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    • 专利摘要:
    The present invention provides a method for producing biomass or its derivatives, which consists in converting a sulfur compound into hydrogen sulfide by means of sulfate-reducing microorganisms and then converting said hydrogen sulfide into biomass by means of sulfide-oxidizing bacteria (SOB), said conversions being mediated by means of electron transfer of one or more energy-rich gases. The present invention also provides a bioreactor system for the production of biomass or derivatives thereof.
    公开号:BE1027695B1
    申请号:E20205680
    申请日:2020-10-01
    公开日:2021-12-03
    发明作者:Willy Verstraete
    申请人:Avecom Nv；
    IPC主号:
    专利说明:

    [6] [6].
    In combination with [4], this results in -40 kJ/mol - 21 kJ/mol = -61 kJ/mol. sulfide oxidizing bacteria (SOB). This S-type cycle corresponds to the oxidation of the electron donor (Hz) via H2S by oxygen to water (H2O).
    This second step consists of [4], [5] and [6] equations in reverse, with a total AG= -118 - (-61) = -57 kJ/mol electron equivalent. The total potential energy of the equations remains AG = -118.48 kJ/mol. Thus, the sulfate reductors only get about 50% (57/118) of the potential energy for their biomass production, while sulfide oxidants get the remaining 50%. SOB are known to use mineral nitrogen (ammonium, nitrate) to grow, but some species can also bind dinitrogens and convert them to ammonia and protein nitrogen, respectively. The fact that the powerful catalytic capability of the SRB can be exploited at the expense of only a limited amount of the potential total energy gain is a new finding and underpins this development.
    The difficulty with fermenting gases is that they are generally poorly soluble in water. Nevertheless, the microbial processes must take place in aqueous environmental conditions. A limiting factor is that the gases must be incorporated into the microbial cells to be part of the metabolic pathways. An important feature of this invention is that it mainly targets enzymes selected for their natural processes and to be able to take up gaseous energy compounds with a high rate and high affinity. For example, different types of hydrogenases are described for a wide variety of organisms. According to Cord-Ruwisch et al. 1988 (Table 2), a high affinity for hydrogen with inorganic electron acceptors is demonstrated by Desulfovibrio and Wollinella. The paper by Cord-Ruwisch et al. 1988 shows that for Hz as an electron donor, when sulphate is present, the sulphate-reducing microorganisms reach by far the lowest residual hydrogen content, about 5 ppm, while for methanogens this is about a factor of 3 higher. and homoacetone genes even about 50-fold higher.
    Table 2: Effect on the electron acceptor on the threshold of Hz in different hydrogenophilic bacteria growing on organic substrates of Hz. Values given are means of at least duplicated experiments. Reproducibility was about 50%.
    2 D. fructosovorans disproportionate fumarate to acetate and succinate, so that fumarate as an electron acceptor can become limiting earlier than Ha at the end of growth.
    Electron acceptor oxidized / reduced | Microorganism Substrate | Ha ppm
    | Methanobrevibacter arberphilus [eG | Desulfovibrio vulgaris | Lactate 19 ee | Pose desarteans Essex aaa |E EE [He [9 Gais [ Desulfouibrio desullurleans Essex Jay [8 Caffeic Acid/Hydorcaffeine | Acetobacterium woodii Ha 3 ea ne OO Te more er [Ra 9 It should be noted that with the total energy flow between the micro-organisms, it is conceivable that the conditions created by the SRM are still such that they coexist prevent the occurrence of other species and thus allow end products other than sulphide alone. Thus, it may be possible that the SRM triggers species such as homoacetogenic bacteria and chain extender bacteria to produce metabolites such as short and long chain fatty acids and even waxes.
