | 1998-05-07 | 2008-04-30 | 三菱電機株式会社 | Gas-liquid two-phase distributor |
US6792336B1 (en) | 1998-05-13 | 2004-09-14 | Bechtel Bwxt Idaho, Llc | Learning-based controller for biotechnology processing, and method of using |
US20020034817A1 (en) | 1998-06-26 | 2002-03-21 | Henry Eric C. | Process and apparatus for isolating and continuosly cultivating, harvesting, and processing of a substantially pure form of a desired species of algae |
WO2000012673A1 (en) | 1998-08-28 | 2000-03-09 | Addavita Limited | Photobioreactor |
WO2000011953A1 (en) | 1998-09-01 | 2000-03-09 | Penn State Research Foundation | Method and apparatus for aseptic growth or processing of biomass |
ATE236245T1 (en) | 1998-10-19 | 2003-04-15 | Ifremer | METHOD FOR IMPROVING THE YIELD OF A PHOTOBIOREACTOR |
JP3248514B2 (en) | 1998-10-29 | 2002-01-21 | 日本鋼管株式会社 | How to reduce carbon dioxide emissions |
US6391238B1 (en) | 1998-11-13 | 2002-05-21 | Kabushiki Kaisha Toshiba | Method of producing algae cultivating medium |
AU3306300A (en) | 1999-03-17 | 2000-10-04 | Biodiversity Limited | Biochemical synthesis apparatus |
IL129101A (en) | 1999-03-22 | 2002-09-12 | Solmecs Israel Ltd | Closed cycle power plant |
DE19916597A1 (en) | 1999-04-13 | 2000-10-19 | Fraunhofer Ges Forschung | Photobioreactor with improved light input through surface enlargement, wavelength shifter or light transport |
US20020130076A1 (en) | 1999-05-07 | 2002-09-19 | Merritt Clifford A. | Aerated pond wastewater treatment system and process for controlling algae and ammonia |
EP1072301B1 (en) * | 1999-07-29 | 2009-11-18 | National Institute Of Advanced Industrial Science and Technology | Method and apparatus for separating and recovering carbon dioxide from combustion exhaust gas |
US6929942B2 (en) | 1999-08-10 | 2005-08-16 | Council Of Scientific And Industrial Research | Process for the treatment of industrial effluents using marine algae to produce potable wafer |
US6284453B1 (en) | 1999-09-29 | 2001-09-04 | Steven Anthony Siano | Method for controlling fermentation growth and metabolism |
IL143421A0 (en) | 1999-09-29 | 2002-04-21 | Micro Gaia Co Ltd | Method for culturing algae |
IN189919B (en) | 1999-11-11 | 2003-05-10 | Proalgen Biotech Ltd | |
US6989252B2 (en) | 1999-12-28 | 2006-01-24 | Midwest Research Institute | Hydrogen production using hydrogenase-containing oxygenic photosynthetic organisms |
NO312413B1 (en) | 2000-01-04 | 2002-05-06 | Forinnova As | Method and apparatus for preventing the bloom of microorganisms in an aqueous system |
US6258588B1 (en) | 2000-01-06 | 2001-07-10 | Oregon State University | Palmaria algal strains and methods for their use |
DE10009060A1 (en) | 2000-02-25 | 2001-09-06 | Dlr Ev | Solar photoreactor |
WO2001068563A1 (en) | 2000-03-15 | 2001-09-20 | Japan Noble Systems Inc. | Method and apparatus for producing organic fertilizer |
FI110533B (en) | 2000-05-04 | 2003-02-14 | Aga Ab | Method for controlling microbial growth |
US6299774B1 (en) | 2000-06-26 | 2001-10-09 | Jack L. Ainsworth | Anaerobic digester system |
FR2810992B1 (en) | 2000-07-03 | 2002-10-25 | Ifremer | METHOD FOR IMPROVING TRANSFER IN A BIOREACTION CHAMBER |
US6667171B2 (en) | 2000-07-18 | 2003-12-23 | Ohio University | Enhanced practical photosynthetic CO2 mitigation |
EP2371942A3 (en) | 2000-08-14 | 2012-11-28 | University of Maryland, Baltimore County | Bioreactor and bioprocessing technique |
CN1218626C (en) | 2000-08-31 | 2005-09-14 | 科学与工业研究委员会 | Improved process for cultivation of algae |
JP4195287B2 (en) | 2000-10-02 | 2008-12-10 | エフ.キャノン トーマス | Automated bioculture and bioculture experimental system |
US20020146817A1 (en) | 2000-10-02 | 2002-10-10 | Cannon Thomas F. | Automated bioculture and bioculture experiments system |
US6571735B1 (en) | 2000-10-10 | 2003-06-03 | Loy Wilkinson | Non-metallic bioreactor and uses |
US7198940B2 (en) | 2000-10-25 | 2007-04-03 | Shot Hardware Optimization Technology, Inc. | Bioreactor apparatus and cell culturing system |
AU783125B2 (en) | 2000-10-31 | 2005-09-29 | Dsm Ip Assets B.V. | Optimisation of fermentation processes |
US6524486B2 (en) | 2000-12-27 | 2003-02-25 | Sepal Technologies Ltd. | Microalgae separator apparatus and method |
EP1249264A1 (en) | 2001-04-11 | 2002-10-16 | Ammonia Casale S.A. | Process for the separation and recovery of carbon dioxide from waste gas or fumes produced by combustible oxidation |
US6723243B2 (en) | 2001-04-19 | 2004-04-20 | Aquafiber Technologies Corporation | Periphyton filtration pre- and post-treatment system and method |
MXPA03011982A (en) | 2001-06-20 | 2004-03-26 | Labatt Brewing Co Ltd | Combination continuous/batch fermentation processes. |
DE10133273A1 (en) | 2001-07-09 | 2003-01-30 | Bayer Cropscience Ag | Device and method for the detection of photosynthesis inhibition |
CA2451597C (en) | 2001-07-12 | 2010-12-14 | Joseph P. Ouellette | Biomass heating system |
CA2353307A1 (en) | 2001-07-13 | 2003-01-13 | Carmen Parent | Device and procedure for processing gaseous effluents |
US20030044114A1 (en) | 2001-09-06 | 2003-03-06 | Pelka David G. | Source wavelength shifting apparatus and method for delivery of one or more selected emission wavelengths |
US6603069B1 (en) | 2001-09-18 | 2003-08-05 | Ut-Battelle, Llc | Adaptive, full-spectrum solar energy system |
US20040077036A1 (en) | 2001-09-26 | 2004-04-22 | Thomas Swati Sebastian | Process to produce astaxanthin from haematococcus biomass |
CA2359417A1 (en) | 2001-10-17 | 2003-04-17 | Co2 Solution Inc. | Photobioreactor with internal artificial lighting |
US20040214314A1 (en) | 2001-11-02 | 2004-10-28 | Friedrich Srienc | High throughput bioreactor |
US6648949B1 (en) | 2001-11-28 | 2003-11-18 | The United States Of America As Represented By The United States Department Of Energy | System for small particle and CO2 removal from flue gas using an improved chimney or stack |
US6918354B2 (en) | 2001-12-20 | 2005-07-19 | Global Biosciences, Inc. | Method and apparatus for butane-enhanced aquatic plant and animal growth |
