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WO2008099252A1 - Conversion en méthane, par digestion anaérobie associée avec des biomasses, du co2 capturé à partir de systèmes de combustion ou d'autres procédés industriels - Google Patents

Conversion en méthane, par digestion anaérobie associée avec des biomasses, du co2 capturé à partir de systèmes de combustion ou d'autres procédés industriels Download PDF

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WO2008099252A1
WO2008099252A1 PCT/IB2008/000288 IB2008000288W WO2008099252A1 WO 2008099252 A1 WO2008099252 A1 WO 2008099252A1 IB 2008000288 W IB2008000288 W IB 2008000288W WO 2008099252 A1 WO2008099252 A1 WO 2008099252A1
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stage
process according
biomasses
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phase
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Cesarino Salomoni
Enrico Petazzoni
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BUSI IMPIANTI SpA
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/84—Biological processes
    • 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
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • C12M43/04—Bioreactors or fermenters combined with combustion devices or plants, e.g. for carbon dioxide removal
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/09—Means for pre-treatment of biological substances by enzymatic treatment
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • C12P5/023—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/95—Specific microorganisms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/50—Carbon dioxide
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/20—Capture or disposal of greenhouse gases of methane
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/59—Biological synthesis; Biological purification

Definitions

  • biomass transformed into biogas could also provide the same result, but in such a case the above constraints would be complemented by another one related to the limits imposed by an anaerobic digestion process still lacking those technologic innovations which would make it really effective. The same can be said for the present state of development of pyrolisis and syngas.
  • this renewable energy source can be alternative to fossil sources when used within the same plant where the capture/transformation processes are carried out, or it can be complementary to fossil sources when, after conversion, it is sent to domestic users or small to medium businesses, or for automotive use, and in general to users who do not carry out the gas capture process.
  • this approach offers a sharp reduction in the CO 2 being present in the atmosphere, while at the same time overcoming any technical or regulatory obstacles related to long-term sequestration and implying minimized costs as well as maximized profits.
  • its possible use along with fossil sources, especially coal promotes its generalized development and application. More particularly, when viewing this approach as a basis for producing energy in general without being limited to large plants, and placing it into the most appropriate context, i.e.
  • the methane thus produced can be used at the single digesters themselves or, when all digesters are connected to an integrated gas distribution network, it may also be used for supplying large or very large plants, as would never be possible by using solid combustible biomass due to plain physical reasons.
  • Patent application no. WO2006108532 also proposes, though in a laborious or hardly feasible manner, to adjust the pH value in the anaerobic system by using bicarbonate obtained during the capture operations in addition to CO 2 .
  • the pH value adjustment is carried out in a much simpler way by using CO 2 only and/or by regulating the substrate flows.
  • the limitations of this approach are apparent: two borderline cases can be distinguished.
  • the first case refers to a deep geologic formation with no further specifications except those related to CO 2 containment, conditions which are not themselves frequently fulfilled: in this case, in addition to the morphology of these articulated, extended and almost inaccessible cavities being substantially unknown, one must also take into consideration the presence of any pits, vaults, gradients creating humid and dry areas, rocks rich in favourable or unfavourable bacteria, etc.; such conditions, which include a great variety of microenvironments, will imply a huge waste of nutritional substances and bacteria, as well as a large quantity of unconverted CO 2 and very long process times.
  • the main and general object of the present invention is to provide a new method for converting into methane the CO 2 being present in a high CO 2 content flow generally derived from a low CO 2 concentration emission, said CO 2 being typically previously captured from combustion systems or other plants used for industrial processes. Said object is achieved through the process incorporating the features set out in the appended claims, which are intended as an integral part of the present description. According to further aspects, the present invention also relates to plants adapted to carry out said process.
  • CO 2 is combined according to predefined ratios with suitably formulated and pre-treated biomass in order to subject the resulting combination to an optimized anaerobic fermentation process based on specially selected bacterial populations.
  • CO 2 is captured and separated from a flue gas flow coming in particular from combustion chambers of fixed plants such as, for example, incinerators, electric or thermal power plants, steel mills, cement works, glassworks, ceramics works, oil refineries, etc. (reference is made herein to the most common type of combustion, i.e. the one which uses air as an oxidant), or from other industrial processes.
  • Said CO 2 is then converted into methane during an industrial multi-stage anaerobic digestion process which uses specialized bacterial populations of acetogenic and methanogenic microorganisms kept at high density and fed with nutritional and alcoholic substrates as well as stimulators.
  • Said substrates are obtained from cocktails of matrices selected among a range which comprises, preferably in multiple combinations, ad hoc agricultural and aquatic cultures, garden and forest prunings, slaughter house wastes, agricultural and agro-industrial wastes, animal sewage, depuration sludge, organic fraction of solid urban refuse, and agro-industrial semi-finished products, all of which are specifically pre-treated according to industrial and/or agro-industrial methods.
  • the proposed process turns out to be more effective and require lower investment and running costs compared with prior-art processes; the term "prior art” is used herein to designate any of the best existing processes for anaerobic CO 2 conversion into methane among the following: the process is started from flows of flue gases produced by the combustion of gasified coal (i.e. combustion in the absence of N 2 ), by using expensive industrial substrates in a low-efficiency single-stage system in the presence of unselected bacterial populations (DE patent no.
  • the above-described drawbacks are overcome through a process which essentially comprises four phases (see claim 1) and through a suitable system (see claim 30) which combines four modules in an integrated manner.