    In general, the free energy change of the reaction of hydrogen with oxygen to give water is divided by two sets of organisms. The first set are the sulfate reductors, which as anaerobic have a low cell yield of the order of 0.1 g cell dry weight (CDW) per g formed COD-Ha and thus capture a relatively limited amount of CO2 to produce microbial products. The second set is the sulfide oxidizing agents. The latter, when grown autotrophically, have a growth yield typical of all chemoautotrophs, i.e. of the order of 0.1-0.2 g CDW per g of COD-H2S converted. To grow and thus form biomass, they can fix CO: or use organic carbon molecules. To get a detailed picture of the energy efficiency of the S-oxidizers, see Klatt and Polerecky 2015. H2S + 1.65 O2 + 0.65 CO: + 0.35 H2O --> SOa - + 0.35 CH:O + 2H: (in which CH2O represents the biomass formed) It is known that sulfide can also be taken up by phototrophic bacteria which have a high cell yield of about 1.0 g of cellulose formed per g of COD added to their phototrophic metabolism subject (Saer & Blankenship 2017; Garcia et al.2017). However, the need to provide light is a concern in the general application of this process.
    Hence for the chemo-autotroph: 4 mol Hz corresponds to the formation of 1 mol HaS and the latter generates: 0.35x 30 g = 10.5 g biomass CH2O 4x 16 = 64 g COD-Ha generate 10.5 g biomass .
    The theoretical maximum yield of the S-oxidizer is: 10.5 g Dry weight of the cell/64 g COD-Ha = 0.16 g CDW/g COD-Hz input using HaS.
    In fact, under low dissolved oxygen and low sulfide conditions, a yield of 0.13 g CDW per g COD-H:5S was reported by Nelson et al. 1986.
    Of course, synergistic effects, such as the stimulation of aerobic hydrogenotrophs by sulfide, have been described by Suylen et al. 1986 (Table 3). Thus, it is conceivable that co-cultures of sulfate reducing agents and hydrogenotrophs could be developed and could bring technical industrial benefits.
    Table 3: Yield data on Hyphomicrobium EG. Dry weight, protein and total organic carbon of Hyphomicrobium EC mixotrophically grown on methylamine (MA) and increasing concentrations of thio (sulfate) and sulfide (Sz-) at D = 0.035 h-1 . All cultures were MA restricted. Sulphide was not detectable in the MA plus sulfide cultures.
    Substrate Dry Protein Total Organic | Residual thio weight (mg1 °1) carbon (mg1 °') | in culture (mM) (mg1) oma [is (was [ane oa Up oa {| oa 1 | aa 1 | 089 mM LE [4636 (wi 8 ma | sma | In one embodiment of the invention, the conversion reaction takes place in which the sulfate-reducing microorganisms convert sulfur compounds into hydrogen sulfide at a pH value between 4 and 10, preferably between 4 and 9.
    Preferably, the pH at the end of the reaction is generally about 7 to
    8.
    In an Embodiment, the conversion reaction takes place wherein said hydrogen sulfide is subsequently converted into biomass and derivatives by sulfide-oxidizing bacteria at a pH between 3 and 9, preferably between 3.5 and 8.5.
    Preferably, the pH at the end of the reaction converting hydrogen sulfide to biomass and derivatives is generally about 6 to 7.5, or generally 0.5-1 lower than at the end of the reaction converting sulfur compounds into hydrogen sulfide, and could be even lower if the acidic H2SO4 can be produced.
    in an Embodiment of the present invention, said reactions of converting a sulfur compound to hydrogen sulfide and then converting said hydrogen sulfide to biomass and derivatives occur in a bioreactor.
    Various types of bioreactors are known in the art, and one skilled in the art will understand which types can be used for said conversion reactions. As non-limiting examples, the following bioreactors can be used: continuous stirred tank reactor (CSTR), trickle bed reactor (TBR), moving bed bioreactor and/or membrane reactor(s). Also, the method can be applied in a batch reactor or continuous reactor or a combination of a batch reactor and continuous reactor. If the reactor is a continuous culture, the biomasses are preferably retained by a membrane or in granules, flasks or biofilms, optionally with additional materials to immobilize the biomass. The different processes illustrated can be performed in different compartments or in different reactors.
    (Energy-tight) gas mixing in the bioreactor also depends on the type of bioreactor and can be, for example, fine gas bubble mixing under low to high pressure or jet mixing. More information on gas liquid transfer can be obtained from Yasin et al. 2015.