CN1219871C (en) | 2002-01-22 | 2005-09-21 | 中国科学院过程工程研究所 | Gas-phase double-dynamic solid fermentation technology and fermentation apparatus |
US7033823B2 (en) | 2002-01-31 | 2006-04-25 | Cesco Bioengineering, Inc. | Cell-cultivating device |
US20030162273A1 (en) | 2002-02-04 | 2003-08-28 | Anastasios Melis | Modulation of sulfate permease for photosynthetic hydrogen production |
SE521571C2 (en) | 2002-02-07 | 2003-11-11 | Greenfish Ab | Integrated closed recirculation system for wastewater treatment in aquaculture. |
US6851387B2 (en) | 2002-02-15 | 2005-02-08 | Automated Shrimp Holding Corporation | Aquaculture method and system for producing aquatic species |
US7507579B2 (en) | 2002-05-01 | 2009-03-24 | Massachusetts Institute Of Technology | Apparatus and methods for simultaneous operation of miniaturized reactors |
AU2005274791B2 (en) | 2002-05-13 | 2011-11-10 | Algae Systems, L.L.C. | Photobioreactor cell culture systems, methods for preconditioning photosynthetic organisms, and cultures of photosynthetic organisms produced thereby |
US20050064577A1 (en) | 2002-05-13 | 2005-03-24 | Isaac Berzin | Hydrogen production with photosynthetic organisms and from biomass derived therefrom |
US8507253B2 (en) * | 2002-05-13 | 2013-08-13 | Algae Systems, LLC | Photobioreactor cell culture systems, methods for preconditioning photosynthetic organisms, and cultures of photosynthetic organisms produced thereby |
US20050239182A1 (en) | 2002-05-13 | 2005-10-27 | Isaac Berzin | Synthetic and biologically-derived products produced using biomass produced by photobioreactors configured for mitigation of pollutants in flue gases |
WO2003094598A1 (en) | 2002-05-13 | 2003-11-20 | Greenfuel Technologies Corporation | Photobioreactor and process for biomass production and mitigation of pollutants in flue gases |
CN101580523A (en) | 2002-07-12 | 2009-11-18 | 三得利控股株式会社 | Novel chemical substance having activity for morphogenesis and growth promotion |
EP1539921B1 (en) | 2002-09-16 | 2007-11-21 | Pan-Biotech GmbH | Device for culturing cells, particularly human or animal cells |
GB2409857A (en) | 2002-10-24 | 2005-07-13 | Pan Pacific Tehnologies Pty Lt | Method and system for removal of contaminants from aqueous solution |
US20060223155A1 (en) | 2002-11-01 | 2006-10-05 | Jackson Streeter | Enhancement of in vitro culture or vaccine production in bioreactors using electromagnetic energy |
CA2411383A1 (en) | 2002-11-07 | 2004-05-07 | Real Fournier | Method and apparatus for concentrating an aqueous suspension of microalgae |
US6887692B2 (en) | 2002-12-17 | 2005-05-03 | Gas Technology Institute | Method and apparatus for hydrogen production from organic wastes and manure |
US7392615B2 (en) | 2002-12-24 | 2008-07-01 | Lee L Courtland | Process to produce a commercial soil additive by extracting waste heat, exhaust gas, and other combustion by-products from a coal power generator |
US7191597B2 (en) | 2003-01-21 | 2007-03-20 | Los Angeles Advisory Services, Inc. | Hybrid generation with alternative fuel sources |
US20070157614A1 (en) | 2003-01-21 | 2007-07-12 | Goldman Arnold J | Hybrid Generation with Alternative Fuel Sources |
US7331178B2 (en) | 2003-01-21 | 2008-02-19 | Los Angeles Advisory Services Inc | Hybrid generation with alternative fuel sources |
US20060258000A1 (en) | 2003-02-26 | 2006-11-16 | Allen Jared W | Use of steady-state oxygen gradients to modulate animal cell functions |
JP4287678B2 (en) | 2003-03-14 | 2009-07-01 | Okiセミコンダクタ株式会社 | Internal power circuit |
US8313921B2 (en) | 2003-03-24 | 2012-11-20 | Ch2M Hill, Inc. | Reclaimable hybrid bioreactor |
KR100420253B1 (en) | 2003-03-31 | 2004-03-02 | 디엔텍 (주) | Composites For Elimination Of Green Algae And Red Algae Having The Effect Of Dissolved Oxygen Increament, Elimination Of Nutrient Sources And Bottom Property Improvement And The Green Algae And Red Algae Eliminating Method Thereby |
DE10322054B4 (en) | 2003-05-15 | 2015-06-18 | Sartorius Stedim Biotech Gmbh | Apparatus and method for culturing cells |
TWI234235B (en) | 2003-05-29 | 2005-06-11 | Univ Nat Chiao Tung | Method for fabrication of monocrystalline silicon thin film transistor on glass substrate |
US7176024B2 (en) | 2003-05-30 | 2007-02-13 | Biolex, Inc. | Bioreactor for growing biological materials supported on a liquid surface |
US20070113474A1 (en) | 2003-05-30 | 2007-05-24 | Biolex, Inc. | Bioreactor for growing biological materials supported on a liquid surface |
CN1860637B (en) | 2003-06-27 | 2010-08-11 | 西安大略大学 | Biofuel cell |
CA2472285C (en) | 2003-07-16 | 2012-08-28 | Frederick J. Dart | Water treatment apparatus and method |
EA200600265A1 (en) | 2003-07-17 | 2006-08-25 | Кеннет Дж. Хсу | METHOD OF SUSPENSING GROWTH OF GREEN ALGAE IN WATER SYSTEMS |
WO2005010140A1 (en) | 2003-07-21 | 2005-02-03 | Algenion Gmbh & Co. Kg | Method and device for cultivating eucaryotic microorganisms or blue algae, and biosensor with cultivated eucaryotic microorganisms or blue algae |
WO2005006838A2 (en) | 2003-07-21 | 2005-01-27 | Ben-Gurion University Of The Negev | Flat panel photobioreactor |
TWI273137B (en) | 2003-08-14 | 2007-02-11 | Far East Microalgae Ind Co Ltd | Method for culturing organic blue-green algae |
JP2007503802A (en) | 2003-09-01 | 2007-03-01 | ノボザイムス アクティーゼルスカブ | Method for increasing the yield of marine microbial biomass and / or components of the biomass |
CN2749890Y (en) | 2003-09-17 | 2006-01-04 | 刘宗翰 | Photosynthetic bacteria culturing reactor |
AU2003282895A1 (en) | 2003-10-01 | 2005-05-19 | Midwest Research Institute | Multi-stage microbial system for continuous hydrogen production |
CA2801065C (en) | 2003-10-02 | 2020-04-28 | Dsm Ip Assets B.V. | Production of high levels of dha in microalgae using modified amounts of chloride and potassium |
WO2005042724A2 (en) | 2003-10-31 | 2005-05-12 | Pseudonym Corporation | An apparatus and method for growing bacteria, for use in wastewater treatment, biological pest management, bioremediation of soil and wastes, and other applications |