  • the process and the system comprise the following modules/phases:
  • the first module/phase comprises the following stages:
  • the second module/phase comprises different combinations of the following stages depending on the nature of the available matrices:
  • the third module/phase comprises different combinations of the following stages depending on the nature of the available matrices;
  • the fourth module/phase comprises the following stages:
  • the adjustment of the pH value in the fermentation reactor and in the methane production reactor is carried out by using CO 2 captured in the first module/phase as an exclusive chemical agent, and/or by regulating the substrate flows to and/or among the reactors; due to the stability of this process, no bicarbonate needs to be used, whether produced in the first module/phase or supplied by an external source.
  • mixed bacterial populations it is meant a culture of two or more aceto genie and methanogenic anaerobic microbial populations which may belong either to the same or different genera as well as to the same or different species, as properly exemplified, as far as acetogenic populations are concerned, by Butyribacterium sp., Eubacterium sp, Clostridium sp., Ruminococcus sp. and Morella sp., or, as far as methanogenic populations are concerned, by Methanosarcina sp., Methanosaeta sp., Methano coccus sp.
  • the first module/phase can be provided in many different ways, some of which are extremely simple and/or already known in the art.
  • a characteristic feature of the invention is the elimination, in the first module/phase, of the need to operate in very caustic conditions while maintaining a quick and efficient CO 2 capture by means of a combination of an absorption process and a chemical reaction in the presence of a solution of alkaline metals supplemented by an immobilized biocatalyst, i.e. carbonic anhydrase, which promotes CO 2 hydration.
  • the advantages of this new process are low investment and running costs and better environmental safety.
  • This problem can be solved, for example, by retrofitting the CO 2 capture module/phase to plants used for removing traditional pollutants (NOx, particulate, SOx) and by using temperatures which may be compatible with the management of the chemical and biotechnological processes contemplated in the present invention.
  • the advantage so achieved is that, in such a condition, the biocatalyst and the alkaline agent last for a long time and thus their cost per ton of captured CO 2 is correspondingly reduced.
  • Said processes comprise different combinations of biological and/or chemical-physical stages among those listed above in the description of the second module, as are needed from time to time depending on the nature of the available vegetable and animal matrices (fresh, ensiled or semi-manufactured). This approach, based on a wide range of raw matrices and on various specific storage and treatment methods, allows to overcome any cost and seasonal problems which are typical of these tasks.
  • the wide range of raw matrices and the various specific treatments to which said matrices are subjected allow to minimize the costs of these tasks.
  • these features allow to solve the above- mentioned seasonal problems which, as far as the alcoholic hydrolyzed product is concerned, are already limited by the possibility of storing said product as a final product of this module/phase. It should also be added that some of the processes mentioned herein take place at farms' level, where costs are lower.
  • this object is achieved by the present invention through a new process which uses large quantities of CO 2 from the first module/phase and nutritional and alcoholic substrates obtained in the second and third modules/phases, thus specializing the mixed populations of microorganisms being present in or added to the anaerobic digestion system and providing an environmental conditioning/selection thereof.
  • These bacterial populations are capable of providing a high rate of conversion of CO 2 into acetates during the acetogenesis stage and a high rate of conversion of acetates, CO 2 and hydrogen into methane during the methano genesis stage.
  • the first version which can be defined as "closed loop"
  • substantially all of the CO 2 produced and captured in a fixed methane combustion plant is transformed into methane through processes fed with biomasses (which supplies the required energy), thus generating a quantity of methane which is substantially equal to the quantity of methane which has to be burnt in that very same plant.
  • the CO 2 produced in a fixed plant using any kind of fossil fuel is transformed into methane through a biochemical biomass fermentation process, and said methane is then sent to decentralized users not involved in CO 2 capture.
  • the integrated technologic components proposed herein represent an engineered system wherein dimensions, speeds, costs and process control are optimized both separately and as a whole.
  • Fig. 1 represents a schematic basic configuration of an integrated process according to the present invention.
  • Fig. 2 represents a schematic basic configuration of the first module/phase of the process of Fig. 1 : the drawing shows the functional structure and the equipment used.
  • Fig. 3 represents a schematic basic configuration of the second module/phase of the process of Fig. 1 : the drawing shows the functional structure and the equipment used.
  • Fig. 4 represents a schematic basic configuration of the third module/phase of the process of Fig. 1 : the drawing shows the functional structure and the equipment used.
  • Fig. 5 represents a schematic basic configuration of the fourth module/phase of the process of Fig. 1 : the drawing shows the functional structure and the equipment used.
  • Fig. 1 shows a diagram of a method for converting into methane CO 2 previously captured from combustion systems or other industrial processes.
  • the CO 2 is combined according to predefined ratios with suitably formulated and pre-treated biomasses in order to subject the resulting combination to an optimized anaerobic fermentation process based on specially selected bacterial populations.
  • the process consists of four integrated modules/phases: the first one is called “gaseous emission treatment”, the second one is called “nutritional substrate preparation”, the third one is called “alcoholic substrate preparation”, and the fourth one is called “optimized anaerobic fermentation and methane production”.
  • the object of capturing the CO 2 contained, in most cases, in a flue gas and of generating a concentrated CO 2 flow at low investment and running costs is attained, for example, in the first module/phase, which represents an optimal way to implement this part of the invention, through a process illustrated schematically in Fig. 2 and described below.
