Classifications

• • 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
  • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
  • C12M29/02—Percolation
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
  • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
  • C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
  • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
  • C12M41/48—Automatic or computerized control
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E50/00—Technologies for the production of fuel of non-fossil origin
  • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

• the invention relates to a bioreactor for the production of biogas.
• the invention also relates to a process for the production of biogas.
• biogas is conventionally meant a mixture of methane (CH 2) and carbon dioxide (CO 2 ).
• a biogas is generally created by the biological degradation of organic and / or inorganic substance under anaerobic conditions.
• methane can also be produced from carbon dioxide and dihydrogen.
• a biogas is a source of energy because of the main fuel agent it contains, such as methane.
• This combustible agent is accompanied by other gases, such as dihydrogen (H 2 ), dinitrogen (N 2 ), water (H 2 O), hydrogen sulphide (H 2 S), ammonia as well as alcohols, fatty acids and carbon dioxide (CO 2 ), which are called impurities in the context of biogas.
• gases such as dihydrogen (H 2 ), dinitrogen (N 2 ), water (H 2 O), hydrogen sulphide (H 2 S), ammonia as well as alcohols, fatty acids and carbon dioxide (CO 2 ), which are called impurities in the context of biogas.
• the main fuel agent in a biogas is methane (CH *).
• CH * methane
• the quality of a biogas is therefore directly related to the weight content of the gas in methane. Therefore, it is crucial to remove the impurities mentioned above.
• certain impurities including hydrogen sulphide, ammonia and carbon dioxide, can attack, mainly because of their corroding power, machines in which one would use a biogas.
• biogas is through the biological degradation of organic substances.
• substances are either agroindustrial waste resulting from the processing of fruit, cereals, grass or vegetables, or waste from wastewater treatment plants or the fermentable fraction of household waste.
• biogas is conventionally done in bioreactors, where anaerobic microorganisms mixed with the aforementioned organic substances are placed.
• the mixture forms a bioreactor medium.
• Organic substances are a source of carbon, nitrogen and energy for microorganisms.
• the bioreactors allow active regulation of the bioreactor medium, in particular by controlling pH, temperature and pressure.
• a key aspect of efficient bioreactor management is finding ideal values for variables that affect biogas production. Indeed, research aims to stabilize a bioreactor under desired conditions through active regulation of various parameters.
• the parameters are generally chosen for a maximum flow rate and therefore a maximum production of biogas.
• bioreactors comprising controllers capable of acting on the pH to minimize the effect of an organic overload are known.
• VFAs volatile fatty acids
• Accumulation would cause a drop in the pH of the bioreactor medium and disrupt the growth of microorganisms.
• biogas production is cumbersome and difficult to implement, as will be discussed in detail below. This is particularly due to the need to implement effective regulation based on a large number of parameters.
• the present invention improves the situation.
• the invention can be applied to a bioreactor for the production of biogas, comprising:
• liquid phase bioreactor medium acting by biological degradation of organic substances under anaerobic conditions, to produce a fuel gas and carbon dioxide
• a gaseous phase in exchange with said liquid phase through a liquid-gas interface, said gaseous phase containing the biogas produced, a control unit for regulating the production of biogas, with the introduction of a chemical substance in the liquid phase,
• the control unit is provided with a control law.
• This control law comprises a predetermined function that calculates a result value, depending essentially on the carbon dioxide content ( in biogas.
• the result value represents a desired content of carbon dioxide dissolved in the liquid phase.
• the control law is arranged in a manner to control a parameter of the introduction of said chemical substance. The steering is in a direction tending to bring the content of dissolved carbon dioxide to said desired content.
• control comprises a regulation. This can be:
• PI Integral proportional
• a regulation of the static type which can take into account a set alkalinity in the liquid phase (Z *), of a set content of dissolved carbon dioxide in the liquid phase and a measured carbon dioxide content in biogas (in the gas phase).