US7635586B2 (en) | 2003-11-26 | 2009-12-22 | Broadley-James Corporation | Integrated bio-reactor monitor and control system |
US7435581B2 (en) | 2003-11-26 | 2008-10-14 | Broadley-James Corporation | Integrated bio-reactor monitor and control system |
US7220018B2 (en) | 2003-12-15 | 2007-05-22 | Orbital Technologies, Inc. | Marine LED lighting system and method |
KR100490641B1 (en) | 2003-12-16 | 2005-05-19 | 인하대학교 산학협력단 | Multiple layer photobioreactors and method for culturing photosynthetic microorganisms using them |
US7510864B2 (en) | 2004-01-27 | 2009-03-31 | Krichevsky Micah I | Decision-making spectral bioreactor |
DE102004019234B3 (en) | 2004-04-16 | 2005-11-24 | Sartorius Ag | Bioreactor for the cultivation of microorganisms |
KR20070009690A (en) | 2004-04-20 | 2007-01-18 | 고쿠리츠 다이가쿠 호우진 카고시마 다이가쿠 | Algae intensive cultivation apparatus and cultivating method |
US20050244957A1 (en) | 2004-04-29 | 2005-11-03 | Healthy Soils, Inc. | Regenerating tank |
WO2005116238A1 (en) | 2004-05-26 | 2005-12-08 | Yamaha Hatsudoki Kabushiki Kaisha | Method of producing xanthophyll |
WO2005121313A2 (en) | 2004-06-07 | 2005-12-22 | Sampath Kumar Thothathri | A composition for growth of diatom algae |
US7662615B2 (en) | 2004-07-27 | 2010-02-16 | Chung Yuan Christian University | System and method for cultivating cells |
US20060134598A1 (en) | 2004-12-20 | 2006-06-22 | Drummond Scientific Company | Cell culture media dispenser |
US7056725B1 (en) | 2004-12-23 | 2006-06-06 | Chao-Hui Lu | Vegetable alga and microbe photosynthetic reaction system and method for the same |
JP2008526203A (en) | 2004-12-29 | 2008-07-24 | バイオジェン・アイデック・エムエイ・インコーポレイテッド | Bioreactor process control system and method |
US20070161095A1 (en) | 2005-01-18 | 2007-07-12 | Gurin Michael H | Biomass Fuel Synthesis Methods for Increased Energy Efficiency |
US7771988B2 (en) | 2005-03-24 | 2010-08-10 | Hitachi, Ltd. | Control device for fermenter |
US7531350B2 (en) | 2005-04-20 | 2009-05-12 | Agricultural Research Institute | Bioreactor for growing fungus, plant cell, tissue, organ, hairy roots and plantlet |
US20080028675A1 (en) | 2005-05-10 | 2008-02-07 | Nbe,Llc | Biomass treatment of organic waste materials in fuel production processes to increase energy efficiency |
US20060275858A1 (en) | 2005-06-02 | 2006-12-07 | Saucedo Victor M | Optimization of Process Variables in Oxygen Enriched Fermentors Through Process Controls |
EP2270132A3 (en) | 2005-06-07 | 2012-07-18 | HR Biopetroleum, Inc. | Continuous-batch hybrid process for production of oil and other useful products from photosynthetic microbes |
WO2006135632A2 (en) | 2005-06-10 | 2006-12-21 | Nanologix, Inc. | System for sustained microbial production of hydrogen gas in a bioreactor |
EP1739165A1 (en) | 2005-06-29 | 2007-01-03 | Cellution Biotech B.V. | Method and apparatus for cultivating cells utilizing wave motion |
US20070042487A1 (en) | 2005-08-19 | 2007-02-22 | Imi Norgren, Inc. | Bioreactor valve island |
BRPI0615085A2 (en) | 2005-08-25 | 2011-06-28 | Solix Biofuels Inc | method, apparatus and system for the production of biodiesel from algae |
US20080254056A1 (en) | 2005-09-06 | 2008-10-16 | Yamaha Hatsudoki Kabushiki Kaisha | Green Alga Extract with High Astaxanthin Content and Method of Producing the Same |
US20070054351A1 (en) | 2005-09-06 | 2007-03-08 | Yamaha Hatsudoki Kabushiki Kaisha | Green algae having a high astaxanthin content and method for producing the same |
US9248421B2 (en) | 2005-10-07 | 2016-02-02 | Massachusetts Institute Of Technology | Parallel integrated bioreactor device and method |
US20070092962A1 (en) | 2005-10-20 | 2007-04-26 | Saudi Arabian Oil Company | Carbon Neutralization System (CNS) for CO2 sequestering |
CA2634234A1 (en) | 2005-12-09 | 2007-06-21 | Bionavitas, Inc. | Systems, devices, and methods for biomass production |
DE102005059089A1 (en) | 2005-12-10 | 2007-06-14 | Nexans | Plug-in coupling for cryogenic pipes |
CN100562564C (en) | 2005-12-12 | 2009-11-25 | 中国科学院过程工程研究所 | The carbon compensator and using method and the purposes that are used for large-scale culturing micro-algae |
AU2006332420A1 (en) | 2006-01-04 | 2007-07-12 | Kenneth J. Hsu | Process for combating water polluted by algae |
MX2008010770A (en) | 2006-02-21 | 2009-03-06 | Univ Arizona State | Photobioreactor and uses therefor. |
US7507554B2 (en) | 2006-02-28 | 2009-03-24 | Propulsion Logic, Llc | Process for the production of ethanol from algae |
US7135308B1 (en) | 2006-02-28 | 2006-11-14 | Propulsion Logic, Llc | Process for the production of ethanol from algae |
US20080096267A1 (en) | 2006-03-15 | 2008-04-24 | Howard Everett E | Systems and methods for large-scale production and harvesting of oil-rich algae |
WO2007118223A2 (en) | 2006-04-06 | 2007-10-18 | Brightsource Energy, Inc. | Solar plant employing cultivation of organisms |
US8470584B2 (en) | 2006-05-10 | 2013-06-25 | Ohio University | Apparatus and method for growing biological organisms for fuel and other purposes |
JP2009536830A (en) | 2006-05-12 | 2009-10-22 | アリゾナ ボード オブ リージェンツ, ア ボディー コーポレイト オブ ザ ステート オブ アリゾナ アクティング フォー アンド オン ビハーフ オブ アリゾナ ステート ユニバーシティー | New Chlorella species and their use |
US8415142B2 (en) | 2006-06-14 | 2013-04-09 | Malcolm Glen Kertz | Method and apparatus for CO2 sequestration |
EP2046938A2 (en) | 2006-07-10 | 2009-04-15 | Greenfuel Technologies Corporation | Photobioreactor systems and methods for treating co2-enriched gas and producing biomass |
US20080009055A1 (en) | 2006-07-10 | 2008-01-10 | Greenfuel Technologies Corp. | Integrated photobioreactor-based pollution mitigation and oil extraction processes and systems |
US8110395B2 (en) | 2006-07-10 | 2012-02-07 | Algae Systems, LLC | Photobioreactor systems and methods for treating CO2-enriched gas and producing biomass |
US7771515B2 (en) | 2006-07-13 | 2010-08-10 | Institut National Des Sciences Appliquees | Method and installation for treating an aqueous effluent, in order to extract at least one dissolved gaseous compound; application to aquaculture in recirculated aqueous medium |