  • the embodiment example described herein relates to a flue gas produced by sludge or urban waste incinerators, gas or coal thermal and/or electric power plants, etc. and subjected to removal of traditional pollutants (NOx, particulate, SOx); if the gas has a low CO 2 concentration and a typical volumetric concentration between 3% and 20% of the total flue gas volume, the optional first module/phase can be useful; if the flue gas is already a concentrated CO 2 flow, said module/phase has no purpose and can be omitted.
  • the removal treatments bring the inflowing gas temperature to values ranging between 30 and 8O 0 C, which are compatible with the management of the chemical and biotechnological processes contemplated in the present invention.
  • the CO 2 rich flue gas enters into the extraction zone, which consists of a contact and dissolution reactor (IA), through a line (1) directly connected to the emission flow.
  • IA contact and dissolution reactor
  • the contact between the gas and the alkaline solution of sodium minerals and between the latter, enriched with CO 2 , and carbonic anhydrase may take place in whatever reactor designed for gas/liquid reactions and capable of ensuring that the biocatalyst be kept at all times in liquid phase or hydrated.
  • the reactor has inlet and outlet ports for the gaseous emission flow; it also has an inlet port for the capture solution coming through line (2) and an outlet port, located at the bottom of the reactor, where the resulting solution is collected to be discharged through an exit line (3).
  • the capture reactor is so equipped as to make it possible to control the two separate flows, i.e. the gaseous emission flow and the capture solution flow.
  • the carbonic anhydrase enzyme is immobilized, according to methods and onto supports known in the art.
  • the alkaline solution of sodium minerals flowing into the reactor has a pH value between 8.3 and 9.6.
  • Sodium carbonate in the alkaline solution reacts with the stoichiometric quantities of the species resulting from CO 2 dissolution, further augmenting in this way the concentration of bicarbonate ions, and consequently their own input into the subsequent precipitation reactor.
  • the obtained solution has a pH value between 7.5 and 8.3.
  • the temperature in the capture reactor may vary between 35 and 75 0 C.
  • One thing to remember is that the CO 2 dissolution rate into water is higher at low temperatures.
  • the sodium carbonate reaction rate with the species resulting from CO 2 dissolution to form bicarbonate is lower at low temperatures. Therefore the alkaline solution temperature must be maintained at such a level as to obtain CO 2 dissolution and hydration in line with the desired rate of reaction between sodium carbonate and the species formed as a result of CO 2 dissolution. Temperature is maintained below 75°C and preferably in the range between 35°C and 6O 0 C.
  • the gas outflowing from the capture reactor is sent to a demister (IB) and then released into the environment.
  • IB demister
  • the solution containing bicarbonate and other species resulting from CO 2 dissolution and from their reactions with sodium carbonate is first collected in the first reactor and then transferred to a second precipitation reactor (1 C), where solid sodium carbonate is added to obtain an oversaturated sodium bicarbonate solution.
  • This second reactor may consist of any type of container known in the art which, in terms of dimensions and equipment, can contain and maintain the solution in suspension as long as it takes to fully convert all the added sodium carbonate into sodium bicarbonate.
  • the pH value is controlled by increasing or decreasing the pH value of the collected solution, i.e. by dissolving and hydrating a smaller or larger quantity of CO 2 .
  • the pH value is controlled by increasing or decreasing the quantity of solid sodium carbonate introduced into the solution.
  • the pH value can be controlled by introducing into the solution protons or substances which may affect it.
  • the best pressure and temperature conditions are maintained in order to obtain sodium, bicarbonate precipitate.
  • the solution is agitated until almost all of the added sodium carbonate is converted into precipitated sodium bicarbonate. "Almost all” is to be understood as any value between 90 and 100% of sodium carbonate added to the solution.
  • the pH value of the solution never falls below 9, being preferably between 9 and 9.6.
  • the precipitation reactor temperature may vary between 35 and 60°C.
  • the solution collected in the precipitation reactor, which contains suspended solid sodium bicarbonate is transferred to an apparatus (ID) known in the art designed for solid/liquid separation.
  • ID apparatus
  • IE storage unit
  • the solid bicarbonate obtained by separation is transferred through line (5) to a subsequent regeneration unit (IF), where CO 2 and steam are released by calcination at a constant temperature ranging between 120 and 140 0 C.
  • IF regeneration unit
  • the following endothermic reaction takes place inside the regeneration reactor:
  • the carbonate (Na 2 CO 3 ) produced in the regeneration unit is recycled as a reagent into the precipitation reactor through line (6), while the gas (CO 2 + H 2 O) is sent through line (7) to an apparatus (IG) for separation and concentration of gaseous CO 2 .
  • the steam is condensed and the released and separated CO 2 is compressed and stored in a container (IH) in view of its further uses in the second "nutritional substrate preparation" module/phase and in the fourth "optimized anaerobic fermentation” module/phase for methane conversion.
  • the object of the industrial production of optimal nutritional substrates for anaerobic microorganisms from selected cocktails of vegetable and animal matrices and specific treatment processes, both of which are essential components of a low-cost solution is achieved in the second module/phase through the process diagrammatically illustrated in Fig. 3 and described below.
  • the second module/phase comprises different combinations of the pre- treatment stages included in said module/phase as needed from time to time depending on the nature of the available matrices capable of producing optimal substrates which can readily be used by anaerobic bacteria.
  • Fig. 3 there is a first stage called “supply and storage", wherein fresh, ensiled or semi-finished vegetable and animal matrices selected among a range including ad hoc agricultural and aquatic cultures (e.g. cereals, forages and macroalgae), agricultural and agro -industrial wastes, slaughter house wastes, animal sewage, depuration sludge, organic fraction of solid urban refuse, agro-industrial semifinished products, etc. enter through line (8).