• static type control and integral proportional control can use the same measured carbon dioxide input years biogas.
• the bioreactor may comprise a controllable introducer of said chemical substance, such as a valve, this introducer being controlled according to said parameter, and may be placed at a recirculation loop.
• a controllable introducer of said chemical substance such as a valve
• the chemical substance capable of acting on the pH of the liquid phase may be an alkaline agent and in particular sodium hydroxide (NaOH), preferentially with a concentration of 50%.
• the chemical may be an acidic agent such as hydrochloric acid (HCl) or orthophosphoric acid
• control law chosen is furthermore a function of the alkalinity (Z) and the content of volatile fatty acids (VFA) both measured in the liquid phase, or estimated according to a model described below.
• the bioreactor medium used for the invention preferably comprises microorganisms capable of synthesizing methane, which is then the agent main fuel of biogas, at least partly.
• the invention provides a process for the production of biogas, comprising the following steps:
• step a. includes a measure related to the carbon dioxide content in the liquid and / or gaseous phase, such as a carbon dioxide content measurement in the gas phase, or a measurement of the dissolved bicarbonate content (Bic 1 ) in the liquid phase.
• a measure related to the carbon dioxide content in the liquid and / or gaseous phase such as a carbon dioxide content measurement in the gas phase, or a measurement of the dissolved bicarbonate content (Bic 1 ) in the liquid phase.
• step b. includes the following operations:
• said parameter in step b1. is a flow.
• said control law comprises a regulation law.
• the process control law may include integral proportional (PI) control based on a difference between a measured carbon dioxide (CO 2 Gmes ) content in the biogas and a set point
• the regulation law of the process may comprise a regulation of the static type taking into account a set alkalinity in the liquid phase (Z *), with a reference content of dissolved carbon dioxide in the liquid phase (CO 2 3 *) and a measured carbon dioxide content in biogas.
• Yet another embodiment uses the same carbon dioxide content input measured in the biogas, for static type regulation and proportional integral control.
• the introduction of the chemical substance in step b. can be performed by means of an introducer.
• the introducer is placed at a recirculation loop.
• the chemical introduced in step b. may be an alkaline agent and in particular sodium hydroxide (NaOH) preferentially at a concentration of 50%.
• the chemical substance introduced in step b. is an acidic agent such as hydrochloric acid (HCl) or orthophosphoric acid
• FIG. 1 shows a flowchart representing the main metabolic steps of the production of a biogas
• FIG. 2 relates to the prior art and represents a bioreactor for the production of a biogas
• FIG. 3 shows a block diagram of a control law according to one embodiment of the invention.
• FIG. 4 schematically and functionally shows a bioreactor for the production of a biogas according to one embodiment of the invention
• FIG. 5 shows an embodiment of a bioreactor of the invention.
• MATTIASSON "Monitoring and control of anaerobic upflow fixed-bed reactor for high-loading-rate operation and rejection of disturbance," Biotechnology and Bioengineering, vol. 87, No. 1, p. 44-55, 2004]; [J. LIU, G. OLSSON & B. MATTIASSON, "Extremum-seeking with variable gain control for intensifying biogas production in anaerobic fermentation," Water Science and Technology, vol. 53, No. 4, p. 35-44, 2006] have stabilized the operation of bioreactors.
• Figure 1 shows the main metabolic steps in the production of a biogas, specifically methane (CH *).
• Organic substances i.e., biopolymers are degraded by hydrolysis to organic monomers.
• Lipids, carbohydrates (especially polysaccharides) and proteins are therefore obtained respectively from fatty acids, degraded carbohydrates (in particular, monosaccharides, oligosaccharides) and peptides or amino acids.
• Hydrolysis is generally catalyzed by exoenzymes of facultative anaerobic microorganisms.
• the organic monomers are mainly degraded on the one hand organic acids (in particular, butyl acid, propionic acid, acetic acid (CH3COOH), and on the other hand into alcohols (in particular, ethanol) by acidogenesis Among the products of acidogenesis, carbon dioxide (CO2) and hydrogen (H) are also present.