EP2041262A4 (en) | 2006-07-14 | 2012-07-18 | Abb Research Ltd | A method for on-line optimization of a fed-batch fermentation unit to maximize the product yield |
US8278087B2 (en) | 2006-07-18 | 2012-10-02 | The University of Regensburg | Energy production with hyperthermophilic organisms |
WO2008053353A2 (en) | 2006-07-18 | 2008-05-08 | Hyperthermics Holding As | Energy production with hyperthermophilic organisms |
US8975065B2 (en) | 2006-07-24 | 2015-03-10 | California Institute Of Technology | Meandering channel fluid device and method |
IL184971A0 (en) | 2006-08-01 | 2008-12-29 | Brightsource Energy Inc | High density bioreactor system, devices and methods |
CA2666162A1 (en) | 2006-08-17 | 2008-02-21 | Algepower, Llc | Hydroponic growing enclosure and method for growing, harvesting, processing and distributing algae, related microorganisms and their by products |
US20080050800A1 (en) | 2006-08-23 | 2008-02-28 | Mckeeman Trevor | Method and apparatus for a multi-system bioenergy facility |
US20100151558A1 (en) | 2006-09-13 | 2010-06-17 | Petroalgae, Llc | Tubular Microbial Growth System |
US7736508B2 (en) | 2006-09-18 | 2010-06-15 | Christopher A. Limcaco | System and method for biological wastewater treatment and for using the byproduct thereof |
US7850848B2 (en) | 2006-09-18 | 2010-12-14 | Limcaco Christopher A | Apparatus and process for biological wastewater treatment |
US7973214B2 (en) | 2006-09-25 | 2011-07-05 | Ut-Battelle, Llc | Designer organisms for photosynthetic production of ethanol from carbon dioxide and water |
ES2326296B1 (en) | 2006-10-02 | 2010-07-15 | Bio Fuel Systems, S.L. | SUBMERSIBLE VERTICAL PHOTOBREACTOR FOR OBTAINING BIOFUELS. |
CN101998876B (en) | 2006-10-02 | 2015-03-25 | 环球研究技术有限公司 | Method and apparatus for extracting carbon dioxide from air |
US20080085536A1 (en) | 2006-10-04 | 2008-04-10 | Board Of Regents, The University Of Texas System | Production of Cellulose in Halophilic Photosynthetic Prokaryotes (Cyanobacteria) |
US20080113413A1 (en) | 2006-10-04 | 2008-05-15 | Board Of Regents, The University Of Texas System | Expression of Foreign Cellulose Synthase Genes in Photosynthetic Prokaryotes (Cyanobacteria) |
EP2086686B1 (en) | 2006-10-06 | 2012-05-16 | BioEnergy Technology Company Limited | Renewable energy recovery from msw and other wastes |
US7687261B2 (en) | 2006-10-13 | 2010-03-30 | General Atomics | Photosynthetic oil production in a two-stage reactor |
US7662616B2 (en) | 2006-10-13 | 2010-02-16 | General Atomics | Photosynthetic oil production with high carbon dioxide utilization |
CN101558146A (en) | 2006-10-20 | 2009-10-14 | 代表亚利桑那大学的亚利桑那校董会 | System and method for growing photosynthetic cells |
US8323958B2 (en) | 2006-11-02 | 2012-12-04 | Algenol Biofuels Switzerland GmbH | Closed photobioreactor system for continued daily in situ production of ethanol from genetically enhanced photosynthetic organisms with means for separation and removal of ethanol |
BRPI0718293A2 (en) | 2006-11-02 | 2013-11-19 | Algenol Biofuels Ltd | CLOSED PHOTO-REACTOR SYSTEM FOR PRODUCTION, SEPARATION, COLLECTION AND REMOVAL IN SITU, DAILY CONTINUED, ETHANOL FROM GENETICALLY OPTIMIZED PHOTOSYTHETIC ORGANISMS |
US20080115500A1 (en) | 2006-11-15 | 2008-05-22 | Scott Macadam | Combustion of water borne fuels in an oxy-combustion gas generator |
US20080138875A1 (en) | 2006-12-08 | 2008-06-12 | Lucia Atehortua | Method to generate fungal biomass from a culture of differentiated mycelium |
US20080318304A1 (en) | 2006-12-11 | 2008-12-25 | Dudley Burton | Cultivation of micro-algae and application to animal feeds, environments, field crops, and waste treatment |
EP2099921B1 (en) | 2006-12-11 | 2011-03-09 | Ralf Salvetzki | Process for the biological generation of methane |
US7750494B1 (en) | 2006-12-13 | 2010-07-06 | Rudolph Behrens | Systems and vessels for producing hydrocarbons and/or water, and methods for same |
WO2008079896A1 (en) * | 2006-12-20 | 2008-07-03 | Carbon Capture Corporation | Diesel exhaust gas scrubbing method for carbon dioxide removal |
US9637714B2 (en) | 2006-12-28 | 2017-05-02 | Colorado State University Research Foundation | Diffuse light extended surface area water-supported photobioreactor |
WO2008083352A1 (en) | 2006-12-29 | 2008-07-10 | Genifuel Corporation | Production of biofuels using algae |
US7977076B2 (en) | 2006-12-29 | 2011-07-12 | Genifuel Corporation | Integrated processes and systems for production of biofuels using algae |
US8030037B2 (en) | 2007-01-10 | 2011-10-04 | Parry Nutraceuticals, Division Of E.I.D. Parry (India) Ltd. | Photoautotrophic growth of microalgae for omega-3 fatty acid production |
ES2308912B2 (en) | 2007-01-16 | 2009-09-16 | Bernard A.J. Stroiazzo-Mougin | ACCELERATED PROCEDURE OF ENERGETIC CONVERSION OF CARBON DIOXIDE. |
US20080268302A1 (en) | 2007-01-17 | 2008-10-30 | Mccall Joe | Energy production systems and methods |
WO2008089321A2 (en) | 2007-01-17 | 2008-07-24 | Joe Mccall | Apparatus and methods for production of biodiesel |
US20080176303A1 (en) | 2007-01-19 | 2008-07-24 | 6Solutions, Llc | Farm Scale Ethanol Plant |
US7736509B2 (en) | 2007-01-24 | 2010-06-15 | Alan Kruse | Probiotic system and aquaculture devices |
US8043847B2 (en) | 2007-01-26 | 2011-10-25 | Arizona Public Service Company | System including a tunable light and method for using same |
US20080213049A1 (en) | 2007-03-01 | 2008-09-04 | Higgins Timothy R | Methods for Controlling Dust and Creating Bio-Crust |
US8198058B2 (en) | 2007-03-05 | 2012-06-12 | Offerman John D | Efficient use of biogas carbon dioxide in liquid fuel synthesis |
EP2134450A2 (en) | 2007-03-08 | 2009-12-23 | Seambiotic Ltd. | Method for growing photosynthetic organisms |
US8569049B2 (en) | 2007-03-19 | 2013-10-29 | Feyecon Development & Implementation B.V. | Photo bioreactor with light distributor and method for the production of a photosynthetic culture |