    In one embodiment, said conversion reactions occur in separate compartments of a bioreactor, or separate bioreactors that are in (liquid) communication with each other. As a non-limiting example, the conversion of sulfur compounds to hydrogen sulfide can be carried out in a trickle bed reactor, while the conversion of hydrogen sulfide to biomass can be carried out in a continuous stirred tank reactor (CSTR).
    In another embodiment, said conversion reactions occur in the same compartment of a bioreactor. Preferably, both reactions are still separated from each other, for example by reactor conditions or by diffusion gradients. As a non-limiting example for the latter, both conversion reactions can occur in microbial granular systems or in reactors equipped with membrane systems to keep them separate.
    In one embodiment, the conversion reactions occur under aqueous environmental conditions. "Aqueous environmental conditions" refers to a condition or condition of an environment in which the environment consists of water, and/or in which the environment is thus moist.
    Examples of such environments are process water, manure, compost and sludge.
    In one embodiment, waste material is used as starting material for the conversion reactions of the present method.
    This waste material can be any type of waste, preferably bio-waste, preferably waste material containing a sulfur compound.
    "Bio-waste" or "biodegradable waste" means any organic matter in waste that can be decomposed by micro-organisms and other living beings into carbon dioxide, water, methane or simple organic molecules through composting, aerobic digestion, anaerobic digestion or similar processes.
    It further includes some inorganic materials that can be degraded by bacteria.
    Such materials include gypsum and its products such as plasterboard and other simple organic sulfates that can decompose to produce hydrogen sulfide in anaerobic conditions.
    Other non-exhaustive examples of (bio)waste are soils, compost, waste water, industrial process water, (sewage) sludge, manure, etc. In the embodiment, this waste material is an industrial by-product or industrial co-product.
    Industrial by-products or co-products can be obtained by the industrial processing of biological materials, whereby process water is generated that is rich in organic compounds, such as rich in proteins, carbohydrates and/or fats.
    They may also contain various minerals.
    Non-exhaustive examples of industrial by-products are waste water, process water, sewage sludge from the agro-industry or urban waste water.
    In one Embodiment, an enrichment culture of wastes, as described above or below, is used as a starting material for the conversion reactions of the present method.
    Preferably, these are enrichment cultures of bio-waste material, preferably of waste material containing a sulfur compound.
    Preferably, the waste, biowaste or waste containing a sulfur compound, is waste originating from the agro-industry, such as in the processing of organic matter, biological and preferably vegetable matter.
    This can also come from another industrial process, preferably there is no material in the waste that is inadmissible for the production of feed or food from the biomass; or impermissible for the production of feed and/or food from biomass derivatives, or impermissible for biomass derivatives for use in agricultural, food, cosmetic and/or pharmaceutical applications or as biopolymer. Preference is given to the guarantee that the waste supplied does not contain harmful components that could inhibit or stop the growth of the micro-organisms.
    Additives and/or additives, such as nitrogen (N), phosphorus (P), trace elements and vitamins, can preferably be added to the waste supply, resulting in optimal growth and multiplication of the micro-organisms and maximum production of the desired biomass derivatives. The additives can also apply special growth conditions for the desired microorganisms in terms of surface tension, viscosity and additional metabolic energy input. The temperature of the processed waste in the reactor is preferably brought to a value between 10 and 70°C, preferably between 20 and 50°C, preferably between 25 and 50°C, more preferably between 27 and 40°C more preferably between 27 and 35°C, more preferably between 28 and 32°C and preferably about 30°C. The pH value in the SRM reactor (compartment) in which the sulphate-reducing micro-organisms convert sulfur compounds into hydrogen sulfide is preferably brought to a value between 4 and 10 and more preferably between 4 and 9, and preferably by adding a buffer solution, an acid or a base. The pH of the effluent from this SRM reactor (component) is generally about 7 to 8.
    The pH value in the SOB reactor (component), in which the hydrogen sulfide is subsequently converted into biomass and derivatives with the aid of sulfide-oxidizing bacteria, is preferably adjusted to a value between 3 and 9, preferably between 3.5 and 8.5.
    The pH of the effluent from the said SOB reactor (component) is generally about 6 to 7.5, or generally 0.5-1 lower than that of the SRM bioreactor (component) and could be even lower if the acidic H2SO4 can be produced. In this document, the term "buffer" refers to an aqueous solution of two substances, i.e. buffer substances, which are in a certain equilibrium and adopt a certain pH value. When diluting, adding an acid or a base, this pH will remain almost constant. The disturbance of the equilibrium and the acidity is thus 'buffered'. Buffer solutions preferably consist of an acid/base couple; either an acid and the salt of the conjugate base or a base and the salt of the conjugate acid. Both are preferably weak acids or bases. The method preferably relates to a method for the production of biomass or derivatives thereof from material containing one or more sulfur compounds, and consists of the following steps: - converting said sulfur compound(s) into hydrogen sulphide by means of sulphate-reducing microorganisms under anaerobic conditions; and then - converting obtained hydrogen sulfide into biomass by means of sulfide-oxidizing bacteria under aerobic conditions; wherein said conversions are mediated by energy-rich gases, and said conversions take place in one or more bioreactors. In another of the further embodiments, the hydrogen sulfide conversion reaction occurs in open systems such as soils, compost, activated sludge and other biotic or abiotic fermentation systems; and therefore not in a previously described (bio)reactor. “Fermentation” is the chemical breakdown of a substance by generally micro-organisms, releasing energy. As indicated earlier, it is known that energy-rich gases can serve as electron donors and, by means of biochemical conversions in which these electrons are converted into good electron acceptor compounds, can give rise to the generation of added value from microbial biomass and/or microbial products, using fermentation reactions.
    From the reaction of converting sulfur compounds into hydrogen sulfide, microbial biomass can be collected that is rich in enzymes that can metabolize gaseous energy-rich compounds, microbial biomass that can reduce iron corrosion by advancing iron reduction and densification (Koolie et al. 2019), products such as reduced iron, sulphur, sulfides and polysulfides/short and long chain fatty acids and wax (Wahlen et al. 2009).), phosphates released by sulfides, phosphines, ammonium, amines, amino acids, proteins, chain extending products and/or sulfur granules.
    The fermentation liqueur of the bioreactor (compartment) of the conversion of sulfur compounds into hydrogen sulfide contains reduced compounds, some of which have the ability to influence various microbial processes (aerobic and anaerobic). The result of the densification of the energy-rich gases by means of the sulfate-reducing microorganisms can be used to modify microbial conversions as such in complex matrices such as, for example, soils, activated sludge, digesters, compost and other biotic or abiotic fermentation systems, in preferably using sulfate-oxidizing bacteria.
    From the conversion of hydrogen sulfide to biomass, microbial biomass can be collected which is rich in proteins such as unicellular proteins, polyhydroxyalkanoate (PHA), various forms of extracellular polymeric substances such as sulfated polysaccharides, polyphosphates, compounds specific for thiobacilli such as sulfur (Janssen et al. .2001) or amphipathic membrane vesicles (Knickerbocker et al. 2000; Zhang et al. 2009), extracellular dissolved organic carbon that could inhibit certain classes of bacteria (Wang et al. 2018), waxes and more.
    When the biomass is produced in one or more bioreactors, it is preferably harvested from the reactor in a manner that guarantees the quality of the biomass and derivatives formed.
    Harvesting of the biomass produced is preferably done by settling, flotation, filtration and/or centrifugation to obtain a paste with a density between 1 and 50%, or between 5 and 25% by weight of the dry biomass. It is essential that the paste is protected from contamination by other unwanted micro-organisms and from spoilage of the proteins present. If necessary, a pasteurization or cooling step is provided.
    Preferably, the harvested biomass is post-treated, one step of this post-treatment being to kill the microorganisms without degrading the quality of their cell proteins. This can be done in one of the ways mentioned in the non-exclusive list of pasteurization, steam treatment, irradiation, chemical methods or mechanical stress. During this step or afterwards, the paste can be dried or extruded while retaining the qualitative properties of the derivatives in or on the biomass, after which the derivatives can optionally be processed.
    In a particularly preferred embodiment, said method of the present invention makes the production of sulfated polysaccharides, said method consists of the following steps: - converting sulfur compound(s) into hydrogen sulfide by means of sulfate-reducing microorganisms under anaerobic conditions; and then - converting obtained hydrogen sulfide into biomass by means of sulfide-oxidizing bacteria under aerobic conditions; wherein said conversions are mediated by energy-rich gases, and said conversions take place in one or more bioreactors.
    These sulfated polysaccharides may be selected from the group of heparin, heparan sulfates, fucoidan, glycosaminoglycans, carrageenans, agar, ulvanes, and mixtures thereof.
    In one embodiment, the biomass or derivatives can then be used in feed (fish feed, animal feed, pet food) and/or food for human consumption and/or as slow-release organic fertilizer. Biomass derivatives can have applications in animal feed and/or food, in agricultural, nutritional, cosmetic and/or pharmaceutical applications or as biopolymer.
    The method for the production of biomass or derivatives thereof of the present invention thus contributes to an economically optimal use of food raw materials.
    In another respect, the present invention relates to a bioreactor system for the production of biomass or derivatives thereof, using sulphate-reducing microorganisms and sulfide-oxidizing bacteria, the system comprising: - a first compartment with at least one sulfate-reducing microorganism culture, one gas inlet configured to supply a quantity of energy-rich gas, preferably at least one gas outlet, at least one liquid inlet and at least one liquid outlet; - a second compartment with at least one sulfide-oxidizing bacterial culture.
    In one Embodiment, the first compartment and the second compartment of the system are both separate bioreactors, preferably in fluid communication with each other.
    In another embodiment, the first compartment and the second compartment of the system are separate compartments in the same bioreactor, preferably in fluid communication with each other.
    The liquid inlet of the first compartment can introduce a liquid, preferably a liquid with a sulfur compound, preferably a waste material such as biowaste, most preferably a biowaste consisting of a sulfur compound, into the first compartment. This liquid may then come into contact with the sulphate-reducing micro-organisms.
    Preferably, the first compartment containing the sulfate-reducing microorganisms is configured to operate under anaerobic conditions. The second compartment containing the sulfide-oxidizing microorganisms is preferably configured to function under aerobic conditions.
    The sulfate-reducing microorganisms are able to use the energy-rich gas to convert a sulfur compound into hydrogen sulfide.
    In the second compartment, this hydrogen sulfide can be converted into biomass and derivatives by means of sulfide-oxidizing bacteria. The system consists of one or more harvesting elements, which are capable of harvesting the biomass and derivatives produced. Such harvesting elements may be suitable for harvesting biomass by any method known in the art. Preferably, these elements are suitable for harvesting via settling, flotation, filtration and/or centrifugation.
    Preferably, said harvesting elements are connected to the second compartment of the bioreactor system. Preferably between the second compartment and the harvesting element(s) is a harvesting port, which can be closed and opened during the production of the biomass to harvest the biomass.
    Preferably, the harvested biomass can be collected in a collection tank, which is in communication with the second compartment of the system, preferably connected via said harvesting element(s).
    A person of ordinary skill in the art will appreciate that elements of the method aspect described above are reflected in the system aspect of the invention. Accordingly, all aspects of the present invention are interrelated. All of the features and advantages described in any of the aspects, as described above and below, may relate to any of these aspects, even when described in conjunction with a specific aspect.
    In one embodiment, the system of the present invention is capable of performing the method of one of the embodiments of the invention.
    In one Embodiment, sulfur-reducing microorganisms, archaea or bacteria (SRB: Desulfo, Desulfuro and similar species, but also Geobacter species and other sulfate-reducing substances) are used as industrial organisms for the densification of energy-rich gases, preferably under low or atmospheric reactor conditions, producing energy-rich products. These products are used as such, or they can be further converted in the same or in a second reactor stage by microorganisms serving the aerobic loop of the sulfur cycle (SOB). These sulfur oxidizing bacteria (SOB) act alone or in combination with other organisms and bring forward metabolism yielding valuable products ranging from biomass to biomass derivatives and metabolites such as mineral and organic nitrogen, organic polymers, sulfur and phosphate. Possible embodiments of the invention may be:
    1. Valuable products resulting from the implementation of the combination of the reductive and the oxidative part of the sulfur cycle, such as various biomasses of sulfur-reducing bacteria, sulfur-oxidizing bacteria, combinations of the latter biomasses and metabolic products of these and the last combinations.