• acidogenesis carbon dioxide (CO2) and hydrogen (H) are also present.
• Acetic acid is in the amount of about 20%, the main product of acidogenesis. stage is followed by acetogenesis, during which the organic acids and alcohols produced by acidogenesis, are metabolized to acetic acid.
• acetic acid (CH3COOH) is metabolized to methane (CH 4 ) by the following reactions:
• FIG. 2 relates to the prior art and shows a bioreactor for the production of a biogas.
• the bioreactor includes a fermenter 100, which comprises a liquid phase bioreactor medium L.
• a biochemical exchange between the liquid phase L and a gas phase G takes place at the interface 102.
• the document [JE BAILEY & DF OLLIS, Biochemical Engineering Fundamentals, Second Edition, New York: McGraw-Hill, 1986], describes in detail the principles of a bioreactor and more particularly the phase transfer taking place between a liquid phase and a gas phase. It can be referred to, and this document is to be considered incorporated by reference to this description, to supplement it if necessary.
• a bioreactor for the production of biogas is provided with a control means or "controller” arranged to implement control laws, as described above.
• the control means commonly include a sensor 104 and a controller CTRL provided with a control law.
• the number of sensors 104 varies according to the parameters taken into account by the control law.
• the known variants of a CTLR controller are diverse and all focus on maximizing biogas flow.
• the biogas comes out in a collector COL, then undergoes purification steps to remove impurities and enrich the biogas methane (CH 4 ).
• the optimization developed by the applicant is based on an approach totally different from those used in the prior art.
• the invention involves a regulation of dissolved carbon dioxide (CO ⁇ 1 ) present in the liquid phase L, which allows active control of the content of combustible agent, especially methane, in the biogas.
• CO ⁇ 1 dissolved carbon dioxide
• the total exchange surface F F is defined by the formula (1) attached.
• the flow rate of volumetric gas Q R is defined by the formula (2) attached, where Q B is the bubble frequency at the head of the column.
• This frequency Q B is defined by the appended formula (3), where the rate of rise V B is given by the appended formula (4), known as the Hadamard-Rybczynski formula for mobile interface bubbles [I. LEIFER & R. K PATRO, "The Bubble Mechanism for Methane Transport Forms the Seabed to the Surface: A Review and Sensitivity Study," Continental Shelf Research, Vol. 22, p. 2409-2428, 2002], where g is gravity.
• the total number of bubbles N ⁇ is then defined by the formula (5) attached.
• Kifl is described by the formula (6) attached, where IC L O represents the transfer coefficient per unit area of bubbles.
• the average flow rate qc of dissolved carbon dioxide (CO 2) in the liquid phase L is expressed by the formula (8) appended, where K H and Pc are respectively the Henry constant and the partial pressure, both for the dioxide of carbon.
• K H and Pc are respectively the Henry constant and the partial pressure, both for the dioxide of carbon.
• This model therefore directly relates the quality of the biogas to the content of dissolved carbon dioxide (CO 2 1 ) in the liquid phase L. Therefore, the composition and therefore the quality of the biogas produced in a bioreactor using the model described below. above, is reached by the regulation of dissolved carbon dioxide in liquid phase L.
• control law in which the model described is implemented.
• This control law comprises a predetermined function which calculates a result value serving as a parameter for controlling the introduction of a chemical substance in order to vary the content of dissolved carbon dioxide in the liquid phase (CO 2).
• Figure 3 shows a block diagram of said control law, according to a particular embodiment.
• the predetermined function of the control law comprises:
• STAT a law of regulation in static mode
• the blocks 200 and 300 respectively reflect a measurement of carbon dioxide (CO 3 ) in the gas phase and a measurement of the pH in the liquid phase. Note that the measures mentioned are in no way limiting. In fact, as will be seen below, the bicarbon content or the content of volatile fatty acids in the liquid phase may in particular be measured.