WO2008122029A1 (en) | 2007-04-02 | 2008-10-09 | Inventure Chemical, Inc. | Simultaneous esterification and alcohol ysis/hydrolysis of oil-containing materials with cellulosic and peptidic content |
DE102007018675B4 (en) | 2007-04-18 | 2009-03-26 | Seyfried, Ralf, Dr. | Biomass breeding plant and method for growing biomass |
WO2008131019A1 (en) | 2007-04-20 | 2008-10-30 | Bionavitas, Inc. | Systems, devices, and, methods for releasing biomass cell components |
EP2152848A2 (en) | 2007-04-27 | 2010-02-17 | Greenfuel Technologies Corporation | Photobioreactor systems positioned on bodies of water |
ES2660667T3 (en) | 2007-05-07 | 2018-03-23 | Protalix Ltd. | Large-scale disposable bioreactor |
US20090215155A1 (en) | 2007-05-31 | 2009-08-27 | Xl Renewables, Inc. | Algae Producing Trough System |
BRPI0812174A2 (en) | 2007-06-01 | 2014-12-30 | Wacker Chemie Ag | Photoreactor |
US20090061493A1 (en) | 2007-06-01 | 2009-03-05 | Solazyme, Inc. | Lipid Pathway Modification in Oil-Bearing Microorganisms |
US9966763B2 (en) | 2007-06-07 | 2018-05-08 | Allen L. Witters | Integrated multiple fuel renewable energy system |
US20080305539A1 (en) | 2007-06-08 | 2008-12-11 | Robert Hickey | Membrane supported bioreactor for conversion of syngas components to liquid products |
US8198055B2 (en) | 2007-06-08 | 2012-06-12 | Coskata, Inc. | Process for converting syngas to liquid products with microorganisms on two-layer membrane |
CA2691007A1 (en) | 2007-06-18 | 2008-12-24 | Choudhary, Vidhi | Golden yellow algae and method of producing the same |
TWI429745B (en) | 2007-06-19 | 2014-03-11 | Renewable Algal Energy Llc | Process for microalgae conditioning and concentration |
EP2009092A1 (en) | 2007-06-25 | 2008-12-31 | BIOeCON International Holding N.V. | Method for producing aquatic biomass |
ITMI20071278A1 (en) | 2007-06-26 | 2008-12-27 | Eni Spa | PROCEDURE FOR CULTIVATION OF MICRO-ALGAES |
US20100120134A1 (en) | 2007-07-19 | 2010-05-13 | Texas Clean Fuels, Inc. | Micro-organism production apparatus and system |
US20090023199A1 (en) | 2007-07-19 | 2009-01-22 | New England Clean Fuels, Inc. | Micro-organism production system and method |
US7838272B2 (en) | 2007-07-25 | 2010-11-23 | Chevron U.S.A. Inc. | Increased yield in gas-to-liquids processing via conversion of carbon dioxide to diesel via microalgae |
US8993314B2 (en) | 2007-07-28 | 2015-03-31 | Ennesys Sas | Algae growth system for oil production |
IL184941A0 (en) | 2007-07-31 | 2008-12-29 | Slavin Vladimir | Method and device for producing biomass of photosynthesizing microorganisms mainly halobacteria halobacterium as well as biomass of the said microorganisms pigments bacteriorhodopsin in particular |
CN101139113B (en) | 2007-08-01 | 2011-01-19 | 李贵生 | High-efficienct algae-removing and clean water reduction method |
WO2009018498A2 (en) | 2007-08-01 | 2009-02-05 | Bionavitas, Inc. | Illumination systems, devices, and methods for biomass production |
US8097168B2 (en) | 2007-08-14 | 2012-01-17 | Earth Renaissance Technologies, Llc | Wastewater photo biomass/algae treatment method |
US20090068727A1 (en) | 2007-08-28 | 2009-03-12 | Greg Karr | Closed system, shallow channel photobioreactor |
US20090068715A1 (en) | 2007-09-06 | 2009-03-12 | OGAKI Bio. Technology Research Co., Ltd. | Method of producing bio-ethanol |
AU2008294406A1 (en) | 2007-09-07 | 2009-03-12 | Csir | Non-invasive automated cell proliferation apparatus |
US20090203067A1 (en) | 2007-09-18 | 2009-08-13 | Eckerle Matthew W | Photobioreactor Systems and Methods for Growing Organisms |
WO2009039358A1 (en) | 2007-09-19 | 2009-03-26 | Tm Industrial Supply, Inc. | Renewable energy system |
CZ2007657A3 (en) | 2007-09-20 | 2009-04-01 | Ecofuel Labs Llc | Method of processing stillage |
US20090077864A1 (en) | 2007-09-20 | 2009-03-26 | Marker Terry L | Integrated Process of Algae Cultivation and Production of Diesel Fuel from Biorenewable Feedstocks |
US20090081743A1 (en) | 2007-09-24 | 2009-03-26 | Hazelbeck David A | Transportable algae biodiesel system |
US8033047B2 (en) | 2007-10-23 | 2011-10-11 | Sartec Corporation | Algae cultivation systems and methods |
US7905049B2 (en) | 2007-11-01 | 2011-03-15 | Independence Bio-Products, Inc. | Algae production |
US7662617B2 (en) | 2007-11-03 | 2010-02-16 | Rush Stephen L | Systems and processes for cellulosic ethanol production |
US7514247B2 (en) | 2007-11-03 | 2009-04-07 | Wise Landfill Recycling Mining, Inc. | Systems and processes for cellulosic ethanol production |
US7449313B2 (en) | 2007-11-03 | 2008-11-11 | Rush Stephen L | Systems and processes for cellulosic ethanol production |
US20090137013A1 (en) | 2007-11-07 | 2009-05-28 | Sustainable Green Technologies, Inc. | Microorganisms and methods for increased hydrogen production using diverse carbonaceous feedstock and highly absorptive materials |
US20090130747A1 (en) | 2007-11-16 | 2009-05-21 | Mon-Han Wu | System and Method of Enhancing Production of Algae |
US20090134091A1 (en) | 2007-11-24 | 2009-05-28 | Green Vision Energy Corporation | Method for removing undesirable components from water while containing, cultivating, and harvesting photosynthetic marine microorganisms within water |
US20090137025A1 (en) | 2007-11-24 | 2009-05-28 | Green Vision Energy Corporation | Apparatus for containing, cultivating, and harvesting photosynthetic marine microorganisms within water |
CN101932714A (en) | 2007-12-04 | 2010-12-29 | 俄亥俄州立大学研究基金会 | Optimization of biofuel production |
US20090148927A1 (en) | 2007-12-05 | 2009-06-11 | Sequest, Llc | Mass Production Of Aquatic Plants |
CN101254364A (en) | 2007-12-11 | 2008-09-03 | 云南德林海生物科技有限公司 | Blue algae slurry dewatering process method |
US20090151241A1 (en) | 2007-12-14 | 2009-06-18 | Dressler Lawrence V | Method for producing algae in photobioreactor |
US20090155864A1 (en) | 2007-12-14 | 2009-06-18 | Alan Joseph Bauer | Systems, methods, and devices for employing solar energy to produce biofuels |
ITMI20072343A1 (en) | 2007-12-14 | 2009-06-15 | Eni Spa | PROCESS FOR THE PRODUCTION OF ALGAL BIOMASS WITH HIGH LIPID CONTENT |