    2. Microbial systems employing enzymes with a very high affinity for CO, H 2 and CHa such as are naturally available in the groups of bacteria that can reduce thiosulfate and sulphate respectively by direct or mediated electron transfer and are typically able to reduce the latter convert electron donors into valuable electron dense products such as sulfide, sulfur and organic compounds such as acetate or higher reduced organic compounds such as long chain fatty acids and waxes. The latter compounds can subsequently be upgraded under conditions of higher redox levels in general in combination with CO binding by chemolithotrophic or phototrophic microorganisms, but also by mixotrophic organisms, to products such as microbial biomass and various microbial metabolites such as sulfur, sulphate , protein, exocellular organics, phosphate.
    The main feature: Use of SRB (Desulfo, Desulfuro and similar species, but also Geobacter species and other sulphate reducing agents) as industrial organisms for the densification of energy-rich gases which can then be further converted advantageously in a second phase by micro-organisms that second loop of the sulfur cycle or any other beneficial metabolism.
    3. Microbial systems as described above, present in pure or mixed culture, which can act as pacemakers for other groups of fermentative enzymes and bacteria that upgrade the electron-dense products of the first group to other products, even at low redox conditions. Examples of this are homoacetogens that grow alongside the group of sulphate-reducing bacteria and related species that are able to form waxes in the presence of sufficient energy-rich gas as an electron donor. Another example is aerobic mixotrophs that are able to work in environments with a high sulfide/sulphate content and which produce valuable composites and EPS from soluble COD.
    4. The systems as described above, wherein the actuators, being the micro-organisms, are separated in time or space in order to optimize the quality and/or the production speed of the end products.
    5. The systems as described above, where the actuators are the microorganisms, all grow together in one reactor configuration.
    6. The systems described above operate, but using oxidized nitrogen species (nitrite/nitrate) or light or electrogenesis as drivers for upgrading the intermediates formed by the SRB.
    7. The systems as described above, but where the second step is not performed in the reactor, but in open systems such as soils, compost, activated sludge and other biotic or abiotic fermentation systems.
    8. The combination of SRB as an all-round transformer of different types (solid, dissolved, dispersed, gaseous) metabolizable compounds into products that can then be upgraded to valuable compounds by SOB and associated bacteria.
    9. A new method based on combining the reductive and oxidative loops of the sulfur cycle by using low-value reducing agents such as wastes as input to capture COZ, possibly in combination with organic carbon, in microbial biomass and products that have value.
    10. The systems described above operate under extreme conditions of pH, temperature, light, salinity, redox values, absence of mineral nitrogen.
    An important property could be to produce sulphate-reducing microorganisms coated with sulfide-oxidizing bacteria (dark or phototrophic) and the latter combination are catalysts in the feed (gut, rumen); in the waste conversion, and so on.
    Below, the invention is described by way of non-exhaustive examples which illustrate the invention and which are not intended or intended to be construed to limit the scope of the invention.
    EXAMPLES Example 1: SRBs or a consortium of SRBs, such as Desulfovibrio sp., Desulfotomaculum orientis, Desulfobacterium autotrophicum, Desulfobulbus sp., Desulfotomaculum sp., Desulfosporomusa sp., Desulfosporosinus sp. and/or Thermodesulfovibrio sp. are introduced into a trickle bed reactor in which the waste water seeps over a carrier (eg 200"2 surface/m3 carrier volume) at a velocity close to the flooding rate of the carrier and where the energy dense gas (Hz, CO, CO») countercurrently flows circulates at a rate comparable to the flow rate of the liquid.The reactor temperature range is between 10-60 °C, but preferably around 30 °C. The reactor operates at atmospheric pressure and consumes normal amounts of mixing energy (100-500 W installed per m3 reactor). The latter configuration ensures intensive exposure of the biomass to gas and also ensures adequate biomass retention on the carrier material. Thus, a volume load of 10 g COD-Hz per L reactor per day is achieved when hydrogen is the electron donor and sulfate, the sulfur compound, is the electron acceptor.Typical conditions are a pH in the range of about 4 to about 8.5 and the hydraulic connection age is about 0.5 to about 2 days. The pH is controlled by dosing acid such as dilute H 2 SO 3 . The amount of H:S in the gas phase can be controlled by adjusting the pH in the alkaline range. In addition, by installing a contact interface between the gas and a liquid containing an H:S-reacting reagent, such as, for example, a ferric or ferrous solution, an organic amine that binds the H:S, or a basic solution that captures the H2S, the level of the gaseous H2S can be controlled and the H:S can be harvested as a valuable recovery product.