• Blocks 202 and 302 respectively correspond to the establishment of a reference value of carbon dioxide content (CO 3 *) in the biogas and a reference value of alkalinity (Z *) in the liquid phase.
• This instruction 302 is calculated as a function of pH measurements and measurements or estimates of the content of volatile fatty acids (VFA) and / or bicabonates (Bic) in the liquid phase.
• VFA volatile fatty acids
• Bic bicabonates
• the method according to one embodiment therefore comprises the measurement in the liquid phase or the estimation of the alkalinity (Z), and / or the content of volatile fatty acids (VFA) and / or bicabonates (Bic).
• the measurement 200 and the setpoint 202 are used in the control mode integral proportion (PI) of the block 204.
• the measurement 300 and the instruction 302 are used in the static mode control (STAT) of the block 304.
• the regulators 204 and 304 here provide respective rates Qu 1 and Q112. These flows are then added to give a total flow Qu.
• the flow rate corresponds to the rate at which a chemical substance is added to the bioreactor medium in order to vary the content of dissolved carbon dioxide in the liquid phase.
• the addition of a carbon source (such as, for example, acetate) in the fermenter is accompanied by an addition of a "neutralizing" chemical substance.
• This substance is therefore an alkaline agent, such as sodium hydroxide (NaOH).
• Na + ions are not consumed by the bioreactor medium, and lead to an increase in the alkalinity (Z) in the liquid phase, and consequently an increase in the pH.
• Z alkalinity
• a higher percentage of methane in the biogas is achieved by a higher dissolution of the liquid phase carbon dioxide.
• Equation (11) The expression of the alkalinity results from equation (11) of electroneutrality of the liquid phase, that is to say to equilibrium in cations and anions (see annex for the equation).
• equation (11) In the usual pH range in anaerobic digestion (close to neutral), strong acids and strong bases are completely dissociated, and bases and weak acids are partially dissociated.
• the main acid / base pairs to be considered are for a pH close to 7: T.
• the term HAc encompasses the different pairs of weak acids. Equation (11) can then be reduced to equation (12), appended.
• Cations (especially Z) and anions (especially S ⁇ / ⁇ ) mainly come from strong acids and strong bases, and are not consumed during the degradation of organic matter. As a result, their concentration varies little without external input, and the alkalinity Z is calculated by equation (13), appended.
• the cation / anion set is stable. This set follows a value related to the carbon source feed (this is called incoming alkalinity). If one takes into account the dissociation constant Kco2 of the CO2 / HCO3 ' pair, equation (13) can also be written in the form of the equation (14) appended. Note that in the range of pH considered, AGV are almost completely dissociated.
• Equation (14) allows to calculate the concentration in dissolved when alkalinity, pH, and AGV concentration are known. Note that in the absence of alkalinity or AGV measurements, it is possible to replace these quantities by estimates obtained for example by means of software sensors [O. BERNARD, B. CHACHUAT & J. -P. STEYER, State Estimation for Wastewater Treatment Processes. Water Quality Measurements Series, "Wastewater Monitoring, Wiley, 2006]. In particular, these quantities can be estimated from measurements on the flow rate as well as on the composition of the biogas.
• the control law comprises a regulation law in integral proportional mode (PI), and a regulation law in static mode (STAT).
• PI integral proportional mode
• STAT regulation law in static mode
• the laws of regulation are defined by equations (15) to (20) of the appendix, which are described in a precise manner below.
• the regulation is governed by the combination of integral proportional control and static control.
• the total flow rate Q u of chemical substance to be added to the bioreactor is defined by the formula (15) attached.
• This flow rate Q 11 is composed in the embodiment by the addition of the flow rate Q u j and the flow rate Q U 2-
• PL Kp Proportional Gain
• Ki Integral Gain
• sat (.) is a saturation function, which limits in amplitude the flow rate of the chemical substance applied, and ensures a positive realistic control, that is to say that the result of the computation is maintained at a value zero if this it is negative, and at the maximum value allowed by the pump "Qu m " if it was beyond.