US20090227003A1 (en) | 2007-12-21 | 2009-09-10 | Roger Blotsky | Methods and Systems for Biomass Recycling and Energy Production |
US7927491B2 (en) | 2007-12-21 | 2011-04-19 | Highmark Renewables Research Limited Partnership | Integrated bio-digestion facility |
US8759068B2 (en) | 2008-01-02 | 2014-06-24 | Missing Link Technologies, L.L.C. | System for fermentation using algae |
WO2009094440A1 (en) | 2008-01-25 | 2009-07-30 | Aquatic Energy Llc | Algal culture production, harvesting, and processing |
US20090203116A1 (en) | 2008-02-13 | 2009-08-13 | Bazaire Keith E | System to improve algae production in a photo-bioreactor |
US20090232861A1 (en) | 2008-02-19 | 2009-09-17 | Wright Allen B | Extraction and sequestration of carbon dioxide |
US20090205638A1 (en) | 2008-02-19 | 2009-08-20 | Peter Corcoran | Solar Receiver for a Photo-Bioreactor |
US20090221057A1 (en) | 2008-02-28 | 2009-09-03 | Kennedy James C | Bio-Breeder System for Biomass Production |
US20090233334A1 (en) | 2008-03-11 | 2009-09-17 | Excellgene Sa | Cell cultivation and production of recombinant proteins by means of an orbital shake bioreactor system with disposable bags at the 1,500 liter scale |
AR071748A1 (en) | 2008-03-13 | 2010-07-14 | Evolution Energy Production Inc | METHODS AND SYSTEMS TO PRODUCE BIOFUELS AND BIOENERGETIC PRODUCTS FROM XENOBIOTIC COMPOUNDS |
GB2458529A (en) | 2008-03-25 | 2009-09-30 | Saigas Ltd | Extracting energy products from biomass using solar energy |
US20090249685A1 (en) | 2008-03-28 | 2009-10-08 | Flowers Troy D | Closed loop biomass energy system |
US8017377B1 (en) | 2008-04-11 | 2011-09-13 | Agoil International, Llc | Mass culture of microalgae for lipid production |
US20090325253A1 (en) | 2008-04-25 | 2009-12-31 | Ascon Miguel | Methods and systems for production of biofuels and bioenergy products from sewage sludge, including recalcitrant sludge |
WO2009134358A1 (en) | 2008-04-28 | 2009-11-05 | Optiswitch Technology Corporation | Apparatus and method for producing biofuel from algae by application of shaped pulsed pressure waves |
US20090275120A1 (en) | 2008-04-30 | 2009-11-05 | Edward John Koch | Extraction of co2 gas from engine exhaust |
US8236535B2 (en) | 2008-04-30 | 2012-08-07 | Xyleco, Inc. | Processing biomass |
US20090324799A1 (en) | 2008-05-15 | 2009-12-31 | Robert Michael Hartman | Maximizing utilization of municipal sewage treatment effluents to produce a biofuel, fertilizer and/or animal feed for environmentally sustainable minded communities |
US8058058B2 (en) | 2008-05-19 | 2011-11-15 | Coskata, Inc. | Submerged membrane supported bioreactor for conversion of syngas components to liquid products |
WO2009142765A2 (en) | 2008-05-23 | 2009-11-26 | Orginoil, Inc. | Apparatus and methods for photosynthetic growth of microorganisms in a photobioreactor |
US8464540B2 (en) | 2008-05-23 | 2013-06-18 | Pacific Waste, Inc. | Waste to energy process and plant |
US20090291485A1 (en) | 2008-05-23 | 2009-11-26 | Steven Shigematsu | Apparatus and method for optimizing photosynthetic growth in a photo bioreactor |
CN101280328B (en) | 2008-05-27 | 2011-06-29 | 清华大学 | Method for producing biodiesel by autotrophic culture and heterotrophic culture of chlorella |
WO2009149260A1 (en) | 2008-06-04 | 2009-12-10 | Solix Biofuels, Inc. | Compositions, methods and uses for growth of microorganisms and production of their products |
US8197857B2 (en) | 2008-06-06 | 2012-06-12 | Dressler Lawrence V | Method for eliminating carbon dioxide from waste gases |
US7855061B2 (en) | 2008-06-19 | 2010-12-21 | Adrian George Vance | Fuel farm process for producing butanol |
HUE037653T2 (en) | 2008-06-20 | 2018-09-28 | Stroiazzo Mougin Bernard A J | Continuous process for the generation of high nutritional value and energy resources |
CN101384056B (en) | 2008-06-23 | 2012-09-26 | 中兴通讯股份有限公司 | Scheduling method for service division sector access by uplink packet |
WO2009158028A2 (en) | 2008-06-26 | 2009-12-30 | Novus Energy Llc | Integreated systems for producing biogas and liquid fuel from algae |
BRPI0914593A2 (en) | 2008-06-26 | 2015-12-15 | Univ Colorado State Res Found | photobioreactors, algal growth systems, algal growth methods and systems, for algae growth control in flat panel photobioreactor, algal harvest scheduling and model-based and bioreactor error and adaptive control diagnostics photobioreactor |
US20100003741A1 (en) | 2008-07-01 | 2010-01-07 | Fromson Howard A | Integrated power plant, sewage treatment, and aquatic biomass fuel production system |
US20100003717A1 (en) | 2008-07-03 | 2010-01-07 | Oyler James R | Closed-Loop System for Growth of Algae or Cyanobacteria and Gasification of the Wet Biomass |
US20100173375A1 (en) | 2008-07-03 | 2010-07-08 | Oyler James R | Closed-loop system for growth of aquatic biomass and gasification thereof |
US20100005711A1 (en) | 2008-07-09 | 2010-01-14 | Sartec Corporation | Lighted Algae Cultivation Systems |
US8383870B2 (en) | 2008-07-18 | 2013-02-26 | Federal Express Corporation | Environmentally friendly methods and systems of energy production |
US8510985B2 (en) | 2008-07-22 | 2013-08-20 | Eliezer Halachmi Katchanov | Energy production from algae in photo bioreactors enriched with carbon dioxide |
US20100018214A1 (en) | 2008-07-22 | 2010-01-28 | Eliezer Halachmi Katchanov | Energy Production from Algae in Photo Bioreactors Enriched with Carbon Dioxide |
WO2010011320A1 (en) | 2008-07-23 | 2010-01-28 | Global Energies, Llc | Bioreactor system for mass production of biomass |
US20100028977A1 (en) | 2008-07-30 | 2010-02-04 | Wayne State University | Enclosed photobioreactors with adaptive internal illumination for the cultivation of algae |
WO2010017337A1 (en) | 2008-08-06 | 2010-02-11 | Praxair Technology, Inc. | System and method for controlling a mammalian cell culture process |
WO2010017002A1 (en) | 2008-08-08 | 2010-02-11 | Diversified Energy Corp. | Algae production systems and associated methods |