    Exclusion of undesired species in the sulfur-reducing microorganism reactor system, e.g. methanogens, can be achieved both by working under slightly acidic conditions at the start of the enrichment and subsequently working at the level of H 2 S in the liquid close to the tolerance level of the sulfur-reducing microorganisms, ie about 10 mM.
    For the aerobic conversion of the reduced products, a CSTR reactor is used in which the microorganisms, in particular SOBs or a consortium of SOBs such as Thiobacillus sp., Thiothrix sp., Halothiobacillus sp., Acidithiobacillus sp., Thioalkalivibrio sp.
    Thiomicrospira sp., Thermothrix sp., Chlorobaculum sp. and/or Beggiatoa sp.. receive adequate oxygen (DO levels 0.1-10 mg/L) and are selected for rapid growth and high cell productivity by imposing short cell residence times on the order of 0.5-4 days , usually about 2 days.
    However, other types of reactors can also be used, such as, for example, trickle bed, moving bed bioreactors, membrane reactors.
    The use of other drivers of the upgrading of the products of the SRB can also be used, such as oxidized nitrogen species (nitrite/nitrate) or light.
    Reactor systems operate at atmospheric pressure with normal energy input (100-500 W installed per m3 reactor). Example 2: Two Reactor System Two reactor systems refer to a trickle bed filter for SRBs or a consortium of SRBs such as Desulfovibrio sp., Desulfotomaculum orientis, Desulfobacterium autotrophicum, Desulfobulbus sp., Desulfotomaculum sp., Desulfosporomusa sp.sporosinus, Desulfobacterium. and/or Thermodesulfovibrio sp. followed by aerobic upgrading of energy-rich gases in a continuous stirred tank reactor using SOBs or a consortium of SOBs such as Thiobacillus sp. , Thiothrix sp. , Halothiobacillus sp. , Acidithiobacillus sp. , Thioalkali vibrio sp.
    Thiomicrospira sp. , Thermothrix sp. , Chlorobaculum sp. and/or Beggiatoa sp.
    An energy-rich gas, in particular hydrogen, is dosed under normal atmospheric pressure at a volume load of approximately 10 g chemical oxygen consumption per liter of contact reactor per day at a normal temperature of 30°C.
    The gas is converted into an energy-tight compound (sulphur compound or organic compound compound) which is present in the liquid reactor phase with an efficiency in the range of 95% or more.
    The main product is sulfide, but organic acids and waxes can also be detected at levels of g per L of fermentation broth. Next, the densified form of the initially energy-rich gas is aerobically fermented in a continuously stirred tank reactor, trapping significant amounts of CO: to produce microbial biomass, known as single-cell proteins, and potentially valuable metabolites as well. The products are recovered and represent in chemical oxygen demand equivalents up to a value of approximately 17 %, but possibly higher in case of advantageous co-culture, of the original COD entering in gaseous form (= 83 % on the initial input of the 2 -step system x 0.16 (yield coefficient expressed in dry matter) x 1.3 (conversion of dry matter to COD equivalent) The biomass is rich in valuable amino acids and contains other valuable compounds such as, but not limited to, polyhydroxyalkanoates, polyphosphates and various forms of extracellular polymeric substances such as sulfated polysaccharides The residual liquid from the SOB process can be recycled to the first reactor Example 3: One-reactor system The sulfur compound (thio(sulfate)) reduces the reaction and subsequent use of the products of the SRB (H:S, optionally organic acids and/or waxes) as in example 1 or 2 are carried out in the same reactor system, separated by the reactor conditions or by diffusion gradients. In the latter case, both reactions can occur in microbial bead systems or in reactors equipped with membrane systems to keep them separate.
