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WO2010142004A2 - Système d'élevage aquatique biologiquement sûr contrôlé dans un environnement confiné - Google Patents

Système d'élevage aquatique biologiquement sûr contrôlé dans un environnement confiné Download PDF

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Publication number
WO2010142004A2
WO2010142004A2 PCT/BE2010/000044 BE2010000044W WO2010142004A2 WO 2010142004 A2 WO2010142004 A2 WO 2010142004A2 BE 2010000044 W BE2010000044 W BE 2010000044W WO 2010142004 A2 WO2010142004 A2 WO 2010142004A2
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WIPO (PCT)
Prior art keywords
farming
bioreactor
water
farming system
reactor
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.)
Ceased
Application number
PCT/BE2010/000044
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English (en)
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WO2010142004A8 (fr
WO2010142004A3 (fr
Inventor
Jean-Marie Aerts
Daniel Berckmans
Peter De Schryver
Bruno Goddeeris
Patrick Sorgeloos
Stijn Van Hoestenberghe
Willy Verstraete
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Katholieke Universiteit Leuven
Universiteit Gent
Original Assignee
Katholieke Universiteit Leuven
Universiteit Gent
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from GB0910007A external-priority patent/GB0910007D0/en
Priority claimed from GB0910178A external-priority patent/GB0910178D0/en
Priority claimed from GB0911415A external-priority patent/GB0911415D0/en
Priority claimed from GB0913882A external-priority patent/GB0913882D0/en
Priority claimed from GB0915161A external-priority patent/GB0915161D0/en
Application filed by Katholieke Universiteit Leuven, Universiteit Gent filed Critical Katholieke Universiteit Leuven
Publication of WO2010142004A2 publication Critical patent/WO2010142004A2/fr
Publication of WO2010142004A3 publication Critical patent/WO2010142004A3/fr
Publication of WO2010142004A8 publication Critical patent/WO2010142004A8/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • A—HUMAN NECESSITIES
    • A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
    • A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
    • A01K63/00—Receptacles for live fish, e.g. aquaria; Terraria
    • A01K63/04—Arrangements for treating water specially adapted to receptacles for live fish
    • 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
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/58—Reaction vessels connected in series or in parallel
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C12M29/12—Pulsatile flow
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates generally to a controlled farming system, in particular an intensive and recirculating aquatic farming system (IRAFS) in a confined space. More particularly present invention concerns a system and method for farming of crops or aquatic multicellular consumer organism (e.g. animals) with improved control of the systems components for optimal use of the biomass and energy input and less energy and biomass waste output.
  • IRAFS intensive and recirculating aquatic farming system
  • Such recirculating farming systems are for aquatic multicellular consumer organism (e.g. aquatic animals) or for (soil less) crops (recirculating hydroponics) or a combination thereof and they are in a confined space whereby the farming system is monitored and controlled by a hard and soft sensing system for energy efficient and bio secure farming of aquatic organisms or crops in such a confined space.
  • the present invention relates to improving the bio security and the stability of an aquatic farming system, in particular an intensive recirculating farming system for aquatics animals or hydroponics plant, by a control system that controls reactors to restore the biosystem's homeostasis.
  • Aquatic farming systems can integrate the interaction of condominiums each of diverse organisms and the recirculation of water or watery media at least in part and at least between some of the condominiums.
  • the bulk of the aquaculture waste produced by aquatic animal, which constitutes metabolic wastes and uneaten feed, can for instance be bioremediated by condominiums of other organisms.
  • aerobic nitrifying bioreactors are for instance used to transform ammonium to nitrate.
  • Such aerobic biological water filtration (aerobic BOD removal and nitrification) is commonly used to prevent the accumulation of nitrogen compounds, as ammonium and nitrite, which have a deleterious impact on water quality and the growth of aquatic animals (e.g. fish growth).
  • Aerobic biological water filtration mainly digest dissolved organic material and oxidizes ammonium-ions via nitrite to nitrate (two-step nitrification) by heterotrophic bacteria like Nitrosomona sp., Nitrospria sp. and Nitrobacter sp.
  • MBB moving bed biofilters
  • nitrate nitrogen is usually removed in the drain and part of the water is replaced by clean water.
  • Modern recirculating aquaculture systems combine aerobic nitrification with mechanical removal of the particulate and colloidal organic matter of the solved nitrogen compounds to remediate the toxic ammonia to less toxic nitrates. In general at least 10% of the water has to be replaced by daily fresh water input.
  • the recirculating aquaculture systems aquatic animal farming thus produces different organic waste streams that are typically of higher temperature, loaded with high organic and nutrient loads. Approximately 3 to 10 kg of phosphorus and 39 to 55 kg of nitrogen are released to the environment for every metric ton of fish that is produced (Bureau et al. N.AM J. Aquaculture: 65 (1): 33 - 38).
  • Bacterial bioreactors and units with aquatic animals can eventually used to deliver irrigating water to soilless aquatic plants or terrestic plants with their roots in aquatic medium.
  • greenhouse hydroponics crop culture on the other hand, and in particular the soilless culture re -uses only a part of its heated culture water.
  • 50% of the first culture water is drained (waste drain) to avoid salt and mineral accumulation by recirculation.
  • the current aquaculture bioremediation systems do not deliver a watery drain medium that as such can be used for efficient integration of aquatic animal and soilles crop culture.
  • the integration of aquatic animal farming in intensive aquaculture with soilless aquatic plants or terrestic plants culture with recirculation of the culture water to the aquatic animal has been found to be difficult and is so far not commercially successful.
  • Present invention provides such system by a controlled biomass input (for instance aquatic animal feed without or with low fishmeal diets), by a controlled energy production and by controlled energy and biomass redistribution through a controlled exchange of organic matter, CO 2 , nitrogen, O 2 and heat between the connected bioreactors of this farming system and between the farming system and the drain (e.g. the drain storage tank) and by solving the biosecurity problems that are inherent at intensive aquaculture in recirculating systems and its integration with soilless crop culture.
  • a controlled biomass input for instance aquatic animal feed without or with low fishmeal diets
  • a controlled energy production for controlled energy production and by controlled energy and biomass redistribution through a controlled exchange of organic matter, CO 2 , nitrogen, O 2 and heat between the connected bioreactors of this farming system and between the farming system and the drain (e.g. the drain storage tank)
  • the drain e.g. the drain storage tank
  • the correct dosage is the crucial step, otherwise toxic compounds like nitrite nitrogen or hydrogen sulphide can be formed.
  • the quantity required for denitrification has to be calculated on basis of the influent nitrate, nitrite and dissolved oxygen concentrations. This level of complexity prevents that denitrification is commonly used in recycling closed systems aquaculture. There is a clear need in the art for improving nitrogen removal of the culture water of aquatic organisms.
  • the current recycling closed systems for the cultivation of aquatic multicellular consumer organism e.g.
  • aquatic animals provide also removal techniques, such as sedimentation, filtration and flotation, for the removal of particulate wastes (faeces, uneaten feed, and bacteria floes) and reduction of load of suspended organic solids and in particular to very fine organic particles, which generally will impact negatively the water quality in such systems with insufficient bioreactor digestion.
  • the systems can also be provided with an ozone or UV disinfection units. UV disinfection is generally used in recirculating farming systems for aquatic multicellular consumer organism (e.g. aquatic animals) or recirculating hydroponics for (soilless).
  • the invention is broadly drawn to an energy efficient controlled farming system in a confined environment.
  • the fluid in this system may be a gas, a liquid or a combination of both.
  • the gas is can be an atmospheric gas and the liquid is preferably water or a watery medium, which can carry various other organic and inorganic compounds.
  • the controlled biomass farming system is designed for processes of redistribution of energy and biomass in a controllable manner.
  • the present invention 1) solves the problems of the related art of the high cost of intensive agriculture systems in confined environments such as land based in indoor aquaculture recirculating systems and of the greenhouse crop culture, in particular the hydroponics and 2) prevents the well known occasional event biosystem collapse in such farming systems in particular if indoor recirculating aquaculture is integrated with hydroponics crops culture. Moreover, it solves the problem of the negative impact of these systems on the outer environments.
  • the farming system of present invention comprises a bioenergy producing bacterial bioreactor system, which is integrated in the farming system for bioremediation of organic and inorganic compounds in the farming system.
  • the controlled farming system comprises reactors, e.g. bioreactors for bioremediation and/or energy production (e.g. biofermentor, biogasification reactor or microbial fuel cell) and physicochemical reactors (e.g. photocatalytic or electrochemical), where under at least some are bioreactors and storage containers, which are interconnected and exchange fluids, energy and biomass with other bioreactors or with the confined environment in a controlled or controllable manner.
  • the flows or transport of the energy, biomass or molecule in the internal environment of the reactors, in the storage containers and eventually also in the confined space (which comprise the reactors and storage container) are at least in a particular embodiment, controlled for energy efficient farming of aquatic multicellular consumer organism (e.g. aquatic animals) and crops with a minimal waste of energy and material in the external environment.
  • pH control The pH is an important abiotic factor for biocatalysts operations, electrochemical and photocatalytic operations and the survival and function of plants, animals and microbial. Hard and soft sensing can be also used to monitor and control the pH and alkalinity and to obtain optimal pH and/or alkalinity in particular in the aquatic organism farming units by activation of reactor actuators, such as a photocatalytic reactor, bioreactor and nitrogen removal in the aquatic farming system.
  • reactor actuators such as a photocatalytic reactor, bioreactor and nitrogen removal in the aquatic farming system.
  • This pH and alkalinity control is aimed at reducing toxicity, in particular nitrogen toxicity, on the living organism and at preventing bio system collapse.
  • the system of present invention to control the pH, alkalinity and solved nitrogen is particularly suitable for an aquatic farming system that needs a normo-pH suitable for the integration intensive recirculating farming of aquatic multicellular consumer organism (e.g. animals) with the farming of soilless hydroponics crop farming.
  • Components included in the recirculation system are in an embodiment a specific coating used to enhance the biosecurity and or biosafety.
  • the biosafety for farmed organisms can be further enhanced by an antimicrobial and in particular an antibiofilm forming coat on the insight surface of fluid transport tools (piping) or at least in part of the fluid transport tools (pipings) between different reactors of the farming system.
  • This antimicrobial and in particular antibiofilm forming coat is a layer in side the fluid transport systems that contacts the fluids in particular the watery fluids that pass such transport piping.
  • This coating enhances the disinfection activity of photolytic systems such as the UV lamp disinfectors or the photocatalytic (near UV or UV-VIS) systems or the hybrid photocatalytic ultrasound/photocatalyis microbial cell destruction systems.
  • photolytic systems such as the UV lamp disinfectors or the photocatalytic (near UV or UV-VIS) systems or the hybrid photocatalytic ultrasound/photocatalyis microbial cell destruction systems.
  • Less living or viable micro organisms (in particular bacteria) pass the photolytic disinfection system, in particular the US disinfectors, which can be demonstrated by plating on a nutrient bottom.
  • Reduced uncontrolled biofilm forming on places of low liquid velocity and hydrodynamic forces in zones between the diverse bioreactors and consequent biofilm detachments can be demonstrated.
  • Photolytic disinfection systems or surface treatments. Biofilm organised organism (floes) passing the photolytic systems might be at the basis of higher survival than for planktonic microbial.
  • Such coat can be further foreseen by a zero-valent iron capable of adsorbing waterborne viruses.
  • This extra safety control system is efficient for preventing bio system collapse.
  • This biomass farming system comprising in a particular embodiment separate bioreactor units in a shared confined environment or in different fluid flow interconnected confined environments with a fluid input and fluid output, whereby the biomass farming system comprises 1) an aquaculture system for the culture of aquatic multicellular consumer organism such as aquatic vertebrate animals or such as aquatic invertebrate animals, and further
  • At least one bacterial bioreactors system comprising condominiums of producers bacteria and condominiums of consumer bacteria in a same or separate bioreactor
  • this further comprises 4) a photocatalytic bioreactor system comprising at least one bioreactor of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)).
  • the bacterial bioreactors system comprises an energy production system (bioenergy system) bioreactor, whereby the energy is used to drive actuators of the system.
  • the bioreactor system hereby comprise a least one circuit to feed electricity generated by the bio-electrochemical bacteria assisted biotransformation system or electricity generated by a gas fired electricity/heating or cooling generator
  • CHP unit e.g. a Stirling engine or a Dash Micro CHP, that is fired by the energy rich gas from a biofermentor, to at least one of the systems actuators (for instance a pump actuator to move system fluids or the chemoelectric reactor or the radiation source (for instance the lamp, the microwave generator or the ultrasound generator ) of a photocatalytic reactor).
  • the systems actuators for instance a pump actuator to move system fluids or the chemoelectric reactor or the radiation source (for instance the lamp, the microwave generator or the ultrasound generator ) of a photocatalytic reactor.
  • the systems actuators for instance a pump actuator to move system fluids or the chemoelectric reactor or the radiation source (for instance the lamp, the microwave generator or the ultrasound generator ) of a photocatalytic reactor.
  • the systems actuators for instance a pump actuator to move system fluids or the chemoelectric reactor or the radiation source (for instance the lamp, the microwave generator or the ultrasound generator ) of a photocatalytic reactor.
  • bioenergy system comprises in a particular embodiment an anaerobic bioreactor with methanogenic reaction function that produces energy rich that drives a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • the degradation of organic matter by anaerobic respiration releases electrons that for disposal are accepted or 1) by an anode and distributed by an electric circuit to produce electricity or 2) by molecule electron acceptors such as CO 2 , or NO 3 " to produce energy rich gas or a combination of both.
  • Power to drive the actuator of the aquatic farming system is directly generated by the anaerobic bioreactor system or indirectly by burning its gas in a CHP system.
  • the electron acceptor is an anode connected by a circuit to a cathode bioelectricity can be produced.
  • a suitable bioreactor for the production of energy rich gasses is the high rate anaerobic reactor up flow anaerobic sludge blanket (UASB) the anaerobic sequencing batch reactor (ASBR), the fluidized expanded bed reactor, the static granular bed reactor (SGBR), the anaerobic membrane reactor, the anaerobic expanded-bed reactor (EBR) and the granular bed baffled reactor (GRABBR).
  • UASB anaerobic sequencing batch reactor
  • SGBR static granular bed reactor
  • EBR anaerobic expanded-bed reactor
  • GRABBR granular bed baffled reactor
  • Such bacterial reactor system can receive the solved and particulate waste material.
  • the organic material is first collected in a collection tank that feeds the gasification bioreactor.
  • Such collection tank can function as a concentration tank or as a buffer tank.
  • the organic matter particles are first fluidized for instance by ultrasound or before the organic and inorganic matter is fed into the gasification bioreactor.
  • the organic and inorganic matter is fed into the gasification bioreactor it is preferably partially mineralized in a photocatalyst reactor hybrid ultrasonic/ photocatalytic or hybrid microwave/ photocatalytic.
  • the gaseous products such as CH 4 of the gasification bioreactor is transported to a gas collection container and transported to a heat burner that drives the gas driven heat pump system.
  • the bacterial bioreactors system is an energy production system
  • a gas driven heat pump system preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • This heat pump preferably is a reversible absorption heat pump such as a reversible air-water absorption heat pump.
  • the reversed absorption heat pump is in a preferred embodiment connected in a variable flow control system (as outlined for instance in fig 10 and fig. 11).
  • the farming system can have a closed container for collecting of rain and or ground water (water input tank or clean water basin).
  • the reversed absorption heat pump system with variable flow control system can distribute heat between the water input tank, that farming system and the drain.
  • variable flow control system is a indoors with outdoors mixed system that is connecting at least one heat releasing or heat extracting unit with the outer environment for instance with the bottom under frost line and/or the air of the out environment.
  • the farming system can have a closed container for collecting of rain and or ground water (water input tank).
  • the reversed absorption heat pump system with variable flow control system can distribute heat between the water input tank, that farming system and the drain.
  • the variable flow control system is a indoors with outdoors mixed system that is connect an heat releasing or heat extracting unit with the outer environment for instance with the bottom under frost line and/or the air of the out environment.
  • drive energy is gas it is particularly energy efficient in maintaining the fluids of the different units at a desired temperature. Not only produces farming system its own drive energy but it also has a considerable lower energy loss.
  • Electrically-driven heat pumps for heating buildings typically supply 100 kWh of heat with just 20-40 kWh of electricity. But the efficiency of electric power plants is only about 25-40%.
  • such gasification bioreactor is foreseen with an in situ pH sensor for monitoring the pH.
  • the bioreactor systems are constructed to exchange watery fluid and gas fluid in a controlled manner under control of a monitoring and control system.
  • the system can for instance comprise a hard sensing tool to produce a signal indicative of an abiotic parameter such as pH, and temperature and a controller to control at least one programmable actuator to adapt these abiotic parameters.
  • the system comprises at least one programmable actuator adapted to deliver a pH regulator agent to said system at an administration rate and at least one programmable heat and/or cool actuator to cool or heat the system.
  • this controlled biomass farming system in confined environment with controlled biomass input and output and energy input and output comprises a controlled biotransformation system for bioremediation or redistribution of nutrients and energy in a controlled manner between bioreactors of living organisms.
  • biotransformation system comprises at least one pump actuator to move the system fluids and at least three bioreactor systems of communicating fluids where under
  • At least one of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)) assisted biotransformation for instance an autotrophic plant assisted biotransformation unit, and
  • bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and to produce bioelectricity that drives actuators of the farming system b) at least one autotrophic (chemolithotrophic) bio-electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD and to produce bioelectricity that drives actuators of the farming system or at least one bio- electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor to reduce nitrogen and decrease cBOD and to produce bioelectricity that drives actuators of the farming system
  • chemolithotrophic bio-electrochemical bacteria and heterotrophic bio-electrochemical bacteria can be an up flow sludge blanket filter
  • USBF Ultraviolet
  • Such USBF fuel cell operates a process of up flow sludge blanket filtration which has a substantially higher specific rate of separation that the conventional sedimentation USBF technology and uses up flow sludge blanket filtration in a prism or cone shaped clarifier.
  • the activated sludge floes or granules that have been generated by high shear in the aerated unit will enter the clarifier at the bottom and, as it rises, upward velocity decreases until the floes of cells become stationary, effectively filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity, while descending to the bottom of the clarifier and are transferred back into the anoxic zone of the sludge floes or sludge (bio)granules that become large and heavy.
  • USBF fuel cell operates aeration, nitrification, denitrification, clarification and sludge thickening and stabilization without need of different dedicated vessels. All these processes can be integrates into one bioreactor and can be operates inside one compact bioreactor.
  • this controlled biomass farming system in confined environment with controlled biomass energy input and output and energy input and output comprises a controlled biotransformation system for bioremediation or redistribution of nutrients and energy in a controlled manner between bioreactors of living organisms, whereby the biotransformation system comprises at least one pump actuator to move the system fluids and at least three bioreactor systems of communicating fluids where under 1) at least one heterotrophic aquatic animal assisted biotransformation unit; 2) at least one of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)) assisted biotransformation for instance an autotrophic plant assisted biotransformation unit and
  • the biotransformation system comprises at least one pump actuator to move the system fluids and at least three bioreactor systems of communicating fluids where under 1) at least one heterotrophic aquatic animal assisted biotransformation unit; 2) at least one of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)) assisted biotransformation for instance an autotroph
  • bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio-electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio- electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor whereby the system is further characterised in that the bio-electrochemical bacteria assisted biofilters are bioelectricity producers that are connected by a circuit to drive one or more heat pump system on the bioelectricity from the bio-electrochemical bacteria assisted biofilter or bioremediation system and further characterised in that heat pump system is connected by a loop with
  • the controlled biomass farming system further comprises a system for photocatalytic oxidation of water from or to the aquaculture system.
  • a system for photocatalytic oxidation is particular suitable for preventing unwanted algae growth, for oxidizes the organic matter, for reducing BOD and for destroying unwanted microbiological organisms and delivers the minerals free of toxic metabolites as a nutrient to the (photo)autotrophic micro organisms and plants.
  • Such systems is preferably placed above the aquaculture system in a confined environment (e.g. a greenhouse) for solar driven photocatalytic oxidation or on the roof of the confined environment of the aquaculture system (e.g.
  • the photocatalytic oxidation system can also be incorporated in a lamp (e.g. UV, near UV or UV-VIS light) radiated fluid flow through case or container that receives fluid from the aquaculture system and/or the photocatalytic bioreactor system (combi photocatalytic oxidation / UV lamp) witch lamps can be system actuators that receive drive current generated by the system.
  • a lamp e.g. UV, near UV or UV-VIS light
  • the photocatalytic bioreactor system combi photocatalytic oxidation / UV lamp
  • lamps can be system actuators that receive drive current generated by the system.
  • photocatalytic oxidation suspended solids can be removed by mechanical filtration to further reduce BOD, COD, Chemicals and TSS.
  • such photcatalytic bioreactor is used to mineralise organic molecules in fluids before presenting to the bioreactors and/or before presenting to cultured crops in particular to the hydroponics culture, the soilless (photo)autotrophic crop culture or the suspended unicellular (photo)autotrophic crops.
  • the bioreactor operation is integrated with a physicochemical (e.g. photocatalysis or electrochemical) operation whereby a bioreactor, a physicochemical reactor and a control system operationally connected to 1) a sensing means that feeds signals into the control system whereby the sensing means are for analysing physical quantities in reactor or reactor output (physicochemical reactor and/or bioreactor) and for converting such it into a signal which when operational is be fed into the control system and 2) to an actuator system of said physicochemical reactor to feed a control system into said actuator system to control the physicochemical reaction.
  • a physicochemical e.g. photocatalysis or electrochemical
  • the control system can operate as a feed back system but can also comprise a model, preferably an adaptive model to control said the physicochemical reaction directly and indirectly the biofiltration operations.
  • Physical measurements of the sensors that are converted into an input signal for the control system are for instance measurements of oxidizable species (RX a d) of intermediates (from for instance a OH or end products quantities (e.g.
  • factors that determine the model are reactor volume of the physicochemical reactor and bioreactor , concentration of the chemical species to be oxidized, the catalyst concentration, time in the physicochemical reactor, catalytic physicochemical reaction rate, mixing and circulation rates of the fluids, in case of a photocatalytic physicochemical reactor the irradiation and/or the irradiation volume.
  • Quantities of the ferric ion, Fe 3 + photoxidation rate modifier can be sensed for feeding a signal into a controller to control the levels of the ferric ion below a certain threshold for instance a value below 5 ppm and above 0.5 ppm.
  • the bacterial bioreactors system is an energy production system (bioenergy system) that drives a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • the bacterial reactor system that produces the energy to drive the heat pump system comprises an anaerobic bioreactor (fig 2) or aerobic bioreactor (fig 3) or the combination of both (fig 5) comprising a condominium of bioelectrical bacteria whereby the degradation of organic matter on release electrons that for disposal are accepted by an electrode (anode) and distributed by an electric circuit.
  • Such bacterial reactor system can receive the solved and particulate material.
  • the organic material is first collected in a collection tank that feeds the gasification bioreactor.
  • Such collection tank can function as a concentration tank or as a buffer tank.
  • the fluidization of the organic matter particles for instance by ultrasound before the organic and inorganic matter is fed into the gasification bioreactor.
  • the organic materials in the fluid of this collection tank is mineralized by photocatalysis. If the organic material is mineralized by the photoctalytic reaction or reactor higher yields of bioenergy production (bioelectricity) are obtained in the bioelectrical reactor (MFC).
  • the electrical circuit of the bioelectrical reactor delivers the energy that drives the heat pump system.
  • the bacterial bioreactors system is an energy production system (bioenergy system) that produces the electricity that drives a heat pump system preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • This heat pump preferably is a heat pump that preferably operates in a reversible manner for instance a reversible absorption heat pump such as a reversible air-water absorption heat pump (described in EP 1558881).
  • the reversed absorption heat pump is in a preferred embodiment connected in a variable flow control system.
  • the autotrophic bacteria assisted biotransformation unit can be a nitrifying bacterial fuel cell comprising autotrophic bio-electrochemical bacteria and the heterotrophic bio- electrochemical bacteria assisted biotransformation unit can be a denitrifying bacterial fuel cell.
  • the denitrifying bacterial fuel cell and the nitrifying bacterial fuel cell can be flow through fuel cells whereby the water of the farming systems flows through the bacterial fuel cell(s) .
  • the autotrophic bio-electrochemical bacteria assisted biotransformation unit comprises Nitrosomonas europea.
  • the heterotrophic bio-electrochemical bacteria assisted biotransformation comprises Geobacter sulfurreducens, Shewanella oneidensis, Rhodoferax ferrireducens or a combination thereof.
  • the electricity produced by the bioelectrical energy system generates electrical energy to at least one of the actuators of the system for instance to a pump actuator of the system or to a heat pump that transports heat from the drain to bioreactors of the farming system.
  • the controller of the system furthermore can control the fluid flows between the bioremediation units.
  • the bacterial bioreactors system is an energy production system (bioenergy system) that drives a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • the bacterial reactor system that produces the energy to drive the heat pump system comprises an anaerobic bioreactor or aerobic bioreactor or the combination of both (Fig 5) comprising a condominium of bacteria whereby the degradation of organic matter on release electrons that for disposal are accepted by molecule electron acceptors such as
  • the organic material is first collected in a collection tank that feeds the gasification bioreactor.
  • a collection tank can function as a concentration tank or as a buffer tank.
  • the fluidization of the organic matter particles for instance by ultrasound before the organic and inorganic matter is fed into the gasification bioreactor.
  • the organic materials in the fluid of this collection tank is mineralized by photocatalysis, eventually by ultrasound or a combined ultrasound photocatalysis mineralization. If the organic material is mineralized by the photoctalytic reaction or reactor with higher yields of bioenergy production (energy rich gas) are obtained in the gasification tank).
  • Gasification tank delivers the energy rich gas to a burner that drives the heat pump system.
  • the gasification system is an energy production system (bioenergy system) that produces the electricity that drives a heat pump system preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • This heat pump preferably is an absorption heat pump or a Vuilleumier heat pump that preferably operates in a reversible manner for instance a reversible absorption heat pump such as a reversible air- water absorption heat pump (described in EP 1558881).
  • the reversed absorption heat pump is in a preferred embodiment connected in a variable flow control system.
  • the bacterial bioreactors system is an up flow anaerobic sludge blanket reactor or an up flow aerobic sludge blanket reactor or a combination of both.
  • a bacterial bioreactors system to filter the water of the farming system while generating floe particles or generating biogranules.
  • Floe particles are for instance agglutinated microbial for instance by bacterial enzyme rich polysaccharide slime. They may comprise condominiums of different microbial, such heterotrophic bacteria, alga (e.g. dinoflagellates & diatoms), fungi, ciliates, flagellates, rotifers, nematodes, metazoans).
  • the average floe diameter is generally 0.2 mm to 2 mm. Particularly interesting is that the floes have 25% to 56 % proteins and about 25 % to 29% organic carbons and high levels of amino acids that can be processed in useful feed biomass to be redistributed in the farming systems in feed for the aquatic multicellular consumer organism (e.g. aquatic animals).
  • the formation aerobic and anaerobic granules can be enhanced under aerobic or anaerobic conditions by subjecting bacterial sludge shear conditions and eventually a substrate. Such biogranules have a diameter of 2 to 8 mm.
  • biogranules formed under aerobic conditions are composed of an inner denitrifying microbial zone and an outer nitrifying zone, hi an embodiment of present invention such biogranules are used to inoculate biofilters. Premineralization or photocatalysis enhances the bioremedciation activity of the floe or biogranule reactor.
  • biogranules are produced in separate controlled biofloculation units inoculated with selected bacteria for inoculating biofilters or selected probiotic bacteria to protect the faming system against the invasion of unwanted microbials.
  • probiotic bacteria can for instance be bacterial of the bacillus species such as the bacteria of the group consisting of Bacillus licheniformis (B. licheniformis), B. subtilis, B. polymixa, B. laterosporus and B.
  • circulans that are facultative anaerobes and can contribute to nitrification and denitrif ⁇ cation and bacillus species that are probiotic for the aquatic organisms and can protect the farming systems against invasion of food spoiler microbials or against pathogens that are known to be pathogens (for instance food born pathogens) to animals such as aquatic animals or to mammalian which consume the aquatic multicellular consumer organisms (e.g. aquatic animals) or the crops of the farming system of present invention.
  • pathogens for instance food born pathogens
  • biogranules are used to remove nitrogen and phosphate and in an embodiment of present invention such biogranules are sterilized and used as a raw material in designer feed to protect the aquatic organisms against pathogens.
  • the controlled a farming system comprising a controller to control the programmable pH actuator to normalize the pH between 5,5 and 8 (preferably between 6 — 7.5) and to control the heat and/or cool actuator to normalize the temperature between 15 - 30°C (preferably between 20 — 25°C).
  • a particular useful pH regulator agent is an alkalis of the group consisting of calcium bicarbonate, calcium carbonate, calcium hydroxide, magnesium bicarbonate, magnesium carbonate, magnesium hydroxide, sodium bicarbonate, sodium carbonate and sodium hydroxide.
  • a bacterial assisted unit of chemo organotrophic bacteria derives carbon and energy of oxidation of organic compounds and decrease cBOD (by concerting it in carbon dioxide, water, ammonium ions, phosphate ions and sulphate ions) and increase the alkalinity/pH.
  • the unit is assisted by bio-electrochemical bacterial heterotrophs that generate bioelectricity.
  • a condominium of autotrophic bacteria oxidize nBOD (that oxidize ammonium and nitrite ions).
  • the bioelectricity drives actuators of the IRAFS.
  • the mineralized nutrients are delivered to a mixing unit or mixing tank (167) that delivers the water to an hydroponics or soilless plant culture.
  • the water storage (168), the drain water tank (159) that receives the (dirty) water of the hydroponics culture, the soilless crop culture system or the crop greenhouse culture (163) ) and the clean water tank (157) that stores ground water, rain water or other clean water, are connected with a transport piping or irrigation system to a mixing unit or mixing tank (167).
  • There water supply to the mixing unit or mixing tank (167) is under control of a multiple switch valve (160) to control their water flow towards the mixing unit or mixing tank (167).
  • a sterilization and/or mineralization unit preferably a flow through sterilization unit that comprises a UV radiation source (166) to radiate the passing through water or eventually an ozonation system as a germicidal treatment or a that comprises a photocatalyst with a near UV, near UV or UV- VIS radiation source (166) depending on the type of photocatalyst.
  • the hydroponics culture, the soilless crop culture system or the crop greenhouse culture (163) comprises chemical (nutrient) stock solution tank(s) (162), of which one a acid stock solution tank (162) and another base stock solution tank (162), that all have an transport pipe that passes dosing or reservoir pumps (159) for comprising a desired nutrient solution, pH and alkalinity for instance in the diluter (161) or in the mixing unit or mixing tank (167).
  • the diluter (161) or the mixing unit or mixing tank (167) have an irrigation or transport piping to the plant growing troughs (164).
  • the plant growing troughs (164) are connected by a transport piping or irrigation with a drain pit (165) that is connected by a transport piping or irrigation with the drain storage tank (158).
  • the system is be controlled by a liquid control system that controls the (nutrient) dosing or reservoir pump, the nutrient solution pH, the nutrient electric conductivity, nutrient solution and condensate water levels.
  • another embodiment of present invention is a condominium of chemo organotrophic bacteria (heterotrophs) in a bioelectricity (bioelectricity generating) reactor unit or microbial fuel cell (MFC) in a setup to generate current to drive the heat pumps system for transporting heat from one reactor unit of the IRAFS or to transfer heat of the drain that otherwise would be lost into the IRAFS or to drive specific actuators in the controlled farming system.
  • chemo organotrophic bacteria heterotrophs
  • MFC microbial fuel cell
  • the IRAFS can comprise a nitrification bacterial fuel cell for addition of oxygen to nitrogen while generating bioelectricity.
  • reduced substrates such as reduced nitrogen
  • ammonium and nitrite ions are oxidized resulting in a decrease of nBOD with the generation of oxidized nitrogen species and in the generation of electrons and protons.
  • the bioelectricity is used to drive specific actuators of the IRAFS for instance the heat pumps system for transporting heat from one reactor unit of the IRAFS or to transfer heat of the drain that otherwise would be lost into the IRAFS or to drive specific actuators in the controlled farming system.
  • an embodiment of present invention is a fluid communication system between separate systems and units of the controlled farming system, IRAFS of present invention whereby the both autotrophic bacteria nitrifying and chemo organotrophic bacteria (heterotrophs) denitrifying bacterial condominiums are produce current to drive the heat pump system or specific actuators (for instance the sensors , pumps or controllers) in the controlled agriculture system.
  • the bioelectricity is used to drive specific actuators of the IRAFS for instance the heat pumps system for transporting heat from one reactor unit of the IRAFS or to transfer heat of the drain that otherwise would be lost into the IRAFS or to drive specific actuators in the controlled farming system.
  • a bacterial assisted unit of chemo organotrophic bacteria drives carbon and energy of oxidation of organic compounds and decreases cBOD (by concerting it in carbon dioxide, water, ammonium ions, phosphate ions and sulphate ions) and increase the alkalinity/pH.
  • the unit is assisted by bio-electrochemical bacterial heterotrophs that generate bioelectricity.
  • As displayed right upper in fig 1 concerns a condominium of autotrophic bacteria that oxidize nBOD (that oxidize ammonium and nitrite ions ) and decrease the alkalinity/pH.
  • a certain embodiment of present invention of a combined anaerobic denitrifying / aerobic nitrifying bacterial fuel cell sharing the cathode can be subjected to active or passive aeration.
  • the IRAFS farming system can in an embodiment comprise one or more drainage water collection system (drain storage tank) to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse horticulture system (GCS).
  • This drainage water collection system is a heat source or sink of the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS) or of the IRAFS.
  • the IRAFS comprises a reversed absorption heat pumps that is fired by energy rich gas of the gasification bioreactor that is integrated in the IRAFS.
  • a reversed absorption heat pumps connected in a variable flow control system and achieve the desired temperature Tx in the various reactors of the IRAFS.
  • Such temperature and heat flow system control system is important to reduce heat loss but also since aquatic animals and plants can need a different temperature regime and can need a different temperature regime in day and night time..
  • such IFARS with variable flow control system comprises at least one clean water (ground water and/or rain water) collection or storage tank (400), at least one drain water collection or storage tank with drain water of the hydroponics or a soilless plant culture unit (e.g. the greenhouse culture system (GCS)) (401), a gasification bioreactor (402), aquatic animal farming system in particular the fish culture (e.g. the recirculating aquaculture system (RAS) or recirculating aquatic animal farming system (403) which can comprise bioreactor units and drain organic waste into the gasification bioreactor or its confined environment or building (404), a hydroponics or a soilless plant culture unit (405) (e.g.
  • GCS greenhouse culture system
  • RAS recirculating aquaculture system
  • 403 recirculating aquatic animal farming system
  • 410 is a place under the frost line ground water.
  • the IRAFS systems can comprise one or more drainage water collection system to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS). This drainage water collection system is a heat source or sink for the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS) or the IRAFS.
  • At least one thermal loop comprising at least one of the compressor and working fluid expansion means (for instance an expansion valve) components and at least two heat exchangers each of the evaporator and condenser type connected in the form of a closed circuit for circulating a volatile liquid (working fluid or refrigerant), circulates through the components.
  • At least one evaporator type heat exchanger of the closed loop is in contact with a drainage water collection system.
  • the thermal loop between the drainage water collection system and the RAS and/or GCS can comprise a reversing valve and force the heat flow in the other direction.
  • Heat is then transferred in the opposite direction, from the RAS and/or GCS that is cooled, to the drainage water collection system.
  • the drainage water collection system is contacted with at least one condenser heat exchanger of a closed loop and the RAS and/or GCS with at least one evaporator type heat exchanger.
  • the IFARS comprises an heat pump system driven by bioenergy generated by at least one of its bioreactors whereby the heat pump system variable flow control system as displayed in Fig. 11.
  • the heat pump system with variable flow control system comprises heat transfer switches with reversible operation in heating mode or in cooling mode.
  • the different components are expansion valves (304), 4 way switch valve (308), two switch valves (309), condenser (301), evaporator (302), compressor (303), drain water container (300), Rain water / groundwater or clean water tank (305), aquatic animal culture tank or tanks (306), hydroponics or soilless crop culture unit(s) (307) and under frost line ground (water) (308).
  • heat can be transferred from the soilless crop culture unit(s) (307) to the aquatic animal culture tank or tanks (306) this is particularly suitable in a day and night regime.
  • the optimal or desired temperature for crop growth is maintained different from the optimal or desired temperature of the aquatic multicellular consumer organisms (e.g. aquatic animals).
  • the optimal temperature for crops in the soilless crop culture unit difference between day and night (for instance 25.5 °C at day and 17.7 °C 's at night.
  • the temperate is generally kept equal and stabilized. Controlled heat transfer maintains these different temperature regimes.
  • a removal apparatus for suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD)) for instance a screening apparatus for mechanical removal of the suspended organic solids, particulate organic matter and colloidal organic matter ((coBOD ) colloidal
  • BOD and (pBOD) particulate BOD or for instance a microscreen apparatus for removal of the suspended solids which in this picture is displayed as a side view of an incline belt screen filter (132) with a screen belt (143), or such combined with an installation for the removal of settleable solids for instance gravity separation (sedimentation) or alternatively a centrifuging or hydrocycloning apparatus can be used for removal of the suspended organic solids, particulate organic matter and colloidal organic matter or combined with a foam fractionation apparatus are used to remove organic matter.
  • the water collection tank (133) is provide with a transport line (e.g. transport pipe (141) and pump (135)) to deliver the waste to an input (131) of a gasification tank (134) as for instance displayed in fig. 13 or in fig. 14.
  • a gasification tank (134) can optionally be foreseen of a closed loop (146 & 147) to recirculate its supernatant out put.
  • the gasification tank (134) furthermore comprises on or more out put and distribution line (transport pipe) (136) to transport the energy rich gas to the heat pump firing drive system (441, 216, 204).
  • This distribution line (transport pipe) (136) can optionally distribute the gas first towards a deshydratation unit (150) and the deshydratation unit that can be connected by a distribution line (transport pipe) (151) with a gas storage unit (152) which is connected by a distribution line (transport pipe) (153) with the heat pump firing drive system (441, 216, 204).
  • the IRAFS comprises a photocatalyst bioreactor (as displayed in Fig. 15) the photocatalyst bioreactor has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • the photoctalyst unit is foreseen with a radiation unit (103) to radiate the photocatalytic material (104).
  • the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquatic animal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • An output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (134) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (134, effluent collection (137).
  • the gasification unit is provided with switch valves (154) to release its processed water via an out put or transport piping (155) or to return the water via a transport piping (99b) to the photocatalytic reactor unit (100).
  • the gasification tank (134) furthermore comprises on or more out put and distribution line (transport pipe) (136) to transport the energy rich gas to the heat pump firing drive system (441, 216, 204).
  • This distribution line (transport pipe) (136) distribute the gas first towards a deshydratation unit (150) and the deshydratation unit can be connected by a distribution line (transport pipe) (151) with a gas storage unit (152) which is connected by a distribution line (transport pipe) (153) with the heat pump firing drive system (441, 216, 204).
  • the IRAFS comprises (as displayed in Fig. 16) a photocatalytic reactor (100) and a radiation source (103) for UV light, near UV light, UV-VIS light or solar light depending on the type of photocatalyst and the photocatalyst function and optionally with function enhancement by microwave or ultrasound radiation for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytic material (104) to an aerobic bioreactor that enhances a larger part of ammonium removal through oxidizing ammonium directly into N 2 , or ammonium into NO 2 " or to reduce NO 3 " into NO 2 ' depending on the photocatalyst and/or the reaction time.
  • a radiation source for UV light, near UV light, UV-VIS light or solar light depending on the type of photocatalyst and the photocatalyst function and optionally with function enhancement by microwave or ultrasound radiation for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytic material (104) to an aerobic bioreactor that enhances a larger
  • the photocatalytic reactor can deliver such treated water to a pretank unit (101) automatically monitoring toxicity in such pretank unit to detect or measure quantities of toxicity of the photocatalytic end product and eventual intermediates of photocatalytic processing by a toxicity sensor (for instance such sensor described in this application) and subsequently at the detection of the photocatalytic function is an aspect of this invention.
  • a toxicity sensor for instance such sensor described in this application
  • a toxicity sensor for instance such sensor described in this application
  • This bioreactor is preferably a (bio)granule (144) producing bioreactor foreseen of turbulence or shear force creation means for instance a stirrer (105) for inducing biof ⁇ lm forming into (bio)granules (144).
  • the photocatalytic reactor is for seen with a transport pipe input (99) to receive water load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the aquatic farming system.
  • a transport piping connects the out put (107) eventually over a pump (108) of the photocatalytic reactor with pretank unit (101) such as an aeration or oxygenation unit (101) which is connected with a transport piping (110) with the aerobic bioreactor (102).
  • pretank unit (101) such as an aeration or oxygenation unit (101) which is connected with a transport piping (110) with the aerobic bioreactor (102).
  • a loop (106) eventually with pump (111) allows under control of a valve system (154) to return water treated in the bioreactor via a transport piping (99a) to the photocatalytic reactor input (99) or to the aeration or oxygenation unit (101).
  • This photocatalytic aerobic bioreactor system can release the photocatalyst / aerobic bioreacted water via an output (112) into the aquatic animal farming system or into the storage tanks of the soilless plant culture or hydroponics.
  • the photocatalytic reactor can also been foreseen with a transport pipe or irrigation output (98) to transport water to other units for instance to the plant hydroponics or soilless crop culture unit (Fig. 19).
  • a transport pipe or irrigation output (98) to transport water to other units for instance to the plant hydroponics or soilless crop culture unit (Fig. 19).
  • the pretank (101) and the photocatalytic reactor (100) are one.
  • COD in the aquatic environment can be quantified by measuring the amount of electrons captured at a nanostructured thin-layer photoelectrochemical TiO2 electrode of Zhang, SQ et al. (Zhang, SQ; et al. Source Sensors and actuators B-Chemical 141 (2):634-640 2009).