• the value "Qum” determines the maximum flow chemical substance that can be applied, which will depend on pumps, especially used solenoid valves, but also other constraints, such as economic constraints (cost of the chemical).
• Q u2 is calculated as a function of STAT static regulation from the appended formula (18).
• This regulation involves the alkalinity setpoint Z * and makes it possible to control the dissolution of CO 2 . Therefore, the quality of the biogas is conducted in an active way by directly controlling the alkalinity of the digester.
• Z in and Z u are respectively the alkalinity of the feed (variable over time) and the chemical substance (especially in the alkalinity embodiment of the soda) used for the regulation.
• the concentration Z u is therefore a fixed quantity according to the chemical substance used.
• Qi n is the total feed rate and Z is the total alkalinity and ⁇ is a setting gain that sets the speed of convergence of the closed loop system.
• sat (.) Is a saturation function, which limits in amplitude the flow rate of the applied chemical, ensuring a positive realistic control, and the value determines the maximum rate that can be applied.
• the set point Z * is defined by the formula (20), and is of course directly dependent on the pH measurements made in a liquid medium and the dissociation constant Kco2 of the CO 2 / HCO3 " pair.Substitute also in the formula (20) a quantity S 2 which is a representative parameter of the AGV, which is obtained either by means of a dedicated sensor, such as an automated titrimeter, or by means of computer evaluation by means of software sensors [O BERNARD, B. CHACHUAT & J.-P. STEYER, "State Estimation for Wastewater Treatment Processes, Water Quality Measurements Series", Wastewater Monitoring, Wiley, 2006].
• control without the other. It will therefore be possible separately to implement in the predetermined function, included in the control law, either the PI regulation, or the STAT regulation, or both at the same time.
• a measurement unit U.MES using various sensors measures the magnitudes involved in the predetermined function.
• a CO 2 sensor 106 measuring the percentage of carbon dioxide in the biogas for the measurement of the carbon dioxide content in the biogas ( and a pH sensor 108 for measuring the pH in the liquid phase, which substantially correspond to the blocks 200 and 300.
• the measurements made by the measurement unit U.MES serve as input variables for a control unit U. COM.
• the control unit is a complex controller that includes the control law described above and comprising a predetermined function FUNC which implements, according to the embodiment described here, the control laws PI and STAT.
• the assembly consisting of measurements carried out by the unit U.MES and instructions CONS allows to drive the regulation of the bioreactor according to the regulation defined by the formulas (15) to (20).
• This conduct is done by means of an introducer INT, which comprises in the described mode an alkaline container 110 and an acid container 112, according to whether the embodiment tends to increase or decrease the CO 2 content of the biogas.
• the INT introducer is thus arranged to selectively control the addition of chemical substance to vary the content of CO 2 dissolved in the fermenter 100. This is done via a result value, calculated by the predetermined function. This result value serves as a parameter for said regulation.
• the parameter can actuate a control valve to control a flow.
• the introducer can operate at a recirculation loop 114, as shown in Figure 4. This loop ensures a rapid homogenization of the chemical in the reactor.
• FIG. 5 comprises a bioreactor of the type described in the document [IP. STEYER et al., "Evaluation of a Four Year Experience With a Fully Instrumented Anaerobic Digestion Process". Water Science and Technology, Vol 45, No. 4-5, pp. 495-502, 2002]. This document is to be considered as incorporated herein by reference and the reader is invited to refer to it.
• a fermenter 100 ascending fixed bed was used for the implementation of the invention.
• the fermenter 100 is of circular column type with a height of about 3.5m, a diameter of about 0.6m, and a volume of about Im 3 . Fermentors of this type are generally made of Cloisonyl.
• the bioreactor is provided with a storage tank 500 which allows the carbon source feed as described above (in particular industrial vinasses).