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    权利要求:
    Claims (15)
    [1]
    1. Method for the production of biomass or its derivatives, consisting of converting a sulfur compound into hydrogen sulfide by means of sulphate-reducing microorganisms and then converting this hydrogen sulfide into biomass by means of sulfide-oxidizing bacteria (SOB), these conversions are mediated by electron transfer from one or more energy-rich gases.
    [2]
    The method of claim 1, wherein said energy-rich gases are selected from hydrogen, CO, H:S, PH 3 , CH 4 , volatile organic compounds, gases produced by fermentation, and mixtures of such gases.
    [3]
    The method of claims 1 to 2, wherein said energy-rich gas is hydrogen.
    [4]
    A method according to any one of the preceding claims, wherein said biomass derivatives are selected from proteins, unicellular proteins, polyhydroxybutyrate and analogs, polyphosphates, carbohydrates, cell wall components, preferably exopolysaccharides, lipids, extracellular dissolved organic carbons and metabolites.
    [5]
    A method according to any one of the preceding claims, wherein said sulfate-reducing microorganisms are selected from sulfate-reducing bacteria (SRB) and sulfate-reducing archaea (SRA).
    [6]
    A method according to any one of the preceding claims, wherein said conversion of sulphate to hydrogen sulfide takes place under anaerobic conditions.
    [7]
    A method according to any one of the preceding claims, wherein the reduction of said sulfur compound takes place in the presence of a carbon dioxide source.
    [8]
    A method according to any one of the preceding claims, wherein said sulfur compound is sulfate or thiosulfate.
    [9]
    A method according to any one of the preceding claims, wherein said conversion of hydrogen sulfide to biomass or derivatives takes place under aerobic conditions.
    [10]
    A method according to any one of the preceding claims, wherein said conversion reactions take place in a bioreactor.
    [11]
    A method according to claim 10, wherein said conversion reactions occur in separate compartments of a bioreactor, or separate bioreactors.
    [12]
    A method according to any one of claims 1 to 9, wherein the hydrogen sulfide conversion reaction takes place in open systems such as soils, compost, activated sludge and other biotic or abiotic fermentation systems.
    [13]
    A method according to any one of the preceding claims, wherein waste material is used as starting material for the conversion reactions, preferably bio-waste.
    [14]
    14. The method for producing biomass or derivatives thereof from material containing one or more sulfur compounds comprises the following steps: - converting said sulfur compound(s) into hydrogen sulfide by means of sulfate-reducing microorganisms under anaerobic conditions; and subsequently - converting obtained hydrogen sulfide into biomass by means of sulfide-oxidizing bacteria under aerobic conditions; wherein said conversions are mediated by energy-rich gases, and said conversions take place in one or more bioreactors.
    [15]
    15. A bioreactor system for the production of biomass or its derivatives, using sulphate-reducing micro-organisms and sulphide-oxidizing bacteria, the system comprising: - a first compartment with at least one sulphate-reducing micro-organism culture, one gas inlet configured to deliver a quantity of energy-rich gas, preferably at least one gas outlet, at least one liquid inlet and at least one liquid outlet; - a second compartment with at least one sulfide-oxidizing bacterial culture.
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    同族专利:
    公开号 | 公开日
    EP3800274A1|2021-04-07|
    BE1027695A1|2021-05-17|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US4666852A|1982-07-26|1987-05-19|Institute Of Gas Technology|Photosynthetic bioconversion sulfur removal|
    WO2014200598A2|2013-03-14|2014-12-18|The University Of Wyoming Research Corporation|Conversion of carbon dioxide utilizing chemoautotrophic microorganisms systems and methods|
    法律状态:
    2022-01-19| FG| Patent granted|Effective date: 20211203 |
    优先权:
    申请号 | 申请日 | 专利标题
    BE201905647|2019-10-01|
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