  • the UV-LED PeCOD system enables end-users to perform on-site COD analysis in a simple, rapid, sensitive and accurate manner. Under the optimal conditions, the system can achieve a practical detection limit of 0.2 ppm COD with a linear range of 0-300 ppm COD
  • the IRAFS system comprises a photocatalytic reactor (as displayed in Fig. 17) for oxidizing and mineralizing of the complex organic molecules or for ammonium directly into N 2 , or ammonium into NO 2 " or to reduce NO 3 " into NO 2 " depending on the photocatalyst and/or the reaction time and for presentation of the photocatalytic material to an bioreactor system aerobic bioreactor and anaerobic bioreactor that can be tuned to enhance a larger part of ammonium removal through oxidizing ammonium directly into N 2 . While not wishing to be bound by theory, it is believed that this ammonium/NO 2 " relationship is important to drive an aerobic biofilter into an annamox operation.
  • This bioreactor is preferably a (bio)granule (144) producing bioreactor foreseen of turbulence or (hydrodynamic) shear force creation means for instance a stirrer (105) for inducing biof ⁇ lm forming into (bio)granules (144).
  • a floe or sludge bioreactor is also a suitable.
  • the photocatalytic reactor is foreseen with a transport pipe input (98) to receive water load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the aquatic farming system.
  • a transport piping connects the out put (125) eventually over a pump (129) of the photocatalytic reactor with a pretank (118) for instance an aeration or oxygenation unit (118) and eventually in situ sensors provides information of measured quantities of mineralization and of toxicity of contaminants or intermediates.
  • a pretank for instance an aeration or oxygenation unit (118)
  • in situ sensors with a signal output that is representative for ammonium, nitrite and/or nitrate the ammonium to nitrite proportion can be controlled in the pretrank (118) in a particular embodiment.
  • This pretank (118) is connected with a transport piping (126) with the aerobic bioreactor (119), preferably a granule aerobic bioreactor that is foreseen of a turbulence or a shearing means (123) to force biof ⁇ lm forming microorganisms to form (bio)granules.
  • a loop (100) eventually with pump (130) allow under control of a valve system (154) to return water treated in the bioreactor via a transport piping (99a) to the photocatalytic reactor input (99) or to the pretank or the aeration or oxygenation unit (118).
  • This photocatalytic aerobic bioreactor system can release the photocatalyst / aerobic bioreacted water via an output (127) into anaerobic bioreactor, preferably an anaerobic granule bioreactor (120) foreseen of a turbulence or shear force means to force the biofilm forming microorganisms to form granules (144b).
  • This anaerobic bioreactor can release the water that has been photocatalytic, aerobic bioreactor and anaerobic bioreactor processed via an output or an output transport piping (131) into the aquatic animal farming system or into the storage tanks of the soilless plant culture or hydroponics.
  • the anaerobic bioreactor is foreseen with a loop of a transport pipeline (100) and eventually a pump (130) under control of a switch valve system back into the photocatalytic unit (117).
  • a switch valve system back into the photocatalytic unit (117).
  • the ERAFS (as displayed in Fig. 18) comprises photocatalyst reaction unit to pretreat the water that is loaded with organic materials and to oxidize complex organic molecules, suspended organic solids, particulate organic matter and colloidal organic matter ((coBOD ) colloidal BOD and/or (pBOD) particulate BOD and/or solved nBOD, cBOD into mineral molecules for instance for organic phosphorus, nitrogen and carbon mineralization or partial mineralization.
  • the photocatalytic unit (100) is provided with a radiation source (103) to radiate the photocatalytic material (104), for instance a UV lamp (103) or alternatively collector sun light or a photocatalytic surface that is exposed to sun light.
  • This output transport piping or irrigation means (107) is provided with a switch valve that allows to return the processed water via a transport piping or irrigation means (147b) to the photocatalytic reactor unit.
  • the photocatalytic reactor unit can be foreseen with a gas transport piping (136) to transport the gas fluids generating in the photocatalytic reactor unit.
  • the photocatalytic unit (100) comprises an alternative output (156) under control of a valve (154) that can provide processed water to other units for instance to the aquatic animal farming units.
  • the gasification unit (134) is preferably foreseen of a shear force tool or (136) to force the microorganisms into biogranules (144).
  • the watery fluid out put(s) (137) of the gasification tank (134) is or are connected via a transport piping or irrigation system (118) with an oxygenation or aeration unit (147) which is connected with a transport piping or irrigation system ( 126) to deliver the aerated or oxygenated water to an aerobic biofilter (119) is preferably an aerobic (bio)granule biofilter foreseen with a shear forces or water disturbance tool (123) to force the microbials into (bio)granules.
  • This aerobic biofilter is connected by a transport piping or irrigation unit (127) to deliver its processed water into an anaerobic biofilter unit (120) which is preferably an anaerobic (bio)granule biofilter foreseen with a shear forces or water disturbance tool (124) to force the microbials into (bio)granules.
  • This anaerobic biofilter unit (120) has an output and output transport piping or irrigation tool ( 131) to transport its processed water to the aquatic farming animal system or to the crop hydroponics or the soilless plant culture system.
  • the anaerobic biofilter unit (120) comprises further a transport piping or irrigation unit (127) to recirculate its processed watery fluid to aeration tank (147).
  • the IRAFS comprises a nutrient feeding and recirculating system of the plant hydroponics or soilless crop culture (greenhouse) whereby processed water of the other reactor units is delivered to a mixing unit or mixing tank (167) for proper mixing and dosing before the nutrients are delivered to the crops.
  • a water collection unit can receive water of a transport piping (98 or 156) directly from a photocatalytic reaction unit or of a transport piping (131) indirectly from a photocatalytic reaction for instance of a photocatalyst / aerobic bioreactor / anaerobic bioreactor unit (17 or 18 (whereby at least one of the anaerobic bioreactors is a gasification tank) and eventually an other anaerobic is an anaerobic microbial fuel cell (with heterotrophic bioelectrochemical bacteria for anaerobic denitrification), or of a transport piping (112) of a photocatalyst / aerobic bioreactor system (Fig.
  • a photocatalytic reactor input (99)
  • an aerobic bioreactor unit autotrophic bioelectrochemical bacteria for aerobic nitrifying bacterial fuel cell
  • a separate aeration or oxygenation unit (101) the transport piping (112) to release the photocatalysed and aerobic bioreacted water into a storage tank (168) or in one of the tanks (157, 158 or 167) of the photocatalyst / aerobic bioreactor system (Fig. 16).
  • the water storage (168) that receives water from the photocatalytic reactors (fig 15, 16, 17, 18, 21, 22, 23 or 24) , the drain water tank (159) (that receives the (dirty) water of the hydroponics culture, the soilless crop culture system or the crop greenhouse culture (163) ) and the clean water tank (157) that stores ground water, rain water or other clean water, are connected with a transport piping or irrigation system to a mixing unit or mixing tank (167).
  • There water supply to the mixing unit or mixing tank (167) is under control of a multiple switch valve (160) to control their water flow towards the mixing unit or mixing tank (167).
  • a sterilization unit 165 preferably a flow through sterilization unit that comprises a UV radiation source (166) to radiate the passing through water or eventually an ozonation system as a germicidal treatment .
  • the hydroponics culture, the soilless crop culture system or the crop greenhouse culture (163) comprises chemical (nutrient) stock solution tank(s) (162), of which one acid stock solution tank (162) and another base stock solution tank (162), that all have an transport pipe that passes dosing or reservoir pumps (159) for comprising a desired nutrient solution , pH and alkalinity for instance in the diluter (161) or in the mixing unit or mixing tank (167).
  • the diluter (161) or the mixing unit or mixing tank (167) have an irrigation or transport piping to the plant growing troughs (164).
  • the plant growing troughs (164) are connected by a transport piping or irrigation with a drain pit (165) that is connected by a transport piping or irrigation with the drain storage tank (158).
  • the system will be controlled by a liquid control system that controls the (nutrient) dosing or reservoir pump, the nutrient solution pH, the nutrient electric conductivity, nutrient solution and condensate water levels.
  • Fig. 20 which provides A) a view of a transverse section of a transport fluid pipe between the different units such as the rain water / groundwater or clean water tank (305), the aquatic animal culture tank or tanks (306), the hydroponics or soilless crop culture unit(s) (307) the soilless crop culture unit(s) (307) and the bioreactor units and B) a 3D side view of such transport pipe (113)) in an embodiment of present invention
  • the outer layer of the liquid transport piping (114) is inside coated by or contacting another antimicrobial layer (116), in particularly a bactericidal layer.
  • Suitable coatings have been provided in this application.
  • the antimicrobial layer (116) van also be provided with virucidal properties.
  • at least some of the water storage tanks have been coated inside by the same antimicrobial coating.
  • 115 is the inner lumen of the transport pipe.
  • the antimicrobial material can be incorporated in material of the piping or the tanks itself.
  • the IRAFS comprises a photocatalyst reactor (as displayed in Fig. 21) that is connected by its processed water output with a transport piping (125) to a microbial fuel cell unit.
  • the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved cBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • the photoctalyst further comprises a radiation unit (122) to radiate the photocatalytic material (121).
  • This radiation unit can be an UV lamp, near UV or UV- VIS lamp but alternatively the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquatic animal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • the photocatalytic reactor (117) is for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytized molecules to enhance the productivity of a microbial fuel cell.
  • An output and transport piping (125) provides the water wherein the organic load has been mineralized from the photocatalytic reactor (117) to the microbial fuel cell (511 and 501).
  • the microbial fuel cell can be an aerobic microbial fuel cell (511) for instance inoculated with aerobic bacteria (e.g. aerobic nitrifies or aerobic bioelectrichemical autotrophes) such as Bacillus subtilis, an anaerobic microbial fuel cell (501) or both (as displayed in Fig. 21).
  • the microbial fuel cell receives water from a transport piping (125) of the photocatalytic reaction unit eventually over a pump (129).
  • the aerobic microbial fuel cell (511) is preceded by an aeration or oxygenation unit (118) that is connected with its output via a transport piping or irrigation system with the aerobic microbial fuel cell (511) (e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers).
  • the aerobic microbial fuel cell (511) e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers.
  • the anode chamber of the microbial fuel cells or the oxygenation or aeration chamber can recycle the processed water back to the photocatalytic reactor unit (100) via a transport piping such as 99b.
  • the output of this hybrid photocatalytic / microbial fuel cell system can release its processed water via a transport piping or irrigation system (131) into water storage (168) or other storage tanks or the mixing tanks (167) of a hydroponics culture, soilless crop culture system or crop greenhouse culture (163).
  • the microbial full cells are provided with an external circuit that comprises a load (502 or 512), with a separator ( 505 or 510), with the anodes (503 or 516) in their anodes chamber and with the cathodes ( 504 or 517) in their cathode chamber.
  • the IRAFS comprises a photocatalytic reactor (117) that receives watery fluid loaded with organic molecules or organic matter from an input transport piping (99) or irrigation system (99).
  • the photocatalytic reactor comprises a photocatalytic material (121) UV radiation source (122) or receives sun light radiation.
  • the output for the photocatalytic processed watery fluid is connected with a transport piping (125) or irrigation system (125) which eventually passes a pump (129) and which is connected with a multitubular or multi column microbial fuel cell (525) or a reactor in which micro-organisms generate current (525) so that the photocatalytic water flows over anodic material (521) able to host microbials and able to accept electrons in a series of tubes that are 3 dimensionally surrounded by a cation exchange membrane (526).
  • anodic material (521) comprises an electric conductive material (for instance conductive graphite pellets or (macro)porous graphite).
  • the cation exchange membrane (526) is three dimensionally surrounded by a cathodic material (520) and is separating the cathode from the anode.
  • This cathodic material (520) can be ferricyanide catholyte fluid that overflow the out surface of the cation exchange membrane (526) which ferricyanide catholyte fluid is for instance pumped by a pump (129b) over the outer surface of the cation exchange membrane (526) of the multitubular or multi column microbial fuel cell (525) and can be recycled in a loop (528) and eventually passing an aeration or oxygenation unit (524) provided with an aerator (128).
  • the multitubular or multi column microbial fuel cell (525) is provided with at least one external circuit that comprises a load (522).
  • the external circuit (128) is able to receive electrons from the anode and to transport the electrons to the cathodic material (520).
  • the anode is able to accept electrons from the microbials and the cathode is able to transfer the electrons from the external circuit to an electron acceptor or sink.
  • the IRAFS of present invention comprises a combined photocatalyst reactor (100) / gasification unit (134) that is connected by its processed water output (137) with a transport piping (155) to deliver its processed water to a microbial fuel cell unit (as displayed in Fig. 23).
  • the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the from the aquatic animal farming units.
  • the photoctalyst unit is foreseen with a radiation unit (103) to radiate the photocatalytic material (104).
  • the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquatic animal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • An output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (135 (the lowest 134 in fig 23 is 135)) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (135 (the lowest 134 in fig 23 is 135)), effluent collection (137)) .
  • the gasification unit is provided with switch valves (154) to release its processed water via an out put or transport piping (155) or to return the water via a transport piping (99b) to the photocatalytic reactor unit (100).
  • the out put (137) of the combined photocatalyst reactor (100)/ gasification unit (134) is connected via a transport piping or irrigation tool (155) with the microbial fuel cell reactor wherein microbials provide electrons, an anode is provided to accept electrons from the microbials which are transorted by a circuit (502, 512) to the cathode which is able to transfer the electrons from the external circuit to an electron acceptor or sink.
  • the photocatalytic reactor (100) is for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytized molecules to the gasification unit (134) and a microbial fuel cell (511, 501) to enhance their productivity.
  • An output and transport piping (155) provides the water wherein the organic load has been mineralized and passed the gasification unit (134) to the microbial fuel cell (501 and/or 511).
  • the microbial fuel cell can be an aerobic microbial fuel cell (511) for instance inoculated with aerobic bacteria (e.g. aerobic nitrif ⁇ ers or aerobic bioelectrichemical autotrophes) such as Bacillus subtilis, an anaerobic microbial fuel cell (501) or both as in Fig. 23.
  • the gasification tank receives water from a transport piping (107) from the photocatalytic reaction unit 100), eventually over a pump (108).
  • the aerobic microbial fuel cell (511) is preceded by an aeration or oxygenation unit (118) that is connected with its output via a transport piping (126) or irrigation system with the aerobic microbial fuel cell (511) (e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers).
  • anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers.
  • the anaerobic fuel cell receives water that has been processes in the photocatalytic reactor (100) and gasification unit (134) from the transport piping or irrigation system of the combined photocatalytic reactor (100) / gasification unit (134).
  • the anode chamber of the microbial fuel cells or the oxygenation or aeration chamber can recycle the processed water back to the photocatalytic reactor unit (100) via a transport piping such as 99b.
  • the output of this hybrid photocatalytic / microbial fuel cell system can release its processed water via a transport piping or irrigation system (131) preferably into water storage (168), the mixing tank (167) or other storage tanks of the hydroponics culture, soilless crop culture system or crop greenhouse culture (163).
  • the IRAFS of present invention comprises a combined photocatalyst reactor / gasification unit that is connected by its processed water output with a transport piping (125) to deliver its processed water to a tubular microbial fuell cell.
  • the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • the photoctalyst untis for ween with a radiation unit (103) to radiate the photocatalytic material (104).
  • the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquatic animal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • An output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (134) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (134), and effluent collection (137)).
  • the gasification unit is provided with switch valves (154) to release its processed water via an out put or transport piping (155) or to return the water via a transport piping (99b) to the photocatalytic reactor unit (100).
  • the transport piping (155) is connected with a transport piping (125) or irrigation system (125) which eventually passes a pump (129) and which is connected with a multitubular or multi column microbial fuel cell (525) or a reactor in which micro- organisms generate current (525) so that the photocatalytic water flows over anodic material (521) able to host microbials and able to accept electrons in a series of tubes that are 3 dimensionally surrounded by a cation exchange membrane (526)
  • Such anodic material (521) comprises an electric conductive material (for instance conductive graphite pellets or (macro)porous graphite).
  • the cation exchange membrane (526) is three dimensionally surrounded by a cathodic material (520) and is separating the cathode from the anode.
  • This cathodic material (520) can further comprise a catholyte fluid, for instance a ferricyanide catholyte fluid that overflows the out surface of the cation exchange membrane (526).
  • the catholyte fluid is for instance pumped by a pump (129b) over the outer surface of the cation exchange membrane (526) of the multitubular or multi column microbial fuel cell (525) and can be recycled in a loop (528) and eventually passing an aeration or oxygenation unit (524).
  • 522 is the load of the external circuit (522).
  • the multitubular or multi column microbial fuel cell (525) furthermore comprises an external circuit (128) able to receive electrons from the anode and to transport the electrons to the cathodic material (520).
  • the anode is able to accept electrons from the microbials and the cathode is able to transfer the electrons from the external circuit to an electron acceptor or sink.
  • the combined gasification / MFC system is used for bioremediation and production of energy to drive actuators of the IRAFS.
  • 500 kg of fish in weight produces 550 m biogas per year (biogas/a), ca. 3500 kWha, or at least 200 - 500 (800) m 3 biogas/a, depending on the energy content of the biogas with a energy content 6.0 - 6.5 kWh m ⁇ 3 or a fuel equivalent 0.60 - 0.65 L oil/m 3 biogas.
  • the energy efficiency (jiMFC) the ratio of power produced by the MFC over a time interval divided by the heat of combustion of the organic substrate is up to 50% when easily biodegradable substrates are used. In comparison the electric energy efficiency for thermal conversion of methane is ⁇ 40%. But treated materials leaving the gasification or the MFC process still have energy content and can be reused or used in other energy extracting processes.
  • a biomass farming system with controlled fluid flow input and/or fluid output for producing useful biomass comprising a bioreactor system with various bioreactor units in a shared confined environment or different confined environments that are connected
  • the farming system comprises
  • a drain such as a drain removal system or line to optionally a drain storage container
  • At least one aquaculture system for the culture of aquatic multicellular consumer (heterotrophic) organism (aquatic animals) comprising the drain and further comprising a suspended solids (SS), colloidal BOD (coBOD) or particulate BOD (pBOD) removal apparatus with an out put and a transport line connected to one or more collection containers or directly to the gasification bacterial bioreactor system, and further
  • SS suspended solids
  • coBOD colloidal BOD
  • pBOD particulate BOD
  • At least one collection tank or basin with connected with the removal apparatus and transport line of the aquaculture system to receive solids (TSS), colloidal BOD (coBOD), particulate BOD (pBOD) from the aquaculture system and/or to receive sludge from the bacterial bioreactor system, and further
  • At least one bacterial bioreactor system comprising condominiums of producers bacteria and condominiums of consumer bacteria in a same or separate bioreactor and comprising an input to receive solved and particulate organic and inorganic material from the aquaculture system, and further
  • gasification bioreactor connected with the removal apparatus and transport line of the removal apparatus or with the one or more collection containers to receive the removed material from the aquaculture system and the gasification bioreactor further comprising a gas collection means and a gas distribution line to transport the energy rich gaseous products toward to a gas burn driver of the heat pump system.
  • gasification bioreactor comprises a methanogenic reaction function for producing the energy rich gaseous product (e.g. methane).
  • gas collection container is in the gas transport line between gasification bioreactor and the gas burn driver of the heat pump system.
  • drain is a drain water tank or basin with out put to the outer environment.
  • variable flow control system 15.
  • variable flow control system is a mixed indoors with outdoors system that connects an heat releasing component or heat extracting component in the outer environment with a confined environment that comprises the biomass farming system.
  • the outer environment is the bottom under frost line.
  • the operating system of the heat pump system comprises a in situ temperature sensors in the water input container (clean water basin), in the bioreactor units of farming system and in the drain connected to a signal processor to feeds the input signals from the temperature sensor network system into the signal processor and a controller that controls the heat pump system to adapt the temperature.
  • the signal processor comprises a mathematical model that is described on the relationship of a plurality of temperature variables and a plurality of comfort, stress or welfare variables of a plurality of living organisms in relating to the temperature (and eventually the time period of the day) and a controller that controls the heat pump system to adapt the temperature.
  • the signal processor comprises an adjuster to adjust the controller to control the heat pump system or an extra heating means to maintain the temperature between 15 - 30°C, preferably between 20 - 25 °C.
  • the at least one bacterial bioreactors system comprises a fluid input to receive organic and inorganic material form collection tank or basin that receives organic and inorganic material form the aquaculture system.
  • the bacterial reactor system comprises a reactor of the group consisting of an anaerobic reactor up flow anaerobic sludge blanket (UASB), an anaerobic sequencing batch reactor (ASBR), a fluidized expanded bed reactor, a static granular bed reactor (SGBR), an anaerobic membrane reactor, an anaerobic expanded-bed reactor (EBR) and a granular bed baffled reactor (GRABBR).
  • UASB anaerobic reactor up flow anaerobic sludge blanket
  • ASBR an anaerobic sequencing batch reactor
  • SGBR static granular bed reactor
  • EBR anaerobic expanded-bed reactor
  • GRABBR granular bed baffled reactor
  • biofilter comprises a shear for subjecting the autotrophic (chemolithotrophic) bacteria and heterotrophic (chemo organotrohic) bacteria to fluid shear and inducing biogranuation
  • biogranulate operated biofilter further comprises means for filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity.
  • biofilter comprises a shear for subjecting the autotrophic (chemolithotrophic) bacteria and heterotrophic (chemo organotrohic) to fluid shear and inducing biogranulation.
  • biogranulate operated biofilter further comprises means for filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity.
  • the biomass farming system of any of the previous embodiments whereby gasification the bacterial reactor system is connected with the farming unit to receive molecular electron acceptors, such as CO 2 , or NO 3 " , and a gas collection and a gas distribution system to collect the energy riches gasses produced after electron acceptation, such as CH 4 and N 2 .
  • molecular electron acceptors such as CO 2 , or NO 3 "
  • gas collection and a gas distribution system to collect the energy riches gasses produced after electron acceptation, such as CH 4 and N 2 .
  • biomass farming system of any of the previous embodiments whereby the bacterial bioreactor system is a bioelectricity producer integrated operational system that connects and drives farming systems actuator with the bioelectricity.
  • biomass farming system of any of the previous embodiments whereby the bacterial reactor system that produces the energy to drive system actuators comprises an anaerobic bioreactor
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system that produces the energy to drive system actuators comprises aerobic bioreactor
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system that produces the energy to drive system actuators comprises the bioreactor that combines an aerobic and anaerobic zone.
  • the bacterial reactor system comprises a condominium of bioelectrical bacteria that degradates molecular or organic nitrogen compounds releasing electrons.
  • each electrical circuit is connected to at least one of the systems actuators to drive it by electricity generated by the bio-electrochemical bacteria assisted biotransformation system.
  • the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD.
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises at least one autotrophic (chemolithotrophic) bio- electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio- electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor. 50.
  • the bacterial reactor system comprises at least one autotrophic (chemolithotrophic) bio- electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio- electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor.
  • the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio- electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD.
  • the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio- electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD.
  • the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio- electrochemical bacteria in one condominium or bioreactor.
  • biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises a shear for subjecting the autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria to fluid shear and inducing biogranulation.
  • autotrophic chemolithotrophic
  • heterotrophic chemo organotrohic
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biotransformation system assisted by electrochemical bacteria assisted or a biotransformation unit assisted by autotrophic bacteria is a nitrifying bacterial fuel cell comprising autotrophic bio-electrochemical bacteria 56.
  • biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a nitrifying bacterial fuel cell is a flow through fuel cells accepting water of the farming systems flows
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biotransformation unit assisted by heterotrophic bio- electrochemical bacteria can be a denitrifying bacterial fuel cell.
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biotransformation system assisted by heterotrophic bio- electrochemical bacteria comprises Geobacter sulfurreducens, Shewanella oneidensis, Rhodoferax ferrireducens or a combination thereof.
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is an electrochemical bacteria assisted biotransformation system or combined nitrifying/denitrifying bacterial fuel cell comprises an anode chamber with heterotrophic bio-electrochemical bacteria, an anode chamber with autotrophic bioelectrochemical bacteria in contact with a common cathode chamber isolated by a selective hydrogen ion permeable separator.
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system, whereby the anode chamber with heterotrophic bio- electrochemical bacteria and the anode chamber with autotrophic bioelectrochemical bacteria are flow through fuel cells accepting water flows of the farming systems.
  • the farming system of any of the previous embodiments further comprising at least one photocatalytic bioreactor
  • a conductivity sensor network of sensors in the chemical stock solution container, in the aquaculture drain water and the gasification bioreactor drain is connected with a computer comprising a controller or with an electronic controller to process the sensor signals in to a signal that activates actuator for mixing the fluid (of the water of the aquaculture system, the clean water, the drain water of the gasification tank and/or the chemical stock solution water or injecting the fluids in to an irrigation system to the photocatalytic bioreactor.
  • the farming system further comprises an operating system comprising a in situ pH sensors in the water input container (clean water basin) and in bioreactor units of farming system connected to a signal processor to feeds the input signals from the pH sensor network system into the signal processor which signal processor comprises a mathematical model that is described on the relationship of a plurality of pH variables and a plurality of comfort, stress or welfare variables of a plurality of living organisms in relating to the pH and a controller that controls a at least one programmable actuator to adapt the pH.
  • an operating system comprising a in situ pH sensors in the water input container (clean water basin) and in bioreactor units of farming system connected to a signal processor to feeds the input signals from the pH sensor network system into the signal processor
  • signal processor comprises a mathematical model that is described on the relationship of a plurality of pH variables and a plurality of comfort, stress or welfare variables of a plurality of living organisms in relating to the pH and a controller that controls a at least one programmable actuator to adapt the pH.
  • the signal processor comprises an adjuster to adjust the controller to control the programmable pH actuator to maintain the pH between 5,5 and 8 preferably between 6 - 7.5. 79.
  • the programmable actuator is a delivery pump to deliver a pH regulator agent (for instance an agent of the group consisting of an alkalis of the group consisting of calcium bicarbonate, calcium carbonate, calcium hydroxide, magnesium bicarbonate, magnesium carbonate, magnesium hydroxide, sodium bicarbonate, sodium carbonate and sodium hydroxide) to said system to adapt pH.
  • a pH regulator agent for instance an agent of the group consisting of an alkalis of the group consisting of calcium bicarbonate, calcium carbonate, calcium hydroxide, magnesium bicarbonate, magnesium carbonate, magnesium hydroxide, sodium bicarbonate, sodium carbonate and sodium hydroxide
  • a biomass farming system with controlled fluid flow input and/or fluid output for producing useful biomass comprising a bioreactor system with various bioreactor units in a shared confined environment or different confined environments that are connected whereby the farming system comprises 1) a distribution line or distribution lines and at least one pump actuator to flow system fluids between selected bioreactor systems, 2) at least one water input for instance a water input container (clean water basin) for collecting or storing of rain water, surface water, municipal tap water and/or ground water, 3) a drain for drain water removal for instance a drain removal line to optionally a drain storage container, 4) an heat pump system with condenser and evaporator heat exchangers, 5) at least one bacterial bioreactor system and whereby the bioreactor system with various bioreactor units comprises a) at least one gasification bioreactor, b) at least one aquaculture system for the culture of aquatic multicellular consumer (heterotrophic) organism (aquatic animals) with at least one suspended solids (SS), colloidal BOD (coBOD) and/
  • a photocatalytic reactor unit (100) which has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the from the aquatic animal farming units and which comprises at least one fluid transport pipe connected with or which irrigate the bacterial bioreactor system
  • a photocatalytic reactor unit (100) which has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the from the aquatic animal farming units and which photocatalytic unit (100) comprises an output0 transport piping or irrigation means (107) to transport its processed water to the input system of an aerobic biofilter (119).
  • SS suspended solids
  • coBOD colloidal BOD
  • pBOD particulate BOD
  • a photocatalytic reactor unit (100) for oxidizing and mineralizing of the complex organic molecules which photocatalytic unit (100) comprises an output transport piping or irrigation5 means (107) to transport its processed water to the input system of a microbial fuel cell for the presentation of the photocatalytized molecules to enhance the productivity of a microbial fuel cell.
  • a unit with photoautotrophic organisms e.g. aquatic plants
  • the farming system of any of the previous embodiments whereby the operating system of the heat pump system comprises a in situ temperature sensors in the water input container (clean water basin), in the bioreactor units of farming system and in the drain connected to a signal processor to feeds the input signals from the temperature sensor network system into the signal processor and a controller that controls the heat pump system to adapt the temperature.
  • the signal processor comprises a mathematical model that is described on the relationship of a plurality of temperature variables and a plurality of comfort, stress or welfare variables of a plurality of living organisms in relating to the temperature (and eventually the time period of the day) and a controller that controls the heat pump system to adapt the temperature.
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises at least on bioelectric bioreactor 21.
  • the biomass farming system of any of the previous embodiments whereby the bacterial bioreactor system is a bioelectricity producer integrated operational system that connects and drives farming systems actuator with the bioelectricity 1022.
  • the farming system of any of the previous embodiments further comprising photocatalyst reactor with a radiation unit and photocatalyst material that functionalised for photocatalytic denitrification
  • the photocatalytic reactor can deliver such treated water to a pretank unit (101) and by in situ hard sensor with a signal output that is representative for a measure of ammonium, nitrite and/or nitrate the ammonium to nitrite proportion can be controlled in the pretrank (101) before the water is transferred to bioreactor to set or maintain said bioreactor in an annamox mode.
  • bioreactor is a (bio)granule (144) producing bioreactor foreseen of turbulence or shear force creation means for instance a stirrer (105) for inducing biofilm forming into (bio)granules (144).
  • the photocatalyst reactor is a reactor type of the group consisting of falling Film Reactor (FFR), Fiber Optic Cable Reactor (FOCR), Multiple Tube Reactor (MTR), Packed Bed Reactor (PBR), Rotating Disk Reactor with Controlled Periodic Illumination (RDR-CPl), Spiral Glass Tube Reactor (SGTR), Tube Light Reactor (TLR) and Photo CREC Water I.
  • FFR falling Film Reactor
  • FOCR Fiber Optic Cable Reactor
  • MTR Multiple Tube Reactor
  • PBR Packed Bed Reactor
  • RDR-CPl Rotating Disk Reactor with Controlled Periodic Illumination
  • Spiral Glass Tube Reactor SGTR
  • Tube Light Reactor TLR
  • gasification bioreactor comprises a methanogenic reaction functions for producing the energy rich5 gaseous product (e.g. methane).
  • variable flow control system The farming system of any of the previous embodiments whereby the reversed0 absorption heat pump is connected in a variable flow control system. 43. The fanning system of any of the previous embodiments whereby the variable flow control system being connected with the water input container, one or more other units of the farming system and the drain.
  • the farming system of any of the previous embodiments whereby the operating system of the heat pump system comprises at least one pump and at least one heat pump actuator to drive the heat pump system.
  • the pump actuator is a gas burner to drive the heat pump by heat 2553.
  • the biomass farming system of any of the previous embodiments whereby the at least one bacterial bioreactors system comprises a fluid input to receive organic and inorganic material form collection tank or basin that receives organic and inorganic material form the aquaculture system
  • 10 bacterial reactor system comprises a reactor of the group consisting of an anaerobic reactor up flow anaerobic sludge blanket (UASB), an anaerobic sequencing batch reactor (ASBR), a fluidized expanded bed reactor, a static granular bed reactor (SGBR), an anaerobic membrane reactor, an anaerobic expanded-bed reactor (EBR) and a granular bed baffled reactor (GRABBR).
  • UASB anaerobic reactor up flow anaerobic sludge blanket
  • ASBR an anaerobic sequencing batch reactor
  • SGBR static granular bed reactor
  • EBR anaerobic expanded-bed reactor
  • GRABBR granular bed baffled reactor
  • biofilter comprises a shear for subjecting the autotrophic (chemolithotrophic) bacteria and heterotrophic (chemo organotrohic) bacteria to fluid shear and inducing biogranulation
  • biomass farming system of any of the previous embodiments whereby the 20 biogranulate operated biofilter further comprises means for filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity
  • 25 organotrohic) bacteria are in an up flow sludge blanket filter (USBF) bioreactor) with an anoxic and an aerated compartment and up flow sludge blanket filtration with automatic or continued removal device of poor settling active sludge floes or sludge granule and automatic or continued distribution well settling active sludge floes or sludge granule to the anoxic zone.
  • USBF up flow sludge blanket filter
  • biofilter comprises a shear for subjecting the autotrophic (chemolithotrophic) bacteria and heterotrophic (chemo organotrohic) to fluid shear and inducing biogranulation.
  • biogranulate operated biofilter further comprises means for filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity.
  • biomass farming system of any of the previous embodiments whereby the bacterial reactor system that produces the energy to drive system actuators comprises an anaerobic bioreactor
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system that produces the energy to drive system actuators comprises aerobic bioreactor
  • biomass farming system of any of the previous embodiments whereby the bacterial reactor system that produces the energy to drive system actuators comprises 0 the bioreactor that combines an aerobic and anaerobic zone
  • the biomass farming system of any of the previous embodiments whereby the 5 bacterial reactor system further comprise at least one anode connected with a least one electric circuit to accept and distribute the electrons.
  • each electrical circuit is connected to at least one of the systems actuators to drive it by electricity generated by the bio-electrochemical bacteria assisted biotransformation 0 system
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biof ⁇ lter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises at least one autotrophic (chemolithotrophic) bio- electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio- electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor
  • the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio- electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises at least one bio-electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio- electrochemical bacteria in one condominium or bioreactor
  • the biomass farming system of any of the previous embodiments whereby the bacterial reactor system comprises a shear for subjecting the autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria to fluid shear and inducing biogranulation
  • biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biogranulate operated biofilter further comprises means for filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity.
  • biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biotransformation system assisted by electrochemical bacteria assisted or a biotransformation unit assisted by autotrophic bacteria is a
  • biomass farming system of any of the previous embodiments, whereby the 15 bacterial reactor system is a nitrifying bacterial fuel cell is a flow through fuel cells accepting water of the farming systems flows
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biotransformation unit assisted by heterotrophic bio- electrochemical bacteria can be a denitrifying bacterial fuel cell.
  • the biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is a biotransformation system assisted by heterotrophic bio- electrochemical bacteria comprises Geobacter sulfur reducens, Shewanella oneidensis, Rhodoferax ferrireducens or a combination thereof.
  • biomass farming system of any of the previous embodiments, whereby the bacterial reactor system is an electrochemical bacteria assisted biotransformation system or combined nitrifying/denitrifying bacterial fuel cell comprises an anode
  • Plantae e.g. herbs, grasses, vines.
  • drain water and the gasification bioreactor drain is connected with a computer comprising a controller or with an electronic controller to process the sensor signals in to a signal that activates actuator for mixing the fluid (of the water of the aquaculture system, the clean water, the drain water of the gasification tank and/or the chemical stock solution water or injecting the fluids in to an irrigation system to the 10 photocatalytic bioreactor
  • the farming system further comprises an operating system comprising a in situ pH sensors in the water input container (clean water basin) and in bioreactor units of farming system connected to a signal processor to feeds the input signals from the pH sensor network system into the signal processor which signal processor comprises a 0 mathematical model that is described on the relationship of a plurality of pH variables and a plurality of comfort, stress or welfare variables of a plurality of living organisms in relating to the pH and a controller that controls a at least one programmable actuator to adapt the pH.
  • an operating system comprising a in situ pH sensors in the water input container (clean water basin) and in bioreactor units of farming system connected to a signal processor to feeds the input signals from the pH sensor network system into the signal processor which signal processor comprises a 0 mathematical model that is described on the relationship of a plurality of pH variables and a plurality of comfort, stress or welfare variables of a plurality of living organisms in relating to the pH and a controller that controls a at least one programmable actuator to adapt the pH.
  • the signal 5 processor comprises an adjuster to adjust the controller to control the programmable pH actuator to maintain the pH between 5,5 and 8 preferably between 6 - 7.5.
  • a programmable actuator is a delivery pump to deliver a pH regulator agent (for instance an agent of the group consisting of an alkalis of the group consisting of 0 calcium bicarbonate, calcium carbonate, calcium hydroxide, magnesium bicarbonate, magnesium carbonate, magnesium hydroxide, sodium bicarbonate, sodium carbonate and sodium hydroxide) to said system to adapt pH.
  • a pH regulator agent for instance an agent of the group consisting of an alkalis of the group consisting of 0 calcium bicarbonate, calcium carbonate, calcium hydroxide, magnesium bicarbonate, magnesium carbonate, magnesium hydroxide, sodium bicarbonate, sodium carbonate and sodium hydroxide
  • the photocatalyst reactor is provided with a Ru (bpy)3 2+ photocatalyst or another suitable photocatalyst for visible light decomposition of aqueous NH4+/NH 3 to N2 and H2.
  • actuators that receive energy are of the group of sensors, pumps, chemoelectric reactors, valves lamp, the microwave generator, ultrasound generator, programmable actuator adapted to deliver a pH regulator agent to said system, programmable heat and/or cool actuator to cool or heat the system.
  • chemo organotrophic bacteria heterotrophs
  • bioelectricity bioelectricity generating
  • MFC microbial fuel cell
  • a nitrification bacterial fuel cell is incorporated in the aerobic autotrophic nitrifying bioreactor for addition of oxygen to nitrogen while generating bioelectricity whereby the anode chamber reduced substrates (such as reduced nitrogen), ammonium and nitrite ions are oxidized resulting in a decrease of nBOD with the generation of oxidized nitrogen species and in the generation of electrons and protons.
  • the farming system of embodiment 110 whereby the both autotrophic bacteria nitrifying and chemo organotrophic bacteria (heterotrophs) denitrifying bacterial condominiums are designed to producing current to drive the heat pump system or specific actuators in the controlled agriculture system.
  • the farming system of any of the previous embodiments comprising a controlled fluid communication for atmospheric gas that transports the oxygen production by the plant bioreactor or photoautotrophic bioreactor and in particular the bioreactor with photoautotrophic organism (e.g. green plants and photosynthetic 5 bacteria are photoautotrophs is transported to the reactor with producer bacteria.
  • a controlled fluid communication for atmospheric gas that transports the oxygen production by the plant bioreactor or photoautotrophic bioreactor and in particular the bioreactor with photoautotrophic organism (e.g. green plants and photosynthetic 5 bacteria are photoautotrophs is transported to the reactor with producer bacteria.
  • the recirculating aquatic farming system comprises one or more drainage water collection system (drain storage tank) to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse horticulture system (GCS), these
  • the recirculating aquatic farming system comprises one or more drainage water collection system (drain storage tank) to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse horticulture system (GCS), these
  • RAS recirculating aquaculture system
  • GCS greenhouse horticulture system
  • drainage water collection system is a heat source or sink of the recirculating aquatic farming system and heat is collected by an evaporation heat exchanger and transported by the heat pump to a condensing heat exchanger.
  • the farming system of any of the previous embodiments 1 - 119 comprising at least one clean water (ground water and/or rain water) collection or storage tank (400), at least one drain water collection or storage tank with drain water of the hydroponics or a soilless plant culture unit (e.g. the greenhouse culture system (GCS)) (401), a gasification bioreactor (402), aquatic animal farming system in particular the fish culture (e.g. the recirculating aquaculture system (RAS) or
  • GCS greenhouse culture system
  • RAS recirculating aquaculture system
  • recirculating aquatic animal farming system which can comprise bioreactor units and drain organic waste into the gasification bioreactor or its confined environment or building (404), a hydroponics or a soilless plant culture unit (405) (e.g. the greenhouse culture system (GCS)) or its greenhouse (406), evaporators (407) to absorb heat and condensers (408) to release heat, the reverse switch system(s) (409)
  • a hydroponics or a soilless plant culture unit e.g. the greenhouse culture system (GCS)
  • GCS greenhouse culture system
  • evaporators to absorb heat and condensers (408) to release heat
  • the reverse switch system(s) 409
  • the system comprises a reversed absorption heat pumps that is fired by energy rich gas of the gasification bioreactor of present invention and whereby the reversed absorption heat pumps connected in a variable flow control system to control the temperature of the aquatic animal farming system in particular the aquatic animal culture (Tf), the temperature
  • a gasification bioreactor unit Tb
  • Tp temperature of the hydroponics or a soilless plant culture unit by realising or extracting heat at the aquatic animal farming system, the gasification bioreactor unit, the hydroponics or a soilless plant culture unit, the E rain water/ground water or clean water storage unit, the drain water tank and the ground (410), a place the under the frost line ground water.
  • the farming system of embodiment 120 whereby the systems further comprises one or more drainage water collection system to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS).
  • RAS recirculating aquaculture system
  • GCS greenhouse culture system
  • drainage water collection system is a heat source or sink for the recirculating aquaculture system and/or the greenhouse culture system and/or the integrated system of both.
  • a screening apparatus e.g. a incline belt screen filter (132) with a screen belt (143)
  • this solid removal apparatus is foreseen of an input to receive the (dirty) water (148) and an out put (149) to return the (clean) water to the aquatic farming system and is furthermore foreseen to deliver the waste (142) to a waste collection tank (133) whereby the water collection tank (133) is provide with a transport line (e.g.
  • transport pipe (141) and pump (135)) to deliver the waste to an input (131) of a gasification tank (134) and whereby the gasification tank (134) furthermore comprises on or more out put and distribution line (transport pipe) (136) to transport the energy rich gas to the heat pump firing drive system (441, 216, 204) with gasification heat pump mechanism or to a gas fired electricity/heating or cooling generator (CHP unit) that delivers current to the systems actuators.
  • CHP unit gas fired electricity/heating or cooling generator
  • the farming system of any of embodiments 128 to 130 whereby the heat pump firing drive system (441, 216, 204) comprises a gasification heat pump mechanism with he condenser (201) to release heat into its environment and an evaporator (203) extracts heat from the environment and whereby the gas heater (204) receives energy rich gas from the gasification tank transport piping (153), heats the condenser (203) and drives the heat pump.