• a selection system 501 makes it possible to discriminate between the entry of the content coming from the storage tank 500 and a water inlet 502.
• the carbon source either sterile nor homogeneous
• the water are mixed at a reservoir 504 dilution for form an inlet mixture.
• the flow of the inlet mixture is ensured and regulated by a peristaltic pump 508. This flow rate is controlled by a feed flow sensor 510. Upstream of the fermenter 100, there is a heat exchanger 512 which is in direct communication with a heater 514. The heat exchanger 512 allows a regulation of the temperature of the input mixture, poured into the fermenter 100. Generally, the temperature is at about 35 ° C and is controlled by a temperature sensor 516. The feed liquid enters the lower part in the fermenter 100. The liquid is then homogenized by a mixing pump 518. In the embodiment described, the bioreactor is provided with a recirculation loop whose flow is ensured and regulated by a recirculation pump 542.
• the recirculation liquid joins the supply liquid at the heat exchanger. 512.
• the bioreactor comprises two systems for measuring and regulating pH. On the one hand there is a system on the input mixture side, comprising an alkaline reservoir 530, a pump 532 and a pH sensor 506. At the recirculation loop, there is another alkaline reservoir 534, another pump 536 and a pH sensor 538.
• the supply of NaOH is exclusively on the recirculation loop side so that the distribution of sodium hydroxide is rapidly homogeneous in the reactor.
• the bottom of the fermenter is provided with a sewer outlet 520 allowing in particular the evacuation of waste.
• the collection of the biogas is done by a 550 exit from the top of the fermenter.
• a container 539 allows recovery of the overflow liquid.
• a part of the overflow liquid is sent into the recirculation loop (about 150 1 / h), another part is sent to the outlet of the sewer 520.
• the biogas produced by the bioreactor is controlled by a CH 4 / CO 2 analyzer 544, an H 2 546 sensor and a gas flow meter 548.
• the bioreactor is generally provided with a dryer (not shown) which removes moisture by cooling the biogas.
• the gas flow meter 548 is generally of the type comprising an electromagnetic float.
• the H 2 546 sensor makes it possible to measure the concentration of hydrogen in the biogas by means of an analyzer of the AMS 6400 H 2 type (from the company Pekly Hermann-Moritz).
• the H 2 546 sensor is very sensitive to the hydrogen sulphides contained in the biogas.
• CHjZCO the sensor 2544 is of the type Ultramat 22P (from Siemens) and allows the measurement of the percentage of carbon dioxide and methane of biogas.
• the fermenter 100 is provided with a pressure sensor 522, as well as an analysis loop. In this loop is an ultrafiltration membrane 522 with a diameter of about 10 mm, a filtration area of about 0.045 m 2 and allowing an elimination of particles exceeding about 0.14 microns.
• the recirculation is ensured by a pump 525, and the filtrate analysis is done by a Total Organic Carbon Analyzer (COT) 526 and a titrimetric sensor 528 allowing the analysis of the total alkalinity (AT), the partial alkalinity (AP), the total volatile fatty acid (VFA) content, and the bicarbonate content (Bic).
• COT Total Organic Carbon Analyzer
• AP partial alkalinity
• VFA total volatile fatty acid
• Bic bicarbonate content
• the control unit (not shown in FIG. 5) is located in particular at the level of the recirculation loop
• the invention allows a stabilization around set values, and results in particular in a biogas of low carbon dioxide content.
• the invention therefore guarantees the production of a biogas rich in combustible agent. This results in the production of a rich gas in terms of energy.
• the invention provides active regulation that optimizes the performance of a bioreactor. This optimization is synonymous with maximum production of the purest possible biogas fuel agent.
• the bioreactor (as well as the corresponding method) uses microorganisms capable of synthesizing methane (CH 4 ). This is not limiting, and the invention can be applied to other biogas.
• Annex 1 is not limiting, and the invention can be applied to other biogas.

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