US8318416B2 (en) | 2008-08-08 | 2012-11-27 | Biogen Idec Ma Inc. | Nutrient monitoring and feedback control for increased bioproduct production |
US20100034050A1 (en) | 2008-08-11 | 2010-02-11 | Gary Erb | Apparatus and Method for Cultivating Algae |
US20100050502A1 (en) | 2008-08-21 | 2010-03-04 | LiveFuels, Inc. | Systems and methods for hydrothermal conversion of algae into biofuel |
WO2010025345A2 (en) | 2008-08-28 | 2010-03-04 | Innovative American Technology Inc. | Semi-closed loop alga-diesel fuel photobioreactor using waste water |
US8367392B2 (en) | 2008-09-05 | 2013-02-05 | Transalgae Ltd. | Genetic transformation of algal and cyanobacteria cells by microporation |
US8518690B2 (en) | 2008-09-09 | 2013-08-27 | Battelle Memorial Institute | Production of bio-based materials using photobioreactors with binary cultures |
US9051539B2 (en) | 2008-09-12 | 2015-06-09 | Kenneth Matthew Snyder | Algaculture system for biofuel production and methods of production thereof |
CN101669569A (en) | 2008-09-12 | 2010-03-17 | 中国科学院海洋研究所 | Method for processing seaweed fodder |
MX2011003070A (en) | 2008-09-22 | 2011-07-28 | Phycosystems Inc | Device for efficient, cost-effective conversion of aquatic biomass to fuels and electricity. |
WO2010036333A1 (en) | 2008-09-23 | 2010-04-01 | LiveFuels, Inc. | Systems and methods for producing biofuels from algae |
US20100077654A1 (en) | 2008-09-23 | 2010-04-01 | LiveFuels, Inc. | Systems and methods for producing biofuels from algae |
JP4883067B2 (en) | 2008-09-29 | 2012-02-22 | 株式会社日立プラントテクノロジー | Culture apparatus and culture method |
SI2331238T1 (en) | 2008-10-09 | 2014-03-31 | Rogmans, Maria | Method and device for photosynthesis-supported disposal of co2 |
US20100093078A1 (en) | 2008-10-14 | 2010-04-15 | Cleveland State University | Separating device, an algae culture photobioreactor, and methods of using them |
US20100159579A1 (en) | 2008-10-20 | 2010-06-24 | Schuring Christopher S | Photobioreactor systems |
US20100099170A1 (en) | 2008-10-20 | 2010-04-22 | Deepak Aswani | Methods of controlling open algal bioreactors |
CA2773001C (en) | 2008-10-21 | 2018-04-24 | Canadian Pacific Algae Inc. | Method for the efficient and continuous growth and harvesting of nutrient-rich phytoplankton and methods of using the same |
US20100107487A1 (en) | 2008-10-22 | 2010-05-06 | Holland Alexandra D | Methods for estimating intrinsic autotrophic biomass yield and productivity in unicellular photosynthetic algae |
US20100105127A1 (en) | 2008-10-24 | 2010-04-29 | Margin Consulting, Llc | Systems and methods for generating resources using wastes |
US20100105125A1 (en) | 2008-10-24 | 2010-04-29 | Bioprocessh20 Llc | Systems, apparatuses and methods for cultivating microorganisms and mitigation of gases |
US20100105129A1 (en) | 2008-10-27 | 2010-04-29 | Sanchez-Pina Jose L | Biomass production system |
US20100101621A1 (en) | 2008-10-28 | 2010-04-29 | Jun Xu | Solar powered generating apparatus and methods |
US20100159567A1 (en) | 2008-11-07 | 2010-06-24 | Kuehnle Adelheid R | Preservation and composition of bioprocess algae for production of lipids, seedstock, and feed |
AU2009335976A1 (en) | 2008-12-19 | 2011-08-11 | Alpha-J Research Limited Partnership | Optimization of algal product production through uncoupling cell proliferation and algal product production |
US20100159578A1 (en) | 2008-12-22 | 2010-06-24 | Alberto Daniel Lacaze | Method and system for robotic algae harvest |
US8629646B2 (en) | 2009-01-09 | 2014-01-14 | Solar Components Llc | Generation of renewable energy certificates from distributed procedures |
TW201028472A (en) | 2009-01-13 | 2010-08-01 | Alpha J Res Ltd Partnership | Use of plant growth regulators to enhance algae growth for the production of added value products |
ZA200900499B (en) | 2009-01-22 | 2009-09-30 | Energetix Llc | Plastic disposable reactor system |
US8143051B2 (en) | 2009-02-04 | 2012-03-27 | Aurora Algae, Inc. | Systems and methods for maintaining the dominance and increasing the biomass production of nannochloropsis in an algae cultivation system |
US8434626B2 (en) | 2009-02-16 | 2013-05-07 | Combined Power, Llc | System and related method for concentrating biological culture and circulating biological culture and process fluid |
JP5446805B2 (en) | 2009-03-16 | 2014-03-19 | 富士通株式会社 | Fuel cell system and control method thereof |
CN201381254Y (en) | 2009-03-18 | 2010-01-13 | 宜兴市官林工业环保设备厂 | Algae-laden water separation dehydractor |
WO2010108049A1 (en) | 2009-03-19 | 2010-09-23 | Solix Biofuels, Inc. | Systems and methods for delivery of gases to algal cultures |
US20100267122A1 (en) | 2009-04-17 | 2010-10-21 | Senthil Chinnasamy | Microalgae cultivation in a wastewater dominated by carpet mill effluents for biofuel applications |
CN102448286A (en) | 2009-04-20 | 2012-05-09 | Pa有限责任公司 | Cultivation, harvesting and processing of floating aquatic species with high growth rates |
US20100297749A1 (en) | 2009-04-21 | 2010-11-25 | Sapphire Energy, Inc. | Methods and systems for biofuel production |
US8535906B2 (en) | 2009-04-27 | 2013-09-17 | Woods Hole Oceanographic Institution | Biofuel manufacturing methods and systems incorporating radiocarbon analysis techniques |
US20100297739A1 (en) | 2009-05-21 | 2010-11-25 | Tm Industrial Supply, Inc. | Renewable energy system |
US8623634B2 (en) | 2009-06-23 | 2014-01-07 | Kior, Inc. | Growing aquatic biomass, and producing biomass feedstock and biocrude therefrom |
US20110027827A1 (en) | 2009-07-30 | 2011-02-03 | Zhanyou Chi | Integrated system for production of biofuel feedstock |
CN101648092B (en) | 2009-08-25 | 2011-06-01 | 中国船舶重工集团公司第七○二研究所 | Dehydration processing method for cyanophyte water |
CN102665871B (en) * | 2009-10-24 | 2015-08-12 | Calix有限公司 | For the treatment of input fuel gas and steam with manufactures carbon dioxide and output fuel gas system and method |
CN101696389B (en) | 2009-10-29 | 2012-03-07 | 新奥科技发展有限公司 | Microalgae culture method and photo-bioreactor system thereof |