  • ad hoc agricultural and aquatic cultures e.g. cereals, forages and macroalgae
  • agricultural and agro -industrial wastes e.g. cereals, forages and macroalgae
  • slaughter house wastes e.g., animal sewage, depuration sludge, organic fraction of solid urban refuse, agro-industrial semifinished products, etc. enter through line (8).
  • the raw matrices selected for feeding the second stage have specific distinctive features; in particular, they may vary considerably as to qualitative and quantitative composition, homogeneity, fluid dynamics and biodegradability; some matrices may contain 1% of total solids, while other matrices may contain over 40%; the organic material content may vary between 70% and 95% of total solids; the nutritional ratio (C:N) may vary between 6 and 500; the distribution of organic macromolecules such as carbohydrates, proteins and lipids may also change substantially among the different matrices; all of these features are extremely important, since the composition and high degradability of said matrices, obtained during the various pre-treatments provided, will lead to the formation of all the fundamental components making up the main substrate readily available to bacteria in the fourth module/phase.
  • the storage method contemplated by this invention is ensilage (at farms), a process traditionally used for preserving forage for animal feeding.
  • soluble carbohydrates contained in vegetable organic materials undergo lactic acid fermentation, which causes the pH value to drop and inhibits the growth of undesired microorganisms; in addition, lactic acid fermentation can be controlled through acidification or else by inoculating bacterial populations or enzymes in order to degrade the cellular wall of vegetable cells as well and to release soluble intracellular carbohydrates to be used for lactic acid fermentation.
  • Ensilage therefore allows to obtain intermediate products for the formulation of optimal cocktails as well as to partially degrade any structural polysaccharides contained in the vegetable material.
  • Ensilage storage which may last two to six months, can thus be considered as a pre-treatment also ensuring a more appropriate utilization of the stored matrix within the overall pre-treatment process of the second module/phase.
  • the formulations of the optimal cocktails are obtained on the basis of the parameters and the respective ranges listed below: a) the particle size of the solids being present in the cocktails is preferably in the range between 0.5 and 3 cm, more preferably between 0.5 cm and 1.5 cm; b) the total solid content is preferably in the range between 10 and 35%, more preferably between 10 and 20%; c) the volatile solid content is preferably between 70 and 95% of total solids, more preferably between 85 and 95 % of total solids; d) as to the distribution of organic macromolecules, the carbohydrate content is preferably between 40 and 60% of total solids, raw protein content is preferably between 20 and 40% of total solids, raw lipid content is preferably between 10 and 30% of total solids; e) as to main minerals (e.g.
  • the optimal biomasses cocktails formulated according to the desired characteristics of homogeneity, size, solid content, volatile solid content, general nutritional ratio, and carbohydrate, lipid, macroelement and microelement composition are wholly transferred through line (10) into the reaction container (2F) of the thermo-cheniical and pressure treatment stage; alternatively, in the event that distinct treatments must be carried out for the different cocktail components, only a portion of said cocktails will be sent through line (10) to the reaction container (2F), while the remaining portion will be sent directly to the enzymatic hydrolysis stage (2H) through line (11) without going through the thermo-chemical and pressure treatment stage.
  • the cocktails undergo a thermal pre-treatment by direct or indirect heating or a combination thereof, according to methods known in the art, in the range between 36 and 160°C; when the desired temperature has been reached, the reaction container (2F) is pressurized by injecting gaseous CO 2 supplied by the first module/phase through line (12) up to a level preferably comprised between 3 and 50 bar, more preferably between 3 and 12 bar, for a variable time preferably between 5' and 1 hour, more preferably between 5' and 30'; when the programmed time has elapsed, the reaction container (2F) is slowly depressurized down to a level preferably comprised between 3 and 5 bar, more preferably between 3 and 4 bar; the treated cocktails in the reactor (2F) are thus wholly transferred by sending the gas outputted from the head of the reaction container (2F) to the fourth module/phase through line (13), by means of a quick and complete depressurization through line (14), which connects the bottom of the reaction container (2F) to the expansion container (2G), which
  • the described treatment allows to obtain a partial break down of the cellular wall of the cocktail constituents, as well as to obtain a safe hygienization thereof (in accordance with the health provisions contained in EC Animal By-Product Regulation No. 1774 /2002) and an increase in the biodegradability of the matrices, resulting in the latter being more susceptible to the subsequent acid enzymatic hydrolysis.
  • Those cocktails which have been subjected to the thermo-chemical and pressure treatment are transferred through line (16) to the container (2H) in the enzymatic hydrolysis stage.
  • the enzymatic hydrolysis of the nutritional cocktails is conducted in the container (2H) within an environment saturated with CO 2 coming from the first module/phase through line (17); the CO 2 partial pressure is so adjusted at this stage as to keep the pH value of the cocktails preferably in the range between 3 and 6, more preferably between 4 and 5.5, while temperature is kept preferably in the range between 15 and 60°C, more preferably between 45 and 55 0 C.
  • Multi-enzymatic complexes are introduced into the container through line (18), while mixed hydrolytic and cellulolitic bacterial populations, which may belong either to the same or different genera as well as to the same or different species, as properly exemplified, among others, by Clostridium sp., Pseudomonas sp. and Bacillus sp., are introduced through line (19) together with any necessary integrating stimulators, catalysts and nutritional factors.
  • the acid hydrolyzed effluent obtained through enzymatic hydrolysis in sent to the apparatus (21), dedicated to the separation of solids, substrate particles and microorganism particles, by means of any of the various techniques known in the art.
  • the solid component separated from the liquid component is partly recirculated through line (21), whereas the other portion that cannot be used for this purpose is sent through line (22) to an industrial application or to the third module/phase for further treatment; on the other hand, the liquid component is sent to the fourth module/phase through line (23).
  • the hydrolysis stage attains the result of significantly speeding up the conversion of polymers (polysaccharides, proteins, nucleic acids and lipids) into oligomers and monomers (sugars, amino-acids, purines, pyrimidines, fatty acids, glycerol, etc.) and of making the nutritional substances being present in the liquid hydrolyzed product readily available to and usable by the bacterial populations of the fourth module/phase.
  • polymers polysaccharides, proteins, nucleic acids and lipids
  • oligomers and monomers sucrose, amino-acids, purines, pyrimidines, fatty acids, glycerol, etc.
  • the object of an agro -industrial production of optimal alcoholic substrates for anaerobic microorganisms from high carbohydrate content vegetable matrices and specific treatment processes, both of which are essential components of a low-cost solution is achieved in the third module/phase through the process diagrammatically illustrated in Fig. 4 and described below.
  • the third module/phase comprises different combinations of the pre- treatment stages included in said module/phase as needed from time to time depending on the nature of the available matrices capable of producing alcoholic substrates containing different types and/or combinations of alcohol, as properly exemplified, among others, by ethanol, methanol and butanol, all of which can readily be used by anaerobic bacteria.
  • a first stage called “supply and storage” is supplied with matrices consisting of fresh, ensiled or semi-finished vegetable material having the desired energetic characteristics of high carbohydrate content (sugars, starch, cellulose, hemicellulose), selected among a range preferably comprising, but not limited to, ad hoc agricultural and aquatic cultures, agricultural, garden, forest, agro-industrial and industrial wastes, agro-industrial semi-finished products, etc.
  • the raw matrices used for feeding this module/phase may have distinct features while still maintaining the basic characteristic of a high carbohydrate content.
  • high carbohydrate content matrices it is meant a total value of the different components (sugars, starch, cellulose, hemicellulose) preferably comprised between 50 and 85% of the matrix dry weight, more preferably between 70 and 85% of the matrix dry weight.
  • matrices rich in carbohydrates mainly consisting of structural substances having a high molecular weight, such as hemicellulose, cellulose and lignin, which enter the container (3A) through line (24), will undergo the whole series of treatments executable in the module/phase
  • matrices rich in carbohydrates consisting of substances having a high molecular weight, such as cellulose, hemicellulose and other polysaccharides, but a limited quantity of lignin, which enter the container (3B) through line (25) will only go through the saccharification and alcoholic fermentation processes
  • matrices rich in carbohydrates consisting almost only of simple sugars, which enter the container (3C) through line (26) will only go through the final alcoholic fermentation stage.
  • the different matrices selected from time to time are thus stored according to the type thereof in containers designated (3 A, 3B, 3C), and are then taken and sent through lines (27, 28 and 29), respectively, to the second stage called "detailed preparation" in containers designated (3D, 3E, 3F), respectively, wherein they are made homogeneous in size and brought to the desired solid content.
  • Matrices rich in carbohydrates prevalently consisting of structural substances having a high molecular weight, such as hemicellulose, cellulose and lignin, are transferred through line (30) from the container (3D) to stage (3G), wherein a hydrolysis process is carried out by means of ligninolitic multi-enzymatic complexes (mainly phenoloxidasi) introduced through line (31) and/or by inoculating mixed populations of microorganisms, which may belong either to the same or different genera as well as to the same or different species, as properly exemplified, among others, by Basidiomycetes, Pseudomonas sp.
  • ligninolitic multi-enzymatic complexes mainly phenoloxidasi
  • Saccharification is carried out through multi- enzymatic ⁇ complexes (cellulase) introduced through line (35) and/or by means of a plurality of populations of microorganisms, which may belong either to the same or different genera as well as to the same or different species, as properly exemplified, among others, by Clostridium sp., Trichoderma sp. and Pseudomonas sp., which are introduced through line (36) together with any necessary integrating stimulators, catalysts and nutritional factors for the purpose of improving the efficiency of the production of oligosaccharides and free sugars.
  • stage (3H) The sacchariferous hydrolyzed product outputted from stage (3H) is then transferred to the alcoholic fermentation stage (31) through line (37), together with the matrices rich in carbohydrates prevalently consisting of oligosaccharides and free sugars coming from stage (3F) through line (38).
  • Alcoholic fermentation is carried out by means of populations of microorganisms which may belong either to the same or different genera as well as to the same or different species, as properly exemplified, among others, by Saccaromyces sp., Zymomonas sp.
  • the effluent from stage (31) is sent through line (40) to the solid separation apparatus (3L), mainly consisting of ligno-cellulosic materials and microorganisms; from this apparatus, the latter are recirculated and/or sent to an industrial application through line (41), while the alcohol-rich liquid component is sent to the fourth module/phase through line (42).
  • the object of converting CO 2 into methane is attained in the fourth module/phase through the process diagrammatically illustrated in Fig. 5 and described below.
  • the first stage of the fourth module/phase comprises the distribution of CO 2 supplied by the storage container (IH) of the first module/phase through line (43), of nutritional hydrolyzed product supplied by the apparatus (21) of the second module/phase through line (23), of alcoholic hydrolyzed product supplied by the apparatus (3L) of the third module/phase through line (42), as well as of any integrating stimulators, catalysts and nutritional factors introduced through line (44), to the fermentation reactor (4A), thereby providing the microorganism cultures being present in or supplied to the reactor (4A) through line (45) with all necessary substrates and components readily available for the implementation of an extremely fast fermentation process, thus allowing for a low-cost production of large quantities of acetates from CO 2 .
  • the optimized nutritional substrate is supplied into the reactor (4A) on a daily basis, according to a direct relationship, expressed in terms of weight, with the bacterial population biomass being present at that time, said ratio being preferably in the range between 1 : 8 and 1 :25, more preferably between 1 :12 and 1 :25; CO 2 is supplied daily up to the maximum total load that can be used by the acetogenic populations being present therein; the alcoholic substrate is supplied daily up to the maximum total load that can stimulate the desired oxido-reductive reactions in the fermentation reactor.
  • the fermentation reactor (4A) can be any reactor known in the art designed to sustain the growth of suspended bacteria or bacteria fixed to inert supports and capable, in terms of dimensions and equipment, of containing and maintaining the exogenously introduced CO 2 in solution or mixed with the bacterial culture medium for a time long enough to allow substantially all of the exogenously introduced CO 2 to be converted into acetates.
  • the selected mixed acetogenic bacterial populations being present in and/or supplied to the reactor (4A) may belong to the same or different genera as well as to the same or different species, as properly exemplified, among others, by Butyribacterium sp., Eubacterium sp, Clostridium sp., Ruminococcus sp. and Morella sp..
  • Acetogenic fermentation is obtained at a density of said mixed bacterial populations, expressed in terms of dry weight, preferably in the range between 6 and 12%, more preferably between 9 and 12%; environmental conditions are kept constant and are defined by a pH value preferably in the range between 4.5 and 6.3, more preferably between 5 and 6, and by a temperature preferably between 30 and 80 °C, more preferably between 30 and 60 °C.
  • the pH value of the reactor must not rise over 6.3, so that hydrogenotrophic methano genesis stays blocked, thus preventing hydrogen from being consumed by methanogenic microorganisms, while on the other hand it must not drop below 4.5 in order to sustain a competitive growth of acetogenic bacteria.
  • acetogenic populations are more resistant to ammonia than methanogenic ones, it is also possible to use higher nitrogen content substrates, in particular with ammonia concentrations over 1.2 grams per litre.
  • the effluent from the acetogenic fermenter (4A) is sent through line (46) to the apparatus (4B) for the separation of substrate particles and microorganisms being present therein, which may use any of the various techniques known in the art; after having been collected, these solid materials are recirculated through line (47) into the reactor itself or else they are recirculated for degradation to the head of the module/phase 2, whereas the liquid component is conveyed through line (48) to the next methane production digester (4C); the gas in the upper part of the fermentation reactor (4A), which contains unused undissolved CO 2 , is also collected in the upper part of the same reactor as a mixed gas (CO 2 , H 2 , other) and sent to a storage container (4D) through line (49), after which it is recirculated into the same fermentation reactor still by using line (49) or else conveyed to the lower part of the methane production digester (4C) through line (50).
  • a mixed gas CO 2 , H 2 , other
  • the output of the methane production reactor (4C) therefore comprises both the distribution of a high acetate content liquid substrate through line (48), integrated through line (51) with any necessary stimulators, catalysts and nutritional factors, and the distribution of a gaseous substrate which combines the acetate supply with the hydrogen and CO 2 supply being present in the gas itself, thereby ensuring an efficient production of a large quantity of methane from said substrates.
  • all the liquid substrate exiting the apparatus (4B) is supplied into the reactor (4C) on a daily basis, according to a direct relationship, expressed in terms of weight, with the bacterial population biomass being present at that time, said ratio being preferably in the range between 1 : 8 and 1 :25, more preferably between 1 : 12 and 1 :25, while the gas coming from the reactor (4A) is supplied daily up to the maximum total load that can be used by the methanogenic populations being present therein.
  • the methane production reactor (4C) may be any reactor known in the art designed to sustain the growth of suspended bacteria or bacteria fixed to inert supports and capable, in terms of dimensions and equipment, of containing and maintaining the CO 2 and hydrogen introduced from the container (4D) in solution or mixed with the bacterial culture medium for a time long enough to allow substantially all of the introduced acetates, CO 2 and hydrogen to be converted into methane.
  • the selected mixed methanogenic bacterial populations being present and/or introduced through line (52) in the reactor (4C) may belong either to the same or different genera as well as to the same or different species, as properly exemplified by Methanosarcina sp., Methanosaeta sp., Methanococcus sp. and Metanobacterium sp..
  • Methane production is obtained at a density of said mixed bacterial populations, expressed in terms of dry weight, preferably in the range between 6 and 12%, more preferably between 9 and 12%; environmental conditions are kept constant and are defined by a pH value preferably in the range between 7 and 9, more preferably between 7.5 and 8.5, and by a temperature preferably between 30 and 80 0 C, more preferably between 30 and 60 °C.
  • the effluent from the methane production reactor (4C) is sent through line (53) to the apparatus (4E) for the separation of particles and microorganisms being present therein, which may use any of the various techniques known in the art; after having been collected, these solid materials are recirculated through line (54) into the reactor itself for maintaining/increasing the density of the active bacterial populations, or else they are recirculated for degradation to the head of the module/phase 2, whereas a portion of the liquid component is conveyed to the base of the fermentation reactor (4A) through line (55) for contributing to the regulation of the pH value and of the retention time in this latter reactor; the remaining portion is sent to subsequent agricultural or agro- industrial applications or to depuration through line (56).
  • the biogas thus produced is collected in the upper part of the reactor (4C) as a mixed gas (CH 4 , CO 2 , other) and is then recirculated in the lower part of the same reactor or else conveyed through line (57) to a downstream storage unit (4F) and processing unit (not shown) before the biogas/methane can be used for feeding fixed power plants or delivered to a network of final users who are not involved in CO 2 capture.
  • the fermentation reactor (4A) and the methane production reactor (4C) are equipped with a suitable monitoring system capable of detecting the most important process parameters (temperature, pH value, output gas composition, etc.), which are then used for controlling and optimizing the process for converting CO 2 into methane.
  • the main controlled functions comprise: temperature and pH value; supply flow rate and composition of nutritional and alcoholic substrates, integrators and stimulators, and CO 2 ; circulation rate of liquids and gases between the fermentation reactor and the methanogenic reactor, and vice versa.

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Abstract

Cette invention a trait à un procédé rapide de conversion du CO2 en méthane. Selon ledit procédé, le CO2 est d'abord combiné avec des biomasses formulées et traitées de manière appropriée en fonction de proportions prédéfinies, puis il est soumis à un processus de digestion anaérobie optimisé reposant sur des populations bactériennes de microorganismes acétogènes et méthanogènes de forte densité et sélectionnés spécifiquement. Le procédé décrit intègre quatre modules : un premier module adapté pour préparer un courant de CO2 concentré; un deuxième module permettant de préparer, par des procédés industriels, des substrats nutritifs obtenus à partir de cocktails de matrices végétales et animales extrêmement dégradables et de faible coût; un troisième module permettant de préparer, par des procédés agro-industriels, des substrats alcooliques à partir de matrices végétales de faible coût ayant une forte teneur en hydrates de carbone; un quatrième module permettant d'effectuer la conversion industrielle du CO2 obtenu à partir du premier module en acétates puis en méthane, en le combinant selon des proportions définies avec précision avec les substrats nutritifs et alcooliques optimaux respectivement obtenus avec le deuxième module et le troisième module, puis en soumettant ladite combinaison à un processus de digestion anaérobie entièrement conçu. Le procédé proposé est très utile pour les industries émettant des gaz à effet de serre, ainsi que pour toute unité impliquée dans la production d'énergie à partir de biomasses ou dans l'élimination des déchets organiques.
PCT/IB2008/000288 2007-02-14 2008-02-09 Conversion en méthane, par digestion anaérobie associée avec des biomasses, du co2 capturé à partir de systèmes de combustion ou d'autres procédés industriels Ceased WO2008099252A1 (fr)

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2941157A1 (fr) * 2009-01-20 2010-07-23 Agronomique Inst Nat Rech Procede de fixation de co2 et de traitement de dechets organiques par couplage d'un systeme de digestion anaerobie et d'un systeme de production de microorganismes phytoplanctoniques.
WO2010089144A1 (fr) * 2009-02-09 2010-08-12 Rogmans, Maria Procédé et dispositif d'élimination de gaz rejetés, notamment de co2, à l'aide de biomasse
US20120083026A1 (en) * 2009-06-26 2012-04-05 Haeder Donat-Peter Method for removing CO2 from a smoke or exhaust gas of a combustion process
US20120288898A1 (en) * 2009-12-22 2012-11-15 Lovley Derek R Microbial production of multi-carbon chemicals and fuels from water and carbon dioxide using electric current
US8354261B2 (en) 2010-06-30 2013-01-15 Codexis, Inc. Highly stable β-class carbonic anhydrases useful in carbon capture systems
US8354262B2 (en) 2010-06-30 2013-01-15 Codexis, Inc. Chemically modified carbonic anhydrases useful in carbon capture systems
US8420364B2 (en) 2010-06-30 2013-04-16 Codexis, Inc. Highly stable beta-class carbonic anhydrases useful in carbon capture systems
WO2013134879A1 (fr) 2012-03-14 2013-09-19 Co2 Solutions Inc. Utilisation de dioxyde de carbone pour améliorer la production de composés à base de bicarbonates par voie enzymatique
US8926927B2 (en) 2008-06-19 2015-01-06 Shell Oil Company Process for the removal of carbon dioxide from a gas
ITUB20155703A1 (it) * 2015-11-18 2017-05-18 Bioreweal S R L Processo per la produzione di metano mediante conversione biologica di anidride carbonica.
WO2022217284A1 (fr) * 2021-04-09 2022-10-13 Lanzatech, Inc. Plateforme de fermentation flexible pour une conversion améliorée du dioxyde de carbone en produits
WO2022259022A1 (fr) 2021-06-09 2022-12-15 Cyprus University Of Technology Système et procédé de capture et d'utilisation de carbone

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4696746A (en) * 1984-10-30 1987-09-29 Institute Of Gas Technology Two phase anaerobic digestion
DE4230644A1 (de) * 1992-09-12 1994-03-17 Johannes Martin Dipl I Mueller Verfahren zur Umwandlung organischer Reststoffe im Rauchgas durch bakterielle Vergärung zu Methan, als Endstufe der Rauchgasreinigung in Kraftwerken
EP0963780A1 (fr) * 1998-06-08 1999-12-15 Werner Wild Procédé pour éliminer le CO2 des gaz d'échappement de combustion, conversion en CH4 et stockage en dehors de l'atmosphère terrestre
EP1574581A2 (fr) * 2004-03-08 2005-09-14 E.M. Engineering F.T.S. B.V. Méthode et appareil pour la preparation de méthane
WO2006108532A1 (fr) * 2005-04-08 2006-10-19 Cesarino Salomoni Capture de co2 et utilisation dans la digestion de matiere organique en vue de la production de methane

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4696746A (en) * 1984-10-30 1987-09-29 Institute Of Gas Technology Two phase anaerobic digestion
DE4230644A1 (de) * 1992-09-12 1994-03-17 Johannes Martin Dipl I Mueller Verfahren zur Umwandlung organischer Reststoffe im Rauchgas durch bakterielle Vergärung zu Methan, als Endstufe der Rauchgasreinigung in Kraftwerken
EP0963780A1 (fr) * 1998-06-08 1999-12-15 Werner Wild Procédé pour éliminer le CO2 des gaz d'échappement de combustion, conversion en CH4 et stockage en dehors de l'atmosphère terrestre
EP1574581A2 (fr) * 2004-03-08 2005-09-14 E.M. Engineering F.T.S. B.V. Méthode et appareil pour la preparation de méthane
WO2006108532A1 (fr) * 2005-04-08 2006-10-19 Cesarino Salomoni Capture de co2 et utilisation dans la digestion de matiere organique en vue de la production de methane

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8926927B2 (en) 2008-06-19 2015-01-06 Shell Oil Company Process for the removal of carbon dioxide from a gas
FR2941157A1 (fr) * 2009-01-20 2010-07-23 Agronomique Inst Nat Rech Procede de fixation de co2 et de traitement de dechets organiques par couplage d'un systeme de digestion anaerobie et d'un systeme de production de microorganismes phytoplanctoniques.
WO2010084274A1 (fr) * 2009-01-20 2010-07-29 Institut National De La Recherche Agronomique - Inra Procede de fixation de co2 et de traitement de dechets organiques par couplage d'un systeme de digestion anaerobie et d'un systeme de production de microorganismes phytoplanctoniques
CN102292140A (zh) * 2009-01-20 2011-12-21 国家农业研究院 通过联用厌氧消化系统和浮游植物微生物生产系统来固定co2和处理有机废弃物的方法
WO2010089144A1 (fr) * 2009-02-09 2010-08-12 Rogmans, Maria Procédé et dispositif d'élimination de gaz rejetés, notamment de co2, à l'aide de biomasse
US20120083026A1 (en) * 2009-06-26 2012-04-05 Haeder Donat-Peter Method for removing CO2 from a smoke or exhaust gas of a combustion process
CN102458616A (zh) * 2009-06-26 2012-05-16 西门子公司 用于将co2从燃烧过程的烟气或者废气中移除的方法
US20120288898A1 (en) * 2009-12-22 2012-11-15 Lovley Derek R Microbial production of multi-carbon chemicals and fuels from water and carbon dioxide using electric current
US9175408B2 (en) * 2009-12-22 2015-11-03 University Of Massachusetts Microbial production of multi-carbon chemicals and fuels from water and carbon dioxide using electric current
US8569031B2 (en) 2010-06-30 2013-10-29 Codexis, Inc. Chemically modified carbonic anhydrases useful in carbon capture systems
US8354261B2 (en) 2010-06-30 2013-01-15 Codexis, Inc. Highly stable β-class carbonic anhydrases useful in carbon capture systems
US8512989B2 (en) 2010-06-30 2013-08-20 Codexis, Inc. Highly stable beta-class carbonic anhydrases useful in carbon capture systems
US8420364B2 (en) 2010-06-30 2013-04-16 Codexis, Inc. Highly stable beta-class carbonic anhydrases useful in carbon capture systems
US8354262B2 (en) 2010-06-30 2013-01-15 Codexis, Inc. Chemically modified carbonic anhydrases useful in carbon capture systems
EP2825660A4 (fr) * 2012-03-14 2015-12-09 Co2 Solutions Inc Utilisation de dioxyde de carbone pour améliorer la production de composés à base de bicarbonates par voie enzymatique
CN104302774A (zh) * 2012-03-14 2015-01-21 二氧化碳处理公司 利用二氧化碳的碳酸氢盐化合物的酶增强的制备
WO2013134879A1 (fr) 2012-03-14 2013-09-19 Co2 Solutions Inc. Utilisation de dioxyde de carbone pour améliorer la production de composés à base de bicarbonates par voie enzymatique
ITUB20155703A1 (it) * 2015-11-18 2017-05-18 Bioreweal S R L Processo per la produzione di metano mediante conversione biologica di anidride carbonica.
WO2017085080A1 (fr) * 2015-11-18 2017-05-26 Bioreweal S.R.L. Procédé de production de méthane à partir de dioxyde de carbone par coculture
CN108291239A (zh) * 2015-11-18 2018-07-17 拜瑞威有限责任公司 通过共培养从二氧化碳产生甲烷的方法
US20190055584A1 (en) * 2015-11-18 2019-02-21 Bioreweal S.R.L. Method for producing methane from carbon dioxide by co-culture
US10947564B2 (en) 2015-11-18 2021-03-16 Bioreweal S.R.L. Method for producing methane from carbon dioxide by co-culture
WO2022217284A1 (fr) * 2021-04-09 2022-10-13 Lanzatech, Inc. Plateforme de fermentation flexible pour une conversion améliorée du dioxyde de carbone en produits
WO2022259022A1 (fr) 2021-06-09 2022-12-15 Cyprus University Of Technology Système et procédé de capture et d'utilisation de carbone

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