  • the heat pump firing drive system (441, 216, 204) comprises a gasification heat pump mechanism with he condenser (201) to release heat into its environment and an evaporator (203) extracts heat from the environment and whereby the gas heater (204) receives energy rich gas from the gasification tank transport piping (153), heats the condenser (203) and drives the heat pump.
  • the farming system of any of embodiments 1 to 129 whereby the system further comprises a photocatalyst bioreactor with an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • a photocatalyst bioreactor with an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • SS suspended solids
  • coBOD colloidal BOD
  • pBOD particulate BOD
  • transport piping provides the water wherein the organic load has been partially mineralized to a (photo)autotrophic organisms bioreactor
  • the (photo)autotrophic organisms bioreactor is provided with switch valves (to release its processed water via an out put water to return the water via a transport piping to the photocatalytic reactor unit.
  • a photocatalytic reactor 100
  • a radiation source (103) for oxidizing and mineralizing of the complex organic molecules
  • an aerobic bioreactor (102) which enhances a larger part of ammonium removal through oxidizing ammonium directly into N 2 , or ammonium into NO 2 " or to reduce NO 3 " into NO 2 " depending on the photocatalyst and/or the 0 reaction time.
  • the radiation source can be a solar light collector, UV source, near UV source, UV-VIS source, VIS source.
  • the farming system of any of the embodiments 1 to 129 comprising a 15 photocatalytic reactor for oxidizing and mineralizing of the complex organic molecules or for ammonium directly into N 2 , or ammonium into NO 2 " or to reduce NO 3 " into NO 2 " depending on the photocatalyst and/or the reaction time and for presentation of the photocatalytic material to an bioreactor system aerobic bioreactor and anaerobic bioreactor that can be tuned to enhance a larger part of ammonium 20 removal through oxidizing ammonium directly into N2.
  • this pretank (118) is connected with a transport piping (126) with the aerobic bioreactor (119), preferably a granule aerobic bioreactor, floes or sludge bioreactor.
  • the aerobic bioreactor preferably a granule aerobic bioreactor, floes or sludge bioreactor.
  • the anaerobic bioreactor is foreseen with a loop of a transport pipeline (100) and eventually a pump (130) under control of a switch valve system back into the photocatalytic unit (117).
  • the photocatalytic bioreactor (117) In a particular embodiment the photocatalytic bioreactor (117).
  • the farming system of any of the embodiments 1 to 129 comprising a photocatalyst reaction unit to pretreat the water that is loaded with organic materials and to oxidize complex organic molecules, suspended organic solids, particulate organic matter and colloidal organic matter ((coBOD ) colloidal BOD and/or (pBOD ) particulate BOD and/or solved nBOD, cBOD into mineral molecules for instance for organic phosphorus, nitrogen and carbon mineralization or partial mineralization, disinfection and/or metal reduction.
  • a photocatalyst reaction unit to pretreat the water that is loaded with organic materials and to oxidize complex organic molecules, suspended organic solids, particulate organic matter and colloidal organic matter ((coBOD ) colloidal BOD and/or (pBOD ) particulate BOD and/or solved nBOD, cBOD into mineral molecules for instance for organic phosphorus, nitrogen and carbon mineralization or partial mineralization, disinfection and/or metal reduction.
  • a radiation source (103) to radiate the photocatalytic material (104) for instance a UV lamp (103), UV-VIS, Near UV, VIS depending on the type of photocatalyst, or alternatively collector sun light or a suitable photocatalytic surface that is exposed to sun light.
  • the farming system of any of the embodiments 158 to 159 whereby the photocatalytic unit (100) comprises an output transport piping or irrigation means (107) to transport its processed water to the input system (135) to feed a gasification unit (134) and whereby the output transport piping or irrigation means (107) is provided with a switch valve that allows to return the processed water via a transport piping or irrigation means (147b) to the photocatalytic reactor unit.
  • the photocatalytic unit (100) comprises an output transport piping or irrigation means (107) to transport its processed water to the input system (135) to feed a gasification unit (134) and whereby the output transport piping or irrigation means (107) is provided with a switch valve that allows to return the processed water via a transport piping or irrigation means (147b) to the photocatalytic reactor unit.
  • the farming system of any of the embodiments 158 to 162, whereby the gasification unit is for seen with at least one gas collection unit (145) to collect the energy rich gas ((139 gas bubble) and a transport piping (136) to transport the gas5 fluid to eventual an dehydratation unit (150) and over a gas storage unit (152) via the transport piping (153) or directly via the transport piping (153) to an gas driven heat pump system.
  • a recirculation system of the plant hydroponics or soilless crop culture (greenhouse) is incorporated in the aquatic farming system that further comprises a water collection unit that can receive water of a transport piping (98 or 156) directly from a photacatalytic reaction unit or of a transport piping (131) indirectly from a
  • the photacatalytic reaction unit comprises a photocatalytic reactor input (99), an aerobic bioreactor unit (autotrophic bioelectrochemical bacteria for aerobic nitrifying bacterial fuel cell) (102) and eventually a separate aeration or oxygenation unit (101) and whereby the transport piping (112) releases the photocatalysed and aerobic bioreacted water into a photocatalytic reactor input (99), an aerobic bioreactor unit (autotrophic bioelectrochemical bacteria for aerobic nitrifying bacterial fuel cell) (102) and eventually a separate aeration or oxygenation unit (101) and whereby the transport piping (112) releases the photocatalysed and aerobic bioreacted water into a photocatalytic reactor input (99), an aerobic bioreactor unit (autotrophic bioelectrochemical bacteria for aerobic nitrifying bacterial fuel cell) (102) and eventually a separate aeration or oxygenation unit (101) and whereby the transport piping (112) releases the photocatalysed and aerobic bioreacted water into
  • a mineralization and/or sterilization unit preferably a flow through sterilization unit that comprises a UV radiation source or UV source, near UV source, UV-VIS source, VIS source or solar light source (166) depending on the photocatalyst material and can be assisted by ultrasound or microwave source to radiate the passing through water or eventually an ozonation system as a germicidal 10 treatment.
  • a flow through sterilization unit that comprises a UV radiation source or UV source, near UV source, UV-VIS source, VIS source or solar light source (166) depending on the photocatalyst material and can be assisted by ultrasound or microwave source to radiate the passing through water or eventually an ozonation system as a germicidal 10 treatment.
  • the photocatalytic reactor depending on the photocatalyst material and on the radiation source (166), e.g. UV, Near US, VIS light or Sun light, can for obtaining a sterilisation and / or mineralization function.
  • (163) comprises chemical (nutrient) stock solution tank(s) (162), of which one a acid stock solution tank (162) and another base stock solution tank (162), that all have an transport pipe that passes dosing or reservoir pumps (159) for composing a desired nutrient solution , pH and alkalinity for instance in the diluter (161) or in the mixing 5 unit or mixing tank (167) and whereby the diluter (161) or in the mixing unit or mixing tank (167) receives minerals from the photocatalytic unit and whereby such diluter (161) or the mixing unit or mixing tank (167) have a an irrigation or transport piping to the plant growing troughs (164) and whereby the plant growing troughs
  • drain pipes (164) are connected by a transport piping or irrigation with a drain pit (165) that is 0 connected by a transport piping or irrigation with the drain storage tank (158), such system being controlled by a liquid control system that controls the (nutrient) dosing or reservoir pump, the nutrient solution pH, the nutrient electric conductivity, nutrient solution and condensate water levels.
  • the farming system of any of the embodiments 1 to 129, whereby the transport fluid pipe (114) between the different units such as the rain water / groundwater or clean water tank (305), the aquatic animal culture tank or tanks (306), the hydroponics or soilless crop culture unit(s) (307) the soilless crop culture unit(s) (307) and/or the bioreactor units comprises an outer layer of the liquid transport piping (114) which is coated in the inside or on the inner lumen of the piping (115) of the transport pipe (114) by an antimicrobial layer in particularly a virucidal and/or a layer prevents biofilm forming (116)
  • the microbial fuel cell is an aerobic microbial fuel cell (511) for instance inoculated with aerobic bacteria (e.g. aerobic nitrifiers or aerobic bioelectrochemical autotrophes ) such as Bacillus subtilis, or an anaerobic microbial fuel cell (501) or both and whereby the microbial fuel cell receives water from a transport piping (125) of the photocatalytic reaction unit eventually over a pump (129) and whereby such aerobic microbial fuel cell (511) is preceded by an aeration or oxygenation unit (118) that is connected with its output via a transport piping or irrigation system with the aerobic microbial fuel cell (511)
  • aerobic bacteria e.g. aerobic nitrifiers or aerobic bioelectrochemical autotrophes
  • the microbial fuel cell receives water from a transport piping (125) of the photocatalytic reaction unit eventually over a pump (129) and whereby such aerobic microbial
  • the farming system of any of the embodiments 1 to 129 comprising a photocatalytic reactor (117) that receives watery fluid loaded with organic molecules or organic matter from an input transport piping (99) or irrigation system (99) and whereby the output for the photocatalytic processed watery fluid is connected with a transport piping (125) or irrigation system (125) which eventually passes a pump (129) and which is connected with a multitubular or multi column microbial fuel cell (525) or a reactor in which micro-organisms generate current (525) so that the photocatalytic water flows over anodic material (521) able to host microbial and able to accept electrons in a series of tubes that are 3 dimensionally surrounded by a cation exchange membrane (526) and whereby such anodic material (521) comprises an electric conductive material and whereby the cation exchange membrane (526) is three dimensionally surrounded by a cathodic material (520) and is separating the cathode from the anode and whereby the multitub
  • the farming system of any of the embodiments 1 to 129 comprising a combined photocatalyst reactor (100) / gasification unit (134) that is connected by its processed water output (137) with a transport piping (155) to deliver its processed water to a microbial fuel cell unit and whereby the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the from the aquatic animal farming units and whereby the output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (135) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (135 (the lowest
  • 5 combined photocatalyst reactor (100)/ gasification unit (134) is connected via a transport piping or irrigation tool (155) with the microbial fuel cell reactor wherein microbials provide electrons, an anode is provided to accept electrons from the microbial which are transorted by a circuit (502, 512) to the cathode which is able to transfer the electrons from the external circuit to an electron acceptor or sink.
  • the farming system of any of the embodiments 1 to 129 comprising a combined photocatalyst reactor / gasification unit that is connected by its processed water output with a transport piping (125) to deliver its processed water to a tubular 5 microbial fuell cell and whereby the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units and whereby the photoctalyst unites foreseen with a radiation unit (103) to radiate the photocatalytic 0 material (104).- and whereby an output and transport piping (107) provide the water wherein the organic load has been partially mineralized to the feed distributor (134) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (
  • bioelectricity whereby the oxygen is generated at a radiated (near UV, UV - VIS, preferably visible light or solar light radiation) photo anode in water to produce gaseous oxygen and hydrogen : H 2 O + 2h + -> 2H + + 1 A O 2 and whereby the H + is transported to the anode chamber with electrochemical bacteria (heterotrophic nitrifiers) and oxygen is transported to the cathode chamber.
  • radiated near UV, UV - VIS, preferably visible light or solar light radiation
  • the farming system of any of the previous embodiments comprising a 5 photocatalytic reactor with a mixture of particles that function microphotoelectodes whereof a portion of the first microphotoelectodes if radiated (e.g. under visible light or near infrared ) perform water splitting H 2 O -> ⁇ H 2 + 1 A O 2 and another portion of the second microphotoelectodes perform OH # radicals generation if radiated (e.g. under visible light or near infrared) and oxidize organic adsorbed pollutants (RXad) 0 onto the surface and whereby the molecular oxygen produced by the first microphotoelectodes acts as an acceptor species in the electron-transfer reaction.
  • a portion of the first microphotoelectodes if radiated (e.g. under visible light or near infrared ) perform water splitting H 2 O -> ⁇ H 2 + 1 A O 2 and another portion of the second microphotoelectodes perform OH # radicals generation if radiated (
  • the farming system of any of the previous embodiments comprising a photocatalytic reactor comprising different units, first init(s) with an OH* radicals generation and adsorbed pollutants (RXad) and eventual metal reduction function (down hill photocatalysis function) and second unit(s) with a water splitting function
  • a photocatalytic reactor comprising different units, first init(s) with an OH* radicals generation and adsorbed pollutants (RXad) and eventual metal reduction function (down hill photocatalysis function) and second unit(s) with a water splitting function
  • in situ aqueous sensor comprises any of the sensing of the group consisting of oxygen, conductivity, alkalinity, reduced nitrogen ad oxidized nitrogen
  • in situ aqueous sensor comprises any of the physical measurements of the sensors that are converted into an input signal for the control system are for instance measurements of oxidizable species (RX a( j) of intermediates (from for instance a OH or end products quantities (e.g.
  • in situ aqueous sensor comprises any of the sensing of the group consisting of NH4+/NH3 sensing, simultaneous determination of nitrate and nitrite , pH and the electrical conductivity (EC) , phosphate sensing, continuous NH4+ measurement, NH4+ & NO3- , in situ total solids , the biological oxygen demand, the total oxygen demand (TOC), toxicity monitor , flow of liquid , salinity , electrical conductivity, alkalinity, individual ions like K+, Ca 2 +, NO 3 -, SO 4 2" , NH 4 + , Na + and CF.
  • in situ aqueous sensor comprises any of the sensing of the group consisting of NH4+/NH3 sensing, simultaneous determination of nitrate and nitrite , pH and the electrical conductivity (EC) , phosphate sensing, continuous NH4+ measurement, NH4+ & NO3- , in situ total solids , the biological oxygen demand, the total oxygen demand (TO
  • CO carbon monoxide
  • a photocatalyst is a substance that is activated by absorption of a photon and that helps accelerate a reaction without being consumed.
  • Factors that influence its photocatalytic activity are for instance structure, particle size, surface properties, preparations, spectral activation, and resistance to mechanical stress.
  • Direct (solar) radiation for the meaning of this application is the solar radiation that reaches ground level without being absorbed or scattered.
  • Diffuse (solar) radiation for the meaning of this application is the solar which has been dispersed before reaching the ground is called.
  • Global radiation is the sum of direct (solar) radiation and diffuse (solar) radiation
  • a photocatalyst is defined as a substance that is activated by the absorption of a photon and helps accelerate a reaction, without being consumed.
  • Photocatalytic processes are divided into two groups: homogeneous photocatalytic oxidation, e.g. UV/hydrogen peroxide; and heterogeneous photocatalytic oxidation, such as UV/semiconductor photocatalysis.
  • homogeneous photocatalytic oxidation e.g. UV/hydrogen peroxide
  • heterogeneous photocatalytic oxidation such as UV/semiconductor photocatalysis.
  • hydroxyl radicals one of the most oxidative chemical species
  • Heterogeneous photocatalysis couples low-energy ultraviolet light with semiconductors acting as photocatalysts. The process is catalytic and allows the semiconductor to remain active for long periods of time.
  • the heterogeneous photocatalytic process is initiated when a photon with energy equal to or greater than the band gap energy (Ebg) of the photocatalyst reaches the photocatalyst surface, resulting in molecular excitation.
  • Ebg is defined as the difference between the filled valence band and the empty conduction band of the photocatalyst, in the order of a few electron volts. This molecular excitation results in the generation of mobile electrons in the higher energy conduction band (Ecb) and positive holes in the lower energy valence band (Evb) of the catalyst.
  • electron hole pairs that are generated by the band-gap excitation carry out in situ degradation of the organic molecules whereby a complete mineralization is obtainable to carbon dioxide, water, and mineral acid.
  • Semiconductors are electrical solids. Electrical solids are divided into three groups depending on their ability to conduct electricity: metals; insulators; and semiconductors. Metals are good thermal and electrical conductors due to their chemical bonding structure. Insulators are poor conductors as they are covalently bonded non-metals. Lying between these two groups are semiconductors, whose band structure can, under certain circumstances, allow electrical and thermal conductivity. semiconductors have been of interest since the 1950's due to their unique optical and electronic properties. In an isolated atom, electrons occupy various discrete energy levels which are closely spaced. In a crystal, these energy levels are modified into millions of separate levels, collectively termed an energy band.
  • a semiconductor contains two energy bands known as: the valence band (the highest occupied band (VB)); and the conduction band (the lowest unoccupied band (CB)). At normal temperatures, due to thermal promotion, a metal possesses electrons in the CB, whereas an insulator possesses no electrons in the CB. A semiconductor falls between these two categories.
  • Fig 27 A shows the relative positions of the conduction and valence bands, with the corresponding area between them known as the band gap, in which no electron energy levels exist.
  • Most of the semiconductors which have been investigated as photocatalysts for water treatment have been metal oxides (e.g. TiO2, ZnO, SnO2, WO3) and chalcogenides (CdS, ZnS, CdSe).
  • Metal chalcogenides possess narrower band gaps, which make them sensitive to visible irradiation; however they are subject to photocorrosion.
  • the photocatalysts' effectiveness for oxidation of organics in water treatment is dependent on the oxidation potential of the VB and the reduction potential of the CB.
  • Typical Semi conductor photocatalysts for oxidation purpose are TiO2 (rutile) with band gap energy of 3.0 and with (eV) Wavelength (nm) of 413; TiO2 (anatase) with band gap energy of 3.2 and with (eV) Wavelength (nm) of 388; ZnO with band gap energy of 3.2 and with (eV) Wavelength (nm) of 388; ZnS with band gap energy of 3.6 and with (eV) Wavelength (nm) 335; CdS with band gap energy of 2.4 and with (eV) Wavelength (nm) 516; Fe 2 O 3 with band gap energy of 2.3 and with (eV) Wavelength (nm) 539 and WO 3 with band gap energy of 2.8 and with (eV) Wavelength (nm) 443.
  • the process can be run with any of these photocatalysts.
  • TiO 2 semiconductor Metal oxide semiconductors have been found to be the most suitable photocatalysts given their photo corrosion resistance and their wide band gap energies. TiO 2 is an inexpensive metal oxide semiconductors photocatalyst (100-200 dollars per tonne) and allows photocatalytic operations at low lamp wattage or solar energy. TiO 2 as catalyst is active, inexpensive, no hazardous, stable, and reusable. TiO 2 possesses high photocatalytic efficiency. The light required to activate the catalyst is low-energy UV-A ( ⁇ 380 nm) of intensity around 1-5Wm '2 for photo excitation. It is also possible to use solar light as an alternative and TiO 2 can be functionalized for this.
  • UV-A ⁇ 380 nm
  • the CB of TiO 2 is sufficiently negative for the reduction of 02, while the VB is sufficiently positive for the oxidation of OH making it an excellent semiconductor for the oxidation of organics in water.
  • Adherence of the catalyst to the supporting substrate is can be in accordance with immobilisation techniques such as electrophoretic deposition and sol-gel related methods, among others.
  • the reduction potentials of SrTiO 3 , WO 3 and ZnS could also be used for the photocatalytic oxidation of organic pollutants; however it is often found that TiO 2 is the most efficient semiconductor for the treatment of water containing organic pollutants.
  • Properties of TiO 2 preparations, such as crystalline phase, grain size, surface area and volume can be controlled by synthetic procedures.
  • TiO2 Although the final properties of the TiO 2 are dependent upon its synthesis, it has been established that post-synthetic treatments such as hydrothermal processing and microwave irradiation have significant effects on crystallinity and grain size.
  • the anatase and rutile forms are commonly available in industrial TiO 2 products, with anatase most often used for catalytic purposes due to its larger photoreactivity than rutile.
  • Anatase is thermodynamically stable up to 800 0 C, above which a phase transformation to rutile occurs. The backward transition is not observed on cooling due to the high activation energy required.
  • Commercially available anatase is typically less than 50 nm in size with the particles possessing a band gap of 3.2 eV, corresponding to a UV wavelength of 387 nm.
  • the adsorptive affinity of anatase for organic compounds is higher than that of rutile and anatase exhibits lower rates of recombination in comparison to rutile due to its 10-fold greater rate of hole trapping.
  • thermodynamically stable rutile phase generally contains particles larger than 200 nm with a smaller band-gap of 3.0 eV with excitation wavelengths that extend into the visible spectrum at 410 nm.
  • anatase is generally regarded as the more photochemically active phase, due to the combined effect of lower rates of recombination and higher surface adsorptive capacity.
  • TiO 2 synthesis methods such as vapour phase oxidation, hydrolysis of TiCW and titanium alcoholates delivering TiO 2 with different structures, crystallinities and impurities resulting in different properties. Photocatalytic activity is influenced by crystal structure, porosity, surface area, particle size distribution and surface hydroxyl density.
  • TiO 2 as a photocatalyst include its insolubility in water and its non-toxicity.
  • the photocatalytic process does not require the addition of consumable chemicals and a waste sludge is not produced.
  • Anatase TiO 2 has a band gap energy of 3.2 eV equivalent to light of ⁇ 387 run or less. Since TiO 2 absorbs near-UV light, the exploitation of solar energy is a real possibility. A small but significant proportion of light between 300 - 400 nm of the solar spectrum reaches the earth's surface and could be utilised for the photocatalytic treatment of water.
  • the final product of the reduction may also be OH* radicals and the hydroperoxyl radical HO 2 .
  • Hydroxyl radicals have long been known as strong, indiscriminate oxidizing agents. During photocatalysis they can react with organic compounds and bacterial species adsorbed onto, or very close to the semiconductor surface resulting in degradation (total oxidation of pollutant results in production of carbon dioxide and water). TiO 2 has been produced in various forms.
  • TiO 2 particles can be loaded with metals and metal oxides such as vanadium oxide, platinum, manganese oxide, palladium and ruthenium. Metals on TiO 2 ease the separation of charges with electrons collected in metal particles.
  • TiO2 and activated carbon composites can have excellent activity for NOx conversion due to the strong TiOi photocatalytic activity and activated carbon adsorption, while the addition of metal oxides such as Fe 2 O 3 , CO 3 O 4 and NiO to the Ti ⁇ 2 -activated carbon composite catalyst increases the activity.
  • Degussa P25 is TiO 2 produced by vapour phase oxidation characterised by a narrow particle size distribution, high photoactivity, minimal impurities (99.5% pure TiO 2 ) and containing up to 25% rutile in anatase or a , which has a composition ratio of 75:25 anatase: rutile, and crystallites, which are non- porous and cubic with rounded edges.
  • Degussa P25 has an average particle size of ⁇ 21 nm, a specific area of 50 ⁇ 15 m2 g-1. The high activity of Degussa P25 is thought to be due to a more positive CB potential in rutile compared to anatase.
  • Degussa P25 is a mixed phase semiconductor, whereby negative charges produced on rutile by visible light are stabilised through electron transfer to lower energy anatase lattice trapping sites (et) allowing electrons to reach the surface. Transfer of the photogenerated electron to anatase lattice trapping sites allows holes that would have been lost to recombination to also reach the surface via lattice trapping sites (ht).
  • Degussa P25 can be immobilized on amorphous silica and glass plates.
  • BOD means for present application 'biological oxygen demand' or 'biochemical oxygen demand;
  • K 2 O 'potassium monoxide'
  • mM 'milliMole' (A chemical unit of concentration)
  • N 'nitrogen' (An element, existing predominantly in compounds with other elements, such as oxygen and hydrogen, in the environmental systems )
  • NH 3 'ammonia', or 'non-ionised ammonia' (Inorganic nitrogen compound)
  • NH 3 -N 'nitrogen as ammonia' (The amount of nitrogen present in the form NH 3 NH 4 'ionised ammonia' / 'ammonium' (Inorganic nitrogen compound.
  • NO 2 'nitrite' Inorganic nitrogen compound.
  • NO 2 -N 'nitrogen as nitrite' (The amount of nitrogen present in the form NO 2 )
  • NO 3 'nitrate' (Inorganic nitrogen compound.
  • CB or cb Conduction band
  • CoA Co-enzyme A
  • CV Cyclic voltammogram
  • DI Distilled water
  • Dp Particle diameter
  • e- Electron
  • EAP Electrochemically-assisted photocatalysis
  • Ebg Band gap
  • Er Reference potential
  • Es S ample potential
  • et Lattice trapping site for electrons
  • eV Electron volt
  • FTIR Fourier transform infrared
  • FWHM Full width half maximum
  • Lattice trapping sites or holes
  • hv Photon of light/energy
  • ip In-plane vibration
  • MW Microwave
  • nm Nanometer
  • O2-- Superoxide
  • OH* Hydroxyl radical, Ox.
  • a drain is in present invention in the meaning of this invention is a pipe or channel that carries off waste fluid, preferably waste water or waste atmosphere from the agriculture system of present invention or it can be the container (the drain storage tank) that contains the waste fluid before its is released from the confined agriculture environments. Eventually some of this drain water can be used to mix it again with water from the clean water basin.
  • “Chemoautotrophic” bacteria in the meaning of present invention are bacteria that grow by consuming inorganic nitrogen compounds. Many species of nitrifying bacteria have complex internal membrane systems that are the location for key eri2ymes in nitrification: ammonia monooxygenase which oxidizes ammonia to hydroxylamine, and nitrite oxidoreductase, which oxidizes nitrite to nitrate.
  • Photoautotrophic organisms in the meaning of present invention are organisms, typically a plant, that obtain energy from sunlight as its source of energy to convert inorganic materials into organic materials for use in cellular functions such as biosynthesis and respiration. In order to capture light as source of energy, photoautotrophs carry out photosynthesis, converting energy from sunlight, carbon dioxide and water into organic materials. Photoautotrophs provide nutrition for many forms of life. They include the plants, algae and certain protists bacteria.
  • Photoheterotrophs are heterotrophic organisms which use light for energy, but cannot use carbon dioxide as their sole carbon source. Consequently, they use organic compounds from the environment to satisfy their carbon requirements. They use compounds such as carbohydrates, fatty acids and alcohols as their organic "food”. Examples are purple non-sulfur bacteria, green non- sulfur bacteria and heliobacteria .
  • Oxygenic for the present invention is in the meaning of not producing oxygen, especially to describe certain forms of bacterial photosynthesis.
  • anoxygenic is most often used to describe the form of photosynthesis in purple bacteria, green sulfur bacteria, green non-sulfur bacteria, and heliobacteria.
  • the electron flow is cyclic with all electrons used in photosynthesis eventually being transferred back to the single reaction centre and oxygen is not produced.
  • Crops are in the meaning of this invention of multicellular or unicellular photosynthetic producer organisms for instance plants that are cultured for a particular use for instance for gaining useful biomass. Crops can be chemoautotrophic or photoautotrophic organisms.
  • Plants photoautotrophic (multicellular or unicellular) organisms belonging to the Plantae.
  • Glycogen accumulating organisms are organisms that use energy from glycolysis to accumulate substrate (e.g. glucose ) fermentations products (e.g. acetate in the form of poly-hydroxy-butyrate (PHB).
  • substrate e.g. glucose
  • PLB poly-hydroxy-butyrate
  • Polyphosphate accumulating organisms use energy stored in poly-P to store exogenous substrate in the form of poly-hydroxy-butyrate (PHB).
  • Activated sludge concerns the active biological material produced by activated sludge plants and which affects all the purification processes.
  • This activated sludge which in healthy sludge (healthy activated sludge) which is a brown floe, is largely composed of saprotrophic bacteria but also has an important protozoan flora mainly composed of amoebae, Spirotrichs, Peritrichs including Vorticellids and a range of other filter feeding species.
  • Other important constituents include motile and sedentary Rotifers.
  • nanoparticle particles having nanometric dimensions, and nanoparticles may have, for example, dimensions in the order of a few nanometres to several hundred nanometres. The nanoparticles may be of a similar size to or smaller size than any given target virus or viruses.
  • Biof ⁇ lm for the meaning of this invention is a community of microbials forming at a phase boundary generally, but not always, at a liquid:solid interface. Spatially and temporally heterogeneous. May have specific mechanisms for attachment to surface. Generates EPS for adhesion, protection and to facilitate community interactions.
  • Bacterial colony for the meaning of this invention is a group of organisms growing on a surface, often fed with nutrient from below and incorporating gas exchange from above. May be a clone formed from a single cell. Shows recognizable pattern, limited morphogenesis and spatial and temporal heterogeneity.
  • a floe for the meaning of present invention is a loosely associated mixed community of microbials showing irregular radial symmetry and temporal and spatial heterogeneity.
  • Anaerobic (digester) granules for the meaning of present invention is a reasonably symmetrical radially organized microbial community showing spatial differentiation and metabolic co-operation, often leading to the oxidation of organic substrates, leading in the end to gas such as energy rich methane or as N 2 .
  • Aerobic (digester) granules for the meaning of present invention is a reasonably symmetrical radially organized microbial community, preferably with diameter: 2-8 mm, formed in an aerobic environment and showing spatial differentiation and metabolic co-operation with phosphate removal and anoxic growth in the corn, nitrification in a middle zone and heterotrophic growth in an outer layer.
  • the system of present invention can be in situ monitored by the following hard sensors and on-line analyzers for water analysis and water process monitoring to produce a signal indicative for the measure of a selected biotic or abiotic parameter and control and automatically monitoring the fluid systems of the aquatic farm systems to detect and measure abiotic and biotic parameters; and subsequently at the detection of an unwanted shift van be controlled by a soft sensor system in operational contacts with a programmable actuator adapted to regulate said biotic or abiotic parameter.
  • Several commercially available hard sensors have been identified as particularly suited for the monitoring of the aquatic farm systems of the present invention.
  • the physical arrangement of hard sensor and the soft sensor controller can take many forms including but not limited to the few arrangements described herein.
  • An aspect of the invention uses a model-based predictive controller based on an adaptive dynamic reactor model to predict a future response of said bioreactors to said interaction physicochemical and/or electrochemical reactors as a function of time and compensates effects of external disturbance on said bioreactors by adjusting said operation rate of said physicochemical and/or electrochemical reactors regulators to achieve a norm status in culture units of the aquatic organisms.
  • the parameter settings are here by adapted by the incoming signal to more closely approximate the dynamic behaviour of the biof ⁇ lters.
  • the controller pro-actively compensates a future effect of known current or future disturbances by using said adaptive dynamic model in order to minimise deviation from norm biofilter function and in such way protects the aquatic organisms culture units.
  • liquid good candidates are of hard sensor, in particular for integration in the sensor network of present invention but are not limited to, are:
  • Aqueous NH 4 + ZNH 3 can be measured using a gas sensing electrode for instance model 95 - 12 Therma Orian, Beverly, MA.
  • reagent less UV spectrophotometry with simultaneous determination of nitrate and nitrite are available for nitrogen cycling in waters.
  • the in situ UV spectrophotometric sensor ProPS, TriOS GmbH, Oldenburg, Germany
  • the real time, in situ, high resolution simultaneous mapping of nitrate/nitrite linearity 0.01 - 6 mg N L-I, RSD's NO 3 -N 4-10%, NO 2 -N 7-14%) in fresh and estuarine waters.
  • a particular aspect of present invention is a in situ monitoring by the following sensors.
  • In situ reagentless UV spectrophotometry with simultaneous determination of nitrate and nitrite are available for nitrogen cycling in waters.
  • the in situ UV spectrophotometric sensor ProPS, TriOS GmbH, Oldenburg, Germany
  • the in situ UV spectrophotometric sensor can be used for the real time, in situ, high resolution simultaneous mapping of nitrate/nitrite (linearity 0.01 - 6 mg N L-I, RSD's NO 3 -N 4-10%, NO 2 -N 7-14%) in fresh and estuarine waters.
  • Conventional pH probe connected to a pH amplifier can be used to monitor the pH and the electrical conductivity (EC) with an EC sensor (e.g. Models EC250 & EC350 Stevens-Greenspan) and with dissolved oxygen sensor (Stevens-Greenspan Dissolved Oxygen Sensor). It is particularly suitable to monitor and adjust O 2 , pH and electrical conductivity in the injection of acid, base and/or various nutrient mixes in nutrient reservoir tank to the photocatalytic bioreactor.
  • EC sensor e.g. Models EC250 & EC350 Stevens-Greenspan
  • dissolved oxygen sensor Stevens-Greenspan Dissolved Oxygen Sensor
  • actuators such as injectors of acid, base and/or various nutrient mixes in nutrient reservoir tank to the photocatalytic bioreactor.
  • a phosphate sensor for instance the Helios Phosphate Process Buoy (Envitech Ltd), measures phosphate through direct immersion in aeration basins or final effluent.
  • the Stip Helios phosphate process buoy measures phosphate through direct immersion in aeration basins or final effluent.
  • the buoy is filled by the hydrostatic pressure of the water, and emptied by air pressure. This eliminates the need for pumps in the waste water. Valves contact only air, reagents and calibration standards, assuring a high level of reliability.
  • the buoy is equipped with a filtration cell, in which wastewater is separated from sludge and solids before it is fed into the reaction cell.
  • the buoy automatically calibrates itself daily using the standard addition method, and at the same time compensates for variability in the wastewater.
  • the Helios Phosphate Process Buoy measures phosphate through direct immersion in aeration basins or final effluent. The buoy is filled by the hydrostatic pressure of the water, and emptied by air pressure. This eliminates the need for pumps in the wastewater. Valves contact only air, reagents, and calibration standards, assuring a high level of reliability.
  • the Phosphate Buoy is equipped with a filtration cell, in which wastewater is separated from sludge and solids before it is fed into the reaction cell.
  • a low volume of reagent is accurately regulated to assure high measuring accuracy with low reagent consumption.
  • the buoy automatically calibrates itself daily using the standard addition method, and at the same time compensates for variability in the wastewater.
  • the On-Line PO 4 measurement Spectron (Envitech Ltd) is a spectrophotometric analyser for quasi continuous on-line measurement of Phosphate in wastewater.
  • the Spectron is equipped with signal outputs of 0-20 or 4-20 mA.
  • a built-in graphical display shows concentration data and other important information, which are stored for the last 14 days.
  • An optional diskette drive provides long-term data storage.
  • the Spectron is a spectrophotometric analyser for quasi continuous measurement of phosphorus in wastewater.
  • the sample is thermally digested.
  • specific reagents are added, which form an intense yellow complex with phosphorus with concentration dependent absorbance between 380 and 480 nm.
  • the analyser is equipped with a diode array spectrophotometer that operates from 380 to 780 nm, and automatically calibrates itself daily using two standards. Both these Spectron analysers have a bypass which is the fast feed loop to the analyser.
  • the peristaltic pump transfers a portion of the sample to the measuring cell, where it is mixed with reagents delivered by the reagent pumps.
  • the farming system comprises at least one ammonia and/or nitrate sensor for sensing ammonium and/or nitrate in the liquids.
  • ammonia and/or nitrate sensor for sensing ammonium and/or nitrate in the liquids.
  • AmNiSys ammonia and nitrate measuring system (Envitech Ltd) AmNiSys is a specification ammonia and nitrate measuring system with true continuous reading for use in wastewater applications which also can accommodate fluorescent DO measurement.
  • the completeness of the nitrification can also be followed in situ by an ammonium probe (e.g. the "NtLjD sc Ammonium Probe") combined with colorimetric or spectrophotometric nitrite ion and nitrate ion analysis.
  • an ammonium probe e.g. the "NtLjD sc Ammonium Probe”
  • the GENION 1 is an on-line analyzer for continuous NH 4 + measurement using a gas-selective electrode. The analyzer automatically calibrates itself daily using a standard. The bypass is the fast feed loop to the analyzer. The peristaltic pump transfers a portion of the sample to the measuring cell. In the mixing cell wastewater and dilution water are combined. Oil and fat are separated by the rotation of the agitator.
  • the rotating slit is the inlet to the measuring cell and the only flow restriction inside the system.
  • the slit is continuously cleaned by the rotary motion of the axle.
  • the NH 4 + concentration of the wastewater is maintained at a constant, low level.
  • the desired value of the electrode is thus also maintained at a high-sensitivity bias point.
  • the actual value is calculated from the NH 4 + concentration and the dilution ratio.
  • the measuring point corresponds to the calibration point.
  • Another possibility is the Isco-Stip in-situ process boys for NH 4 + & NO 3 " (Envitech Ltd). This Process Buoys measure nitrate and ammonium through direct immersion in aeration basins or final effluent.
  • the buoy is filled by the hydrostatic pressure of the water, and emptied by air pressure. This eliminates the need for any pumps in the wastewater. Valves contact only air, reagents, and calibration standards, assuring a high level of reliability.
  • the Isco-Stip Process Buoy PBS 1 (NH 4 + ) is equipped with a purgeable cell, in which, wastewater is separated from sludge and solids before it is fed into the reaction cell. During the ammonium measurement, the necessary pH value is accurately regulated to assure high measuring accuracy with low reagent consumption.
  • the buoy automatically calibrates itself daily using the standard addition method, and at the same time compensates for variability in the water.
  • the spectroscopic sensor, Stip-scan of Envitech Ltd uses a light spectrum from 190 to 720 nm with settlement phase can be used for on-line measurement of Total Solids and SVI (Sludge Volume Index) with simultaneous accurate and reliable in-situ measurement of a wide range of parameters such as NO3, SAC(UV 254), COD, and TOC with accommodation the interfering effects of turbidity, colour and "overlapping" absorption spectra.
  • the biological oxygen demand is measured by a BIOX-1010 apparatus, which is an on-line analyser for continuous BOD measurement (Envitech Ltd). It operates by continuously pumping sampled water through a sample bypass. The peristaltic pump built into BIOX continuously feeds a small stream of wastewater from the sample bypass to the bioreactor. Before it reaches the bioreactor, this wastewater stream is diluted with oxygen-saturated dilution water supplied by a gear pump. Another suitable sensor is the PHOENIX-1010 (Envitech Ltd). It is a does continuous rapid COD measurement which is a procedure for quick analysis of Chemical Oxygen Demand. In the PHOENDC-1010 analyser, this procedure uses ozone for oxidation and thus operates with one of the most powerful oxidizing agents available. The analysis lag time between sample entering the intake and data output is 3 to 15 minutes for a measurement range of 10 to 1500 mg/litre COD. The analyzer automatically calibrates itself each day.
  • the total oxygen demand (TOO is analysed in situ for instance by the STIP-toc (Envitech Ltd) is an analytical apparatus that functions as a high temperature TOC analyzer without ultra- or fine filtration.
  • a large sample stream is taken in via an automatically self-cleaning coarse filter in the sample bypass.
  • inorganic carbon is removed through acidification and sparging.
  • a sub stream for analysis is split off directly before the furnace.
  • the analysis stream is thermally and catalytically oxidized. After the evolved gas mixture is dried and neutralized, it is measured as CO 2 in the IR detector, and reported as TOC.
  • the system automatically calibrates itself daily with two TOC standards (two point calibration.
  • the Isco-STIP-toc (Envitech Ltd), on the other hand, functions as a high-temperature TOC analyser without ultra or fine filtration.
  • Isco-STIP-toc (Envitech Ltd) is a TOC analysers that functions as a high-temperature TOC analyser without ultra or fine filtration.
  • In situ Toxicity monitor is used to monitor microbial effects.
  • a suitable sensor is the STIPTOX-adapt (W) (Envitech Ltd), which is a toxicity analyser with immobilized turbulent- bed biology.
  • BIOX-1010 the microbes grow on the inner surface of small hollow cylinders.
  • the microbial population in the bioreactor is adapted to the conditions of the wastewater.
  • the organisms in the bioreactor take up dissolved oxygen.
  • a toxic impact inhibits the respiration of the organisms, causing an increase in the dissolved oxygen level. If the respiration rate decreases by more than about 20%, an additional dilution of the wastewater is triggered, and is regulated such that the overall depression of microbial activity does not exceed 20%. This protects the microbes and provides the mechanism for toxicity measurement.
  • the mixing ratio of wastewater and dilution water, together with the oxygen difference, are used to calculate the toxicity reading.
  • the photocatalytic detoxification efficiency and removal of toxic intermediates is sensed in situ by an online toxicity sensor.
  • New reliable and continuous monitors which can provide (near) real-time information on water quality are available. They can be used for control of the water output of a the photocatalytic bioreactor.
  • the chemical analytical monitoring systems identify and quantify specific water contaminants, biomonitoring on the other had gives an indication of the total quality, including the effects of unknown toxic substances.
  • the TOXcontrol a biological toxicity monitor using luminescent bacteria (Biesbosweg 2 • 5145 PZ Waalwijk), the s::can spectrolyser(TM), a submersible UV-VIS spectrophotometer probe (Mefitechnik GmbH), is used to biomonitor and sense the a broad range of quantities of intermediates at low concentrations in the reactor output to guarantee full mineralization.
  • Continuous measurement of acute toxicity in water can be done by a solid state microrespirometer such as the microrespirometer described by Fco. Javier Del Campo et al Sensors and Actuators B: Chemical Volume 126, Issue 2, 1 October 2007, Pages 515-521 which consists of a naturally developed biofilm of Pseudomonas aeruginosa over a Nafion modified array of gold microdisc electrodes. They system warns against the presence of toxic substances in the environment where it is placed.
  • MicroLAN BV (Waalwijk, the Netherlands) or microLAN US (Wilmington Delaware, US) combines biomonitor using luminescent bacteria (Vibrio fischeri) with s::can UV-VIS sensor technology in an integrated system for on-line monitoring and for global effect monitoring for instance the aquatic toxicity.
  • a microbial fuel cell based biosensor generates electrical current as a direct linear measure of metabolic activity of the electrochemically active microorganisms.
  • the microorganisms gain energy from the anodic over potential and a direct control of the over potential allows to detect a toxic event and prevents false positives (Stein, NE et al. Bioelectrochemistry 78 (1): 87 - 91 2010).
  • Solid state microrepspirometers are available for the continued measurement of acute toxicity events in water (Del Campo, FJ. Sensor and actuators B - Chemical 126515 - 521 2007).
  • the photoluminescence biosensors incorporate a biological component coupled to a transducer which translates the interaction between the analyte and the biocomponent into a signal that can be processed and reported (Reardon, KF et al. Optical sensor systems in biotechnology 11699- 123 , 2009) These sensor are particularly suitable for sensing toxicity in an aqueous environment.
  • On-Line PO 4 is measured online by the Spectron (Envitech Ltd), which is a spectrophotometric analyser for quasi continuous on-line measurement of Phosphate in wastewater.
  • the SPECTRON is equipped with signal outputs of 0-20 or 4-20 mA.
  • a built-in graphical display shows concentration data and other important information, which are stored for the last 14 days.
  • An optional diskette drive provides long-term data storage.
  • the SPECTRON (Ptotal) (Envitech Ltd) is a spectrophotometric analyser for quasi continuous measurement of phosphorus in wastewater. The sample is thermally digested. Then specific reagents are added, which form an intense yellow complex with phosphorus with concentration dependent absorbance between 380 and 480 nm.
  • the analyser is equipped with a diode array spectrophotometer that operates from 380 to 780 nm, and automatically calibrates itself daily using two standards. For both systems a bypass is the fast feed loop to the analyser.
  • the peristaltic pump transfers a portion of the sample to the measuring cell, where it is mixed with reagents delivered by the reagent pumps. As the sample and reagent streams mix, they form the yellow colour complex, which is analysed between 380 and 480 nm
  • the flow of liquid in and from the separate reactors is measured by a flow meter.
  • a flow meter is an instrument used to measure linear, nonlinear, mass or volumetric flow rate of a liquid or a gas. Water flows can be read from permanent flow meters (e.g. type: B ⁇ rkert, mod. 8035). Where the fluid systems are gas the flow can be measured by measuring the gravimetric flow rate of that gas with a mass flow meter.
  • Salinity meters are used to assess the salinity in the watery fluids and the nutrient solutions of the aquatic farming system.
  • electronic meters commonly available for measuring the salinity of water or a nutrient solution.
  • the two most popular meters are electroconductivity (EC) and Total Dissolved Solids (TDS) meters.
  • EC electroconductivity
  • TDS Total Dissolved Solids
  • an EC meter measures the ability of an aqueous solution to carry an electric current. It does this by measuring the electric current between two electrodes (the electricity flows by ion transport).
  • a nutrient-rich solution will have a higher electroconductivity than a solution with less ionic salts.
  • Microprocessor technology scales the measurement of electroconductivity into either milliSiemens/cm (mS/cm) or microSiemens/cm (mS/cm).
  • EC meters are favoured by commercial growers, simply because they give the best estimate of the strength of a nutrient solution.
  • TDS is the concentration of a solution as the total weight of dissolved solids. These meters are widely used by hobbyists, and actually measure the electroconductivity of a solution. They do this by measuring the electric current between two electrodes. A greater concentration of nutrients will cause the electric current to flow faster than a solution with a lower concentration.
  • Microprocessor technology uses an in-built conversion factor to scale the readout in so-called parts per million (ppm).
  • hi situ salinity measurements in can be done with a fibre-optic probes based on a multi-channel axial optical fibre spectrograph (N D'laz-Herrera et al. Meas. Sci. Technol. 17 (2006) 2227-2232)
  • the EC and pH sensors are the simplest form of direct measurement in electrolyte solutions.
  • the EC sensors are used in equipment for the processing of molecular nutrient measure using three equidistant ring-shaped electrodes which are mounted inside reactor tanks or inside water transport system e.g. a water pipe at equal distances.
  • the temperature of the fluid is measured and is used to modify the value of the alternating current (AC) voltage applied between the central electrode and the ground electrodes as a means of temperature compensation.
  • This AC voltage is typically around 1 V.
  • the AC frequency that may range from 400 Hz to 50 kHz AC voltage is used to avoid polarization of the electrodes.
  • the EC is determined by dividing the AC voltage by the electric current measured between the central electrode and the two end-electrodes. The current ranges from 0.1 to 10 mA. Both end electrodes are connected to each other and to the electrical ground terminal to allow the serial or parallel connection of several EC electrodes in one water supply system. The security is enhanced by using two or more distinct EC electrodes in parallel to provide a check on the functioning of both EC sensors against each other.
  • the pH of a solution indicates how acidic or basic (alkaline) it is.
  • the pH sensor measures the potential across a thin glass bulb or membrane caused by the difference in activity of H 3 O + ions (protons) in the electrolyte on one side of the membrane and the measurant on the other side.
  • a gel is generally as an electrolyte, which means that the electrolyte needs no further replenishing. In this way, the slow deterioration of the pH sensor is avoided.
  • pH sensing is about one year. Also for the pH sensing, two or sensors are preferably used , so that one sensor is checked against the other.
  • ISE Ion-selective Electrode
  • the sensing part of the electrode is usually made as an ion-specific membrane, along with a reference electrode.
  • ISEs are used to measure the activity of cations and anions in the root environment. ISE sensors are available for most macro-nutrients, like K + , Ca 2+ , NO 3 " , SO 4 2" , NH4 + and for Na + and CF
  • hard sensors and on-line analyzers for gas fluid analysis and gas process monitoring and control, in particular for in air measurement which are suitable for the system of present invention:
  • FTIR technology allows for simultaneous quantification of up to 50 different gas components including H 2 O, CO 2 , CO, SO 2 , NO, NO 2 , N 2 O, HF, HCL, NH 3 , VOCs, Hydrocarbons and Formaldehyde. (Libraries are available for 300 different compounds). Speciation of VOCs is also possible.
  • An O 2 /CO 2 analyser can also be used to determine the atmospheric concentrations of CO 2 and O 2 .
  • the O 2 analyzer with zirconia sensor Cambridge Sensotec
  • the controller can actuate the opening of a flow controllers for regulating or a gas flow or mass flow controller (FC) or with a controllable gas flow rate (e.g. from Qualiflow Inc.
  • Infrared CO 2 sensor provide precise CO 2 control and fast response by actuators opening of doors or FCs.
  • Some sensors can specifically measure H 2 and N 2 levels in the atmosphere.
  • the Hydrogen Analyser TG-1500XA- has an excellent sensitivity (no response to other flammable or toxic gases and oxygen is not required) for measuring of H 2 in N 2 .
  • the Fluke 975 simultaneously measures, logs and displays temperature (wet bulb and dew point), velocity, humidity, carbon dioxide (CO 2 ) and carbon monoxide (CO) levels.
  • Absorption-based humidity sensors are available (Honeywell) which provide both temperature and %RH (Relative Humidity) outputs.
  • Such relative humidity/temperature and relative humidity sensors can be configured with integrated circuitry to provide on-chip signal conditioning.
  • a controller can active an actuator such as an air fan for internally air circulation in the confined environment to prevent gradients or such as a heat exchange coil connected to hot or chilled water for temperature control.
  • a controller can also active a de-ionized water injector for adaptation of the atmospheric humidity for instance at levels of 70% which in case of discontinued or staggered culture of the plants can eventually not been controlled by the water evaporation from the plants.
  • in situ sensors can be used to analyse abiotic factors (e.g. O 2 , CO 2 , N 2 ) in a gas or atmosphere that as been stored in a separate buffer tanks or in the atmosphere in the confined environment(s).
  • abiotic factors e.g. O 2 , CO 2 , N 2
  • At least one embodiment of present invention provides the monitoring and control of the hydrogen ion concentration in the water in the environment of the aquatic crops or the roots of the corps and/the aquatic animals of the recirculating culture systems, hi an aquatic farming systems aside temperature and oxygen, pH turned out to be most important abiotic factor that exerts great effect in a short period on the aquatic organisms or on the plants which make contact with their root system in the recirculating water (e.g. soilless culture or crop hydroponics or aquatic animals ) is the hydrogen ion concentration (pH) of their water environment.
  • pH hydrogen ion concentration
  • Hydrogen ions have the ability to move and combine with other ions, this activity (aH) is the effect of the active effective concentration (C H e.g; in gm- moles per liter) and the pH (-log (an) or - log ⁇ * C H ) express this concentration or activity.
  • the pH has a major impact in the aquatic farming systems by shifting the equilibrium of chemical reactions in or surrounding the organisms. Moreover the living organisms are directly affected by the pH of their watery culture medium for instance by a pH induced shift in the ammonium/ammonia equilibrium. For instance nutrient uptake by plant's root systems is temperature and pH dependent. Control of the pH in the various units or bioreactor of an aquatic farming system is important in the farming performance.
  • An embodiment of present invention provides solutions to this problem by control and monitoring system that provides a stable compromised hydrogen ion concentration range (normoPH) for the various Ie farming and bioreactor units with different pH requirements.
  • the present invention provides in an embodiment a monitoring and control systems of the hydrogen ions concentration in the different units of the recirculating farming system and more particularly in water the makes contact with the aquatic animals, the crops (e.g. the roots systems of the soilless corps) and the condominiums of bioremediating microbials (e.g. the nitrifying bacteria and denitrifying bacteria).
  • Present invention foresees in situ pH mentoring and control in the watery environment of the crop.
  • the optimal pH values recommended in soilless crops culture or hydroponics are usually within the range of 5.0-6.0 to obtain optimal nutrient uptake, while pH values between 6.0 and 7.0 will be still adequate for the majority of crops.
  • High pH values (>7.0) in the irrigation water to the soilless plant culture are undesirable, because Ca and Mg carbonates and orthophosphates may precipitate in the irrigation lines and drippers to the crops.
  • the proportion of H 2 PO 4 species decreases and that of HPO 4 2 increases. Since the H 2 PO 4 ion is much more available to plants than HPO 4 2 , high pH may induce P- deficient conditions, even if there is adequate total P in the solution, and high substrate pH may reduce micronutrients availability to plants, because of precipitation reactions.
  • acidic pHs may be detrimental to root membranes and may increase the Al and Mn concentrations in the substrate solution to toxic levels.
  • Very low pH e.g. ⁇ 4.5
  • high pH e.g. > 9.0
  • the main effects of nitrogen source on soilless-grown plants is, modification of the rhizosphere pH, availability of further nutritional elements, NH 4 + toxicity and incidence of physiological disorders such as chlorosis and blossom-end rot (BER).
  • the pH and alkalinity of the watery culture medium in an aquatic farming system for instance in an aquaculture or in a crop hydroponics is thus a major concern for productive and cost effective farming. In particular when recirculating aquaculture systems are integrated with soilless crops in hydroponics culture systems.
  • a range of pH values acceptable for proper flock formation by facultative anaerobes and denitrification is 6.5 to 8.5.
  • the pH in the anaerobic tank is preferably maintained at a pH value greater than 7.0.
  • the optimal pH range for denitrification is 7.0 to 7.5.
  • Present invention foresees in situ pH mentoring and control in the watery environment of the condominiums of microbials that generate the bioremediation and generate the energy to drive the systems actuators (e.g. the systems heat pump system).
  • Stress in a complex organism such as plant or aquatic animal is generally defined as the disturbance of the internal equilibrium (homeostasis) of the organism.
  • Stress on multiple organisms in a condominium can be defined as the disturbance of the equilibrium which such condominium controls and stress on a biosystem of different interacting condominiums can be controlled as disturbance of the equilibrium between this interacting condominiums.
  • Stress on an organism is the first step towards disease occurrence. Stress reduces the resistance of these organisms and makes them more susceptible to diseases which eventually lead to a collapse of the condominium of these organisms and of the biosystem which the condominium of organism controls. Therefore, the extent of stress and the ability of these complex organisms such as aquatic organisms (e.g.
  • PH electrodes offer a great sensitivity and range ability in the farming process management.
  • the sensor can track a minute change of 0.000000005 in hydrogen ions concentration at pH 7.
  • Conventional pH probes connected to a pH amplifier e.g. Crison pH Rocon 18
  • the pH sensor measures the potential across a thin glass bulb or membrane caused by the difference in activity of H 3 O + ions (protons) in the electrolyte on one side of the membrane and the measurant on the other side.
  • the pH can be measured with a standard combination type of sensor and includes a measuring electrode and a reference electrode in the same sensor body.
  • a gel can be used as an electrolyte, which means that the electrolyte needs no further replenishing. In this way, the slow deterioration of the pH sensor is avoided.
  • the lifetime expectancy of these pH sensors is about one year. Two sensors can be used, so that one sensor is checked against the other. .
  • pH is continued sensed in different reactor unit to feed sensor signals in the processes of a controller to control the pH per bioreactor unit in the farming system or maintain systems normo-pH.
  • the present invention obtains such tight controlled pH by a controlled integration of different bioreactor units.
  • the control system of present invention can also be used to maintain a different normo-pH in the aquaculture unit (aquaculture normo-pH or slightly acidic to slightly basic pH (6-7.5)) than the plant normo-pH (range of 5.0-6.0) at the root of the plants in the soilless or hydroponics crop culture.
  • Such systems normo-pH is a pH value between 6- 8, preferably 6.5 to 7.5 and most preferably 7.7 to 7.2.
  • Nitrification bio filters are commonly used in recirculating aquatic animal farming systems. They are however not a common practice in soilless crop culture.
  • integrating the recirculating aquatic animal farming systems with recirculating soilless crop culture we face new problems of biosecurity and maintaining biosystem equilibrium.
  • the pH monitoring and control was found important to realise such integration of nitrifying biofilters in this integration.
  • the pH or concentration of hydrogen ions has an effect on the condominiums of aerobic nitrifying microbials and function of such in the aerobic nitrifying reactor unit or the aerobic nitrifying zone of a nitrifying reactor unit.
  • Such nitrifying bioreactor or nitrifying zone in bioreactors are generally used to convert the ammonia and nitrite ions (that are at relatively low concentrations toxic for aquatic vertebrate and invertebrate animals but also for the photosynthetic cyanobacteria and plants) to less toxic nitrate nutrients. It can be operational run a ammonium oxidation in two consecutive stages: ammonium to nitrate oxidation NH 4 + + 1.5 O 2 ⁇ NO 2 ⁇ + 2H + + H 2 O (e.g. by Nitrosomonas europae ⁇ ) and nitrite to nitrate NO 2 " + 0.5 O 2 — > NO 3 " (e.g.
  • nitrification is about 28°C to 32 °C while at 16 °C the nitrification is approximately 50% of nitrification rate at 30 °C.
  • the pH of the medium has been reported to be another most important influencing factor in nitrification processes, and the tendency for nitrification rates to decrease under acid conditions, is generally recognised.
  • An acidic pH causes low concentrations of carbonates, and a lack of the carbon sources required for microbial growth could be the direct cause of the reduction of nitrification rates.
  • a drop in pH may shut down the nitrifying biofiltering operation resulting into an accumulation of ammonium and/or nitrite.
  • NO 2 -oxidising bacteria were found to be more sensitive to acidic conditions than the NH 4 + oxidisers, and accumulation of toxic levels of nitrogen dioxide (NO2 ⁇ ) under low pH has been reported.
  • the pH has a direct impact on the oxidation process OfNH 4 + to NO 2 " , as H + is a product of this reaction, and consequently, accumulation of free protons in the solution inhibits further oxidation OfNH 4 + .
  • Nitrifying condominiums of organisms affect the pH in the watery medium that is fed to the nitrification bio filters. For instance the there is an effect of the aerobic nitrifying reactor unit on the pH and alkalinity: Furthermore, alkalinity is lost during aerobic nitrification.
  • This loss occurs through the use of alkalinity as a carbon source by nitrifying bacteria and the destruction of alkalinity by the production of hydrogen ions (H + ) and nitrite ions during nitrification.
  • Hydrogen ions are produced when ammonium ions are oxidized to nitrite ions.
  • Alkalinity loss during nitrification thus occurs through the use of alkalinity as a carbon source by nitrifying bacteria. But significantly more alkalinity is lost through the oxidation of ammonium ions namely the destruction of alkalinity by carbon dioxide (CO 2 ) consumption for autotrophic growth, the production of hydrogen ions (H + ) and nitrite ions by the process.
  • alkalis for alkalinity addition to control pH.
  • alkalis are for instance the compounds of the group consisting of sodium bicarbonate (NaHCO 3 Baking soda), Calcium carbonate (CaCO 3
  • Hydroponics greenhouse systems are generally foreseen with stock solution of nutrient/fertilizer which are provided with an extra acid or base solution for pH correction.
  • An extra amount of an acid or base solute can be used to control pH of the batch of nutrient solution in the mixing tank diluter/dispenser units wherein the concentrated fertilizers are diluted to a nutrient solution to be taken up by the plant.
  • hydroponics greenhouse do generally not have microbial nitrifying bioreactors and only recycle a part of there drain water to avoid the negative effects of mineral accumulation crop root.
  • alkalis is limited.
  • Sodium for instance, is an element that is at higher concentration damaging to the plant, the sodium concentration in the water to the plant roots should be less than 0.5 mmol 1 l . It has been shown that high salinity and high sodium concentration displace calcium from membrane-binding sites, and so cause malfunctioning and alteration of the membrane permeability and selectivity in plants.
  • Nitrite ions in relatively low concentrations may be toxic to many aquatic organisms, including bacteria.
  • nitrite ions With decreasing pH, nitrite ions are more easily converted to free nitrous acid.
  • the conversion of nitrite ions to free nitrous acid and its accumulation are a function of nitrite ion concentration and aeration tank pH. Nitrous acid further destroys the alkalinity.
  • pH monitoring and control systems and systems to prevent nitrite ions accumulation and to avoid biofilter wash out. This is especially the case if the farming systems are designed to integrate aquaculture with plant hydroponics or soilless crop culture.
  • facultative anaerobes for instance in anaerobic respiration bioreactor
  • denitrifying bacteria can compensate lost alkalinity or in part restore alkalinity.
  • These organisms have the enzymatic ability to use free molecular oxygen, nitrite ions, or nitrate ions to degrade cBOD.
  • Denitrifying bacteria degrade cBOD using nitrite ions and nitrate ions in the absence of free molecular oxygen. These bacteria degrade cBOD in order to obtain energy for cellular activity and carbon for cellular synthesis (growth and reproduction).
  • Alkalinity is for instance produced when organic nitrogen compounds are deaminated and nitrate ions are destroyed during denitrification.
  • the hydroxyl ion (OH " ) and some of the carbon dioxide produced during denitrification are returned to the activated sludge process as alkalinity.
  • the present invention provides control systems to balance aerobic nitrification and anaerobic denitrification or anoxic respiration with reduction of nitrite ions and nitrate ions.
  • the recirculating aquatic farming comprises in situ hard sensors, preferably continued sensors, that produce a signal indicative of pH, aqueous NH 4 + ZNH 3 , aqueous nitrate or aqueous nitrite in a microbial condominium, preferably microbial condominium in biogranules, and preferably comprising microbials of the group consisting of Brocadia, Kuenenia, Anammoxoglobus, Scalindua and Planctomycetes whereby their output signals are processed online in a processor that controls a programmable actuator adapted to regulate the proportion of aqueous nitrate versus aqueous nitrite and a control system is adapted to regulate the rate of removal of addition of H 4 + ZNH 3 , aqueous nitrate or aqueous nitrite.
  • a model-based predictive controller based on an adaptive dynamic microbial condominium model can predict a future response of said condominium's pH to said administration or removal rate of said aqueous NH 4 + ZNH 3 , aqueous nitrate or aqueous nitrite as a function of time and compensates effects of external disturbance on said condominiums' pH by adjusting said administration rate of said aqueous NH 4 + ZNH 3 , aqueous nitrate or aqueous nitrite to achieve a status of normo-PH and maintained alkalinity in said microbial condominium and the parameter settings are adapted by the incoming signal to more closely approximate the dynamic nitrogen behaviour of the microbial condominium.
  • the programmable actuator can be an inflow controller of clean water, water of the aquatic animal farming unit, water of the soilless crop farming unit water that has been processed in a photocatalytic unit.
  • the control system can furthermore comprise a continuous feedback of said condominiums' pH that is under control and the controller can be feedback controller based on an adaptive dynamic condominium model.
  • the control system strives to nitriteZammonium ratio of 1 or equimolar amounts OfNH 4 + ZNH 3 and nitrite in to watery environment of the condominium of bacteria for instance by partial ammonium removal, nitrate to nitrite reduction (e.g. photochemical-induced reduction), or partial nitrification of ammonium to nitrite to achieve optimal maintenance of the alkalinity.
  • External disturbance can be one selected from the group of disturbances consisting of: increased or decreased input of inhibitory compounds, toxicity, bacterial washout, deficiency of essential nutrients, change in nutrient intake, temperature change, nitrous oxide (N 2 O), microbial contaminants, redox potential change, change in carbon availability and excess in cBOD.
  • the adaptive dynamic condominium model can be based on a low-order (N)ARX-model or it can be based on a state-space model.
  • prefiltered input and output variables i.e. instrumental variables
  • this system is configured to maintain H4+/NH 3 and nitrite in to watery environment of the condominium of bacteria in about equal amounts to enhance anaerobic oxidation of ammonium.
  • the system is configured to maintain normo-pH in the reciculating aquatic farming system. Loss of pH and a shift from systems normo- pH (systems normo-hydrogen ion activity) in integrating recirculating aquatic farming systems of aquatic vertebrate or invertebrate animals with hydroponics or soilless plant culture with a bacterial loop of nitrifying bacterial and denitrifying bacterial condominiums can occur due to denitrification malfunction.
  • the security of the biosystem is further improved and secured by an in situ measurement of nitrous oxide to predict pH collapse.
  • the nitrous oxide can be measured in the gas exit of a nitrifying bioreactor or of a bioreactor with an anoxic or anaerobic zone.
  • nitrous oxide is in situ sensed. For instance a nitrous oxide sensor to quantify nitrous oxide in a nitrous oxide, oxygen and nitrogen gas mixture or directly into the water environment of such bioreactor.
  • the signal produced by the nitrous oxide sensor indicative for instability in the microbial condominium for instance by external disturbance can be processed online in a processor that controls the programmable actuator adapted to adaptive dynamic microbial condominium model can predict a future response of said condominium's pH to said administration or removal rate of said aqueous NH 4 + ZNH 3 , aqueous nitrate or aqueous nitrite as a function of time and to compensate the effects of external disturbance on said condominiums' pH.
  • Nitrous oxide sensors are available in the art. For instance the Unisense nitrous oxide microsensor is a miniaturized Clark-type nitrous oxide sensor with a guard cathode designed reliable and fast measurements at high spatial resolution.
  • the Unisense nitrous oxide microsensor is equipped with an oxygen front guard making it insensitive to oxygen.
  • In situ measurements of nitric oxide in exhaust of a denitrifying bioreactor is possible using a sensor based on a widely tuneable external-cavity GaN diode laser (Thomas N. et al. Applied Optics, Vol. 46, Issue 19, pp. 3946-3957) or by microsensors (Andersen K, Kjaer T, Revsbech NP (2001) An oxygen insensitive microsensor for nitrous oxide. Sensor Actuat B-Chem 81:42-48).
  • the production and release of nitrous oxide usually occurs under strongly fluctuating conditions or when denitrifying bacteria are adversely affected.
  • the amount of nitrous oxide released is relatively small.
  • Nitric oxide is not ordinarily released from the bacterial cells and is this indicative for biofilter instability.
  • the Unisense N 2 O sensor can directly measure levels of dissolved N 2 O in aqueous environments and is not sensitive to O 2 .
  • N 2 O is continued sensed to feed sensor signals in the processes of a controller warn for bioreactor instability and to react to control the pH per bioreactor unit in the farming system or to maintain systems normo-pH.
  • the alkalinity rebuild is important because much alkalinity is lost in the activated sludge process during nitrification. Approximately 50% of the alkalinity lost during nitrification is returned during denitrification.
  • the amount of alkalinity produced or returned to an activated sludge process during denitrification is 3.57 mg as CaCO3 per milligram of nitrate ions that are reduced to molecular nitrogen.
  • the amount of alkalinity produced or returned to an activated sludge process during denitrification is 3.57 mg as CaCO 3 per milligram of nitrate ions that are reduced to molecular nitrogen.
  • This amount of alkalinity that is returned during denitrification is approximately one-half the amount of alkalinity that is lost during nitrification.
  • the net alkalinity change in an activated sludge process through bacterial activity is a function of organic-nitrogen compounds deaminated, ammonium ions converted to nitrite ions, ammonium ions assimilated into new cells or Mixed Liquor Volatile Suspended Solids (MLVSS), and nitrate ions destroyed during denitrification.
  • Denitrification removes nitrogen from the wastewater by converting it to insoluble gases that escapes to the atmosphere. This nitrogen-containing gas is insoluble in wastewater and escapes to the atmosphere.
  • nitrite ions and nitrate ions When nitrite ions and nitrate ions are reduced to ammonium ions inside the bacterial cell, the nitrogen in the ammonium ions is incorporated into cellular material. This reduction of nitrogen is termed "assimilatory" nitrite or nitrate reduction. Assimilatory nitrite reduction and assimilatory nitrate reduction do not remove nitrogen from the wastewater. Condominiums of denitrification can thus be used in a controlled manner to compensate at least the alkalinity destruction by the nitrifying bacterial condominiums if the stability of such bacterial system is controllable. The stability of such cooperating nitrifying and denitrifying bacterial system is critical and difficult to guarantee in recirculating aquatic farming systems wherein the equilibrium is multifactorial.
  • nitrous oxide N 2 O
  • Nitrous oxide also is produced and released by denitrifying bacteria. Nitrous oxide sensor to quantify nitrous oxide in a nitrous oxide, oxygen and nitrogen gas mixture or directly into the water environment of such bioreactor that nitrous oxide sensors are available in the art.
  • the Unisense nitrous oxide microsensor is a miniaturized Clark-type nitrous oxide sensor with a guard cathode designed reliable and fast measurements at high spatial resolution.
  • the Unisense nitrous oxide microsensor is equipped with an oxygen front guard making it insensitive to oxygen.
  • In situ measurements of nitric oxide in exhaust of a denitrifying bioreactor is possible using a sensor based on a widely tuneable external-cavity GaN diode laser (Thomas N. et al. Applied Optics, Vol. 46, Issue 19, pp. 3946-3957) or by microsensors (Andersen K, Kjaer T, Revsbech NP (2001) An oxygen insensitive microsensor for nitrous oxide.
  • nitrous oxide usually occurs under strongly fluctuating conditions or when denitrifying bacteria are adversely affected.
  • the amount of nitrous oxide released is relatively small.
  • Nitric oxide is not ordinarily released from the bacterial cells and is this indicative for biofilter instability.
  • the Unisense N 2 O sensor can directly measure levels of dissolved N 2 O in aqueous environments and is not sensitive to O 2 .
  • An embodiment of present invention foresees in situ measurement of nitrous oxide and to feed the signals of said sensor to a controller to predict aerobic biof ⁇ lter collapse.
  • the present invention optimally uses the integration of aerobic nitrification and denitrification to save on oxygenation cost and maintain the alkalinity.
  • nitrous oxide usually occurs under strongly fluctuating conditions or when denitrifying bacteria are adversely affected. Since in the system of present invention, at least one bioreactor with condominiums of denitrifying bacteria is introduced to compensate at least in part the alkalinity reducing effect of the condominiums of denitrifying bacteria we hypothesized that the increase of nitrous oxide in said the denitrifying bioreactor is a sentinel or early warning before the denitrifying bioreactor loses its compensatory alkalinity rebuilding effect.
  • An embodiment of present invention integrates such in situ nitric oxide sensor in a sensor network of the aquatic pH, nitrate, nitrite and ammonium to control actuators that control ammonium, nitrate and nitrite proportions.
  • present invention it is a particular embodiment of present invention to have the nitrifying condominiums which decline alkalinity and reduce pH are compensated by the alkalinity building up and pH increasing activity of the denitrifying condominiums. This can be achieved under control of a hard and soft sensing system. These condominiums can be in different bioreactor units or can be in different zone of the same bioreactor system. For instance present invention provides a security ammonium removal system to reduce the ammonium-ion toxicity and to maintain the pH at systems normo-pH by switching on alternative ammonium removal.
  • the pH monitoring system is organised to maintain a dual pH regime of an aquaculture normo-pH and a crop normo-pH in the plant culture unit for instance in the hydroponics or soilless plant culture.
  • a sensor network with hard sensors monitor the different bioreactor (plant culture, aquatic animal culture, microbial nitrification / denitrification) and balance their pH and alkalinity effects towards normo-PH (system normo-pH or aquaculture normo-pH in combination with crop normo-pH).
  • normo-PH system normo-pH or aquaculture normo-pH in combination with crop normo-pH
  • IRAFS recirculating intensive aquatic farming system
  • the hard sensors can measure N 2 O, NH 4 + ZNH 3 , NO 2 " and NO 3 " and feed a signal representative for the measurement to a processor with a model based controller to activate if required the bioreactor system to transfer ammonium and nitrite directly into N 2 while preserving the alkalinity (e.g. by modulating the ammonium / nitrite proportion in the water to be treated).
  • a processor with a model based controller to activate if required the bioreactor system to transfer ammonium and nitrite directly into N 2 while preserving the alkalinity (e.g. by modulating the ammonium / nitrite proportion in the water to be treated).
  • turbulence or an up flow gas velocity of more than 1.2 cm/s biogranules are formed in an aerobic or anaerobic conditions, e.g.
  • the biogranules will comprise an outer zone of heterotrophic growth (COD + O 2 ⁇ CO 2 + H 2 O), hereunder a nitrification zone (NH 4 + O 2 — * NOx) and in the core an anoxic zone capable of phosphate removal (COD + NOx + PO 4 3" ⁇ N 2 + CO 2 + H 2 O + poly-P).
  • the turbulence is preferably carried out by rotors instead of direct aeration to form more stable biogranules.
  • Aeration or oxygenation is preferably done in a separated tank that feeds its water into the tank or bioreactor with the biogranulation process.
  • the bioreactor with the microbial granules can be up flow sludge blanket reactor (AUSB) whereby the reactor contents are kept in turbulence for instance by a rotor. Poor settable granules being removed in a discontinued a sequencing batch reactor (SBR) with settling periods or a continued process.
  • AUSB up flow sludge blanket reactor
  • SBR sequencing batch reactor
  • the system of present invention with control the bioreactor to work on direct transformation of ammonium ions in N 2
  • the farming system of present invention can in an embodiment be foreseen with alternative ammonium removal systems to response to a change in for instance ammonium toxicity, pH and a change in NO 2 production in the bioreactor units.
  • ammonium removal systems can be alternative microbial roots or can be non microbial physical systems with and actuator that responds to a signal from a controller.
  • An embodiment of invention provides a hard sensing means for sensing NO 2 .
  • NO 2 is indicative for an unstable denitrification process and adds to acidification and alkalinity breakdown by the aerobic nitrification process.
  • NH 4 + ZNH 3 and NO 2 " are preferably in situ measured to control adequate ammonium and nitrite to N 2 conversion.
  • Nitrification is operationally run by an ammonium oxidation in two consecutive stages: ammonium to nitrate oxidation NH 4 + + 1.5 O 2 - NO 2 " + 2H + + H 2 O (e.g. by Nitrosomonas europaed) and nitrite to nitrate NO 2 " + 0.5 O 2 - NO 3 " (e.g. by Nitrobacter winogradskyi e.g. strain Nb-255) whereby dissolved oxygen is removed from the water by the bacteria and added to the ammonium ions and nitrite ions.
  • the aquatic farming system is provided with a unit that switch to an anaerobic ammonium oxidation instead.
  • Hard sensors that measure a pH drop and /or measure an increase in nitrous acids in the nitrification bioreactor can activate an actuator to switch that bioreactor operates on a mode of partial nitrification or anaerobic ammonium oxidation. Aerobic oxidation of ammonium is switched to ammonium oxidation under of conditions limited molecular oxygen (O2). For instance a sensor that picks up a signal of NO 2 increase will provide a signal to a computer compressor with a controller or to a controller to provide signals to activate such activator. One such actuation is preventing that nitrite and oxygen are available as electron acceptors.
  • anaerobic ammonium oxidation can be induced by imposed CO 2 and O 2 limitation such that the nitrite is used as a oxidant to ammonia forcing the bioreactor to operate in partial nitrification with the direct transformation of ammonium ions in N 2 or simultaneously transforming nitrite and ammonium into in N 2 ( NH 4 + NO 2 " ⁇ N 2 + 2H 2 O). Van Cleemput, O., and L. Baert. and Smith, D. H., and F. E.
  • Clark demonstrated that NH 4 + and NO 2 " under low pH and under an NO atmosphere (to prevent decomposition of nitrite) have been demonstrated to produce N 2 from ammonium and nitrite been confirmed (Van Cleemput, O., and L. Baert. 1984. Plant Soil 76:233-241 and Smith, D. K, and F. E. Clark. 1960.
  • Soil Sci.90:86- 92 a process of anaerobic ammonium oxidation that dad also been suggested by Engelbert Broda (1977) Mulder, Arnold described anaerobic ammonium ion oxidizing microorganisms (US5078884 A (1992)) in which ammonium ion is used as electron donor in the denitrification whereby for the ammonium ion oxidation no extra carbon- source is necessary to achieve denitrification and of course less oxygen is required than for aerobic ammonium oxidation.
  • Van de Graaf et al confirmed in a denitrifying fluidized bed reactor that this direct conversion of ammonium to dinitrogen gas without oxygen and with nitrite as the electron acceptor (NH 4 + + NO 2 " -> 2H 2 O + N 2 ) is a bacterial process (Van de Graaf et al Microbiology, Apr. 1995, p. 1246-1251). Important nitrogen losses (40 — 70 %) hde been observed earlier in rotating biological contactor bt Baumgarten and Seyfried, 1996 (Baumbaum and Seyfried, 1996 G. Baumgarten and CF. Seyfried, Water Science and Technology 34 (7—8) (1996), pp.
  • Such bioreactor can host for instance Brocadia, Kuenenia, Anammoxoglobus and/or Scalindua.
  • the anaerobic ammonium oxidation is a method comprising converting a part of ammonium to nitrite by nitrite-type nitrification reaction using ammonium oxidizing bacteria, with ammonium as an electron donor and nitrite as an electron acceptor, and simultaneously denitrifying the nitrite and the remaining ammonium using anaerobic ammonium oxidizing bacteria without requiring an addition of extra organic substance (such as methanol).
  • the anaerobic ammonium oxidation requires only a small amount of oxygen in nitrification reaction, does not require an organic substance (such as methanol) in denitrification reaction, and thus can be operated at a considerably reduced running cost, advantageously.
  • Present invention demonstrates that a proper amount of nitrite can be maintained by reducing nitrate to nitrite for instance by heterotrophic denitrifying bacteria or by a catalyst e.g. Pt-Cu/Al 2 O 3 , molybdenum-mediated atom transfer or AgATiO 3 .
  • nitrate is produced into nitrite for instance by such reduction than the ammonium and nitrite under anoxic or anaerobic condition can easily been denitrified into dinitrogen gas.
  • An embodiment of present invention provides in a IRAFS such in a catalytic reactor in a water unit that feeds its water to the microbial bioreactor.
  • Another useful system, which can be combined with the photocatalytic reduction of nitrate to nitrite is an aerobic bioreactor for partial oxidation of ammonium into nitrite (partial nitrification of ammonium under aerobic oxidation conditions or nitrite-type nitrification reaction using aerobic ammonium oxidizing bacteria) preferably with oxygenation and stirring or fluidizing .
  • This aerobic bioreactor is provided with an outflow of NO 2 -N and NH 4 -N (preferably in equal proportions) to a second bioreactor with limited oxygen wherein nitrite acts as the electron acceptor for oxidation of ammonium to dinitrogen gas (NH 4 + + NO 2 " ⁇ 2H 2 O + N 2 ).
  • nitrite acts as the electron acceptor for oxidation of ammonium to dinitrogen gas (NH 4 + + NO 2 " ⁇ 2H 2 O + N 2 ).
  • the microbial can be enrichment in a biofilm system to prolong the sludge age or the bioreactor can drive on granular sludge for instance in a sequencing batch reactors (SBR) or in gas-lift- loop reactors.
  • SBR sequencing batch reactors
  • the partial oxidation of ammonium into nitrite (partial nitrification) and the anaerobic or anoxic oxidation of ammonium and nitrite to dinitrogen (N 2 ) gas can be in a multiple gas lift reactor with a serious of gas lift components.
  • the partial nitrification (nitrite-type nitrification reaction) is carried out by immobilized autotrophic nitrifying bacteria in the aerobic zone part and in the second anaerobic zones part immobilized ammonium oxidizing bacteria. Anaerobic ammonium oxidation converts ammonium and nitrite further into dinitrogen.
  • the first bioreactor is replaced by a photocatalytic reactor to convert ammonium and nitrite into dinitrogen.
  • the bioreactor actuator is single-stage aerobic bioreactor with intermeshing aerobic, anoxic, and anaerobic zones with completely autotrophic nitrogen removal over nitrite, The intermeshing aerobic, anoxic, and anaerobic zones provide habitat for the coexistence of different microbial communities (stoichiometry: NH 4 + 0.85 O 2 -» 0.435 N 2 + 0.13 NO 3 ' + 13 H 2 O + 1.4 H + ).
  • the system comprises a first aeration tank, that delivers water to the first aerobic bioreactor for partial oxidation of ammonium into nitrite which provides NO 2 -N and NH 4 -N in near to in equal proportions to the second bioreactor with limited oxygen, whereby the first and second bioreactor are respectively a aerobic and an anaerobic biogranulation tank.
  • aerobic ammonium oxidation is induced in bioreactor wherein the biofilm forming microbial are under turbulence self granulating into biogranules or biofilm granules.
  • the anaerobic ammonium oxidation system comprises a first tank wherein the level of molecular oxygen and the level of CO 2 is regulated for instance by aeration and optionally the pH is adjusted this first tank is connected by a discharge pipe to a second tank, the biograulation tank wherein self granulation of the bacteria is enhanced by turbulence or shear, for instance by a rotor.
  • a pre-tank tank feeds water with a controllable dissolved oxygen, CO 2 content and pH towards the biogranulation bioreactor.
  • For aerobic granulation oxygen-containing gas is fed to the first reactor which is connected with the bioreactor with the biogranules.
  • the second tank or biogranule bioreactor reactor can from time to time partly be emptied by discharging the top part or can remove floating biogranules in a continued process.
  • These tanks can connected in a recircualting loop so that the first tank receives supernatant from the second biogranulation tank for a series of recirculations.
  • the biogranulation tank can 1) in case of sufficient oxygen supply operate as an aerobic granular biofilter with phosphate removal and anoxic growth (COD + Nox + PO 4 3" ⁇ N 2 + CO 2 + H 2 O + poly-P) in the core of the granular biofilm, with nitrification in a layer on the core (NH 4 + O 2 ⁇ NOx) and heterotrophic growth (COD + O 2 ⁇ CO 2 + H 2 O) on the outer layer or 2) under of conditions imposed molecular oxygen (O 2 ) and CO 2 limitation so that the nitrite is used as a oxidant to ammonia and a lower pH (preferably less than 7.3) there will occur partial nitrification in a layer of the biofilm granules and aerobic oxidation of ammonium is at least in part switched to anaerobic ammonium oxidation.
  • CO 2 molecular oxygen
  • the oxygen limitation in the bacterial condominiums of autotrophic nitrification and denitrification results in a direct NH 4 + to N 2 transformation.
  • the system is provided with a transport line or piping for transporting water of the first water treatment (pH adjustment, CO 2 stripping, and/or oxygenation) tank to the biofilm granulation tank (tank for granulation suspended microorganisms with stirring, shearing or turbulence forces) and the biofilm granulation tank can be for seen with a transport line or piping for transporting supernatant water back to the first water treatment tank or to a third biogranulation tank that operates under anaerobic condition.
  • a discharge line can discharge supernatant water of a biogranulation tank or return water to another tank in the system.
  • Valves are activated by actuators that receive signals from a controller that receives input signals from a network of in situ hard sensors comprising sensors of the group consisting of a pH sensor, a NO 2 sensors, an ammonium sensors, a nitrite sensor and a nitrate sensor.
  • RIAFS ammonium oxidation activity by condominiums of autotrophic micro-organisms
  • the ammonium oxidation (NH 4 + + NO 2 " — > N 2 + 2H 2 O) activity by condominiums of autotrophic micro-organisms is obtained by combining condominiums of autotrophic micro-organisms with photocatalysis for nitrate to nitrite reduction. This ammonium removal is obtained with adequate alkalinity rebuild.
  • bioreactor 102 are converted (reduced) to nitrites by contacting at least part of the nitrates with at least a metal catalyst and radiation from a radiation source to produce such nitrite, where after at least some of the ammonium and nitrite are converted to nitrogen gas under anaerobic conditions by autotrophic micro-organisms. Direct ammonium to nitrogen gas with carbon dioxide production this mixed or hybrid catalytic / microbial process results in an alkalinity rebuild.
  • Such metal catalyst can for instance be a metal selected from the group of zinc, iron, silver, iron tin, nickel, manganese, palladium, platinum, magnesium, and alloys or mixtures thereof and preferably of the group consisting of copper, silver, mercury, palladium, platinum and alloys or mixtures thereof on a TiO 2 surface for instance TiO 2 P25 with a surface area of 49m /g and primary crystal size 30 run (Degussa) or TiO 2 Hombikat UV 100 with a surface area of 250 m 2 g "1 primary crystal size ⁇ 10 run (Sachtleben Chemie) and most preferred metal catalyst is AgATiO 2 .
  • a metallic powder which has been coated with catalyst metal may be mixed with the nitrate solution in a stirred reactor tank.
  • the nitrate solution may be passed through a bed of dispersed metal.
  • the nitrate solution may be contacted with a solid non-dispensed metal structure, such as metal sheets, spheres or cylinders.
  • a photocatalyst reactor which have a liquid transport pipe connected with or which irrigate the aerobic and/or anaerobic bioreactor, such as the aerobic (digester) granule bioreactor or as the anaerobic digester) granule bioreactor, is foreseen by a Ru (bpy)3 2+ photocatalyst or another suitable photocatalyst for visible light or UV decomposition of aqueous NH4 + /NH 3 to N 2 and H 2 .
  • Such photocatalyst reactor can be further foreseen with another transport pipe and eventual hydrogen storage tank to provide hydrogen in a controllable to the aerobic and or anaerobic bioreactor. This is particular suitable to enhance the growth of hydrogen consuming bacteria such the methanogenic bacteria the aerobic and/or anaerobic granule bioreactor.
  • UV radiation ultraviolet radiation
  • UV-C UV-C
  • the Sun on the other hand emits most of its radiation in a wavelength band between 100 nm and 4000 nm.
  • the UV lamps radiate is generally in a housing or a container that is provided with an inlet and an outlet to receive water of the aquatic faming system. In general this housing or container is a flow through unit. In an embodiment of present invention is provided with photo catalysis material in at least one such UV unit that receives water from the farming system is provided with a photocatalyst material.
  • the UV unit can be provided with a photocatalytic material that allows the oxidation of ammonium ion to nitrite or nitrate and the reduction of nitrate and nitrite to N 2 or the nitrate to nitrite reduction, hi a particular embodiment such photocatalytic material is titanium (IV) oxide for instance as powder surfaces (TiO 2 particles) or plates.
  • a photocatalytic material is titanium (IV) oxide for instance as powder surfaces (TiO 2 particles) or plates.
  • Other suitable photo-catalyst material is for instance Fe/TiO 2 , TiO 2 and Fe/TiO 2 can by a sol gel synthesis method be produced as a mesoporous material.
  • Variation in the pore size is possible via different assembling strategies that are available in the art using a variety of organic molecules as nano-size templating materials or self assembling surfactant or amphotheric copolymers to synthesize mesoporous TiO 2 , Fe/TiO 2 , CrATiO 2 , Mg/TiO 2 , Ag/TiO 2 or CoTiO 2 with different pore sizes.
  • These mesoporous materials can be in the form of films or membranes.
  • TiO 2 films and membranes can be prepared through methods employing surfactant molecules as a pore directing agent along with a novel acetic acid-based sol-gel route.
  • the sol is composed of polyethylene glycol sorbitan monolaurate surfactant, acetic acid, titanium tetraisopropoxide, and isopropanol.
  • ammonium ion in the presence of air or pure oxygen is converted to either nitrite or nitrate.
  • TiO 2 doped with altervalent cation Fe 3 + , Cr 3 + , Co 2 + and Mg 2 + is a material that under UV radiation induces reduction of nitrite and nitrate ions.
  • Ag/TiO 2 is particularly suitable for nitrate to nitrite reduction.
  • Such photocatalyst material is in a particular embodiment such AgATiO 2 and is position in the housing in such manner that it receives UV radiation when the lamp is operational.
  • Is Ag /TiO 2 preferably in the form of TiO 2 -Ag porous nanocomposites which can be films (e.g. thin-film) membranes or a suspension of TiO 2 -Ag particles.
  • UV AgATiO 2 When by irradiation with UV AgATiO 2 induces reduction of nitrate to N 2 or nitrate to nitrite and Total-N removal.
  • such photocatalyst reactor is used to affect the ammonium / nitrite proportion is used to force a bioreactor into an ammonium + Nitrite conversion to N 2 .
  • AgATiO 2 An AgATiO 2 catalyst with homogeneously dispersion of coated silver clusters, AgATiO 2 (P25, Degussa, Japan; anatase 79%, rutile 21%) can be prepared by a pH-controlled photocatalytic process (F. Zhang, N. et al. , Langmuir 19 (2003), p. 8230).
  • formic acid is added as a hole scavenger. This photocatalyst when irradiation by sunlight is capable of reducing nitrate at 100 % N selectivity to N 2 without generating considerable amounts of ammonium or NO 2 " .
  • a photocatalyst photochemical reactor comprising such photocatalysts either in suspension or in film or membrane is used for removing nitrate to achieve a proper NH 4 + ZNH 3 versus nitrate proportion to feed into an aerobic ammonium oxidation bioreactor.
  • photocatalystic materials either as film, membrane or particle suspension can be used for nitrite and nitrate ion reduction towards ammonia under UV or sunlight radiation.
  • a Ru (bpy)3 2+ photocatalyst can be used for visible light decomposition of aqueous NH 4 I-ZNH 3 to N 2 and H 2 .
  • [Ru (bpy)3] 2+ ions have been know for their electrochemiluminescence and been used to develop sensors for a variety of analytes that range from metal ions and small molecules to DNA, peptides, and proteins.
  • TiO 2 (ST-Ol, average size 7 nm, from Ishihara Sangyo Co.Ltd.) can be used to produce such platinized TiO 2 by photochemical reducing tetrachloroplatinate in a TiO 2 -water suspension in the presence of 2 wt% methanol.
  • This platinized TiO 2 photocatalyst material can be in a suspension of particles, in a films or membrane. Under radiation for example UV or solar light radiation such platinized TiO 2 photocatalyst will photo decompose aqueous NH 4 + ZNH 3 into nitrogen (N 2 ) and hydrogen (H 2 ).
  • the photocatalyst material of present invention is also used for water splitting with UV light so that hydrogen produced via water splitting using the photocatalysist to boost the biofilter activity by delivering hydrogen to a biofilter reactor unit. Hydrogen into contact with the microbial community stimulates hydrogenotrophic methanogens to convert hydrogen to methane.
  • a photo catalyst photochemical reactor is used to feed hydrogen (H 2 ) obtainable from platinized TiO 2 photocatalyst into such anaerobic denitrification bioreactor or into the bioreactor.
  • Gal— xZnx)(Nl— xOx) actually functions as a suitable photocatalyst for hydrogen production from water.
  • Oxynitrides such as TaON, Ta 3 N 5 , and LaTiO 2 N, can be obtained by heating a corresponding metal oxide powder under a flow of NH 3 .
  • (Gal-xZnx)(Nl-xOx ) loading of cocatalysts (typically metal or metal oxide nanoparticles) for instance with RuO2 modification or nanoparticles of Rh2-yCryO3 (to obtain (Gal- ⁇ Znx)(Nl- ⁇ Ox))
  • cocatalysts typically metal or metal oxide nanoparticles
  • RuO2 modification or nanoparticles of Rh2-yCryO3 to obtain (Gal- ⁇ Znx)(Nl- ⁇ Ox)
  • Metal-free polymeric photocatalyst for visible-light-driven H 2 production from water are available.
  • the graphitic carbon nitrides (g-C3N4) with graphitic planes constructed from tri-s-triazine units connected by planar amino groups have such properties (XinchenWang et al. Nature Materials. VoI 8 2009.
  • the carbon nitrides can for instance be prepared by heating cyanamide (Aldrich, 99% purity) to temperatures between 673 and 873 K (ramp: 2:2 K min i) for 4 h.
  • a IRAFS is provided with at least such UV lamp unit that is provided with an ammonium oxidizing photocatalyst and at least one UV lamp unit with a nitrate and/or nitrite reducing photocatalyst.
  • Sensor that sense for pH, NH 4 , NO 3 " and or NO 2 " will provide a signal to a controller that is connected to provide an activation signal to such UV unit. For instance in case that the nitrification bioreactor fails photocatalytic ammonium oxidation can be switched on.
  • the photocatalytic NO 3 " and NO 2 " reduction can be switched on to a non bacterial system for removing nitrogen from the watery culture medium of the aquatic farming system provide a real time optimization of TN, ammonium, nitrate and nitrite in case of failure of the bioreactor biofiltering system.
  • these photocatalytic systems provide a capacity to interact with and optimize the bioreactor systems.
  • Alternative to the UV lamp solar photochemical processes can be used. They generally use only high-energy short-wavelength photons and sunlight at wavelengths over 600 run is normally not useful for the photocatalysis.
  • TiO 2 photocatalysis uses UV or near-UV sunlight (300 to 400 nm) the high-wavelength photons are used to reach a specific temperature and to store, collect, and distribute solar energy in the farming system by converting this higher wavelength solar radiation to heat and transferring this to water that is then pumped to the aquatic farming system.
  • Water is pumped through tubes that that can for instance contact with a flat-plate or step-plate photo reactor (non concentrating photo-reactor) for instance mounted above the aquatic animal farming or aquaculture system or on the roof of the farming building.
  • the latter is a photocatalyst material that absorbs sunlight and optimally insulated on the front with layers of glass and air; the glass allows visible light to fall on the photocatalyst material but also traps the resulting heat, which is then transferred to the water that returns to the aquatic farming system.
  • the fluid is pumped through an evacuated glass tube or a volume of space wit the photocatalytic material onto which a large volume of sunlight has been focused (and hence concentrated) by reflecting mirrors for instance line focusing parabolic through concentrators ( concentrating photo-reactor). They may be provided with sun tracking systems.
  • water is pumped to a (insulated) storage tank, (where it can be used immediately or stored for later use) or to the aquatic farming system.
  • Photocatalysis mineralizes carboneous organic substances into carbon dioxide and inorganic and nitrogen containing molecules in NO 3 " and NH 4 + (equation organic molecules + O 2 ⁇ CO 2 + H 2 O + minerals (e.g. NH 4 + ZNH 3 ' , NO 2 ' or NO 3 ).
  • photocatalyst material suitable for present invention is a semiconductor solid surfaces that are photoexcitated by UV light, near UV, UV-VIS or solar light depending on the type of photocatalyst. As a result, mobile electrons and positive surface charges are generated resulting in excited electron-hole pairs. These excited sites and electrons accelerate oxidation and reduction reactions.
  • a wide band gap semiconductor like titanium dioxide such as polycrystalline TiO 2 catalyst to be irradiated.
  • Such material is used for the photocatalytic mineralization of organic species so that minerals instead of organic species are delivered to the bioreactor units and/or the soilless crop culture systems.
  • UV lamp system are commonly used before the biofilter units in recirculating aquaculture systems to prevent microbial contamination, an hybrid UV lamp / photocatalyst system for hydrogen production to deliver hydrogen to the biofilter units does not necessary need extra energy input.
  • the UV light, near UV or solar light irradiating source and the photocatalyst can be integrated in a rector unit such as a multiple tube reactor, a tube light reactor, a rotating tube reactor, and a Taylor vortex reactor.
  • aqueous NH 4 + ZNH 3 in the water effluents of the aquatic farming system is transformed into N 2 gas by biological and chemical inert photoactivatable material for photocatalysis such as the semiconductor CdS or the semiconductor oxide, ZnO, MgO, WO 3 , Fe 2 O 3 , TiO 2 and under UV light or solar radiation in a photochemical reactor to induce absorption of a photon with energy equal to, or greater than the band gap of the semiconductor (ca. 3.2 eV for anatase).
  • biological and chemical inert photoactivatable material for photocatalysis such as the semiconductor CdS or the semiconductor oxide, ZnO, MgO, WO 3 , Fe 2 O 3 , TiO 2 and under UV light or solar radiation in a photochemical reactor to induce absorption of a photon with energy equal to, or greater than the band gap of the semiconductor (ca. 3.2 eV for anatase).
  • anastase TiO 2 density of 3.9 g/ml
  • Degussa TiO 2 P 25 closely approximating to 25% rutile, 75% anatase with a specific area of 50 ⁇ 15 m 2 /g.
  • the radiation source can come from a UV lamp or from solar light.
  • the photochemical reactor can be an immersion well (in case a UV lamp is used that has to be surrounded by the solution to be irradiated) or flat or trapped wall or tubular photoreaction and the photocatalyst can a suspension or a thin film.
  • NH 4 TNH 3 into N 2 volatilization photochemical reaction system is activated by on switching of a pump, valves and/or an UV radiation tool whereby the to be treated water is contacted with said the photacatalyser under simultaneous radiation.
  • the switch of/on of the photocatalyst actuator is controlled by a control or that receives input signals from sensors in bioreactors or in the drain water of a bioreactor.
  • a signal that is indicative of an instability or disruption in the bioreactor functions such an unacceptable decrease in alkalinity or abbreviation of the pH from norm-pH, can switch on the photocatalytic NH4 + /NH 3 transformation to compensate the alkalinity loss that is function of aerobic nitrification. For every 1 mg/1 of aerobic oxidized ammonium approximately 7.14 mg/1 of alkalinity is required.
  • This NH 4 1 YNH 3 volatilization photoreactors have preferably their outlet connected with the irrigation or piping towards the bioreactor units.
  • the inhibitory threshold concentration of some organic compounds have been documented: Allyl alcohol 20.0, Aniline 8.0, Chloroform 18.0, Mercaptobenzothiazole 3.0, Phenol 6.0, Skatol 7.0, Thioacetamide 0.5 and Thiourea 0.1 mg/1.
  • Photacatalysis removes or destroys organic compounds even non biodegradable compounds that are biocidal, inhibitory or toxic to nitrifying bacteria are removed in the inlet water in the aerobic nitrification.
  • Another reason for decreases bioreactor collapse and the increased biosecurity in the IRAFS is that an input of photodisinfected water from the photochemical reactor into the bioreactor system can prevent inoculation with unwanted micro organisms.
  • Bioreactors and the IRAFS are less vulnerable to invasion of unwanted organisms. It is particularly suitable to have the water photo disinfected before entering the bioreactors to prevent unwanted contamination of the bioreactor units but also to have the water photo disinfected before entering the before the aquatic animal farming system.
  • Photocatalysis removes or destroys organic compounds even non biodegradable compounds that are carcinogenic, mutagenic, endocrine disrupting and that for instance could accumulate in the adipose tissue of the farmed aquatic animals.
  • photacatalysis kills waterborne pathogens. It is therefore a preferred embodiment of present invention to have such photochemical reactor upstream of the bioreactor units and upstream of the aquatic animal farming systems.
  • the aquatic farming system comprises a photochemical reactor for NH4+/NH 3 volatilization, photodisinfected and organic compounds such as alcohols, carboxylic acids, phenolic derivatives, or chlorinated aromatics, into harmless products e.g. carbon dioxide, water, and simple mineral acids upstream from the bioreactor system comprising a nitrification bioreactor and denitrification bioreactor (or a hybrid nitrification/denitrification bioreactor) or in a loop with the bioreactor system for receiving and providing watery medium. Furthermore this photochemical reactor downstream from a coBOD / pBOD removal unit (for instance a micro sieve drum filter) and upstream of the aquatic farming animal system in a second loop.
  • a coBOD / pBOD removal unit for instance a micro sieve drum filter
  • the first water treatment tank is connected with a tank for reducing nitrate to nitrite whereby the nitrate reduction tank feeds water into first water treatment tank.
  • Reducing nitrate to nitrite can for instance by heterotrophic denitrifying bacteria wherein the nitrate reduction treatment is carried out by the nitrate comprising liquid into contact with a catalyst that reduces the nitrate as a nitrogen component to nitrite catalyst.
  • Suitable catalysts are e.g. Pt- Cu/ Al 2 O 3 , Pd — Cu catalyst or catalysts of molybdenum-mediated atom transfer.
  • Photocatalytic nitrate to nitrite reduction can be activated to deliver water loaded with ammonium nitrite approaching equimolar amounts to for an anaerobic bacterial bioreactor into ammonium and nitrite to dmitrogen conversion.
  • This photocatalytic nitrate to nitrite reduction can be carried out in a pre-treatment unit or tank before the water is delivered to the microbial bioreactor.
  • the first water treatment tank is an aerobic biofilter for partial nitrification by controlled operating conditions such as dissolved oxygen between 0.5 - 1 mg O 2 /l), solids retention time at 1-2 d, temperature at 25-37°C and pH at 7.5-8.0.
  • This bioreactor is controlled to reduce ammonium and reduce nitrite and preferably to approach an ammonium/nitrite proportion of 1.
  • the pre-treatment system is provided with a transport line or piping for transporting water of this first water treatment to the biof ⁇ lm granulation tank (tank for granulation suspended microorganisms with stirring, shearing or turbulence forces).
  • the time of photocatalytic treatment affects if organic nitrogen is released as NH 4 + ZNH 3 , NO 3 " or NO 2 " and so will do the selected photocatalyst. Since plant productivity is intimately linked to nutrient uptake and pH regulation the nutrients derived from the aquatic animal farming system is preferably presented in the irrigation to a soilless crop culture or hydroponics are preferably in a mineral form. Hydroponics greenhouse systems are generally foreseen with stock solution of nutrient/fertilizer which are provided with an extra acid or base solution for pH correction.
  • An extra amount of an acid or base solute can be used to control pH of the batch of nutrient solution in the mixing tank diluter/dispenser units wherein the concentrated fertilizers are diluted to a nutrient solution to be taken up by the plant.
  • hydroponics can comprise a buffer tank, nutrient reservoir pump, growing troughs, collecting trough, condensed water tank, acid stock solution, base stock solution tank, nutrient stock solution tank,
  • after mineralization on the photocatalytic reactor or the photocatalytic / photochemical reactor wherein transformation of organic matter to minerals (mineralization) water of this photochemical is flows the hydroponics system for pH adjustment, nutrient completion and mixing with clean and or drain water for irrigation to the (soilless) crop.
  • the computer systems used in hydroponics that guarantee the accurate delivery of minerals to the plant crops can be used to control the integration of mineral delivery from the photocatalytic reactor or the photocatalytic / photochemical reactor.
  • Water irrigation from the aquatic farming system towards the soilless crop culture unit or the hydroponics system preferably undergoes photocatalytic mineralization in the photocatalytic reactor , photocatalytic / photochemical reactor or photochemical reactor unit.
  • photochemical reactor upstream of the soilless crop culture unit or the hydroponics system or upstream of a water collection tank for mixing water with drain water, stock nutrient; pH adjusting compounds and/or clean water under control of nutrient mixing and nutrient injection software before irrigation of the soilless crop culture unit or the hydroponics system.
  • photochemical reactor is upstream connected via a loop with and the aquatic animal farming system and the soilless crop culture unit or the hydroponics system and the microbial bioreactor system.
  • the photoreaction can present NRj + ZNH 3 , NO 3 " or NO 2 " in a controllable manner, the proportions of the different nitrogen compounds are further adjustable by controlled mixing of the different sources before irrigation to the crops.
  • Nitrogen (N) is only presented as NO 3 " salts in the nutrient solution to the plant roots the plant anion uptake exceeds cation uptake and the plant roots will extrude anion equivalents back into the solution to maintain electroneutrality. Further addition of H + is than necessary to maintain pH and overall nutrient availability. IfNH 4 + would be presented to the plant roots as the main N source than the cation uptake would exceed anion uptake. H+ ions will be extruded by the plant roots decreasing the solution pH and base addition would be necessary to maintain overall nutrient availability and stable pH. The ionic balance in plants is highly dependent on the uptake of N and K.
  • N as two charge options NH 4 + and NO 3 - but the only charge option for K is the K + cation.
  • NH 4 + is a key ion to help to maintain electro neutrality.
  • High levels of NH 4 + can inhibit the uptake of K + , Mg 2 + Ca 2 + (plants have generally a high requirement at Ca 2 + .
  • up to 70% of the anions and cations can be presented as NH 4 + or NO 3 " .
  • such plant root exudation are integrated in the control system as a sentinel to provide signals to the controller or the computer processor which contains a controller.
  • pH sensors are integrated to monitor acidification of the rhizosphere and feed signals into the controller to maintain crop normo-pH.
  • Nitrate or NH 4 uptake by plant roots changes the pH of the medium (Marschner, H. and R ⁇ mheld, V. (1996). Root-induced changes in the availability of micronutrients in the rhizosphere.
  • Plant Roots the Hidden Half, 2nd edn (Y. Waisel, A. Eshel, and U. Kafkafi, eds). New York: Marcel Dekker, pp. 557-579 and Marschner, H, R ⁇ mheld, V., Horst, WJ. and Martin, P. (1986)).
  • Root-induced changes in the rhizosphere Importance for the mineral nutrition of plants. Z. Pfanzenennaehr Bodenk, 149, 441— 459).
  • the plant roots are a source and sink of organic compounds and plant hormones and play a function in carbohydrate storage, to enable the following year's propagation, roots become the main carbon (C) storage organ for the plant.
  • C main carbon
  • Fibre optic sensor reported to monitor different soluble analytes are available such as a polyimide-coated fiber Bragg gratings (FBG) or a glucose-selective surface plasmon resonance sensor (as for instance the surface plasmon resonance sensor based e.g. Nanogold-plasmon- resonance-based glucose sensing based on concanavalin A and sugars glucose selectively in the range of 0.1-50 mmol/1) or the surface plasmon resonance sensor based on bacterial glucose/galactose-binding protein and can be used to monitor plant root exudation. .
  • FBG polyimide-coated fiber Bragg gratings
  • a glucose-selective surface plasmon resonance sensor as for instance the surface plasmon resonance sensor based e.g. Nanogold-plasmon- resonance-based glucose sensing based on concanavalin A and sugars glucose selectively in the range of 0.1-50 mmol/1
  • Components included in the recirculation system are photocatalytic reactor used for photocatalytic water splitting, oxidation, degradation of products or disinfection depending on the type of catalyst and the radiation source.
  • Visible light can be used to activate the photocatalyst to induce mineralization or degradation.
  • Visible light induced photocatalytic degradation, decomposition, mineralization or advanced oxidation (e.g. under aerated conditions) of aqueous organic molecules in particular to convert (oxidize) organic molecules into CO2, water and minerals (mineralization — complete mineralization) can be in various photoreactor types, photocatalyst arrangements, light sources, and operation conditions for photocatalytic degradation, decomposition or mineralization of organic molecules.
  • degradation, decomposition, mineralization or advanced oxidation is carried out under LED (light- emitting diode) lights of the wavelength of 450-475 nm is carried out with TiO2 and/or ZnO functionalized or sensitized by conjugated polymer poly(fluorene-co- thiophene (Qiu, RL; et al. Reaction kinetics and catalysis letter 94 (1): 183-189 2008).
  • LED light- emitting diode
  • ZnO functionalized or sensitized by conjugated polymer poly(fluorene-co- thiophene Qiu, RL; et al. Reaction kinetics and catalysis letter 94 (1): 183-189 2008.
  • This photocatalytic degradation, decomposition, mineralization or advanced oxidation can result in detoxification when toxic organic compounds are removed and no toxic intermediates are produced or left by an incomplete process.
  • the total organic carbon (TOC) measurements allows to evaluate the mineralization efficiency and various toxicity assay (e.
  • Daphnia magna or Artemia salina sentinels are available in the art to monitor the detoxification process and the degradation of reaction by-products and without restriction good candidates have been mentioned in this application.
  • Components included in the recirculation system are photocatalytic reactor used for photocatalytic oxidation (in presence of oxygen). Photocatalytoc oxidation and complete mineralizing converting organic molecules to CO2, water, and mineral acids can be by a suitable photocatalysist such as TiO2 and its variants.
  • metal cations reduction is obtainable whereby photogenerated electron e " c b reduces inorganic metal ions with a reduction potential that is less negative than the reduction potential of the conduction band such as the pairs Ni(II)/Ni(0), Pb(II)/Pb(0), Fe(III)/Fe(0), Cu(II)/Cu(I), Cu(II)/Cu(0), Cu(I)/Cu(0), Fe(III)/Fe(II), Ag(I)/Ag(0), and Hg(II)/Hg(0); organic oxidation and inorganic reduction has a synergic effect on photocatalytic oxidation.
  • Photon absorption by photocatalyst is regarded as the first stage of photo excitation of heterogeneous system; the photo excitation pathways of wide band gap solids may involve photo generation of excitons and/or free charge carriers, depending on photocatalyst features such as fundamental absorption band, extrinsic/intrinsic defect absorption bands, or UV-induced colour centre bands.
  • photon absorption has two main effects: (i) it changes the characteristics of photocatalyst surface and (ii) it generates active photo adsorption centres.
  • a typical case of the first effect is that band gap irradiation induces superhydrophilicity (photoinduced superhydrophilicity, PSH) on the TiO 2 surface, which shows hydrophobic features under dark conditions.
  • PSH photoinduced superhydrophilicity
  • This PSH is accompanied by photocatalytic activity, as both phenomena have a common ground, so that the surface-adsorbed compounds may be either photo oxidized or washed away by water.
  • the second important effect is that irradiation absorption generates active states of the photo adsorption centres with trapped electrons and holes.
  • Ultrasound (US) and/or microwave (MW) irradiation on the photocatalyst can induce degradation, decomposition or mineralization of aqueous organic molecules or in combination with UV7VIS radiation or UV radiation it strongly enhances the process.
  • the photocatalytic degradation, decomposition or mineralization of aqueous organic molecules can be enhanced by light and microwave radiation for instance UV/VIS radiation + microwave photolysis or UV radiation + microwave photolysis. For instance by internal lamps (classical UV lamp) or by powered quartz mercury electrodeless discharge lamps in a microwave field.
  • heterogeneous photocatalytic degradation or organic molecules e.g. onTiO2 photocatalysist
  • ultrasound irradiation e.g.
  • Ultrasonic (US) irradiation on a photocatalytic material such as TiO2 results in sonocatalytic microbial inactivation by the generation of hydroxyl (OH) radicals during US irradiation (Shimizu, N; et al; BIOCHEMICAL ENGINEERING JOURNAL 48 (3):416-423 2010).
  • CeO2/TiO2, SnO2/TiO2, ZrO2/TiO2 and F-Si-comodified TiO2 composites, carbon nanotube/TiO2 and nanosized Au doped -TiO2 nanoparticles photocatalyists are particularly suitable for sonocatalytic degradation of organic molecules under ultrasonic irradiation.
  • Bacterial bioreactors and units with aquatic multicellular consumer organism are eventually used to deliver irrigating water to soilless plants (aquatic plants or terrestic plants with their roots in aquatic medium.
  • This form of integration can eventually aid to redistribution of organic, inorganic material and energy in a more cost effective manner on condition that biosystems could be biostable and no biosystem collapses (which is a major cost factor) would occur at least not a regular basis. Since high density and highly productive land-based recirculation systems can have a great potential of production of aquatic organisms near the urban consumer societies, there is a need in the art.
  • pathogens are considered opportunistic, causing disease only in fish with suppressed immune systems. However, if pathogens become sufficiently numerous they can also cause disease in healthy fish. In addition, the continuous flow of water throughout a system can spread pathogens rapidly, despite the ultraviolet sterilization or ozone. Ultraviolet sterilization or ozonation are basically only surface treatments. Bacteria, parasites, fungi and viruses can all become concentrated in recirculating systems.
  • Bacteria that typically increase in number in recirculating systems include Aeromonas spp., Vibrio spp., Mycobacterium spp., Streptococcus spp., and Flavobacterium columnar e (Columnaris disease) (UF/IFAS Fact Sheets FA- 14 Aeromonas Infections, FA-31 Vibrio Infections of Fish and VM-96 Mycobacteriosis in Fish; UF/IFAS Circular 57 Streptococcal Infections of Fish; and SRAC Publication No. 479b Columnaris Disease, respectively).
  • Aeromonas spp. Vibrio spp.
  • Mycobacterium spp. Mycobacterium spp.
  • Streptococcus spp. and Flavobacterium columnar e (Columnaris disease) (UF/IFAS Fact Sheets FA- 14 Aeromonas Infections, FA-31 Vibrio Infections of Fish and VM-96 Mycobacterios
  • Parasites that tend to thrive and spread relatively easily in recirculating systems include Trichodina, Ichthyophthirius, Costia and monogeneans (UF/IFAS Circulars 716 Introduction to Freshwater Fish Parasites and 920 Ichthyophthirius multifiliis (White Spot) Infections in Fish; and UF/IFAS Fact Sheet FA-28 Mongenean Parasites of Fish, respectively). Closed systems can also foster the spread of fungi and viruses (UF/IFAS Fact Sheets VM-97 Fungal Diseases of Fish and FA-29 Introduction to Viral Diseases of Fish, respectively). A combination of decreased immunity of the aquatic organisms and accumulation of pathogenic microbials can lead to a biosystem collapse.
  • UV-LED ultraviolet light emitting diode
  • a fluorescent lamp light source radiation on a TiO2 photocatalytic films for instance obtained by the low-pressure metal-organic chemical vapour deposition
  • UVA covers from 315 to 400 run, UVB from 280 to 315 nm and UVC from 200 to 280 nm. Radiation at UVB and UVC wavelengths has no toxic properties and is invariably harmful to living cells. By damaging the DNA, it can induce deleterious processes such as mutagenesis, carcinogenesis and cell death.
  • Disinfection of secondary wastewater effluents compared to stream and river water by UV requires higher doses (50 - 60 mW cm " ) due to the higher concentration of micro-organisms and increased micro-organism resistance.
  • Uneconomically viable values exceeding 100 mW cm '2 are required to inactivate protozoan pathogens such as Cryptosporidium and Giardia.
  • Typical waterborne pathogens with high health significance are bacteria such as Campylobacter jejuni, C. coli, Pathogenic E. coli, Salmonella typhi, other salmonellae, Shigella spp.
  • viruses such as Adenoviruses , Enteroviruses, Hepatitis A, Enterically transmitted non-A, non-B hepatitis viruses, Hepatitis E, Norwalk virus and Rotavirus and Protozoa such as Antamoeba histolytica, Giardia intestinalis and Cryptosporidium parvum.
  • Some gram- positive bacteria, under extreme environmental conditions produce specialised structures called endospores. Endospores are formed internal to the bacterial membrane, during the process of sporulation. Sporulation represents a dormant stage within the bacterial lifecycle. Endospores are highly durable dehydrated cells with thick walls and additional layers, which are much more complex than that of vegetative cells.
  • endospores The durability of endospores allows them to survive for many years until conditions become favourable for germination, at which time the endospore converts back to a vegetative cell. Endospores can survive extreme heat, lack of water and exposure to many toxic chemicals and radiation. There is thus a need in better disinfection tools than the conventional chemical, radiation and heating water treatments.
  • Components included in the recirculation system are in an embodiment a photocatalytic reactor used for water splitting.
  • a photocatalytic reactor used for water splitting.
  • photocatalysts developed in last years for water splitting reaction under visible light.
  • the properties required by photocatalysts for water splitting are band edge potentials suitable for water splitting, band-gap energy around 2.0-2.2 eV, and stability under reaction conditions.
  • Water decomposition is obtainable by photoelectrochemical or photocatalytic technologies using near-infrared and visible light or solar electromagnetic radiation.
  • This process mimics photosynthesis by converting water into H 2 and O 2 using inorganic semiconductors that catalyze the overall water- splitting reaction, equated as H 2 O -» 1 A O 2 + H 2
  • DGO standard Gibbs free energy change
  • Photon energy is converted in chemical energy (hydrogen), the surface of the semiconductor, the photoinduced electrons and holes reduce and oxidize adsorbed water to produce gaseous oxygen and hydrogen according the equations of oxidation : H 2 O + 2h + — » 2H + + 1 A O 2 , reduction : 2 H+ + 2e —> H 2 .
  • KTaO 3 KTaO 3
  • SrTiO 3 TiO 2
  • ZnS Zero of the strategies for inducing visible-light response in TiO 2 was the chemical doping of TiO 2 with metal ions with partially filled d-orbitals (V, Cr, Fe, Co, Ni, etc.).
  • TiO 2 codoped with a combination of Sb 5+ and Cr 3+ is active for O 2 evolution under visible-light irradiation ( > 440 nm) from an aqueous solution using AgNO 3 as sacrificial reagent
  • Visual light response has been increased for TiO 2 by doping it with Sb, C, Ta or Cr for TiO 2 and SrTiO 3 and by doping ZnS with Cu or Ni.
  • Semiconductor mixing is another strategy for developing photocatalysts with visible-light response from photocatalysts with a wide band gap. Also specific semicondotor composites are used for VIS light photocatalysis.
  • This strategy is based on the coupling of a wide band-gap semiconductor with a narrow band semiconductor with a more negative CB level. In this way, CB electrons can be injected from the small band-gap semiconductor into the large band semiconductor, thereby extending the absorption capacity of the mixed photocatalyst.
  • Suitable semiconductor composites are CdS-TiO 2 , CdS-K 4 Nb 6 O 17 , Ca 2 Fe 2 O 4 and PbBi 2 Nb 1 9 W O iO 9 .
  • Specific semiconductor alloys extend the visible light response of wide band-gap photocatalysts involves making solid solutions between wide and narrow band-gap semiconductors such as the semiconductor alloys GaN-ZnO, ZnO-GeO, ZnS-CdS, ZnS-AgInS2, and CdS-CdSe.
  • the deposition of noble metals (e.g., Pt, Rh) or metal oxides (e.g., NiO, RuO2) onto photocatalyst surfaces is an effective way of enhancing photocatalyst activity.
  • the co catalyst improves the efficiency of photocatalysts.
  • Nitrogen substitution on Sr2Nb2O7 oxides also enables the absorption of the oxynitride in the visible range as a result of the mixing of N 2p with O 2p states near the VB.
  • Photocatalytic reactor used for photocatalytic denitrification.
  • Photocatalytic denitrif ⁇ cation of water with 96% conversion of nitrate ions can be achieved by using silver modified titanium dioxide obtained by the sol-gel method. Silver particles are photo precipitated.
  • a electron donor e.g. formic acid
  • Photocatalytic reaction can be enhanced.
  • Various methods of attempting to post- synthetically enhance the overall efficiency of the photocatalytic process have been investigated. These modifications include doping with transition metals to increase electrical conductivity, loading with metal nanoclusters, annealing the catalyst at elevated temperatures to improve crystallinity and particle size, using electron acceptors other than O 2 and electrochemically-assisting the mechanism by the application of a positive bias.
  • the most important modification to date is the reduction of the TiO 2 particle size to within the nanometre range which has been shown to significantly increase its catalytic activity. This is due to the higher surface-to-volume ratio, and as such it is routine to use nanometre-sized particles.
  • Reactor performance is enhanced by dispersing the TiO 2 nanoparticles in water, because of higher surface contact of the nanoparticles with the target compounds.
  • the difficulty in separating unsupported particles from water for reuse is limiting commercially viable industrial reactors. Therefore, a need to employ supported catalysts is realised where a thin layer of nanometre-sized TiO2 particles can be formed on a supporting surface.
  • These can be particle or fixed supports,74,85 with the majority of research performed in the former case.
  • TiO2 for example, has been fixed onto tubes, glass plates, fibres, membranes, or photo reactor walls. However, catalytic activity approximately five to six times lower is usually seen (compared with the powdered form).
  • Such TiO2 nanotubes can be well produced from bulk crystalline titanium metal (Gong D, Grimes CA, Varghese OK, Hu WC, Singh RS, Chen Z,Dickey EC (2001) J Mater Res 16:3331; Ghicov A, Tsuchiya H, Macak JM, Schmuki P (2005) Electrochem Commun 7:505, Elsanousi A, Zhang J, Fadlalla HMH, Zhang F, Wang H, Ding XX, Huang ZX, Tang CC (2008) J Mater Sci 43:7219 and Jaroenworaluck A, Regonini D, Bowen CR, Stevens R, Allsopp D (2007) J Mater Sci 42:6729).
  • heterogeneous photocatalysis reactors are good candidates for the aquatic farming system present invention.
  • Heterogeneous photocatalysis reactors need optimal light distribution inside the reactor providing high surface areas for catalyst per unit reactor volume, high surface area per unit volume of reaction liquid inside the reactor , with optimal surface-to-volume ratio while eliminating the prospect of light loss by absorption and scattering in the reaction medium.
  • a multiple tube reactor a distributive-type photocatalytic reactor design with hollow tubes in which catalyst is fixed to a structure in the form of glass slabs (plates), rods, or tubes inside the reactor allows for high values of K and will eliminate light passage through the reaction liquid. This is advantageous because when light approaches the catalyst through the bulk liquid phase, some radiation is lost due to absorption in the liquid. For instance K (m '1 ) of 2000 achieved and the reactor and can be scaled-up with small VR.
  • Tube light reactor (TLR) photocatalytic reactor is based on such on the MTR.
  • the lamps can be in various shapes and lengths and can be placed inside a reactor to form a variety of different configurations allowing for uniform light distribution along the length of the tubes (Periyathamby, U., and Ray, A.K., Chem. Eng. Technol. 22, 881 (1999 and Ajay K. Ray, Antonie A.C.M. Beenackers Catalysis Today 40 (1998) 73 ⁇ 83)).
  • UV-LED ultraviolet light-emitting diode
  • UV-LED can be used as alight source for the photocatalytic decomposition of organic materials aqueous media by the UV-LED/ ⁇ O2 process (Chen, HW; et al. Source JOURNAL OF CHEMICAL TECHNOLOGY AND BIOTECHNOLOGY 82 (7):626-635 2007).
  • Artificial UV lamps can power photocatalytic processes.
  • the band gap of TiO2 anatase is 3.2 eV and the irradiation portion that can participate in the photocatalytic reaction is the one below 388 nm.
  • Artificial UV sources are made of different metals including mercury, sodium, zinc/cadmium and rare gases (neon, argon). The mercury emission lines are usually in the desired range of energy for driving the photochemical reactions.
  • Artificial UV lamps can be grouped in low pressure mercury lamp, medium pressure mercury lamp and high pressure mercury lamp categories. Solar light can also activate TiO 2 given that the TiO 2 activation spectrum overlaps with the solar spectrum. LEDs can be used to drive the photocatalytic process with a low level of energy (e.g. 3 - 5 voltages) and thus at high energy efficiency LED to absorb light energy exceeding band gap (WO2001064318 Al).
  • Photocatalytic oxidation and complete mineralizing converting organic molecules to CO 2 , water, and mineral acids can be by a suitable photocatalysist such as TiO 2 and its variants.
  • CO 2 generated by this process is delivered to the bioreactor with plants or to the aerobe bioreactor with autotrophic microorganisms
  • the CO 2 is photocatalysed to hydrocarbons such as methanol to fuel the chemoheterotrophic microbial bioreactor.
  • the process and farming system can be designed to utilize CO2 reduction.
  • TiO 2 nanotube arrays formed by anodic oxidation of titanium have very high surface areas comparable to porous titania nanoparticle films, and proven photocatalytic properties. While the TiO 2 band gap, 3.0 and 3.2 eV for rutile and anatase, respectively, restricts excitation wavelengths to less than ⁇ 400 run, we have succeeded in incorporating nitrogen into the nanotubes in situ during anodization, with a subsequent heat treatment resulting in crystallized nanotubes with N 2p states formed above the titania
  • doped titania nanotube arrays with platinum and/ or copper nanoparticles dispersed upon the top of the nanotube array surface, have been used to convert carbon dioxide and water vapour into hydrocarbons under natural (outdoor) sunlight according to the equation CO 2 + 2 H 2 O ⁇ CH 4 + 2O 2 (Oomman K. et al; Nano Lett., 2009, 9 (2), 731- 737). Titania has been used for such photocatalytic processes due to its powerful oxidation properties, superior charge transport properties, and corrosion resistance.
  • Its e photocatalytic carbon dioxide conversion rates can be enhanced by (i) employing high surface area titania nanotube arrays, with a wall thickness low enough to facilitate efficient transfer of photogenerated charge carriers to the surface species; (ii) modifying the titania band gap to absorb and utilize the visible portion of the solar spectrum where the bulk of the solar energy lies; (iii) distributing cocatalyst nanoparticles on the nanotube array surface to adsorb the reactants and help the redox process.
  • TiO 2 nanotube arrays formed by anodic oxidation of titanium have very high surface areas, comparable to porous titania nanoparticle films, and proven photocatalytic properties (Mor, G. K.; Carvalho, M.
  • titania valence band shifts the absorption edge of titania to ⁇ 540 nm.
  • nitrogen-doped titania nanotube arrays with platinum and/or copper nanoparticles dispersed upon the top of the nanotube array surface, can been used to convert carbon dioxide and water vapour into hydrocarbons under natural (outdoor) sunlight.
  • the nitrogen-doped titania nanotube arrays are synthesized by anodizing titanium foil in an electrolyte consisting of 0.3 M ammonium fluoride (NH4F) in 2 vol % water containing ethylene glycol at 55 V.
  • N4F ammonium fluoride
  • Nanotube array samples up to ⁇ 130 ⁇ m in length are prepared by changing the anodization duration.
  • the debris from the anodization bath redepositing on top of the original nanotubes can be removed by ultrasonic agitation and/or critical point drying (CPD) according to Paulose, M.; Prakasam, H. E.; Varghese, O. K.; Peng, L.; Popat, K. C; Mor, G. K.; Desai, T. A.; Grimes, C. A. J. Phys. Chem. C 2007, 111, 14992.
  • CPD critical point drying
  • the nitrogen-doped titania flow-through nanotube array are loaded into a membrane or photoelectrode for high rate photocatalytic conversion of CO 2 and water vapour into hydrocarbon fuels under UV, near UV and violet, blue or green light radiation.
  • Luisa F. et al use electrodeposited silver particles over TiO2 thin film for CO 2 reduction in aqueous solution.
  • the TiO2 thin films were supported on transparent conductive glass plates were modified by silver particles (250 nm diameter) deposited by electrochemical double pulse from an aqueous solution of silver nitrate (Luisa F. Cueto, Gerardo T. Martinez, Genaro Zavala, Eduardo M. Sanchez Journal of Nano Research (Volume 9) Pages 89-100 February, 2010).
  • Nanostructured Cobalt Oxide Clusters in Mesoporous Silica allow the direct conversion of carbon dioxide and water to methanol.
  • the metal oxide nanocluster catalysts for water oxidation is driven efficiently by visible-light-absorbing binuclear charge-transfer chromophores (H. Han, H. Frei, J. Phys. Chem.
  • Typical intermediates produced by primary active species are for instance (i) aromatic compounds, (ii) carboxylic acids, (iii) nitrogen-containing straight chain compounds, and (iv) inorganic species (ammonium and nitrate ions).
  • UV light with a wave length lower than 388 nm can be absorbed by TiO2 generating a pair of charges e ⁇ cb / h + vb (photogenerated electron e " Cb / photogenerated hole h + vb) • reduction of the e " Cb / h + vb recombination results in more hydroxyl radicals production and a better oxidation efficiency .
  • Effective retardation of recombination of the e-cb-h+vb pair can be obtained if the the electron- and hole-sinks is physically adsorbed or chemically attached to the surface of the semiconductor
  • Fe-TiO 2 -doped catalysts can for instance be prepared by a 48-h period of mixing of the solution containing the catalyst and Fe ions. After mixing, the catalyst can be dried at 393K for 24 h and then calcined at 773K.
  • Ag-doped TiO 2 xerogels can be synthesized in a single step through the simultaneous hydrolysis and condensation of Ti(IV) isopropoxide with an alkoxysilane-functionalized silver complex Whereby the silver is present in the form of metallic nanoparticles and silicon is distributed in the TiO2 matrix and attached by Si-O-Ti bonds.
  • TiO2 doped with silver and silica can for instance be synthesized from a suspension of silver nitrate powder, AgNO3, in half of the 2-methoxyethanol used as solvent, and adding N-[3-(2-aminoethyl) aminopropyl] trimethoxysilane
  • Well crystallized anatase materials with a significant porosity and doped with Ag is obtained through the synthesis method.
  • This amorphous TiO2-based xerogel with very high surface area with enhanced thermal stability and photoactive under UV/Vis light, biologically and chemically inert, photostable is suitable for semiconductor heterogeneous photocatalysis.
  • One of the strategies for insuring visible light response in TiO3 is chemical doping of TiO3 with metal ions with partial filled d-orbitals such as V, Cr, Fe, Co and Ni for instance by ion-implantation.
  • Visible-light response improvement of TiO2 can be obtained in TiO2-N, T ⁇ O2-S or ⁇ 02-C by doping of TiO2 anions such as N, C or S as substitutes for oxygen in the TiO2 lattice.
  • TiO2 anions such as N, C or S
  • the mixing of the p states of doped anion (S, N or C) with the O 2p states shifts the VB edge upward and narrows the band-gap energy of TiO2.
  • band edge potentials suitable for water splitting band-gap energy around 2.0—2.2 eV.
  • Ion doping has been carried out for enhancing the visible-light response of wide band-gap photocatalysts (UV-active). Examples include Sb- or Ta- and Cr-doped TiO2 and SrTiC ⁇ , ZnS doped with Cu or Ni, or C-doped TiO2.
  • the replacement of cations in the crystal lattice of a wide band- gap semiconductor may create impurity energy levels within the band gap of the photocatalyst that facilitates absorption in the visible range. Insertion of dopants into the photocatalyst structure can be carried by advanced ion-implantation technique which more effective than chemical methods for controlling the insertion.
  • Semiconductor mixing can be used for photocatalysts with visible-light response from photocatalysts with a wide band gap which is based on the coupling of a wide band-gap semiconductor with a narrow band semiconductor with a more negative conduction band (CB) level.
  • Such visible light composite photocatalyst can be of the group consisting of: CdS-TiO2, CdS-K4Nb6O17 and Ca2Fe2O4- PbBi2Nbl.9W0.1O9.
  • Another approach to extend to visible light response of wide band-gap photocatalysts involves making solid solutions between wide and narrow band-gap semiconductors with a similar lattice structure, such alloys can be of the group consisting of GaN-ZnO, ZnO-GeO, ZnS-CdS, ZnS-AgInS2 and CdS-CdSe.
  • Photocatalytic reactors can comprise immobilized catalyst (e.g. TiO 2 , TiO 2 /Pt , ZnO) anchored on a support via physical surface forces or chemical bonds on activated carbon, fiber optic cables, fibreglass, glass, glass beads, glass wool, membranes, quartz sand, zeolites, Silica gel, stainless steel, Teflon for instance on the reactor wall surrounding the light source.
  • immobilized catalyst e.g. TiO 2 , TiO 2 /Pt , ZnO
  • the photocatalyst coated beads or particles can be incorporated into membrane.
  • Such substrates can be integrated in immobilized reactor designs such as the know designs of the group consisting of the falling Film Reactor (FFR), Fiber Optic Cable Reactor (FOCR), Multiple Tube Reactor (MTR), Packed Bed Reactor (PBR), Rotating Disk Reactor with Controlled Periodic Illumination (RDR-CPl), Spiral Glass Tube Reactor (SGTR), Tube Light Reactor (TLR) and Photo CREC Water I.
  • FFR falling Film Reactor
  • FOCR Fiber Optic Cable Reactor
  • MTR Multiple Tube Reactor
  • PBR Packed Bed Reactor
  • RDR-CPl Rotating Disk Reactor with Controlled Periodic Illumination
  • Spiral Glass Tube Reactor SGTR
  • Tube Light Reactor TLR
  • the Falling Film Reactor (FFR) of the art comprises an immobilized TiO 2 coating on the internal wall of a column, a descending film of water and a lamp placed in the central section of the column.
  • This reactor configuration may only provide a limited active catalyst surface per unit reactor volume.
  • the Fiber Optic Cable Reactor (FOCR) is a design with fiber optic cables bringing irradiation to the supported photocatalysis (e.g. TiO 2 ). This system can allow the irradiation of a remotely located photocatalyst with minimum scattering and uniform irradiation.
  • a typical FOCR includes Degussa P25 immobilized on quartz optical fibbers and a Xe arc UV- radiation lamp (310-375 nm).
  • the Multiple Tube Reactor is a design with a cylindrical vessel (5-6 cm of diameter) containing 54 hollow quartz glass tubes (diameter 0.6 cm) externally coated with photocatalyst.
  • the MTR resembles a shell and tube heat exchanger with the water to be treated flowing in the shell side of the MTR.
  • the irradiation is distributed in hollow tubes for instance via an aluminium reflector.
  • the MTR provides a large activated photocatalyst area per unit reactor volume.
  • the Packed Bed Reactor is an annular packed unit irradiated by a central lamp. Several variations of the PBR are reported such as TiO2 coated glass mesh, TiO2 coated glass wool, and TiO2 coated glass beads.
  • the Rotating Disk Reactor with Controlled Periodic Illumination contains immobilized TiO 2 films placed on the surface of a rotating disk.
  • the disk is attached to a power-driven shaft that rotates at a rate of 20-100 rpm.
  • An arrangement of lamps are used to irradiate the disk surface.
  • the rotating hydrodynamics provides good reagent access to the catalyst surface.
  • the Spiral Glass Tube Reactor (SGTR) consists of a TiO 2 - coated spiral tube wrapped around a lamp.
  • the Tube Light Reactor (TLR) comprises a stainless steel flat top plate and an inner welded plate characterize the TLR. Several U-shaped Ti02-coated lamps are placed around the welded plate. The assembly is enclosed in a rectangular stainless steel vessel.
  • the Photo-CREC Water I is an annular reactor with a lamp placed at the reactor centerline. This configuration allows high TiO 2 loading of the glass mesh, good catalyst irradiation and uniform contact of the circulating water.
  • the Photo-CREC- Water I reactor was originally proposed by de Lasa and Valladares (de Lasa, H. L, and Valladares, J., 1997, Photocatalytic reactor, US Patent No. 5,683,589. 1997), and Valladares (1995). Modifications were introduced to the original design by Serrano and de Lasa (Serrano, B., and de Lasa, H., 1997, Photocatalytic degradation of water organic pollutants.
  • an annular channel with multiple (16) baskets positioned at 45° angles characterizes the Photo-CREC-Water I.
  • the Photo-CREC reactor is configured with stainless steel spacers placed between the baskets. These spacers secure the basket in position and ensure minimum loss of light.
  • the near-UV lamp is located in the central channel, providing 15 W of monochromatic light (365 nm). Water is circulated in a downward flow, with the only exception being the start-up of the run when an upward flow evacuates the air pockets. Water exiting the reactor is discharged into an oxygenator. This unit is equipped with a perforated pipe air distributor and a magnetic stirrer securing water saturation with oxygen.
  • a variable- flow Gilson pump completes the experimental system. This pump is used to return the water to the upper section of the photoreactor unit, closing in this way the cycle of water oxygenation and recirculation.
  • the reactor comprises a mesh with photocatalyst, such as TiO 2 (Ti ⁇ 2 -mesh - catalyst loading (16.5 wt %)) or TiO 2 activated cabon composite on the impregnated fiberglass mesh) mounted on the inner face of each of the conical baskets.
  • photocatalyst such as TiO 2 (Ti ⁇ 2 -mesh - catalyst loading (16.5 wt %)) or TiO 2 activated cabon composite on the impregnated fiberglass mesh
  • the TiO2 or TiO2 activated cabon composite on such fiberglass mesh can be loaded with metals such as platinum, palladium and ruthenium or with metal oxides such as Fe2O3, Co3O4, or NiO to increase phoytocatalytic activity.
  • the fiberglass mesh can also comprise multiple semi conductor materials with a varying band gap energy (eV) and this a different excitation wave length.
  • TiO2 (rutile) has eV of 3.0 and a excitation wavelength requirement of 413 run (UV)
  • TiO2 (anatase) has eV of 3.2 and a excitation wavelength requirement of 388 run (near violet UV)
  • ZnO has eV of 3.2 and a excitation wavelength requirement of 388 nm (near violet UV)
  • ZnS has eV of 3.6 and a excitation wavelength requirement of 335 nm (UV)
  • CdS has eV of 2.4 and a excitation wavelength requirement of 516 nm (green light)
  • Fe2O3 has as eV of 2.3 and a excitation wavelength requirement of 539 nm (green light)
  • W03 has as eV of 2.8 and a excitation wavelength requirement of 443 nm (violet light).
  • the radiation source can be UV radiation for instance UV-A from 315 to 400 nm (near ultraviolet range) , UV-B from 280 to 315 or UV-C from 200 to 280 nm.
  • the UV-C spectrum (200 to 280 nanometres) is the most lethal wavelength for microorganisms, because it disrupts the bonds in the between the atoms in the chemicals in microorganisms. This range of wavelengths, with 264 nanometres being the peak germicidal wavelength, is known as the Germicidal Spectrum. Generally only a 4-5% portion of the sunlight that reaches the earth is in the 300- 400 nm near ultraviolet range and activates TiO2.
  • UV-A from 315 to 400 nm can excite TiO2 (anatase), ZnO and ZnS.
  • Wavelength converters or spectral converter can to improve the spectral mismatch. Any chelates with suitable absorption and donor properties and able to form kinetically stable 1 : 1 chelates with lanthanide metal ions would could act for wavelength conversion.
  • a class of such chelates and methods for making them are disclosed in European Patent Application No. 0,195,413.
  • Eu chelate is a light-emitting material that can be incorporated in a wave length conversion film due to the high PL quantum efficiency by the ultraviolet excitation. Though the typical transition of trivalent Eu ion generates red emission.
  • Eu chelate such as Eu(TT A)3phen [TTA: thenoyltrifluoronacetone, phen: 1,10-phenanthroline], improves the absorption coefficient per each Eu ion, and reduces the concentration quenching due to the inter-molecular interaction.
  • near-UV is converted to red wavelength by a transparent (in the visible region) thick film containing 38.8 wt% of YVO4:Bi3+,Eu3+ nanoparticles of 10.8 ⁇ 1.6 nm in size (nanoparticle film shows a high transparency( transmittance at 619 nm is ⁇ 96% irrespective of the film thickness) (Satoru Takeshita et al. Material research Society, 2010 Spring Meeting, Volumes 1245 - 1274).
  • Barium ferrite (Alfa Aesar) particles are coated with silica using a St ⁇ ber technique [Watson, S., Scott, J., Beydoun, D., & Amal, R. (2005). Studies on the preparation of magnetic photocatalysts, Journal of Nanoparticle Research, 7, 691-705.].
  • 4000 mg of BaFel2O19 are dispersed in 500 ml of 0.51:0.79:15:0.037 mol ratio of H20:NH4OH:EtOH: TEOS.
  • the particles were stirred for 24 h with a PTFE overhead mixer at 475 rpm.
  • the resulting particles were dried at 65 °C for 24 h resulting in a total mass of - 4.40 g.
  • the silica-coated barium ferrite particles and 18.9 g titanium dioxide (Degussa P25) were then dispersed in an acid catalyzed silica sol-gel [Byrne, H.E., Kostedt, W.L, IV, Stokke, J.M., & Mazyck, D.W. (2009). Characterization of HF-catalyzed silica gels doped with Degussa P25 Titanium Dioxide, Journal of Non- Crystalline Solids, 355, 525-530.].
  • HSAMP8 indicates that a volume ratio of 8:1 and a volume of 2.25 ml HF.
  • the gelation time varied by hydrofluoric acid concentration between 7 and 24 h. This time was determined as the time necessary to reach a viscosity such that visible particle movement was negligible and the vortex near the overhead mixer paddles was no longer apparent.
  • the gel was then poured into plastic specimen containers, sealed and aged at 25°C for 48 h then 60°C for another 48 h.
  • the aged gel was dried in a PTFE container with a small hole on the top. The drying followed a 3°C ramp to 103°C, held for 18 h, then followed another 3°C ramp to 180°C and was held for 6h.
  • the xerogel was heat treated with a 5°C ramp to 450°C, held for 1 h and cooled naturally.
  • the resulting xerogel was ground with a mortar and pestle and wet sieved to retain the 45-90 ⁇ m fraction.
  • the powder is dried at 180°C and stored under vacuum until use.
  • the solar spectrum at 1.5 atmosphere mass according to the ASTM standard comprises 922 W. M " where under about 40% near IR or 375 W. M "2 , 55% visible light or 504 W. M “2 and 5% UV or 43 W. M "2 .
  • Heterogeneous photocatalysis for remediation comprising a photon emitter in a proper wavelength to emit photons with energy edual or g-higher than the ban gap energy of said catalyst in catalyst surface , a catalyst surface (e.g. a semi-conductor material) and a strong oxidation agent (e.g. oxygen).
  • a catalyst surface e.g. a semi-conductor material
  • a strong oxidation agent e.g. oxygen
  • Light with photon energies greater than the band gap can be absorbed by the crystal, exciting electrons from the filled valence band to the empty conduction band (illus. a).
  • the state in which an electron is removed from the filled valence band is known as a hole. It is analogous to a bubble in a liquid. The hole can be thought of as being mobile and having positive charge.
  • the excited electrons and holes rapidly lose energy (in about 10 ⁇ 12 s) by the excitation of lattice phonons (vibrational quanta).
  • the excited electrons fall to near the bottom of the conduction band, and the holes rise to near the top of the valence band, and then on a much longer time scale (of 10 9 to 10 " s) the electron drops across the energy gap into the empty state represented by the hole. This is known as electron- hole recombination.
  • An energy approximately equal to the band gap is released in the process. Electron-hole recombination is radiative if the released energy is light and nonradiative if it is heat.
  • An embodiment of present invention comprises a controlled aquatic farming or water treatment system with a photocatalytic reactor that comprises different for instance an array of different photocatalytic surfaces.
  • a photocatalytic reactor comprises multiple photocatalysts and metal contacts for reacting multiple fluid analytes in water, analyte mixtures in water and intermediates in water produced by the other photocatalytic surface.
  • such photocatalytic reactor is a particulate suspension system (fig 27) which photocatalytic reactor comprises a mixture of particles that function microphotoelectodes whereof a portion of the first microphotoelectodes if radiated (e.g.
  • photoreactor comprises different units , first init(s) with a OH* radicals generation and adsorbed pollutants (RXad) and eventual metal reduction function (down hill photocatalysis function) and second unit(s) with a water splitting function (up hill photocatalysis).
  • present invention provides a security ammonium removal system to reduce the ammonium-ion toxicity and to maintain the pH at systems normo-pH by switching on ammonium removal.
  • the pH monitoring system is organised to maintain a dual pH regime of an aquaculture normo-pH and a crop normo-pH in the plant culture unit for instance in the hydroponics or soilless plant culture.
  • a sensor network with hard sensors monitor the different bioreactor (plant culture, aquatic animal culture, microbial nitrification / denitrif ⁇ cation) and balance their pH and alkalinity effects towards normo-PH (system normo-pH or aquaculture normo-pH in combination with crop normo-pH).
  • Ammonium removal can be by various from the aqueous or watery farming medium can be by various types of actuators. For instance by ion-exchange using packed bed zeolite (e.g. Clinoptilolite) reactor can be activated as a response of a reduced hydrogen activity under the systems normo-pH or the systems normo-hydrogen ion activity.
  • a continuous ammonium removal system based on an ion-exchange medium has for instance been fully disclosed in US7264732 B2. Or the one step anaerobic ammonium oxidation process can be boosted or switched on .
  • This system is under control pH measurements if there is a risk of a downwards pH shift for systems normo-pH for instance in the units that host the aquatic animals or in the water that irrigates the soilleness crop culture units.
  • NH 4 + and NO 2 " under low pH and under an NO atmosphere (to prevent decomposition of nitrite) have been demonstrated to produce N 2 from ammonium and nitrite been confirmed (Van Cleemput, O., and L. Baert. 1984.
  • Nitrite a key compound in N loss processes under acid conditions. Plant Soil 76:233-241 and Smith, D. H., and F. E. Clark. 1960. Volatile losses of nitrogen from acid or neutral soils or solutions containing nitrite and ammonium ions. Soil Sci.90: 86-92). Van de Graaf et al Applied and environmental Microbiology, Apr. 1995, p. 1246—1251 confirmed in a denitrifying fiuidized bed reactor that this direct conversion of ammonium to dinitrogen gas without oxygen and with nitrite as the electron acceptor (NH 4 + + NO 2 " -» 2H 2 O + N 2 T or ) is a bacterial process.
  • the actuator is single-stage aerobic bioreactor with intermeshing aerobic, anoxic, and anaerobic zones with completely autotrophic nitrogen removal over nitrite, which can occur in a system .
  • the intermeshing aerobic, anoxic, and anaerobic zones provide habitat for the coexistence of different microbial communities ( stoichiometry: NH 4 + 0.85 O 2 ⁇ 0.435 N 2 + 0.13 NO 3 " + 13 H 2 O + 1.4 H + ).
  • ammonium removal reactor is a bioreactor based on oxygen limited autotrophic nitrification - denitrification for direct NH 4 + to N 2 transformation. Important nitrogen losses (40 - 70%) have been observed earlier in rotating biological contactor (Baumgarten and Seyfried 1996) under low dissolved oxygen conditions, which were not due to heterotrophic denitrification but due to direct biological conversion of ammonia to nitrogen in (micro)aerobic conditions (aerobic deammonification), probably because their are both aerobic conditions in the outer biofilm and anoxic conditions at the core of the biofilm.
  • Another ammonium removal reactor is an air stripper with surfaces to improve contact between water / gas for instance a packed bed air stripper to remove ammonia (NH 3 ) from water.
  • ammonium stripping can efficiently been achieved by stripping ammonia from the farming water by a two steps process steam at atmospheric pressure and condensing said steam comprising stripped ammonia and second step comprising rectifying said condensed steam comprising ammonia to at least 20% by weight of aqueous ammonia, said second step advantageously being carried out at a pressure above atmospheric pressure.
  • a one step process for stripping ammonia from liquids has been described in US7416644 B2.
  • the stripper system is connected to an evaporator. In the evaporator aqueous liquid is heated at a pressure below atmospheric pressure whereby vapour is developed at a temperature below 100° C.
  • vapour from the evaporator is directed to the liquid medium containing ammonia and this results in ammonia being stripped from the liquid and transferred to the vapour phase.
  • the vapour phase is condensed in a first condenser at a low pressure, and the liquid thus obtained is further treated in a stripper unit at a higher pressure.
  • Granulation is a process in which microorganisms aggregate to form a spherical, dense biomass. Granules have been grown successfully in either anaerobic or aerobic. Environments. The formation of aerobic granules seems to be independent of the characteristics of the organic substrate (Jiang, H. L., Toy, J. H., and Toy, S. T. L. 2002. Aggregation of immobilized activated sludge cells into aerobically grown microbial granules for the aerobic biodegradation of phenol.
  • Biogranules can be simply sterilized by heat.
  • the biogranules products of the anaerobic and/or aerobic biogranulator are preferably properly packed, eventually dehydrated, cooled and sterilized by gamma rays from radioactive nuclides or X-rays emitted by high-energy electron beams which are suitable sources of ionizing energy and are commonly used for food irradiation and which can penetrate substantial thicknesses of solid materials.
  • Gamma rays food irradiation is carried out in gamma-Ray Facilities for instance in a MDS Nordion PalletTM gamma-ray irradiator loaded with Co-60 for large pallet loads of low-density packages MDS Nordion CenturionTM gamma-ray facilities for treating thinner packages of high-density products or the Gray* Star GenesisTM gamma-ray facility, which irradiates products under water are suitable for sterilizing such biogranular biomass.
  • X-Ray food irradiation is for instance done in X-Ray facilities such as the PalletronTM system ( MDS Nordion & IBA).
  • Alternatively food irradiation by energetic electrons in sterilizing electron beam accelerators such as the microwave linear accelerators (linacs) such as the CirceTM Sband Systems (Linac Technologies S. A. France), the L-band systems (Iotron Industries Canada Inc.) or the IMPELATM linac is used for the sterilization of the packed biogranules products.
  • linacs microwave linear accelerators
  • L-band systems Iotron Industries Canada Inc.
  • IMPELATM linac IMPELATM linac
  • the present invention in a particular concerns in a particular embodiment the use of biogranlution units that are integrated in a recirculating aquatic animal culture system for the production of a feed ingredient.
  • the biogranules are collected by a collections means, they are sterilized by a sterilization means, dehydrated and used as a feed additive.
  • This feed reduces loss caused by diseases in recirculating aquatic animal farming systems, in particular the recirculating fish culture. It furthermore concerns the use of sterilized microorganism granules, microgranules comprising microorganism (biogranules) from a granular sludge bioreactor of a recirculating aquatic animal farming system that comprises said granular sludge bioreactor in the manufacture of a medicinal feed to protect said aquatic multicellular consumer organisms (e.g. aquatic animals) against pathogens that host their environment.
  • these biogranules comprise aerobic microorganisms.
  • these biogranules comprise anaerobic microorganisms.
  • the aerobic or anaerobic granule bioreactors can be inoculated or further be inoculated by specific facultative anaerobes (aerobic (O 2 ) or anaerobic) such as Bacillus Pseudomonas, which is particularly suitable for cBOD removal, denitrification and floe formation.
  • specific facultative anaerobes as anaerobic (O 2 ) or anaerobic
  • Bacillus Pseudomonas which is particularly suitable for cBOD removal, denitrification and floe formation.
  • IRAFS intensive recirculating aquatic farming system
  • suitable soilless crops for culture in the IRAFS of present invention are photoauto-heterotrophic which can be raised in the photoauto-heterotrophic bioreactor.
  • suitable is Rhodospirillum rubrum (e.g. the ATCC25903 or ATCCl 1170) of which the cultures do not produce toxins and which delivers an edible biomass that is a suitable complementary food source for animal and human.
  • the R. rubrum biomass produced in the photoauto-heterotrophic bioreactor(s) of the IRAFS of present invention can be reintroduced in the IRAFS as feed additive for the aquatic animals that are cultured in the IRAFS.
  • a particular photoheterotrophic bioreactor integrated in the system of present invention is a plant culture unit for instance a soilless horticulture in a protected or confined space such as greenhouse, preferably in a greenhouse that receives water of the aquatic organism's culture system (e.g. the aquatic animals).
  • a very suitable plant culture unit to be integrated in the system is based on the nutrient film technique (NFT). This provides a thin film of nutrient solution through channels that comprise the root zone (alternatively other techniques may be used such as static aerated technique, intermediate irrigation and root misting).
  • the NFT can further comprise a buffer tank, nutrient reservoir pump, growing troughs, collecting trough, condensed water tank, acid stock solution, base stock solution tank, nutrient stock solution tank, sterilization loop bypass pump, U. V. system, liquid filter and ozonation system as a germicidal treatment
  • the photoheterotrophic bioreactor system will be controlled by a liquid control system that controls the nutrient reservoir pump, the nutrient solution pH, the nutrient electric conductivity, nutrient solution and condensate water levels. Water from the other bioreactor (e.g. the aquatic animal farming unit) is delivered to this photoheterotrophic bioreactor via the liquid control system.
  • the air composition such as O 2 , CO 2 , N 2 and Volatile Organic Compounds such as ethylene is monitored and controlled.
  • Such photo reactive bioreactors need solar or man made lightening.
  • Lightening systems or radiation providing sources that are suitable for present invention can be incandescent lamps, fluorescent lamps, high intensity discharge lamps (metal halide, high pressure sodium lamps ) light emitting diodes and microwave lamps (MW).
  • HPS lamps e.g. PL2000 600 W HPS are useful for plant growth because of their PAR efficiency, long rated life and light intensity drop is slow as the lamp ages.
  • MH lamps for instance PL2000 400 W MH with Hortilux Maxima Reflector emit in the spectrum almost continuously over the 400 and 700 nm waveband which resembles the spectrum of daylight. But they have a shorter rated life than HPS lamps.
  • a combination of MH and HPS is preferably.
  • the radiation is controllable by a lightening control system e.g. Schneider PLC
  • the nitrifying bioreactor is dedicated to degrading ammonium from other compartments into nitrate which can be made available to the photobioreactors as a nitrogen source. With increasing pH ammonium ions are converted to ammonia. Ammonia and nitrite ions are at relatively low concentrations toxic for aquatic vertebrate and invertebrate animals and for the photosynthetic cyanobacteria and plants. Such nitrifying bioreactor an be operational run a ammonium oxidation in two consecutive stages: ammonium to nitrate oxidation NH 4 + + 1.5 O 2 — »NO 2 " + 2H + H 2 O (e.g.
  • nitrite to nitrate NO 2 " + 0.5 O 2 -> NO 3 " e.g. by Nitrobacter winogradskyi e.g. strain Nb-255
  • autotrophic ammonia/nitrite oxidizers are the chemolithotrophs (autotrophs) that absorb cBOD.
  • ammonia oxidizing microbials can be of the genera of the group consisting of Nitrosomonas, Nitrosococcus, Nitrosospira, Nitrosolobus and Nitrosovibrio or nitrite oxidizer of the group of genera consisting of Nitrobacter, Nitrococcus, Nitrospira and Nitrospina.
  • the inorganic carbon source for these organisms in particular for the autotrophic nBOD-oxidising, such as the NH 4 + oxidisers ⁇ Nitrosomonas, Nitrococcus, Nitrocysis, Nitrosolubus, Nitrospira) and the NO 2 " oxidisers ⁇ Nitrobacter, Nitrococcus and Nitrospira) is inorganic carbon CO 2 for the syntheses of their cellular material which can be solved as carbonic acid (H 2 CO 3 ): CO 2 + H 2 O — > H 2 CO 3 , which can disassociate in bicarbonate (HCO 3 " ) and H + : H2CO3 ⁇ -» H + + HCO 3 " .
  • Suitable organisms for inoculation or growing in this aerobic bioreactor are selected bacteria from the group consisting of Arthrobacter, Bacillus, Nitrobacter, Nitrosomonas, Proteus, Pseudomonas and Vibrio. It can be also Actinomycetes organisms selected from the group consisting of Mycobacterium, Nocardi and Streptomyces or it can be Protozoa of the group consisting of Epistylis and Vorticella or it can be fungal organisms such as fungi of the group of the Aspergillus.
  • CO 2 carbon substrate
  • ammonium ions and nitrite as energy substrate
  • the nitrifying bacteria decrease the alkalinity and the pH in their environment, the aerated bioreactors.
  • the Present invention provides solution for biofiltration without destroying the alkalinity or without drastically affecting the alkalinity.
  • the chemolithoautotrophic ammonia oxidizers (CAO) and chemolithoautotrophic nitrite oxidizers (CNO) can be used to inhabit the nitrifying bioreactor for NH 4 + and NO 2 " oxidation to nitrate at condition that is controlled to be permanently at a slightly acid conditions.
  • the system is preferably operated at 15° - 30°C and pH 6.4 — 8.
  • the nitrifying bacteria are generally chemoautotrophic bacteria that grow by consuming inorganic nitrogen compounds.
  • nitrifying bacteria have complex internal membrane systems that are the location for key enzymes in nitrification: ammonia monooxygenase which oxidizes ammonia to hydroxylamine, and nitrite oxidoreductase, which oxidizes nitrite to nitrate.
  • ammonia monooxygenase which oxidizes ammonia to hydroxylamine
  • nitrite oxidoreductase which oxidizes nitrite to nitrate.
  • the operation can, however, be improved if beside the nitrifying chemoautotrophs such bioreactor can be hosting organotrophs (cBOD oxidizing bacteria or heterotrophs) which are able to remove soluble cBOD, particulate BOD (pBOD) and colloidal BOD (coBOD).
  • the autotrophic nitrifying bacteria generally reduce the nBOD in the activated sludge process.
  • organotrophs which oxidize organic wastes through aerobic respiration or anaerobic respiration.
  • organotrophs can be of the group of the strict aerobes consisting of Actinobacter, Arthrobacter, Micrococcus, Nocardia and Thiothrix or they van be facultative anaerobes of the group consisting of the Achromobacter, Actinyces, Aerobacter, Bacillus, Beggiatoa, Cormynebacterium, Enter obacter, Escherichia, Flavaobacterium, Klebsiella, Proteus, Pseudomonas, Spaerotillus and Zoogloe, which use free molecular oxygen or another molecule comprising oxygen to oxidize organic waste but with preference free molecular oxygen since they obtain in this way larger quantities of energy and produce more offspring.
  • This aerobic reactor may contain floe formation initiators of the group consisting of Achromobacter, Aerobacter, Bacillus, Escherichia, Flavobacterium and Pseudumonas whereby he formed floes will contain organotrophs and autotrophic nitrifiers for improved cBOD and nBOD removal.
  • floe formation initiators of the group consisting of Achromobacter, Aerobacter, Bacillus, Escherichia, Flavobacterium and Pseudumonas whereby he formed floes will contain organotrophs and autotrophic nitrifiers for improved cBOD and nBOD removal.
  • a preferred nitrifying bioreactor is the aerated activated sludge bioreactor (e.g. an aerated fluidized microbead reactor) or another preferred reactor is a USBF reactor with an anoxic and an aerated aerobic zone for nitrification conversion oxidation reduced ammonium ion NH 4 + into NO 2 " and into NO 3 " waste substrate conversion to simple substrates CO 2 , H 2 O, NH 4 + , NO 2 ' , NO 3 " , SO 4 2" , PO 4 2" and bacterial cells.
  • aerated activated sludge bioreactor e.g. an aerated fluidized microbead reactor
  • another preferred reactor is a USBF reactor with an anoxic and an aerated aerobic zone for nitrification conversion oxidation reduced ammonium ion NH 4 + into NO 2 " and into NO 3 " waste substrate conversion to simple substrates CO 2 , H 2 O, NH 4 + , NO 2 '
  • a liquefier bioreactor can be integrated in the IRAFS to improve its operations.
  • the aerobic nitrifying bioreactor receives water that is loaded with material from a liquefier bioreactor or that has been pre- treated in this liquefier bioreactor. This can improve the efficiency of the nitrifying bioreactor because macromolecules and polymers have been degraded.
  • Such liquefier bioreactor for hydrolysis macromolecular hydrolysis by hydrolytic fermentative bacteria), acidogenesis (production fermentation products), actenogenesis (degradation of volatile fatty acids and alcohols by actenogenic bacteria) and methanolgenesis (conversion of the fermented products into methane by methanogenic and acetoclastic bacteria).
  • Such water from the liquefier bioreactor can further be mineralized in the photocatalytic reactor (assisted with or without a ultrasound or microwave function) before it is presented to the aerobic bioreactor or to the photo(auto/hetero)trophic bioreactor and in particular for the photoautotrophic bioreactor comprising organism (e.g. green plants and photosynthetic bacteria are photoautotrophs).
  • Such bioreactor can be operational after inoculation with selected strains from faeces and with Fibrobacter to enhance the degradation of fibres.
  • Such liquefier bioreactor is anaerobic or at least a reactor that comprises an anoxic zone, hi a particular embodiment the liquefier bioreactor produces energy rich gas that is transported by a gas transport line to the firing system that drives a heat pump system for redistributing the heat in the IRAFS for instance from the final drain upstream to a bioreactor unit.
  • Particularly interesting for integration in the farming system of present invention is a reactor hosting a heterogeneous community of heterotrophic organisms, denitrifier organisms, nitrifier organisms, for instance the biofloc and/or biogranule bioreactor that is integrated in the IRAFS.
  • the IRAFS can integrate a biofloc based bioreactor.
  • Such biofloc based bioreactor is a reactor hosting a heterogeneous community of heterotrophic organisms, denitrifier organisms, nitrifier organisms and poly-P (polyphosphate) /PHB (poly-hydroxy- butyrate) /glycogen accumulating organisms in a biofloc motive.
  • heterogeneous communities can host floe forming bacteria (e.g. Zoogloea such as Zoogloea ramiger ⁇ ), filamantous bacteria and algae and can be enhanced by abiotic factors such as light, shear rate and temperature and C/N ratios of approximately 5 - 15, preferably 5 - 12 and most preferably approximating 10.
  • Glycogen accumulating organisms are organisms that use energy from glycolysis to accumulate substrate (e.g. glucose ) fermentations products (e.g. acetate) in the form of poly-(beta) hydroxy- butyrate (PHB).
  • substrate e.g. glucose
  • acetate poly-(beta) hydroxy- butyrate
  • a wide range of microorganisms e.g. Alcaligenes eutrophus and Pseudomonas oleovarians accumulate poly-P-beta-hydroxybutyrate (PHB).
  • PEO Polyphosphate accumulating organisms
  • PEO polyphosphate accumulating organisms
  • Such Floe comprise generally 70-80% organic matter including heterotrophic bacteria, algae (dinoflagellates & diatoms), fungi, ciliates, flagellates, rotifers, nematodes, metazoans and detritus. Their composition changes rapidly and frequently through the cycle. Floe particles are agglutinated by bacterial enzyme-rich polysaccharide slime. Average floe diameter is 0.2mm up to 2mm by end of cycle. Floes have 25% to 56% protein, 25% to 29% organic carbon and have high levels of amino acids.
  • the bio-flocs derivable from this system have a suitable nutritional value to supplement the feed of the aquatic organisms and to be reprocessed into animal feed for the aquatic organisms of another unit of the culture system.
  • An alternative embodiment of the invention takes advantage of the fact that extracellular polymers produced by microbial can be used to produce biofilm condominiums of microbial in the form of biogranules (Biogranulation): Another approach of treatment of organic loaded water is by inducing the phenomenon of microbial self-aggregation into biogranules in a biogranule bioreactor that is integrated in the IRAFS. Such biogranule reactors are preferably used in the biofilters of the framing system of present invention.
  • biogranule bioreactor can be used to generate granules of selected bacteria that are used to inoculate the biof ⁇ lters by designer biogranules of selected microorganisms and to deliver such living biogranules as probiotics to prevent an invasion of unwanted pathogens in to the farming systems and into the aquatic multicellular consumer organisms (e.g. aquatic animals).
  • sterilized and mineralized nutrients derived from the waste of the other units of the IRAFS are fed into such biogranule bioreactor to produce the probiotic biogranules by forcing under shear biofilm forming into biogranules.
  • Biogranulation is a controllable process.
  • biofilms are formed on suspended carrier particles. These biofilm-on-carrier pellets are subject not only to the turbulence and liquid shear that affect fixed-support biofilms but also to particle collisions.
  • the formation of natural, mixed-population, suspended biofilm pellets was investigated by. Heijnen, J. J., et al. (Heijnen, J. J., et al 1992. Formation of biofilms in a biofilm air-lift suspension reactor. Wat. ScL Tech. 26: 647-654).
  • Gjaltema, A. et al (1997) further studied the influence of carrier type on adhesion and biofilm formation of pure and mixed cultures ⁇ Gjaltema, A., et al. 1997.
  • Wirtz R. and Dague R. developed a wash out strategies for the poor settling granules in anaerobic sequencing batch reactors. ⁇ Wirtz R., Dague R. (1996) Enhancement of granulation and start-up in the anaerobic sequencing batch reactor. Wat. Env. Res. 68, 883-892.). Van Loosdrecht M., et al. used granular sludge in biofilm airlift suspension reactors (van Loosdrecht M., et al. (1995) Biofilm structures. War. Sci. Tech., 32(8), 35-43.). Wirtz R and Dague R.
  • the anaerobic (digester) granules are multilayer and have a microbiological composition which is different in each layer (Guiot, S.R., Pauss, A., & Costerton, J. W. (1992). Water Sci. Technol., 25, 1-10).
  • the inner layer mainly consists of methanogens that may act as nucleation centres necessary for the initiation of granule development.
  • H 2 -producing and H 2 -utilizing bacteria are dominant species in the middle layer, and a mixed species including rods, cocci, and filamentous bacteria takes predominant position in the outermost layer.
  • the spatial hydrogen consuming methanogenic bacteria rapidly scavenge the hydrogen and keep the level of hydrogen partial pressure extremely low.
  • anaerobic granulation technology has the following disadvantages: 1) requires long start-up period (2 to 4 months) 2) relatively high operation temperature (30 to 35 °C for mesophilic UASB reactors), 3) unsuitable for low-strength organic wastewater 4) not suitable for nutrient (nitrogen and phosphorous) removal. And in order to overcome these drawbacks, Mishima, K and Nakamura developed microbial granules in aerobic up flow sludge blanket reactor (AUSB) and demonstrated that the granules had excellent settleability. The sludge produced in the aerobic AUSB process formed granules (diameter: 2-8 mm), mixed- liquor suspended solids in the AUSB reactor was maintained at 8200 mg/L.
  • Aerobic granular sludge in a sequencing batch reactor Water Res. 31 12, pp. 3191-3194).
  • a suitable method is wherein for the treatment of (waste) water comprising an organic nutrient, wherein the water is brought into contact with microorganisms comprising sludge particles, an oxygen comprising gas is fed to the sludge particles, and furthermore the method comprises the settling of the sludge particles and the discharge of organic nutrient-depleting (waste) water.
  • the method concerns treatment of (waste) water comprising an organic nutrient and wherein the waste water is brought into contact with microorganisms-comprising sludge particles and whereby an oxygen-comprising gas is fed to the sludge particles that the settling of the sludge and the discharge of organic nutrient-depleted waste water can be improved by feeding in a first step sludge granules to this water under anaerobic conditions and after the supply of the water to be treated an oxygen- comprising gas is introduced in a second step and in a third step, a settling step, the sludge granules are allowed to settle and part of the sludge particles that do not settle are removed.
  • Granular sludge demonstrates high settling velocities leading to good solid-liquid separation, high biomass retention, high activity, and an ability to withstand high loading rates.
  • Granular methanogenic sludge can remain well conserved under unfed conditions for several years (Kosaric N. and Blasczyzk R. (1990) Microbial aggregates in anaerobic WWT. Advances in Biochem. Eng. and Biotech. 42, 28-55). Although buoyant densities of granules are equal to densities of discrete bacterial cells, granules show much better settling properties because of their larger size (Guiot S., Pauss A. and Costerton J. (1992) A structured model of the anaerobic granule consortium. Wat. Sci. Tech. 25(7), 1-10.). This has been confirmed.
  • Aerobic granular sludge (AGS) technology improved sludge settling and behaviour in activated sludge systems.
  • the main advantage is that aerobic granular sludge (AGS) can settle very fast in a reactor or clarifier because AGS is compact and has strong structure. It also has good settle ability and a high capacity for biomass retention (A. Nor Anuar et al. , Settling behaviour of aerobic granular sludge Water Science & Technology VoI 56 No 7 pp 55-63 2007). It was generally thought that the up flow velocity in a UASB creates a selective pressure to which the organisms have two responses: to be washed out or to bind together and form easily settle ability granules (Guiot S., Pauss A.
  • Extracellular polymers bridge the bacterial cells together and hold granules together (Ross W. (1984) The phenomenon of sludge pelletization in the anaerobic treatment of a maize processing plant. Water SA, 10(4), 197-204.; Shen C, Kosaric N and Blaszczyk R. (1993) The effect of selected heavy metals on anaerobic granules & their extracellular polymeric substance (EPS). War. Res., 27(1), 25-33.). The composition of the substrate is an important factor for granule formation (Dolfing J., et al (1987) Production of granular methanogenic sludge on laboratory scale.
  • Van der Hock J. (1987) Granulation of denitrifying sludge In: Proc. of the Gasmat Workshop: Granular Anaerobic Sludge; Microbiology and Technology, Lettinga G, Zehnder A., Grotenhuis J, and Hulshojf Pol L. (Eds) Pudoc, Wageningen, The Netherlands, 203-210).
  • Granular sludge demonstrates high settling velocities facilitating efficient solid-liquid separation. With high biomass retention and biological activity a granular sludge reactor can be operated at high volumetric loading rates.
  • phase 1 and 2 Filling and mixing/aerating: Continuous mixing and aeration are achieved through injection of oxygen-rich gas. Turbulent flow conditions are created giving the granule forming bacteria a selective advantage.
  • Phase 3 Settling: The allowed settling times corresponds to settling velocities of 10 to 15 m/h, causing poor-settling biomass to be washed out and the granules to be retained in the reactor.
  • Phase 4 Decanting: In the third phase the reactor is emptied through outlets at the middle of the tank.
  • the selected volume exchange ratio determines the amount of effluent that is drawn off.
  • the added value of biogranulation lies in the use of aerobic granules that settle more rapidly than the other sludge in water treatment.
  • the suspended microorganisms can be granulated into biogranules in container with a shear creating agitator, whereby the reacted water is provided into the granulation tank from a separate aeration tank preferably in the form of upward streams to induce a an upward streams and an agitation power.
  • aeration carried out directly in the granulation tank there is no requirement of an additional solid-liquid separation apparatus for the poorly settling bacterial floes.
  • biogranule biofiltering system as a whole can be made more compact and required less space and as a result the costs are reduced and the energy consumption can be lower.
  • the biogranules derivable form this system have a suitable nutritional value to supplement the diet of the aquatic organisms and to be reprocessed into animal feed in the farming system of present invention for instance for the aquatic organisms of another unit of the culture system.
  • microorganisms release phosphorus out of their cells.
  • NO 3 ' and NO 2 " are reduced into N2 gas by denitrification microorganisms.
  • an aerated biofilter unit organic matters are removed and the phosphorous released from the anaerobic reactor is removed by phosphorous- removing microorganisms that take in the phosphorous overly, and nitrogen is oxidized by nitrogen oxidizing microorganisms.
  • Granulating suspended microorganisms to thereby form granulated activated sludge can simultaneously remove nitrogen and phosphorous because such biogranulated suspended microorganisms in the aerobic condition full of dissolved oxygen, growing aerobic microorganisms on the surface of the activated sludge as well as growing anaerobic microorganisms within the granular activated sludge.
  • the nitrogen and phosphorous can be removed by cultivating microorganisms in one biological reaction tank because these biogranules the aerobic microorganisms inhabit on the surface of the granulated activated sludge where the chances for contacting the dissolved oxygen are relatively high, while anaerobic microorganisms inhabit in the inside of the granulated activated sludge where oxygen exists scarcely or anaerobic condition is maintained.
  • Present invention demonstrates that organic waste bioremediation in biogranule bioreactors that receive aerated water can remove ammonium, nitrite and nitrate from the IRAFS without destroying its alkalinity.
  • Nitrate to N 2 conversion allow less dirty by clean water replacement in the IRAFS which saves on energy and results on less polluting NO 3 " output in the environment. Moreover demonstrable the alkalinity can be maintained by shifting towards a direct ammonium + nitrate to N 2 conversion.
  • the drain water can only partially be re-used for non halo tolerant embryophytes.
  • High salinity water (EC ⁇ 2 mS cm "1 ), for instance from the drain of the IRAFS, can lead to growth depression in the photocatalytic bioreactor if such photocatalytic bioreactor assisted by non halo tolerant embryophytes (e.g. an hydroponics crop or flower culture unit).
  • non halo tolerant embryophytes e.g. an hydroponics crop or flower culture unit.
  • the classic practices of irrigating essential nutrient and essential minerals to such a photocatalytic bioreactor or photoauto-heterotrophic bioreactor and in particular for the photoautotrophic bioreactor comprising organism e.g.
  • green plants and photosynthetic bacteria are photoautotrophs
  • a diluter/dispenser actuator under control of pH and EC sensing combines the irrigated clean water (e.g. from a rain water storage tank or basin) or irrigated clean water already premixed with drain water from this photocatalytic bioreactor with chemical solutes from at least one stock solution tank or basin and eventually acid from a acid storage tank or basin or base form a base storage tank or basin.
  • a mixing tank which is connected with a transport line or irrigation means with the photocatalytic bioreactor assisted to irrigate the non halo tolerant embryophytes (e.g. an hydroponics crop or flower culture unit).
  • the photocatalytic bioreactor assisted by non halo tolerant embryophytes is in a particular embodiment of present invention irrigated with water from a water input container (clean water basin), from an aquatic animal farming unit (aquaculture system), from a water collection tank or basin or from the water collection tank or basin of the gasification unit of from the chemical stock solution tank or basin.
  • present invention prevents that high salinity water (EC ⁇ 2mS cm " or higher) is provided to such photocatalytic bioreactor.
  • the organic and inorganic molecules from the other bioreactor such as the biofilters or the aquatic animal farming are liquefied or from their collection tanks is further mineralized by a photocatalytic reactor before it is delivered to the mixing tank to irrigate the non halo tolerant embryophytes or non halo tolerant crops.
  • Sensors control the pH and conductivity and feed their measurement signals into a processor with a controller to control the actuators (pumps or valves) of the units that deliver water to the mixing tank to provide water with desired salinity nutrients and pH to the photocatalytic organism.
  • Water from aquaculture (aquatic animal farming unit) drain storage container (permeate or clarified), water from the gasification biofilter drain container and eventually drain water of the drain storage tank of the IRAFS system is mixed in the mixing tank which provides the water to irrigate to the photocatalytic reactor.
  • this sensor network of electrical conductivity sensor and pH sensor is connected with a computer comprising a controller or with an electronic controller to process the sensor signals into a signal that activates actuator for mixing the fluid and eventually adding clean water from the clean water storage tank or container.
  • the control can adjusted on disturbance parameters and can be adapted to the needs of the photosynthetic producer organisms.
  • the actuators such as system pumps, measuring pumps and flow sensors are under control of the controller to provide a fluid with proper pH, EC in the irrigation pipe or supply line to the photosynthetic producer organisms.
  • sensors for individual ions of selected of the group consisting of K + , Ca 2 + , NO 3 " , SO 4 2" , NH 4 + , Na + and CF, pH and EC are connected with a computer comprising a controller or with an electronic controller to process the sensor signals in to a new signal that activates specific actuators for providing individual basic or acid fertiliser solutions for instance of the group consisting of Ca(NO3) 2 , NH 4 NO 3 , KH 2 NO 3 , MgSO 4 and KNO3 and of micronutrients .
  • the irrigation delivery system to photocatalytic bioreactor and or the photocatalytic bioreactor is provided with in situ oxygen, temperature sensing with transducers to convert this abiotic sensing into electrical signals towards a computer or electronic controller to control the oxygenation and heat pump or heating devices.
  • a computer or electronic controller to control the oxygenation and heat pump or heating devices.
  • the photocatalytic bioreactor an embryophyte assisted it photocatalytic bioreactor is provided with moisture sensor for instance a tensiometer to measure the moisture tension or a dielectric capacitance of the time domain reflectometry type or the frequency domain reflectometry type and optionally a evapotranspiration sensor such sensors being provided with transducers to transfer this in electrical signals that can be sensed by a computer or electronic controller.
  • High salinity water (EC ⁇ 2 mS cm-1) is important for growth autotrophic halophiles.
  • High salinity water (EC ⁇ 2 mS cm-1) is the end product of an IRAFS that basically operates on freshwater organisms, hi the soilless or hydroponics green water house farming such high salinity water poses serious limitation and recirculation, results in high water consumption and release of salts and nutrients in the environment.
  • a tank or basin that receives drain water from a photocatalytic bioreactor assisted by non halo tolerant embryophytes is irrigated to a second the photocatalytic bioreactor that is assisted by halo tolerant photocatalytic micro organisms or by halo tolerant halophiles for further for effective biological treatment of saline wastewater, to remove salt and BOD of the drain water of the first photocatalytic bioreactor and to produce hydrogen to enhance the growth and activity of a methanogens of the gasification tank and/or the anaerobic biofilter units or the aerobic zone in a biofilter unit of the IRAFS.
  • This second photocatalytic bioreactor is an aerobic photocatalytic bioreactor assisted by halo tolerant organisms.
  • this second photocatalytic bioreactor is an activated sludge type bioreactor in an aerated tank or basin.
  • This reactor can operate in fed-batch operation.
  • the activated sludge type bioreactor can be provided with an immersed porous device to withdraw the permeate, for instance immersed hollow fibre membranes.
  • the first photocatalytic bioreactor is assisted by the salt-tolerant organism ⁇ Halobacter halobium) or Halobacter halobium incorporated in the activated sludge.
  • the second photocatalytic bioreactor assisted by halo tolerant photocatalytic microorganisms in particular the Halobacteriaceae which are aerobic heterotrophs such as Halobacterium halobium, is provided with an immersed anode and electrode it is a bio-photoelectrochemical reactor for providing current to electricity driven actuators of the IRAFS.
  • Halobacterium halobium pumps protons across the membrane upon illumination. Hydrogen gas production can be enhanced electrochemically by leading a current through two electrodes.
  • such bio-photoelectrochemical reactor can be provided by an hydrogen collection device and a transport pipe to transport the hydrogen to the methanogens of the gasification tank and/or the anaerobic biofilter units or the aerobic zone in a biofilter unit.
  • the photocatalytic bioreactor assisted by halo tolerant photocatalytic microorganisms comprises a H 2 acceptor and distribution system to provide hydrogen to the anaerobic bioreactors to activate the organisms that drive chemoautotrophically on hydrogen + carbon dioxide, for example, methanogens growing autotrophically with hydrogen as electron donor to enhance the methanogenic reactions of reduction of CO 2 with hydrogen and the lithoautotroph (e.g.
  • the aerobic photocatalyticbioreactor is a bio-photochemical reactor assisted by photosynthetic halotolerant bacteria, in particular the Halobacter halobium, whereby the halotolerant bacteria are in an anode chamber with an input to receive cBOD form drain water preferably of the first photocatalytic bioreactor in contact with a cathode chamber that can receive light to activate light-dependent translocation of protons in a created electrochemical gradient and is isolated by a selective hydrogen ion permeable separator, for instance a cation exchange membrane which receives electron acceptor molecules for instance O 2 and whereby the aerobic photocatalyticbioreactor further comprises a least one electric circuit between the two electrodes to accept and distribute the electrons from the anode chamber to the cathode chamber.
  • Such biomass produced in the photocatalytic bioreactor can be fed into the anaerobic liquefier bioreactor to produce the energy rich gas stream for driving actuators of the system such as gas fearing of the heat pump or generating current into a circuit to the electricity driven actuators
  • Typical pathogens in recirculating systems are microbials of the group consisting off Aeromonas spp., Vibrio spp., Mycobacterium spp., Streptococcus spp., Flavobacterium columnare, Aeromonas spp, Streptococcal spp, Ichthyophthirius multiflliis.
  • Aeromonas spp Vibrio spp.
  • Mycobacterium spp. Mycobacterium spp.
  • Streptococcus spp. Flavobacterium columnare
  • Aeromonas spp Streptococcal spp
  • Ichthyophthirius multiflliis A continuous flow of water throughout a system can spread pathogens rapidly. There is growing consumer awareness against the use of antibacterial chemical additives to control such.
  • UV sterilization with ultraviolet (UV) sterilizers typically consist of UV-producing lamps encased in a glass or quartz sleeve in a flow through unit to let the water passing over the lamps.
  • the lamps emit ultraviolet light (a wavelength of approximately 254 nm is considered optimal) that penetrates cells and damages genetic material (DNA and RNA).
  • This systems are energy consuming, do not remove the stressor that for instance cause suppressed immune systems in and are at the basis of disease outbreak (Most pathogens are considered opportunistic, causing disease only in fish with suppressed immune systems) and dot not remove pathogen reservoirs for instance floe communities comprising such pathogens can be formed in the recirculation systems out of control of the sterilisation zones.
  • microbial biofilms impact myriad environments spot in the recirculation systems, from the irrigation systems or water pipes to the units holding the farming multicellular consumer organisms (e.g. aquatic animals) or photoauto-heterotrophic organisms and in particular the photoautotrophic organism (e.g. green plants and photosynthetic bacteria are photoautotrophs).
  • Pathogenic microorganisms may be incorporated into biofilms found in aquaculture systems, causing recurring exposure to potential disease agents and such biofilms can become pathogen reservoirs that host a variety of microbials such as bacteria, parasites, fungi and viruses.
  • Biofilms afford bacteria with protection from a wide array of environmental insults, as diverse as antibiotics, predators, and irradiation by UV.
  • UV sterilizers unit can pass the ultraviolet (UV) sterilizers unit, in particular when the water is turbid or when biofilm parts that detached or biof ⁇ lm fiocs pass the UV sterilizers.
  • UV ultraviolet
  • Typical UV radiation sources cannot provide enough photon energy to produce ionization in most materials.
  • the type of material substrate (Buna-N rubber, polyvinyl chloride (PVC), chlorinated PVC, glass, fiberglass, and stainless steel) for the biofilm had no significant (P > 0.05) effect on the effectiveness of the sanitizers (Robin K.
  • Ultra violet light filter or ozonation or ultra violet light ozonation particularly destroy bacteria and other microorganisms if the water is not too loaded by organic materials such as pBOD and coBOD.
  • organic materials such as pBOD and coBOD.
  • this treatments does not prevent regular virus outbreaks in recirculating aquaculture systems with mass mortalities and closing of the entire facility as only solution.
  • antiviral coatings comprising metal, metal oxide and ceramic nanoparticles (nanometre catalysts) and nanoparticles of a compound of general formula MnXy, where M is (i) a metal selected from the group consisting of Calcium (Ca), Aluminium (Al), Zinc (Zn), Nickel (Ni), Tungsten (W) or Copper (Cu); or (ii) a non-metal selected from the group consisting of Silicon (Si), Boron (B) or Carbon (C); in which n is equal to 1, 2 or 3, and X is (iii) a non-metal selected from the group consisting of Oxygen (O), Nitrogen (N), or Carbon (C); or (iv) an anion selected from the group consisting of orthophosphate (PO 4 3" ), hydrogen phosphate (HPO " ), dihydrogen phosphate (H 2 PO 4 ), carbonate (CO 3 ), silicate (SiO 4 " ), sulphate (SO 4 2' ),
  • Nanoparticles for use on the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units according to the present invention may have an average particle size of up to about 100 nm, up to about 200 nm, up to about 300 nm, or up to about 500 nm.
  • the average particle sizes may be in ranges of from about 1 nm to about 90 run, suitably from about 5 nm to about 75 nm or from about 20 nm to about 50 nm.
  • Particularly preferred average particle size ranges are of from about 20 nm to about 50 nm.
  • Preferred specific surface area of said particles may be in the range of from 150 m /g to about 1450 m2/g, preferably, from 200 m2/g to about 700 m2/g, suitable values may comprise 150m 2 /g, 640m 2 /g, 700m 2 /g.
  • the voids in the particles may be of the order of from 0.1 to about 0.8 ml/g, suitably of from 0.2 to about 0.7 ml/g, preferably about 0.6 ml/g.
  • nanoparticles metal or metal oxide such as silver, titanium dioxide, zinc oxide and carbon (nanometre catalysts) and oxides and/or hydroxides of calcium and/or magnesium with virucidal properties can be prepared which have been prepared according to Fang et al (Virologica Sinica, 20, 70-74 (2005)).
  • Such catalysts are supported nanometre-sized catalytic crystal particle compositions of metals wherein the exposed faces of the nanometre-sized catalyst particles comprise predominantly crystal planes.
  • Bentonite which is a colloidal clay material and dolomite which is calcined and partly hydrated is a suitable antiviral component that can be overflown or contacted with water of the IRAFS to prevent biosystem collapse in particular in the aquatic farming units.
  • Nanoparticles of bentonite have also been prepared and have been reported to have a virucidal activity.
  • the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units may be of a material that incorporates antiviral or virucidal nanoparticles or is coated by a coating that incorporates antiviral or virucidal nanoparticles in the form of dry powders, in the form of liquids, in the form of sol-gels or in the form of polymers, as well in the form of nanotubes.
  • the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units may be of a material that incorporates antiviral or virucidal nanoparticles or is coated by a coating that incorporates antiviral or virucidal nanoparticles that are or agglomerated or in free association.
  • the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units may be of a material that incorporates antiviral or virucidal nanoparticles or is coated by a coating that incorporates antiviral or virucidal nanoparticles which comprise single element M for the case where y is equal to 0 in the general formula MnXy and X is therefore not present, or the nanoparticles may comprise a compound as defined above where y has the value 1, 2 or 3 and x varies accordingly with respect to the value of y in conformity with the respective valencies of the elements M and X present in the formula.
  • the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units may be of a material that incorporates antiviral or virucidal nanoparticles or is coated by a coating that incorporates antiviral or virucidal nanoparticles of a single element where y is equal to 0 may be doped with one or more elements selected from the group consisting of Silicon (Si), Boron (B), Phosphorous (P), Arsenic (As), Sulphur (S) or Gallium (Ga); alloyed with one or more elements selected from the group consisting of Aluminium (Al), Manganese (Mn), Magnesium (Mg), Nickel (Ni), Tin (Sn), copper (Cu), Titanium (Ti), Tungsten (W), Silver (Ag) or Iron (Fe).
  • Si Silicon
  • B Phosphorous
  • Arsenic Arsenic
  • S Sulphur
  • Ga Gallium
  • mixed nanoparticles may be composed of different elements as follows: C-P-Ag-Zn, C-P-Cu-S, C-P-Cu-Ni-S, C-Si-Ag-Zn, C- Si-Cu-S, C-Si-Cu-Ni, C-Cu-Zn-W, C-Cu-Zn-Ag, C-Cu-Zn-W-Ag, C-W-Ti-B, C-W- Ti-N, C-Ti-N, Si-N, Ti-N, Al-N, B-N, Al-B.
  • the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units may also be of a material that incorporates or is coated a coating that incorporates such antiviral nanoparticels which further comprise at least one of the following oxides : TiO 2 , Cu 2 O, CuO, ZnO, NiO, A12O 3 , FeO, Fe 2 O 3 , Fe 3 O 4 , CoO, Co 3 O 4 , or Si 2 O 3 , or a combination thereof.
  • Suitable materials of the inner wall of water or drain water storage tanks and on the water distribution lines or pipes between the different bioreactor units for preventing a viral outbreak in the recirculating systems are materials that incorporate or are coated with a coating that incorporates compounds of the general formula MnXy may be oxides, carbonates, silicates, carbides, nitrides and/or phosphates, for instance , aluminium oxide (Al 2 O 3 ), silicon dioxide, (SiO 2 ), zinc oxide (ZnO), aluminium phosphate (i.e.
  • aluminium phosphate AlPO
  • aluminium hydrogen phosphate Al 2 (HPO 4 )S
  • aluminium dihydrogen phosphate A1(H 2 PO 4 ) 3
  • calcium oxide CaO
  • calcium carbonate CaCO 3
  • calcium silicate CaSiO 4
  • calcium phosphate i.e.
  • TiO2 titanium dioxide
  • ZnO zinc oxide
  • TiO2 titanium dioxide
  • Sol-gel processing is a wet chemical synthesis approach that can be used to generate nanoparticles by gelation, precipitation, and hydrothermal treatment. Size distribution of semiconductor, metal, and metal oxide nanoparticles can be manipulated by either dopant introduction or heat treatment. Better size and stability control of quantum-confined semiconductor nanoparticles can be achieved through the use of inverted micelles, polymer matrix architecture based on block copolymers or polymer blends, porous glasses, and ex-situ particle-capping techniques.
  • Other nanoparticle synthesis techniques include sonochemical processing, cavitation processing (e.g. using a piston gap homogeniser), microemulsion processing, and high- energy ball milling.
  • an acoustic cavitation process can generate a transient localized hot zone with extremely high temperature gradient and pressure. Such sudden changes in temperature and pressure assist the destruction of the sonochemical precursor (e.g. organometallic solution) and the formation of nanoparticles.
  • the sonochemical precursor e.g. organometallic solution
  • nanoparticles are generated through creation and release of gas bubbles inside the sol-gel solution. By rapidly pressurizing in a supercritical drying chamber and exposing to cavitational disturbance and high temperature heating, the sol- gel solution is mixed. The erupted hydrodynamic bubbles are responsible for nucleation, growth, and quenching of the nanoparticles. Particle size can be controlled by adjusting the pressure and the solution retention time in the cavitation chamber.
  • Microemulsions can be used for synthesis of metallic, semiconductor, silica, barium sulphate, magnetic, and superconductor nanoparticles.
  • a co surfactant e.g., an alcohol of intermediate chain length
  • these micro emulsions are produced spontaneously without the need for significant mechanical agitation.
  • the technique is useful for large-scale production of nanoparticles using relatively simple and inexpensive hardware. High energy ball milling has been used for the generation of magnetic, catalytic, and structural nanoparticles.
  • gas- phase synthesis is one of the best techniques with respect to size monodispersity, typically achieved by using a combination of rigorous control of nucleation-condensation growth and avoidance of coagulation by diffusion and turbulence as well as by the effective collection of nanoparticles and their handling afterwards.
  • the stability of the collected nanoparticle powders against agglomeration, sintering, and compositional changes can be ensured by collecting the nanoparticles in liquid suspension.
  • Surfactant molecules have been used to stabilize the liquid suspension of metallic nanoparticles.
  • inert silica encapsulation of nanoparticles by gas-phase reaction and by oxidation in colloidal solution has been shown to be effective for metallic nanoparticles.
  • Approaches have been developed for the generation of monodisperse nanoparticles that do not require the use of a size classification procedure.
  • Monodispersed gold colloidal nanoparticles with diameters of about 1 nm can be prepared by reduction of metallic salt with UV irradiation in the presence of dendrimers.
  • Poly(amidoamine) dendrimers with surface amino groups of higher generations have spherical 3-D structures, which may have an effective protective action for the formation of gold nanoparticles.
  • One production method that is suitable for the production of these materials is the Tesima® process (described in WO 01/78471 and WO 01/58625) where a high temperature DC plasma is used to generate plasma within an inert gas envelope.
  • the nanoparticles can also be prepared by a process which comprises the generation of plasma within an inert gas envelope and the insertion into the plasma of a substance and/or liquid comprising an element or elements or compounds of said element or elements, or a mixture thereof, followed by the gas cooling of the resultant vapour upon exit from the plasma.
  • Materials either pre-produced feedstock or mixed feedstock, or liquids, can be placed into the plasma causing them to vaporise very rapidly.
  • the resultant vapour then exits the plasma where it is then cooled by quantities of cold gas.
  • gases can be either inert (such as argon or helium) or can be air, or can have trace components to develop the chemistry/morphology/size that is required.
  • the rapid cooling (greater than 100,000 degree a second) then freezes the particle for subsequent cooling and collection using a combination of techniques that can include solid or fabric filters, cyclones and liquid systems.
  • the materials can also be collected directly into containers under either inert gas or into various liquids.
  • the nanoparticles have to be suitably be formulated in an appropriate carrier to manufacture articles or coatings to be placed between the different bioreactor units of the farming system of present invention, preferably in the distribution lines.
  • the coating process may be by any generally suitable means, such as for example, spray coating, electro-spray coating, dipping, plasma coating.
  • the articles between the different bioreactor units may be fluid filters.
  • the filter may be prepared from any suitable natural or artificial material as described above in relation to the second aspect of the invention.
  • the filters may be prepared from any suitable fibre or fabric, such as natural or artificial fibres. Natural fibres include cotton, wool, cellulose (including paper materials), silk, hair, jute, hemp, sisal, flex, wood, bamboo.
  • Artificial fibres include polyester, rayon, nylon, Kevlar®, lyocell (Tencell®), polyethylene, polypropylene, polyimide, polymethyl methacrylate, Poly (Carboxylato Phenoxy) Phosphazene PCPP, fibre glass (glass), ceramic, metal, carbon.
  • Fig. 1. is a general schematic view showing an embodiment of present invention concerning the fluid communication between separate systems and units of the controlled farming system of present invention.
  • Left upper in fig 1 concerns the aquaculture consumer animals culture unit and left under in fig 1 concerns the chemoorganothropic bioreactor or anaerobic liquefier bioreactor, a bacterial assisted unit of chemo organotrophic bacteria (heterotrophs) that derive carbon and energy of oxidation of organic compounds and decrease cBOD (by concerting it in carbon dioxide, water, ammonium ions, phosphate ions and sulphate ions) and increase the alkalinity/pH.
  • the unit can be assisted by bio-electrochemical bacterial heterotrophs that generate bioelectricity.
  • the autotrophic (nitrifying) bioreactor a condominium of autotrophic bacteria that oxidize nBOD (that oxidize ammonium and nitrite ions ).
  • the photoautotrophic bioreactor to produce useful biomass for consumption or for feeding it into the energy producing chemo organic bioreactor.
  • the in fig. 1 two upper reactors can receive oxygen from an electrochemical or photocatalytic water splitting actuator.
  • Fig. 2 is a display of the chemo organotrophic bacteria (heterotrophs) bioelectricity (bioelectricity generating) reactor unit or microbial fuel cell (MFC) in a setup to generate current to drive the heat pumps system or specific actuators in the controlled farming system.
  • This can be incorporated in the chemoorganotrophic bioreactor or the anaerobic liquef ⁇ er bioreactor. Oxygen in the anode chamber will inhibit electricity generation, so the system must be designed to keep the bacteria separated from oxygen (the catholyte in this example).
  • This separation of the bacteria from oxygen can be achieved by placing a membrane that allows charge transfer between the electrodes, forming two separate chambers: the anode chamber, where the bacteria grow; and the cathode chamber, where the electrons react with the. catholyte.
  • the cathode is sparged with air to provide dissolved oxygen for the reaction.
  • the two electrodes are connected by a wire containing a load (i.e. , the device being powered), but also a resistor can be used as the load.
  • the membrane is permeable to protons that are produced at the anode, so that they can migrate to the cathode where they can combine with electrons transferred via the wire and oxygen, forming water.
  • the current produced by an MFC can be by monitoring the voltage drop across the resistor using either (a) a voltmeter (intermittent sampling) or (b) a multimeter or potentiostat hooked up to a computer for essentially continuous data acquisition.
  • a voltmeter intermittent sampling
  • a multimeter or potentiostat hooked up to a computer for essentially continuous data acquisition.
  • N 2 molecular nitrogen
  • Shewanella putrefaciens, Geobacter sulfurreducens, Geobacter metallireducens and Rhodoferax ferrireducens have electrochemically active redox enzymes on their outer membranes that transfer the electrons to the external materials and therefore, do not require exogenous chemicals to accomplish electron transfer to the electrodes.
  • Fig. 3 displays nitrification bacterial fuel cell for addition of oxygen to nitrogen while generating bioelectricity. This can be incorporated in the aerobic autotrophic nitrifying bioreactor of Fig. 1 (see fig 4).
  • reduced substrates such as reduced nitrogen
  • ammonium and nitrite ions are oxidized resulting in a decrease of nBOD with the generation of oxidized nitrogen species and in the generation of electrons and protons.
  • the nitrification is indicated by the production of nitrite and nitrate ions or can be suspected by physical indicators such as an increase in the liquor oxygen demand or an decrease in the dissolved oxygen by the dissolved oxygen consumption of the nitrifying bacteria during the oxidation of the ammonium ions and nitrite ions and a decrease of the liquor alkalinity/pH by the production of the nitrite ions.
  • the drop occurs through the use of the alkalinity as a carbon source by nitrifying bacteria and the destruction of the alkalinity by the production of hydrogen ions and the nitrite ions during the nitrification.
  • nitrification needs however the measure of the concentrations of the specific ammonium, nitrite and nitrate ions.
  • the oxidation of the reduced nitrogen results in a decrease of the negative charge and an increase of the positive charge due to the loss of the electrons.
  • Oxygen is provided to the cathode through a gas diffusion layer (for instance porous carbon) .
  • the two electrodes are connected by a wire containing a load (i.e., the device being powered) or a resistor.
  • the both chambers are separated by a separation means (e.g.
  • the gas diffusion layer sticked to the cathode can for instance be Teflon treated carbon paper or Teflon treated woven cloth
  • Fig. 4 is a general schematic view showing an embodiment of a fluid communication between separate systems and units of the controlled farming system of present invention whereby the both autotrophic bacteria nitrifying (right upper) and chemo organotrophic bacteria (heterotrophs) denitrifying bacterial condominiums (left under) are designed to producing current to drive the heat pump system or specific actuators in the controlled agriculture system.
  • fig 1 Left under in fig 1 concerns a bacterial assisted unit of chemo organotrophic bacteria (heterotrophs), the chemo organotrophic bioreactor, that derive carbon and energy of oxidation of organic compounds and decrease cBOD (by converting it in carbon dioxide, water, ammonium ions, phosphate ions and sulphate ions) and increase the alkalinity/pH.
  • the unit is assisted by bio-electrochemical bacterial heterotrophs that generate bioelectricity.
  • Right upper in fig 1 concerns a condominium of autotrophic bacteria, the aerobic autotrophic bioreactor, that oxidize nBOD (that oxidize ammonium and nitrite ions ) and decrease the alkalinity/pH.
  • the CO 2 produced by consumer organisms is transported to the producer organism or is CO2 is photocatalysed to hydrocarbons such as methanol as a necessary hydrogen donor for the hemoheterotrophic microbial bioreactor and thus to fuel the chemoheterotrophic microbial bioreactor.
  • Oxygen required by the aquatic animals and the aerobic producer bacteria is obtainable from the electrochemical and photocatalytic water splitting actuators.
  • Fig. 5 displays a certain embodiment of present invention of a combined anaerobic denitrifying / aerobic nitrifying bacterial fuel cell sharing the cathode.
  • the cathode can be subjected to active or passive aeration.
  • Oxygen for the autotrophic bioelectrochemical bacterial cell can be obtained from the electrochemical and photocatalytic water splitting actuators.
  • Fig. 6 is a schematic view of controlled fluid communication more particularly the exchange of nutrient loaded water
  • Fig. 7 is a schematic view of controlled fluid communication, more particular gas fluid communication or gas in liquid fluid communication.
  • the dotted lines demonstrate the transport to the bioreactors that are assisted by autotrophic organisms (tank B and C)
  • Fig. 8 is a schematic view of controlled gas fluid communication and more particularly the oxygen production by the plant bioreactor or photoauto-heterotrophic bioreactor and in particular the bioreactor with photoautotrophic organism (e.g. green plants and photosynthetic bacteria are photoautotrophs).
  • the arrow demonstrates the transport of the oxygen fluid.
  • Fig. 9 is a graphic scheme that demonstrates that the farming system comprises one or more drainage water collection system (drain storage tank) to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse horticulture system (GCS).
  • This drainage water collection system is a heat source or sinks of the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS) or of the IRA.
  • heat is collected by an evaporation heat exchanger and transported by the heat pump to a condensing heat exchanger.
  • Fig. 10 provides a scheme of the use reversed absorption heat pumps fired by energy rich gas of the gasification bioreactor of present invention.
  • the reversed absorption heat pumps connected in a variable flow control system.
  • Tf temperature of the aquatic animal farming system in particular the fish culture (e.g. the recirculating aquaculture system (RAS)) which can comprise bioreactor units and drain organic waste into the gasification bioreactor
  • Tb temperature of a gasification bioreactor unit for instance a sludge blanket bioreactor or a granule bioreactor
  • Tp temperature hydroponics or a soilless plant culture unit (e.g.
  • the system comprises at least one clean water (ground water and/or rain water) collection or storage tank (400), at least one drain water collection or storage tank with drain water of the hydroponics or a soilless plant culture unit (e.g. the greenhouse culture system (GCS)) (401), a gasification bioreactor (402), aquatic animal farming system in particular the fish culture (e.g.
  • the recirculating aquaculture system (RAS) or recirculating aquatic animal farming system (403) which can comprise bioreactor units and drain organic waste into the gasification bioreactor or its confined environment or building (404), a hydroponics or a soilless plant culture unit (405) (e.g. the greenhouse culture system (GCS)) or its greenhouse (406), evaporators (407) to absorb heat and condensers (408) to release heat, the reverse switch system(s) (409) and the gas fired heat pump drive system (411).
  • 410 is a place the under the frost line ground water.
  • the system comprises one or more drainage water collection system to collect the drainage water from the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS).
  • This drainage water collection system is a heat source or sink for the recirculating aquaculture system (RAS) and/or the greenhouse culture system (GCS) or the IRAFS.
  • At least one thermal loop comprising at least one of the compressor and working fluid expansion means (for instance an expansion valve) components and at least two heat exchangers each of the evaporator and condenser type connected in the form of a closed circuit for circulating a volatile liquid (working fluid or refrigerant), circulates through the components.
  • At least one evaporator type heat exchanger of the closed loop is in contact with a drainage water collection system.
  • vapour from the evaporator is compressed (e.g. by a compressor or thermally in an extra solution circuit comprising an absorber, a solution pump and a generator absorber) to a higher pressure and temperature and consequently the hot vapour then enters a condenser heat exchanger which is contact with the RAS or GCS, where it condenses and gives off useful heat to the RAS and/or GCS. Consequently the high-pressure working fluid is expanded again to the evaporator pressure and temperature for instance by asses an in the expansion valve.
  • the working fluid is returned to its original state and once again enters the evaporator.
  • the thermal loop between the drainage water collection system and the RAS and/or GCS can comprising a reversing valve and force the heat flow in the other direction. Heat is then transferred in the opposite direction, from the RAS and/or GCS that is cooled, to the drainage water collection system.
  • the drainage water collection system is contacted with at least one condenser heat exchanger of a closed loop and the RAS and/or GCS with at least one evaporator type heat exchanger.
  • Fig. 11 provides function diagram of possible heat transfer switches of the heat pump system with reversible operation in heating mode or in cooling mode.
  • the different components are expansion valves (304), 4 way switch valve (308), two switch valves (309), condenser (301), evaporator (302), compressor (303), drain water container (300), Rain water / groundwater or clean water tank (305), aquatic animal culture tank or tanks (306), hydroponics or soilless crop culture unit(s) (307) and under frost line ground (water) (308).
  • heat can be transferred from the soilless crop culture unit(s) (307) to the aquatic animal culture tank or tanks (306) this is particularly suitable in a day and night regime.
  • the optimal or desired temperature for crop growth is maintained different from the optimal or desired temperature of the aquatic multicellular consumer organisms (e.g. aquatic animals).
  • the optimal temperature for crops in the soilless crop culture unit difference between day and night (for instance 25.5 °C at day and 17.7 °C 's at night.
  • the temperate is generally kept equal and stabilized. Controlled heat transfer maintains these different temperature regimes.
  • Figure. 12 is a graphic display of a screening apparatus for mechanical removal of the suspended organic solids, particulate organic matter and colloidal organic matter ((coBOD ) colloidal BOD and (pBOD ) particulate BOD (removal apparatus for suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD)) for instance a micro screen apparatus for removal of the suspended solids, which in this picture is displayed as a side view of an incline belt screen filter (132) with a screen belt (143).
  • coBOD colloidal BOD and (pBOD ) particulate BOD
  • SS suspended solids
  • coBOD colloidal BOD
  • pBOD particulate BOD
  • a centrifuging or hydrocycloning apparatus can be used for removal of the suspended organic solids, particulate organic matter and colloidal organic matter. Suspended non filterable particulate matter can be removed by a foam fractionation apparatus. All these are foreseen of an input to receive the (dirty) water (148) and an out put (149) to return the (clean) water to the aquatic farming system. Furthermore they are foreseen to deliver the waste (142) to a waste collection tank (133).
  • the water collection tank (133) is provided with a transport line (e.g.
  • gasification tank (134) As displayed in this Fig. the gasification tank (134) is foreseen of a closed loop (146 & 147) to recirculate its supernatant out put.
  • the gasification tank (134) furthermore comprises on or more out put and distribution line (transport pipe) (136) to transport the energy rich gas to the heat pump firing drive system (441, 216, 204).
  • This distribution line (transport pipe) (136) distribute the gas first towards a deshydratation unit (150) and the deshydratation unit can be connected by a distribution line (transport pipe) (151) with a gas storage unit (152) which is connected by a distribution line (transport pipe) (153) with the heat pump firing drive system (441, 216, 204).
  • Fig. 13 is a schematic view of the gasification heat pump mechanism.
  • the condenser (201) releases heat into its environment and the evaporator (203) extracts heat from the environment.
  • a gas heater (204) receiving energy rich gas from the gasification tank transport piping (153) heats the condenser (203) and drives the heat pump.
  • An extra pump pumps the lubricant fluid through the condenser (203) towards and expansion valve (206) to an absorber (202).
  • the generator is connected by a loop with the evaporator (200).
  • the loop passes through an heat exchanger loop (201a) in the condenser (201) through an expansion valve (206) in the evaporator heat exchanger loop (200a) of the evaporator (200)
  • a pipe loop with an heat exchanger in the absorber (202) and an heat exchanger in the condenser (203) connects the absorber with the condenser (201) and has a open end (202a) in the absorber (202).
  • Fig. 14 provides a scheme of gas driven heat pumps whereby 210 are the expansion valves, 211 is a solvent pump, 213 is an evaporator that releases heat in the environment for instance the aquatic animal farming system, 212 is a condenser that extracts heat from the environment, 215 is the separator, 214 is an absorber that releases heat in the environment for instance the aquatic animal farming system.
  • Heating induces vapour (for instance ammonia) to escape of a micro porous materials for instance zeolites whereby the condenser transfer heat to its environment.
  • vapour for instance ammonia
  • the vapour or instance ammonia is absorbed in the micro porous materials for instance zeolites whereby the heat exchanger of the evaporator extract heats from its environment.
  • Fig. 15 provides a schematic view of a photocatalyst bioreactor with an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • the photoctalyst unit is foreseen with a radiation unit (103) to radiate the photocatalytic material (104).
  • the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquati nimal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • An output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (134) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (134, effluent collection (137)) .
  • the gasification unit is provided with switch valves (154) to release its processed water via an out put or transport piping (155) or to return the water via a transport piping (99b) to the photocatalytic reactor unit (100).
  • the gasification tank (134) furthermore comprises on or more out put and distribution line (transport pipe) (136) to transport the energy rich gas to the heat pump firing drive system (441, 216, 204).
  • This distribution line (transport pipe) (136) distribute the gas first towards a deshydratation unit (150) and the deshydratation unit can be connected by a distribution line (transport pipe) (151) with a gas storage unit (152) which is connected by a distribution line (transport pipe) (153) with the heat pump firing drive system (441, 216, 204).
  • Fig. 16 is a drawing that displays a photocatalytic reactor (100) and a radiation source (103) for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytic material (104) to an aerobic bioreactor that enhances a larger part of ammonium removal through oxidizing ammonium directly into N 2 , or ammonium into NO 2 ' or to reduce NO 3 " into NO 2 " depending on the photocatalyst and/or the reaction time.
  • the photocatalytic reactor can deliver such treated water to a pretank unit (101).
  • a pretank unit (101) By in situ hard sensor with a signal output that is representative for Ammonium, nitrite and/or nitrate the ammonium to nitrite proportion can be controlled in the pretrank (101) in a particular embodiment.
  • This bioreactor is preferably a (bio)granule (144) producing bioreactor foreseen of turbulence or shear force creation means for instance a stirrer (105) for inducing biofilm forming into (bio)granules (144).
  • the photocatalytic reactor is for seen with a transport pipe input (99) to receive water load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the aquatic farming system.
  • a transport piping connects the out put (107) eventually over a pump (108) of the photocatalytic reactor with pretank unit (101) such as an aeration or oxygenation unit (101) which is connected with a transport piping (110) with the aerobic bioreactor (102).
  • a loop (106) eventually with pump (111) allows under control of a valve system (154) to return water treated in the bioreactor via a transport piping (99a) to the photocatalytic reactor input (99) or to the aeration or oxygenation unit (101).
  • This photocatalytic aerobic bioreactor system can release the photocatalyst / aerobic bioreacted water via an output (112) into the aquatic animal farming system or into the storage tanks of the soilless plant culture or hydroponics.
  • the photocatalytic reactor can also been foreseen with a transport pipe or irrigation output (98) to transport water to other units for instance to the plant hydroponics or soilless crop culture unit (Fig. 19).
  • the pretank (101) and the photocatalytic reactor (100) are one.
  • the radiation source can be a solar light collector, UV source, near UV source, UV-VIS source, VIS source.
  • Fig. 17 is a drawing that displays a photocatalytic reactor for oxidizing and mineralizing of the complex organic molecules or for ammonium directly into N 2 , or ammonium into NO 2 " or to reduce NO 3 " into NO 2 " depending on the photocatalyst and/or the reaction time and for presentation of the photocatalytic material to an bioreactor system aerobic bioreactor and anaerobic bioreactor that can be tuned to enhance a larger part of ammonium removal through oxidizing ammonium directly into N2.
  • This bioreactor is preferably a (bio)granule (144) producing bioreactor foreseen of turbulence or (hydrodynamic) shear force creation means for instance a stirrer (105) for inducing biofilm forming into (bio)granules (144).
  • the photocatalytic reactor is foreseen with a transport pipe input (98) to receive water load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the aquatic farming system.
  • a transport piping connects the out put (125) eventually over a pump (129) of the photocatalytic reactor with a pretank (118) for instance an aeration or oxygenation unit (118).
  • nitrite and/or nitrate the ammonium to nitrite proportion can be controlled in the pretrank (118) in a particular embodiment. Furthermore the oxygen and carbon dioxide levels in the water of this pretank unit (118).
  • This pretank (118) is connected with a transport piping (126) with the aerobic bioreactor (119), preferably a granule aerobic bioreactor that is foreseen of a turbulence or a shearing means (123) to force biofilm forming microorganisms to form (bio)granules.
  • a loop (100) eventually with pump (130) allow under control of a valve system (154) to return water treated in the bioreactor via a transport piping (99a) to the photocatalytic reactor input (99) or to the pretank or the aeration or oxygenation unit (118).
  • This photocatalytic aerobic bioreactor system can release the photocatalyst / aerobic bioreacted water via an output (127) into anaerobic bioreactor, preferably an anaerobic granule bioreactor (120) foreseen of a turbulence or shear force means to force the biofilm forming microorganisms to form granules (144b).
  • This anaerobic bioreactor can release the water that has been photocatalytic, aerobic bioreactor and anaerobic bioreactor processed via an output or an output transport piping (131) into the aquatic animal farming system or into the storage tanks of the soilless plant culture or hydroponics.
  • the anaerobic bioreactor is foreseen with a loop of a transport pipeline (100) and eventually a pump (130) under control of a switch valve system back into the photocatalytic unit (117).
  • Biogranules can also be in the form of floes or sludge (biofloc or bio sludge).
  • Fig. 18 displays a photocatalyst reaction unit to pretreat the water that is loaded with organic materials and to oxidize complex organic molecules, suspended organic solids, particulate organic matter and colloidal organic matter ((coBOD ) colloidal BOD and/or (pBOD ) particulate BOD and/or solved nBOD, cBOD into mineral molecules for instance for organic phosphorus, nitrogen and carbon mineralization or partial mineralization, disinfection and/or metal reduction.
  • (coBOD ) colloidal BOD and/or (pBOD ) particulate BOD and/or solved nBOD, cBOD into mineral molecules for instance for organic phosphorus, nitrogen and carbon mineralization or partial mineralization, disinfection and/or metal reduction.
  • the photocatalytic unit (100) is provided with a radiation source (103) to radiate the photocatalytic material (104), for instance a UV lamp (103), UV-VIS, Near UV, VIS depending on the type of photocatalyst, or alternatively collector sun light or a suitable photocatalytic surface that is exposed to sun light. Suitable photocatalyst have been explained in this application.
  • This output transport piping or irrigation means (107) is provided with a switch valve that allows to return the processed water via a transport piping or irrigation means (147b) to the photocatalytic reactor unit.
  • the photocatalytic reactor unit can be foreseen with a gas transport piping (136) to transport the gas fluids generating in the photocatalytic reactor unit.
  • the photocatalytic unit (100) comprises an alternative output (156) under control of a valve (154) that can provide processed water to other units for instance to the aquatic animal farming units.
  • the gasification unit (134) is preferably foreseen of a shear force tool or (136) to force the microorganisms into granules (144).
  • the watery fluid out put(s) (137) of the gasification tank (134) is or are connected via a transport piping or irrigation system (118) with an oxygenation or aeration unit (147) which is connected with a transport piping or irrigation system ( 126) to deliver the aerated or oxygenated water to an aerobic biofilter ( 119) is preferably an aerobic (bio)granule biofilter foreseen with a shear forces or water disturbance tool (123) to force the microbials into (bio)granules.
  • This aerobic biofilter is connected by a transport piping or irrigation unit (127) to deliver its processed water into an anaerobic biofilter unit (120) which is preferably an anaerobic (bio)granule biofilter foreseen with a shear forces or water disturbance tool (124) to force the microbials into (bio)granules.
  • This anaerobic biofilter unit (120) has an output and output transport piping or irrigation tool ( 131) to transport its processed water to the aquatic farming animal system or to the crop hydroponics or the soilless plant culture system.
  • the anaerobic biofilter unit (120) comprises further a transport piping or irrigation unit (127) to recirculate its processed watery fluid to aeration tank (147).
  • Bacterial reactions can be carried out over several different temperature ranges depending on the tolerance of the bacteria, ranging from moderate or room-level temperatures (15- 35 0 C) to both high temperatures (50-60°C) tolerated by thermophiles and low temperatures ( ⁇ 15°C) where psychrophiles can grow. Instead of biogranules the bioreactor can operate on floes or sludge.
  • Fig. 19 displays the nutrient feeding and recirculating system of the plant hydroponics or soilless crop culture (greenhouse) that is incorporated in the IRAFS of present invention.
  • a water collection unit can receive water of a transport piping (98 or 156) directly from a photacatalytic reaction unit or of a transport piping (131) indirectly from a photacatalytic reaction for instance of a photocatalyst / aerobic bioreactor / anaerobic bioreactor unit (17 or 18 (whereby at least one of the anaerobic bioreactors is a gasification tank) and eventually an other anaerobic is an anaerobic microbial fuel cell (with heterotrophic bioelectrochemical bacteria for anaerobic denitrification), or of a transport piping (112) of a photocatalyst / aerobic bioreactor system (Fig.
  • a photocatalytic reactor input (99)
  • an aerobic bioreactor unit autotrophic bioelectrochemical bacteria for aerobic nitrifying bacterial fuel cell
  • a separate aeration or oxygenation unit (101) the transport piping (112) to release the photocatalysed and aerobic bioreacted water into a storage tank (168) or in one of the tanks (157, 158 or 167) of the photocatalyst / aerobic bioreactor system (Fig. 16).
  • the water storage (168) that receives water from the photocatalytic reactors (fig 15, 16, 17, 18, 21, 22, 23 or 24) , the drain water tank (159) (that receives the (dirty) water of the hydroponics culture, the soilless crop culture system or the crop greenhouse culture (163) ) and the clean water tank (157) that stores ground water, rain water or other clean water, are connected with a transport piping or irrigation system to a mixing unit or mixing tank (167).
  • There water supply to the mixing unit or mixing tank (167) is under control of a multiple switch valve (160) to control their water flow towards the mixing unit or mixing tank (167).
  • a mineralization and/or sterilization unit (165) preferably a flow through sterilization unit that comprises a UV radiation source or UV source, near UV source, UV-VIS source, VIS source or solar light source (166) depending on the photocatalyst material and can be assisted by ultrasound or microwave source to radiate the passing through water or eventually an ozonation system as a germicidal treatment.
  • mineralization and/or sterilization unit (165) can comprise a photocatalysts. In the presence of a photocatalyst material and depending on the selected photocatalyst material the radiation source (166) can for obtaining a sterilisation and / or mineralization function radiate also UV-VIS light.
  • a mineralization and/or sterilization unit (165) can comprise beside a photocatalyst and a UV, Near US, VIS light or Sun light source further comprise an hybrid photocatalyst / ultrasound function or an hybrid photocatalyst / microwave function.
  • the hydroponics culture, the soilless crop culture system or the crop greenhouse culture (163) comprises chemical (nutrient) stock solution tank(s) (162), of which one a acid stock solution tank (162) and another base stock solution tank (162), that all have an transport pipe that passes dosing or reservoir pumps (159) for composing a desired nutrient solution , pH and alkalinity for instance in the diluter (161) or in the mixing unit or mixing tank (167).
  • the diluter (161) or the mixing unit or mixing tank (167) have an irrigation or transport piping to the plant growing troughs (164).
  • the plant growing troughs (164) are connected by a transport piping or irrigation with a drain pit (165) that is connected by a transport piping or irrigation with the drain storage tank (158).
  • the system will be controlled by a liquid control system that controls the (nutrient) dosing or reservoir pump, the nutrient solution pH, the nutrient electric conductivity, nutrient solution and condensate water levels.
  • Figure. 20 provides A) a view of a transverse section of a transport fluid pipe between the different units such as the rain water / groundwater or clean water tank (305), the aquatic animal culture tank or tanks (306), the hydroponics or soilless crop culture unit(s) (307) the soilless crop culture unit(s) (307) and the bioreactor units and B) a 3D side view of such transport pipe (113).
  • the outer layer of the liquid transport piping (114) is coated by an antimicrobial layer in particularly a virucidal layer. Such layer prevents biofilm forming (116). Suitable coatings have been provided in this application. In a particular embodiment of present invention at least some of the water storage tanks have been coated inside by the same antimicrobial coating.
  • 115 is the inner lumen of the transport pipe. Instead of in the coating the antimicrobial material can be incorporated in material of the piping or the tanks itself.
  • Fig. 21 displays a photocatalyst reactor that is connected by its processed water output with a transport piping (125) to a microbial fuel cell unit.
  • the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved cBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • the photoctalyst comprises a radiation unit (122) to radiate the photocatalytic material (121).
  • This radiation unit can be an UV lamp but alternatively the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light or alternatively the photocatalytic material is exposed to near UV, UV-VIS light, VIS light or other suitable radiation sources described in this application depending on the photocatalytic material.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquatic animal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • the photocatalytic reactor (117) is for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytized molecules to enhance the productivity of a microbial fuel cell.
  • An output and transport piping (125) provides the water wherein the organic load has been mineralized from the photocatalytic reactor (117) to the microbial fuell Suite (511 and 501).
  • the microbial fuel cell can be an aerobic microbial fuel cell (511) for instance inoculated with aerobic bacteria (e.g. aerobic nitrifiers or aerobic bioelectrichemical autotrophes ) such as Bacillus subtilis, an anaerobic microbial fuel cell (501) or both as displayed in Fig. 21.
  • the microbial fuel cell receives water from a transport piping (125) of the photocatalytic reaction unit eventually over a pump (129).
  • the aerobic microbial fuel cell (511) is preceded by an aeration or oxygenation unit (118) that is connected with its output via a transport piping or irrigation system with the aerobic microbial fuel cell (511) (e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers).
  • anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers.
  • the anaerobic fuel cell receives water that has been processes in the photocatalytic reactor (117) from the transport piping or irrigation system of the photocatalytic reactor (117).
  • the anode chamber of the microbial fuel cells or the oxygenation or aeration chamber can recycle the processed water back to the photocatalytic reactor unit (100) via a transport piping such as 99b.
  • the output of this hybrid photocatalytic / microbial fuel cell system can release its processed water via a transport piping or irrigation system (131) into water storage (168) or other storage tanks or the mixing tanks (167) of a hydroponics culture, soilless crop culture system or crop greenhouse culture (163).
  • 502 and 512 displays a load of an external circuit.
  • the component 505 and 510 displays a separator.
  • the components 503 and 516 display the anodes in their anodes chamber.
  • 504 and 517 is a picture of the cathodes.
  • the anaerobic fuel cell can be hosted by bacterial reactions can be carried out over several different temperature ranges depending on the tolerance of the bacteria, ranging from moderate or room- level temperatures (15-35°C) to both high temperatures (50-60°C) tolerated by thermophiles and low temperatures ( ⁇ 15°C) where psychrophiles can grow.
  • Fig. 22 A displays a photocatalytic reactor (117) that receives watery fluid loaded with organic molecules or organic matter from an input transport piping (99) or irrigation system (99).
  • the photocatalytic reactor comprises a photocatalytic material
  • the output for the photocatalytic processed watery fluid is connected with a transport piping (125) or irrigation system (125) which eventually passes a pump (129) and which is connected with a multitubular or multi column microbial fuel cell (525) or a reactor in which micro-organisms generate current (525) so that the photocatalytic water flows over anodic material (521) able to host microbials and able to accept electrons in a series of tubes that are 3 dimensionally surrounded by a cation exchange membrane (526).
  • anodic material (521) comprises an electric conductive material (for instance conductive graphite pellets or (macro)porous graphite).
  • the cation exchange membrane (526) is three dimensionally surrounded by a cathodic material (520) and is separating the cathode from the anode.
  • This cathodic material (520) can be ferricyanide catholyte fluid that overflow the out surface of the cation exchange membrane (526) which ferricyanide catholyte fluid is for instance pumped by a pump (129b) over the outer surface of the cation exchange membrane (526) of the multitubular or multi column microbial fuel cell (525) and can be recycled in a loop (528) and eventually passing an aeration or oxygenation unit (524) provided with an aerator (128).
  • the multitubular or multi column microbial fuel cell (525) is provided with at least one external circuit that comprises a load (522).
  • the external circuit (128) is able to receive electrons from the anode and to transport the electrons to the cathodic material (520).
  • the anode is able to accept electrons from the microbials and the cathode is able to transfer the electrons from the external circuit to an electron acceptor or sink
  • Fig. 22 B is a follow up of Fig. 22 A. It shows two transfers section of one column or tube of the multitubular microbial fuel cell reactor.
  • the anode material (521) is surrounded by a cation exchange membrane (526) between an outer layer (527) which for contact wit other cathodes in the series of columns or tubes can be a electric conductive layer for instance of graphite.
  • a cathode material (520) which is a solid in a watery medium (in fig 23 B2) that contacts the cation exchange membrane (526) or which is a catholyte fluid (in fig 23 Bl).
  • Fig. 23 displays a combined photocatalyst reactor (100) / gasification unit (134) that is connected by its processed water output (137) with a transport piping (155) to deliver its processed water to a microbial fuel cell unit.
  • the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and nBOD for instance from the from the aquatic animal farming units.
  • SS suspended solids
  • coBOD colloidal BOD
  • pBOD particulate BOD
  • the photoctalyst unit is foreseen with a radiation unit (103) an UV radiator, near -UV radiator, UV-VIS radiator, VIS light radiator depending on the photocatalytic material, to radiate the photocatalytic material (104) and is eventually assisted by an utrasonic or microwave radiator.
  • the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquatic animal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • An output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (135 (the lowest 134 in fig 23 is 135)) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (135 (the lowest 134 in fig 23 is 135)), effluent collection (137)) .
  • the gasification unit is provided with switch valves (154) to release its processed water via an out put or transport piping (155) or to return the water via a transport piping (99b) to the photocatalytic reactor unit (100).
  • the out put (137) of the combined photocatalyst reactor (100)/ gasification unit (134) is connected via a transport piping or irrigation tool (155) with the microbial fuel cell reactor wherein microbials provide electrons, an anode is provided to accept electrons from the microbials which are transorted by a circuit (502, 512) to the cathode which is able to transfer the electrons from the external circuit to an electron acceptor or sink.
  • the photocatalytic reactor (100) is for oxidizing and mineralizing of the complex organic molecules and presentation of the photocatalytized molecules to the gasification unit (134) and a microbial fuel cell (511, 501) to enhance their productivity.
  • An output and transport piping (155) provides the water wherein the organic load has been mineralized and passed the gasification unit (134) to the microbial fuel cell (501 and/or 511).
  • the microbial fuel cell can be an aerobic microbial fuel cell (511) for instance inoculated with aerobic bacteria (e.g. aerobic nitrifiers or aerobic bioelectrichemical autotrophes) such as Bacillus subtilis, an anaerobic microbial fuel cell (501) or both as in Fig. 23.
  • the gasification tank receives water from a transport piping (107) from the photocatalytic reaction unit 100), eventually over a pump (108).
  • the aerobic microbial fuel cell (511) is preceded by an aeration or oxygenation unit (118) that is connected with its output via a transport piping (126) or irrigation system with the aerobic microbial fuel cell (511) (e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers).
  • anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers e.g. with anaerobic bioelectrochemical heterotrophes or anaerobic denitrifyers.
  • the anaerobic fuel cell receives water that has been processes in the photocatalytic reactor (100) and gasification unit (134) from the transport piping or irrigation system of the combined photocatalytic reactor (100) / gasification unit (134).
  • the anode chamber of the microbial fuel cells or the oxygenation or aeration chamber can recycle the processed water back to the photocatalytic reactor unit (100) via a transport piping such as 99b.
  • the output of this hybrid photocatalytic / microbial fuel cell system can release its processed water via a transport piping or irrigation system (131) preferably into water storage (168), the mixing tank (167) or other storage tanks of the hydroponics culture, soilless crop culture system or crop greenhouse culture (163).
  • 502 and 512 displays a load of an external circuit.
  • the component 505 and 510 displays a separator.
  • the components 503 and 516 display the anodes in their anodes chamber.
  • 504 and 517 is a picture of the cathodes.
  • 500 kg of fish in weight produces 550 m 3 biogas per year (biogas/a), ca. 3500 kWh ⁇ or at least 200 - 500 (800) m 3 biogas/a, depending on the energy content of the biogas with a energy content 6.0 - 6.5 kWh m or a fuel equivalent 0.60 - 0.65 L oil/m 3 biogas.
  • the energy efficiency (JIMFC) the ratio of power produced by the MFC over a time interval divided by the heat of combustion of the organic substrate is up to 50% when easily biodegradable substrates are used. In comparison the electric energy efficiency for thermal conversion of methane is ⁇ 40%.
  • Fig. 24 displays a combined photocatalyst reactor / gasification unit that is connected by its processed water output with a transport piping (125) to deliver its processed water to a tubular microbial fuell cell.
  • the photocatalytic reactor unit (100) has an input piping (99) that recieves (organic rich) water with a load of suspended solids (SS), colloidal BOD (coBOD) and/or particulate BOD (pBOD), solved CBOD and/or nBOD for instance from the from the aquatic animal farming units.
  • SS suspended solids
  • coBOD colloidal BOD
  • pBOD particulate BOD
  • the photoctalyst unit is foreseen with a radiation unit (103) an UV radiator, near -UV radiator, UV-VIS radiator, VIS light radiator depending on the photocatalytic material, to radiate the photocatalytic material (104) and is eventually assisted by an utrasonic or microwave radiator.
  • the photcatalytic material is exposed to sun light for instance by having tubings with the photocatalytic material or photoctalytic plates of the photocatalytic apparatus exposed to sun light.
  • the photocatalytic material can eventually receive reflected light from a reflector or the photocatalytic unit of the photocatalytic apparatus can be placed above the aquati nimal farming unit in a green house or can be placed on on the roof of the building of the aquatic animal farm.
  • An output and transport piping (107) provides the water wherein the organic load has been mineralized to the feed distributor (134) of a gasification unit (134) for instance a gasification tank comprising a sludge bed (140), with (bio)granules (144), rising vapour bubbles (139), baffle (138), gas solid separator (145), a feed distributor (134), and effluent collection (137)).
  • the gasification unit is provided with switch valves (154) to release its processed water via an out put or transport piping (155) or to return the water via a transport piping (99b) to the photocatalytic reactor unit (100).
  • the transport piping (155) is connected with a transport piping (125) or irrigation system (125) which eventually passes a pump (129) and which is connected with a multitubular or multi column microbial fuel cell (525) or a reactor in which micro-organisms generate current (525) so that the photocatalytic water flows over anodic material (521) able to host microbials and able to accept electrons in a series of tubes that are 3 dimensionally surrounded by a cation exchange membrane (526)
  • Such anodic material (521) comprises an electric conductive material (for instance conductive graphite pellets or (macro)porous graphite).
  • the cation exchange membrane (526) is three dimensionally surrounded by a cathodic material (520) and is separating the cathode from the anode.
  • This cathodic material (520) can further comprise a chatolyte fluid, for instance a ferricyanide catholyte fluid that overflows the out surface of the cation exchange membrane (526).
  • the catholyte fluid is for instance pumped by a pump (129b) over the outer surface of the cation exchange membrane (526) of the multitubular or multi column microbial fuel cell (525) and can be recycled in a loop (528) and eventually passing an aeration or oxygenation unit (524).
  • 522 is the load of the external circuit (522).
  • the multitubular or multi column microbial fuel cell (525) furthermore comprises an external circuit (128) able to receive electrons from the anode and to transport the electrons to the cathodic material (520).
  • the anode is able to accept electrons from the microbials and the cathode is able to transfer the electrons from the external circuit to an electron acceptor or sink.
  • 500 kg of fish in weight produces 550 m 3 biogas per year (biogas/a), ca. 3500 kWh th or at least 200 - 500 (800) m 3 biogas/a, depending on the energy content of the biogas with a energy content 6.0 - 6.5 kWh m or a fuel equivalent 0.60 - 0.65 L oil/m 3 biogas.
  • JIMFC The energy efficiency
  • Fig. 25 displays nitrification bacterial fuel cell for addition of oxygen to nitrogen while generating bioelectricity.
  • the oxygen is generated at a radiated (near UV, UV - VIS, preferably visible light or solar light radiation) photo anode in water.
  • a photosemiconductor photo anode (of KTaO 3 , SrTiO 3 , TiO 2 , ZnS, and SiC). in water is excited by light photons (hv).
  • the photo anode absorbs light photons with energies greater than its band-gap energy (Eg). This absorption creates excited photoelectrons in the conduction band (CB) and holes in the valence band (VB) of the semiconductor.
  • Eg band-gap energy
  • the photoinduced electrons and holes reduce and oxidize adsorbed water to produce gaseous oxygen and hydrogen : H 2 O + 2h + -> 2H + + Vi O 2 .
  • H + is transported to the anode chamber with electrochemical bacteria (heterotrophic nitrifiers) and oxygen is transported to the cathode chamber.
  • electrochemical bacteria heterotrophic nitrifiers
  • oxygen is transported to the cathode chamber.
  • reduced substrates such as reduced nitrogen
  • ammonium and nitrite ions are oxidized resulting in a decrease of nBOD with the generation of oxidized nitrogen species and in the generation of electrons and protons.
  • the nitrification is indicated by the production of nitrite and nitrate ions or can be suspected by physical indicators such as an increase in the liquor oxygen demand or an decrease in the dissolved oxygen by the dissolved oxygen consumption of the nitrifying bacteria during the oxidation of the ammonium ions and nitrite ions and a decrease of the liquor alkalinity/pH by the production of the nitrite ions.
  • the drop occurs through the use of the alkalinity as a carbon source by nitrifying bacteria and the destruction of the alkalinity by the production of hydrogen ions and the nitrite ions during the nitrification.
  • nitrification needs however the measure of the concentrations of the specific ammonium, nitrite and nitrate ions.
  • the oxidation of the reduced nitrogen results in a decrease of the negative charge and an increase of the positive charge due to the loss of the electrons.
  • Oxygen is provided to the cathode through a gas diffusion layer (for instance porous carbon) .
  • the electrodes are connected by a wire containing a load (i.e., the device being powered) or a resistor.
  • the both chambers are separated by a separation means (e.g.
  • the gas diffusion layer sticked to the cathode can for instance be Teflon treated carbon paper or Teflon treated woven cloth
  • Fig. 26 displays (700) a suspended particles photocatalytic reactor with microparticles, preferably with a magnetic core (704) and a silica layer (703) which are coated by photocatalytic nanoparticles for instance for down hill or up hill photocatalysis; hereby is displayed photon (703) induced electron-hole (704) generation in a photocatalyst particle (702) (for instance Degussa P25 titanium dioxide) and some of the mechanisms involved: a) Ray promotes the formation of the electron-hole and electron, b) electron-hole is used in the formation of the OH* groups promoting oxidation processes, c) the electron is utilized in a number of reduction processes, d) electron and electron-hole can recombine contributing to process inefficiency.
  • a photocatalyst particle for instance Degussa P25 titanium dioxide
  • the system can comprise photocatalyts for O 2 and H 2 generation and photocatalysts that use the O 2 for H 2 O 2 generation and/or for photocatalytic oxidation of the organic material or to convert (oxidize) organic molecules into CO2, water and minerals (mineralization) for instance for use into atmospheric and water based nutrients for the producer organism bioreactors, e.g. the plants or the producer bacteria).
  • the photocatalyst material is immobilized on a substrate, for instance of amorphous silica or glass plates).
  • Fig. 27 displays B a suspended particles photocatalytic reactor with C microparticles, photocatalytic nanoparticles (e.g. TiO2) surrounding a silica layer surrounding a supramagnetic core (for instance barium ferrite) to form a magnetic removable photocatalytic material D is the nanoparticular photocatalytic material (i.e. TiO2) with display of a hole induced by a photon.
  • the photocatalytic material displays in A a band gap which is assigned an energy value (Ebg) and which corresponds to its width in energy, and is the additional energy (denoted as hv) required for an electron (e-) to move from the VB into the CB.
  • Ebg energy value
  • hv additional energy
  • Such photocatalytic reactor can comprise photocatalytic material (suitable photocatalyst have been described in this application) for water into H 2 and O 2 and/or photocatalytic material H 2 O and C 2 O into hydrocarbons for the consumer organism e.g; to fuel anaerobic bacteria bioreactor or the fuel driven farming system actuators.
  • the photocatalyst material is immobilized on a substrate, for instance of amorphous silica or glass plates).
  • the farming system of present invention comprises at least one thermal loop comprising at least one of the compressor and working fluid expansion means (for instance an expansion valve) components and at least two heat exchangers each of the evaporator and condenser type connected in the form of a closed circuit for circulating a volatile liquid (working fluid or refrigerant), circulates through the components.
  • working fluid expansion means for instance an expansion valve
  • at least one evaporator type heat exchanger of the closed loop is in contact with a drainage water collection system (drain storage tank).
  • vapour from the evaporator is compressed (e.g. by a compressor or thermally in an extra solution circuit comprising an absorber, a solution pump and a generator absorber) to a higher pressure and temperature and consequently the hot vapour then enters a condenser heat exchanger which is contact with the RAS or GCS, where it condenses and gives off useful heat to the RAS and/or GCS. Consequently the high-pressure working fluid is expanded again to the evaporator pressure and temperature for instance by means of the expansion valve.
  • the working fluid is returned to its original state and once again enters the evaporator.
  • the thermal loop between the drainage water collection system and the RAS and/or GCS can comprising a reversing valve and force the heat flow in the other direction. Heat is then transferred in the opposite direction, from the RAS and/or GCS that is cooled, to the drainage water collection system, hi a particular embodiment the drainage water collection system is contacted with at least one condenser heat exchanger of a closed loop and the RAS and/or GCS with at least one evaporator type heat exchanger. Eventually the condenser heat exchanger can be in control with the clean water basin that supplies the rain and/or ground water into the RAS and GCS.
  • the closed loop thermal system is or the closed loop thermal system thermally driven by heat supply to drive the cycle (for instance waste heat, gas or biomass firing)
  • the working fluid can comprise an absorbent for instance ammonia (working fluid) and water (absorbent) or water (working fluid) and lithium bromide (absorbent).
  • a working solution circuit which consists of an absorber, a solution pump, a generator and an expansion valve the low-pressure vapour from the evaporator is absorbed in the absorbent whereby the process generates heat.
  • the solution is consequently pumped to high pressure and then enters the generator, where the working fluid is boiled off with an external heat supply at a high temperature.
  • the working fluid (vapour) is condensed in the condenser while the absorbent is returned to the absorber via the expansion valve.
  • Heat is extracted from the heat source in the evaporator. Useful heat is given off at medium temperature in the condenser and in the absorber. In the generator high-temperature heat is supplied to run the process.
  • the system can be a reversed system and the evaporator can be contacting with the drainage water collection system to extract heat thereof and to release the heat via the condenser to the RAS and/or GCS.
  • the condenser heat exchanger can be in control with the clean water basin that supplies the rain and/or ground water into the RAS and GCS.
  • a thermal loop of present invention can comprise multiple evaporators connected to a single condenser or multiple condensers connected to a single evaporators in a multisplit approach or the thermal loop of present invention can be connected to multiple condenser and evaporator heat exchange units and can be operate in a variable refrigerant flow approach under a management and control systems (see Fig. 10).
  • the thermal loop between the drainage water collection system the RAS and/or GCS works in a mixed mode the ground under the frost line or the outdoor air functioning as a heat source and providing cooling or heating towards the RAS and/or GCS.
  • the thermal loop of present invention integrates a ground heat exchanger in which an heat transfer fluid is permanently contained in its closed system (closed loop system) or in which the heat transfer fluid is part of a larger environment (open loop system), most commonly using ground water or surface water as the heat transfer medium
  • the thermal loop of present invention integrates a direct expansion (DX) geothermal heat pump system. Such DX systems may be single or multi-speed.
  • the thermal loop of present invention or the thermal loop of present invention in a mixed mode with an air to air or ground thermal pump is provided with a desuperheater to captures heat from the hot refrigerant as it leaves the heat pump compressor and transfers it to a separate hot water system.
  • the aquaculture system can be integrated in the greenhouse horticulture system or can be a system that communicated with water or atmosphere with the greenhouse horticulture system.
  • the aquaculture system can have two or more fish holding units to subject separate fish communities to a different day-night light and or temperature regime than the greenhouse horticulture system. Such separate fish holding units can be connected to the same biof ⁇ ltering system.
  • Such coatings can be used depending in the components of the system.
  • a protective heat conductive coating or to the dissimilar metal connection points can be applied .
  • Such protective coating can be low density polyethylene, for instance low density polyethylene with a wall thickness of 0.01 to 0.015 inches or 0.02 to 0.1 inches and a heat transfer inhibitive coating for the liquid refrigerant transport tubing that need to prevented of heat exchange (for instance a coating of a low density polyethylene with a wall thickness of at least 0.05 inches.
  • Suitable refrigerants are for instance a R-410A or a R-22 refrigerant.
  • the driving energy is heat is produced by firing of the methane or H2 gas from the Bioenergy Systems
  • this controlled biomass farming system in confined environment with controlled biomass, energy input and output is a controlled biotransformation system for bioremediation or redistribution of nutrients and energy in a controlled manner between bioreactors of living organisms.
  • the biotransformation system comprises at least one pump actuator to move the system fluids and at least three bioreactor systems of communicating fluids where under
  • At least one of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)) assisted biotransformation for instance an autotrophic plant assisted biotransformation unit and
  • bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio-electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio- electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor whereby the system is further characterised in that the bio-electrochemical bacteria assisted biofilters are bioelecu ⁇ city producers that are connected by a circuit to drive one or more heat pump system on the bioelectricity from the bio-electrochemical bacteria assisted biofilter or bioremediation system and further characterised in that heat pump system is connected by a loop
  • the invention relates to a controlled biomass farming system, for processes of redistribution of energy and biomass in a controllable manner.
  • This biomass farming system comprising separate bioreactor units in a shared confined environment or in different fluid flow interconnected confined environments with a fluid input and fluid output, whereby the biomass farming system comprises
  • an aquaculture system for the culture of aquatic multicellular consumer organism such as aquatic vertebrate animals or such as aquatic invertebrate animals, and further
  • the heat pump system is connected by a loop with a drain of the farming system, for instance a container keeping the drain water, to flow heat between drain and the farming system (for instance to move heat from drain to farming system) and whereby the bacterial reactor system is producing the energy that drives the heat pump system.
  • the invention relates to a controlled biomass farming system, for processes of redistribution of energy and biomass in a controllable manner.
  • This biomass farming system comprising separate bioreactor units in a shared confined environment or in different fluid flow interconnected confined environments with a fluid input and fluid output, whereby the biomass farming system comprises
  • an aquaculture system for the culture of aquatic multicellular consumer organism such as aquatic vertebrate animals or such as aquatic invertebrate animals, and further
  • a photocatalytic bioreactor system comprising at least one bioreactor of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)), and
  • At least one bacterial bioreactors system comprising condominiums of producers bacteria and condominiums of consumer bacteria in a same or separate bioreactor
  • an heat pump system characterised in that the heat pump system is connected by a loop with a drain of the farming system, for instance a container keeping the drain water, to flow heat between drain and the farming system (for instance to move heat from drain to farming system) and whereby the bacterial reactor system is producing the energy that drives the heat pump system.
  • the bacterial bioreactors system is an energy production system (bioenergy system) that drives a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • bioenergy system bioenergy system
  • a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • a suitable bioreactor for the production of energy rich gasses is the high rate anaerobic reactor up flow anaerobic sludge blanket (UASB) the anaerobic sequencing batch reactor (ASBR), the fluidized expanded bed reactor, the static granular bed reactor (SGBR), the anaerobic membrane reactor , the anaerobic expanded-bed reactor (EBR) and the granular bed baffled reactor (GRABBR).
  • UASB anaerobic sequencing batch reactor
  • SGBR static granular bed reactor
  • EBR anaerobic membrane reactor
  • EBR anaerobic expanded-bed reactor
  • GRABBR granular bed baffled reactor
  • Such bacterial reactor system can receive the solved and particulate material.
  • the organic material is first collected in a collection tank that feeds the gasification bioreactor .
  • Such collection tank can function as a concentration tank or as a buffer tank.
  • Yet another embodiment is the fluidization of the organic matter particles for instance by ultrasound before the organic and inorganic matter is fed into the gasification bioreactor.
  • the gaseous products such as CH 4 of the gasification bioreactor is transported to a gas collection container and transported to a heat burner that drives the gas driven heat pump system.
  • the bacterial bioreactors system is an energy production system (bioenergy system) that produces the gas that drives a drives gas driven heat pump system preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • This heat pump preferably is a reversible absorption heat pump such as a reversible air-water absorption heat pump.
  • the reversed absorption heat pump is in a preferred embodiment connected in a variable flow control system (as outlined for instance in fig 9).
  • the farming system can have a closed container for collecting of rain and or ground water (water input tank or clean water basin).
  • the reversed absorption heat pump system with variable flow control system can distribute heat between the water input tank, that farming system and the drain, hi a preferred embodiment the variable flow control system is a indoors with outdoors mixed system that is connect an heat releasing or heat extracting unit with the outer environment for instance with the bottom under frost line and/or the air of the out environment.
  • gasification bioreactor is foreseen with an in situ pH sensor for monitoring.
  • the bioreactor systems are constructed to exchange watery fluid and gas fluid in a controlled manner under control of a monitoring and control system.
  • the system can for instance comprises a hard sensing tool to produce a signal indicative of an abiotic parameter such as pH, and temperature and a controller to control at least one programmable actuator to adapt these abiotic parameters.
  • the system comprises at least one programmable actuator adapted to deliver a pH regulator agent to said system at an administration rate and at least one programmable heat and/or cool actuator to cool or heat the system, hi an embodiment at least one of the following parameters dissolved oxygen, conductivity, alkalinity, reduced nitrogen ad oxidized nitrogen and whereby the system is further analysed in situ and modulated by a programmable actuator.
  • the bacterial bioreactors system is an energy production system (bioenergy system), whereby the energy is used to drive actuators of the system.
  • the system can comprise a least one circuit to feed electricity generated by the bio-electrochemical bacteria assisted biotransformation system to at least one of the systems actuators (for instance a pump actuator to move system fluids).
  • this controlled biomass farming system in confined environment with controlled biomass, energy input and output is a controlled biotransformation system for bioremediation or redistribution of nutrients and energy in a controlled manner between bioreactors of living organisms.
  • the biotransformation system comprises at least one pump actuator to move the system fluids and at least three bioreactor systems of communicating fluids where under
  • At least one of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)) assisted biotransformation for instance an autotrophic plant assisted biotransformation unit and
  • bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio-electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio- electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor
  • such bioreactor with both condominium of autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria can be an up flow sludge blanket filter (USBF) bioreactor) with an anoxic and an aerated compartment and up flow sludge blanket filtration with automatic or continued removal of poor settling active sludge floes or sludge granule and automatic or continued distribution well settling active sludge floes or sludge granule to the anoxic zone.
  • USBF up flow sludge blanket filter
  • Such USBF fuel cell operates a process of up flow sludge blanket filtration which has a substantially higher specific rate of separation that the conventional sedimentation USBF technology and uses up flow sludge blanket filtration in a prism or cone shaped clarifier.
  • the activated sludge floes or granules that have been generated by high shear in the aerated unit will enter the clarifier at the bottom and, as it rises, upward velocity decreases until the floes of cells become stationary, effectively filtering out colloid, very fine particles, the floes with poor settling capacity or the bacterial granules with poor settling capacity, while descending to the bottom of the clarifier and are transferred back into the anoxic zone of the sludge floes or sludge (bio)granules that become large and heavy.
  • USBF fuel cell operates aeration, nitrification, denitrification, clarification and sludge thickening and stabilization without need of different dedicated vessels.
  • these processes can be integrates into one bioreactor and can be operates inside one compact bioreactor.
  • this controlled biomass farming system in confined environment with controlled biomass, energy input and output is a controlled biotransformation system for bioremediation or redistribution of nutrients and energy in a controlled manner between bioreactors of living organisms.
  • the biotransformation system comprises at least one pump actuator to move the system fluids and at least three bioreactor systems of communicating fluids where under 1) at least one heterotrophic aquatic animal assisted biotransformation unit; 2) at least one of living photosynthetic producer organisms (belonging to the Plantae (e.g. herbs, grasses, vines)) assisted biotransformation for instance an autotrophic plant assisted biotransformation unit and
  • bio-electrochemical bacteria assisted biofilter or bioremediation system with a) at least one heterotrophic (chemo organotrophic) bio-electrochemical bacteria assisted biotransformation unit to reduce nitrogen and decrease cBOD and b) at least one autotrophic (chemolithotrophic) bio-electrochemical bacteria assisted biotransformation unit to oxidize nitrogen and decrease nBOD or at least one bio- electrochemical bacteria assisted biofilter or bioremediation system with both types autotrophic (chemolithotrophic) bio-electrochemical bacteria and heterotrophic (chemo organotrohic) bio-electrochemical bacteria in one condominium or bioreactor whereby the system is further characterised in that the bio-electrochemical bacteria assisted biofilters are bioelectricity producers that are connected by a circuit to drive one or more heat pump system on the bioelectricity from the bio-electrochemical bacteria assisted biofilter or bioremediation system and further characterised in that heat pump system is connected by a loop with
  • the bacterial bioreactors system is an energy production system (bioenergy system) that drives a heat pump preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • the bacterial reactor system that produces the energy to drive the heat pump system comprises an anaerobic bioreactor (fig 2) or aerobic bioreactor (fig 3) or the combination of both (fig 5) comprising a condominium of bioelectrical bacteria whereby the degradation of organic matter on release electrons that for disposal are accepted by an electrode (anode) and distributed by an electric circuit.
  • Such bacterial reactor system can receive the solved and particulate material.
  • the organic material is first collected in a collection tank that feeds the gasification bioreactor .
  • a collection tank can function as a concentration tank or as a buffer tank.
  • the fluidization of the organic matter particles for instance by ultrasound before the organic and inorganic matter is fed into the gasification bioreactor.
  • the electrical circuit of the delivers the energy that drives the heat pump system.
  • the bacterial bioreactors system is an energy production system (bioenergy system) that produces the electricity that drives a heat pump system preferably a reverse cycle heat pump for regaining the heat from the drain into the controlled biomass farming system.
  • This heat pump preferably is a reversible absorption heat pump such as a reversible air-water absorption heat pump.
  • the reversed absorption heat pump is in a preferred embodiment connected in a variable flow control system.
  • the farming system can have a closed container for collecting of rain and or ground water (water input tank).
  • the reversed absorption heat pump system with variable flow control system can distribute heat between the water input tank, that farming system and the drain.
  • the variable flow control system is a indoors with outdoors mixed system that is connect an heat releasing or heat extracting unit with the outer environment for instance with the bottom under frost line and/or the air of the out environment.
  • the controlled a farming system comprising a controller to control the programmable pH actuator to normalize the pH between 5,5 and 8 (preferably between 6 - 7.5) and to control the heat and/or cool actuator to normalize the temperature between 15 - 30°C (preferably between 20 - 25°C).
  • a particular useful pH regulator agent is an alkalis of the group consisting of calcium bicarbonate, calcium carbonate, calcium hydroxide, magnesium bicarbonate, magnesium carbonate, magnesium hydroxide, sodium bicarbonate, sodium carbonate and sodium hydroxide.
  • the autotrophic bacteria assisted biotransformation unit can be a nitrifying bacterial fuel cell comprising autotrophic bio-electrochemical bacteria and the heterotrophic bio- electrochemical bacteria assisted biotransformation unit can be a denitrifying bacterial fuel cell.
  • the denitrifying bacterial fuel cell and the nitrifying bacterial fuel cell can be flow through fuel cells whereby the water of the farming systems flows through the bacterial fuel cell(s) .
  • the autotrophic bio-electrochemical bacteria assisted biotransformation unit comprises Nitrosomonas europea.
  • the heterotrophic bio-electrochemical bacteria assisted biotransformation comprises Geobacter sulfurreducens, Shewanella oneidensis, Rhodoferax ferrireducens or a combination thereof.
  • the electricity produced by the bioelectrical energy system generates electrical energy to at least one of the actuators of the system for instance to a pump actuator of the system or to a heat pump that transports heat from the drain to bioreactors of the farming system.
  • the controller of the system furthermore can control the fluid flows between the bioremediation units.
  • the controlled biomass farming system further comprises a system for photocatalytic oxidation of water from or to the aquaculture system.
  • a system for photocatalytic oxidation is particular suitable for preventing unwanted algae growth, for oxidizes the organic matter, for reducing BOD and for destroying unwanted microbiological organisms.
  • a photocatalytic oxidation reactor is used to increase the biosecurity in farming of aquatic animals and crops, to mineralise organic molecules that are presented or fed bacterial condominiums to increase their efficiency of bioenergy production (bioelectricity in the microbial fuel cell or energy rich gas in the biogasification unit) and to mineralise organic molecules that are presented or fed to the crops.
  • a photocatalytic oxidation of the of the fluids loaded with organic matters before it is fed to the bacterial condominiums for biotransformation or bioenergy production moreover provides more stable biotransformation system for bioremediation or redistribution of nutrients and energy with surprisingly less biosystem collapse.
  • Such systems are preferably placed above the aquaculture system in a confined environment (e.g. a greenhouse) for solar driven photocatalytic oxidation or on the roof of the confined environment of the aquaculture system (e.g. a building) to receive solar radiation.
  • the photocatalytic oxidation system can also be incorporated in a UV lamp radiated fluid flow through case or container (combi photocatalytic oxidation / UV lamp) that receives fluid from the aquaculture system (aquatic animal farming system) and/or the photocatalytic bioreactor system (aquatic crop, soilless plants or unicellular crops). After photocatalytic oxidation suspended solids can be removed by mechanical filtration to further reduce BOD, COD, Chemicals and TSS.

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Abstract

L'invention concerne en règle générale l'amélioration de la sécurité biologique et de la stabilité de systèmes d'élevage aquatique intensif à recirculation, par exemple au moyen de capteurs matériels et logiciels et sous contrôle du pH et de l'alcalinité dans un système d'élevage aquatique permettant une normalisation optimale du pH et de l'alcalinité et une élimination de l'azote. Une telle régulation vise à réduire la toxicité, en particulier celle qui est liée à l'azote, pour les organismes vivants, et à empêcher l'effondrement du système biologique. Néanmoins, l'invention concerne plus particulièrement un système de surveillance qui permet de rétablir l'homéostasie du système biologique pour les systèmes d'élevage aquatique intensif à recirculation. Le système selon l'invention qui permet de contrôler le pH se prête particulièrement à une utilisation dans un système d'élevage aquatique nécessitant un pH normal approprié à l'intégration d'un système d'élevage aquatique intensif à recirculation et d'un système de culture hydroponique sans sol. L'invention concerne en règle générale un système de culture régulée à maîtrise de l'énergie dans un espace confiné surveillé et régulé au moyen du système de capteurs susmentionnés, c'est-à-dire dans une configuration à réacteurs et récipients de stockage interconnectés et/ou en communication avec l'espace confiné propre au système de culture. Selon un mode de réalisation spécifique, la maîtrise des flux d'énergie, de biomasse et de molécules dans l'environnement interne des réacteurs, des récipients de stockage et de l'espace confiné propre à ces réacteurs et récipients vise à optimiser le bilan énergétique de la production des organismes aquatiques et des cultures, afin de réduire au minimum la dissipation d'énergie et de matériau dans le milieu ambiant. Plus particulièrement, l'invention concerne un système et un procédé de production de cultures et d'organismes aquatiques sous contrôle amélioré des composants de systèmes, visant à optimiser l'utilisation de la biomasse et de l'énergie par une diminution des pertes.
PCT/BE2010/000044 2009-06-10 2010-06-11 Système d'élevage aquatique biologiquement sûr contrôlé dans un environnement confiné Ceased WO2010142004A2 (fr)

Applications Claiming Priority (12)

Application Number Priority Date Filing Date Title
GB0910007.4 2009-06-10
GB0910007A GB0910007D0 (en) 2009-06-10 2009-06-10 Controlled farming system in a confined enviroment
GB0910178A GB0910178D0 (en) 2009-06-15 2009-06-15 Controlled farming system in a confined environment
GB0910178.3 2009-06-15
GB0911415A GB0911415D0 (en) 2009-07-02 2009-07-02 A biosecure aquatic farming system
GB0911415.8 2009-07-02
US27386909P 2009-08-10 2009-08-10
GB0913882A GB0913882D0 (en) 2009-08-10 2009-08-10 Controlled biosecure aquatic farming system in a confined environment
US61/273,869 2009-08-10
GB0913882.7 2009-08-10
GB0915161.4 2009-08-31
GB0915161A GB0915161D0 (en) 2009-08-31 2009-08-31 Controlled biosecure aquatic farming system in a confined environment

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WO2010142004A2 true WO2010142004A2 (fr) 2010-12-16
WO2010142004A3 WO2010142004A3 (fr) 2011-07-07
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