US20110113681A1 (en) | 2009-11-16 | 2011-05-19 | Mathias Mostertz | Use of by-product carbon dioxide from a steam methane reformer in an algae biofuel production process |
US20110124091A1 (en) | 2009-11-24 | 2011-05-26 | Chao-Hui Lu | Industrialized algae culturing method and system thereof |
CN101838606B (en) | 2009-12-30 | 2013-01-02 | 同济大学 | Airlift loop bioreactor through microalgae photoautotrophic-photoheterotrophic coupling for carbon emission reduction in sewage treatment |
US20100173355A1 (en) | 2010-03-08 | 2010-07-08 | Clearvalue Technologies, Inc. | Means for sequestration and conversion of COx and NOx, CONOx |
US20110236958A1 (en) | 2010-03-23 | 2011-09-29 | Lan Wong | Multistory Bioreaction System for Enhancing Photosynthesis |
CA2738461C (en) | 2010-05-20 | 2023-06-06 | Pond Biofuels Inc. | Process for growing biomass by modulating gas supply to reaction zone |
CA2738459C (en) | 2010-05-20 | 2022-09-20 | Pond Biofuels Inc. | Recovering make-up water during biomass production |
CA2738397C (en) | 2010-05-20 | 2022-08-16 | Pond Biofuels Inc. | Producing biomass using pressurized exhaust gas |
CA2738410C (en) | 2010-05-20 | 2022-09-20 | Pond Biofuels Inc. | Diluting exhaust gas being supplied to bioreactor |
US20110287405A1 (en) | 2010-05-20 | 2011-11-24 | Pond Biofuels Inc. | Biomass production |
US20120156669A1 (en) | 2010-05-20 | 2012-06-21 | Pond Biofuels Inc. | Biomass Production |
EP2571978A4 (en) | 2010-05-20 | 2014-09-03 | Pond Biofuels Inc | Biomass production |
EP2422870A1 (en) | 2010-08-26 | 2012-02-29 | SFN Biosystems, Inc. | Extraction of co2 gas |
US20120203714A1 (en) | 2011-02-04 | 2012-08-09 | Pond Biofuels Inc. | Systems for Growing Phototrophic Organisms Using Green Energy |
WO2014063229A1 (en) | 2012-10-24 | 2014-05-01 | Pond Biofuels Inc. | Process of operating a plurality of photobioreactors |
-
2011
- 2011-04-27 US US13/095,490 patent/US20120276633A1/en not_active Abandoned
-
2012
- 2012-04-26 TW TW101114893A patent/TW201243045A/en unknown
- 2012-04-27 WO PCT/CA2012/000403 patent/WO2012145835A1/en active Application Filing
- 2012-04-27 AU AU2012248080A patent/AU2012248080A1/en not_active Abandoned
- 2012-04-27 CN CN201280031706.3A patent/CN103946368A/en active Pending
- 2012-04-27 EP EP12776555.0A patent/EP2702134B1/en active Active
- 2012-04-27 CA CA2834279A patent/CA2834279C/en active Active
-
2016
- 2016-01-08 US US14/991,563 patent/US11124751B2/en active Active
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20090047722A1 (en) * | 2005-12-09 | 2009-02-19 | Bionavitas, Inc. | Systems, devices, and methods for biomass production |
US8262776B2 (en) * | 2006-10-13 | 2012-09-11 | General Atomics | Photosynthetic carbon dioxide sequestration and pollution abatement |
US20090087898A1 (en) * | 2007-09-06 | 2009-04-02 | Clearvalue, Inc. | Methods, processes and apparatus of sequestering and environmentally coverting oxide(s) of carbon and nitrogen |
US20100021361A1 (en) * | 2008-07-23 | 2010-01-28 | Spencer Dwain F | Methods and systems for selectively separating co2 from a multi-component gaseous stream |
Non-Patent Citations (1)
Title |
---|
Stewart et al. A study of methods of carbon dioxide capture and sequestration - the sustainability of a photobioreactor approach. Energy Conservation and Management. 2005. Vol. 46, pages 403-420. * |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11512278B2 (en) | 2010-05-20 | 2022-11-29 | Pond Technologies Inc. | Biomass production |
US11612118B2 (en) | 2010-05-20 | 2023-03-28 | Pond Technologies Inc. | Biomass production |
US9534261B2 (en) | 2012-10-24 | 2017-01-03 | Pond Biofuels Inc. | Recovering off-gas from photobioreactor |
US20140242681A1 (en) * | 2013-02-28 | 2014-08-28 | Julian Fiorentino | Photobioreactor |
US20140242687A1 (en) * | 2013-02-28 | 2014-08-28 | Julian Fiorentino | Photobioreactor |
US9347030B2 (en) * | 2013-02-28 | 2016-05-24 | Julian Fiorentino | Photobioreactor |
US10160941B2 (en) | 2013-02-28 | 2018-12-25 | Julian Fiorentino | Photobioreactor |
US20150007495A1 (en) * | 2013-07-08 | 2015-01-08 | Electric Energy Express Corporation | Autonomously controlled greenhouse cultivation system |
US9161497B2 (en) * | 2013-07-08 | 2015-10-20 | Electric Energy Express Corporation | Autonomously controlled greenhouse cultivation system |
Also Published As
Publication number | Publication date |
---|---|
CA2834279C (en) | 2023-04-11 |
CA2834279A1 (en) | 2012-11-01 |
TW201243045A (en) | 2012-11-01 |
AU2012248080A1 (en) | 2013-11-14 |
EP2702134A4 (en) | 2015-01-21 |
US20160115439A1 (en) | 2016-04-28 |
WO2012145835A1 (en) | 2012-11-01 |
US11124751B2 (en) | 2021-09-21 |
EP2702134B1 (en) | 2017-08-30 |
CN103946368A (en) | 2014-07-23 |
EP2702134A1 (en) | 2014-03-05 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US11124751B2 (en) | Supplying treated exhaust gases for effecting growth of phototrophic biomass | |
CA2738418C (en) | Process for growing biomass by modulating inputs based on changes to exhaust supply | |
AU2020250220B2 (en) | Biomass production | |
US20160115433A1 (en) | Light energy supply for photobioreactor system | |
CA2738410C (en) | Diluting exhaust gas being supplied to bioreactor | |
CA2738459C (en) | Recovering make-up water during biomass production | |
CA2738397C (en) | Producing biomass using pressurized exhaust gas | |
US10876728B2 (en) | Process for managing photobioreactor exhaust | |
US11612118B2 (en) | Biomass production | |
CA2738461A1 (en) | Process for growing biomass by modulating gas supply to reaction zone | |
US20130316439A1 (en) | Biomass production | |
US11512278B2 (en) | Biomass production | |
EP3424306A1 (en) | Biomass production | |
US20110287523A1 (en) | Recovering make-up water during biomass production |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: POND BIOFUELS INC., CANADA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:GONZALEZ, JAIME A.;KOLESNIK, MAX;MARTIN, STEVEN C.;REEL/FRAME:026758/0936 Effective date: 20110713 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |