FR3133859A1 - COMPARTMENTED MICRO-HYDRO-METHANIZATION DEVICE IN VISCOUS WAY - Google Patents

Abstract

The present application relates to a compartmentalized viscous micro-hydro-methanization device intended for the production of biomethane from organic waste, consisting of a compartmentalized fermenter constructed from prefabricated panels, characterized in that it comprises: A compartment thermo-enzymatic hydrolysis (1) maintained at a hyperthermophilic temperature, preferably of the order of 70°C, suitable for the destructuring of said organic waste and the production of hydrogen, At least two methanization compartments (2) maintained at a thermophilic temperature, A hydromethanization compartment (3), with a volume of the order of approximately 1/12 of the cumulative volume of compartments (1) and (2), containing a bacterial support made of digestate depleted in material biodegradable organic suitable for the renewal of hydrogenophilic bacteria, allowing the reduction of CO2 by hydrogen into methane. Figure: Fig 1

Description

COMPARTMENTED MICRO-HYDRO-METHANIZATION DEVICE IN VISCOUS WAY TECHNICAL FIELD OF THE INVENTION

The present invention relates to a Compartmented Micro-Hydro Methanization device, in the Viscous method, also called “MHMCV”, allowing the production of biomethane from organic waste.

STATE OF THE ART

Methanization or anaerobic fermentation of effluents (liquid substrates) and waste (solid substrates) to produce energy in the form of biogas concerns many biodegradable organic substrates such as farm substrates, manure, sewage treatment plant sludge. , the fermentable part of household waste and organic substrates from the food industry.

Fermentation systems are batch or continuous systems.

In batch systems, the substrate is introduced into the fermentation tank, it ferments over a residence time depending on the nature of the substrate, 40 days for example. At the end of the period, the substrate is extracted while keeping a stock base for bacterial seeding of the new loaded substrate. Hydrolysis of the substrate followed by methanization are concomitant.

Continuous systems consist of introducing a quantity of substrate daily, corresponding to the hydraulic residence time, from 20 to 40 days for example. The fermenter suitable for this system can be subdivided into fermentation tanks corresponding to hydrolysis, acidogenesis, acetogenesis and several stages of methanogenesis. The fermenter is maintained at a temperature that is either mesophilic (around 37°C), or thermophilic (around 55°C) or hyperthermophilic (around 70°C).

European patent application EP3642321 describes a process and a device for implementing the so-called “VHBM” process for Visco-Hydro-Bio-Methane for the production of biomethane in a viscous compartmentalized reactor.

The complexity of hydromethanization installations requires large installations to benefit from scale effects and amortize construction costs. This makes this type of devices described in EP3642321 incompatible with small decentralized installations. The collection of waste, the substrates of these installations, generally takes place far from the treatment site, which generates transport and therefore energy costs and greenhouse gas emissions, which must be avoided from an environmental point of view. . The present invention aims to remedy these drawbacks.

The present invention relates to a Viscous Compartmented Micro-Hydro-Methanization device, also designated “MHMCV” organized in small local installations. This device is made up of prefabricated panels, integrating the related equipment, constituting the different stages of hydro-methanization compartmentalized in the viscous route, with in particular a first compartment (1) reserved for thermo-enzymatic hydrolysis at hyperthermophilic temperature at approximately 70°C and at least two methanization compartments (2), preferably at a thermophilic temperature of 55°C, followed by a compartment (3) reserved for the hydro-methanization of CO2 reduction in biogas by endogenous hydrogen produced in the 1st thermo-enzymatic hydrolysis compartment, possibly supplemented by exogenous hydrogen produced on site to produce biomethane.

The panels incorporate different reservations and fixings for the valves for transferring the fermenting substrate from one compartment to another, for the compressed biogas injection nozzles and the biogas diversion plates for mixing the substrate in each compartment, for the opening-closing system of more or less compressed gas in the gas head of the fermenter and other assembly, piloting and control equipment.

This device makes it possible to implement the Visco-Hydro-Bio-Métha or VHBM process in small local and decentralized hydromethanization installations.

In particular, the present invention relates to a viscous compartmentalized micro-hydro-methanization device intended for the production of biomethane from organic waste, consisting of a compartmentalized fermenter constructed from prefabricated panels, characterized in that it comprises :

• A thermo-enzymatic hydrolysis compartment (1) maintained at a hyperthermophilic temperature, preferably of the order of 70°C, suitable for the destructuring of said organic waste and the production of hydrogen,
• At least two methanization compartments (2) maintained at a thermophilic temperature, preferably of the order of 55°C,
• A hydromethanization compartment (3), with a volume of the order of approximately 1/12 of the cumulative volume of compartments (1) and (2), containing a bacterial support made of digestate depleted in biodegradable organic matter suitable for renewal of hydrogenophilic bacteria allowing the reduction of CO2 by hydrogen into methane.

DETAILED DESCRIPTION OF THE INVENTION

Control of the stages of the hydro-methanization process calls for means taking into consideration the interactions between the control of biochemistry and its interaction with fluid mechanics, in particular the control of the viscosity of the mixtures and the avoidance of separation of liquid and solid phases.

This complexity makes hydro-methanization technology economically incompatible with small, efficient methanization installations based on the control of the stages of the hydro-methanization process from a viscous substrate. This complexity induces significant fermentation volumes requiring the transport of substrates (organic waste) more or less distant from the fermentation site, fermenters requiring a complex structure to anchor them to the ground, the transport of the digestate as fertilizer or amendment over a large territory. . All this is accompanied by significant production of greenhouse gases, particularly during the transport of substrates to methanization plants.

In a methanization system according to the invention, comprising in particular a step or phase reserved for hydrolysis and acidogenesis at a preferably hyperthermophilic temperature, of the order of 70°C, and several stages reserved for acetogenesis and at methanogenesis at temperature, particularly thermophilic 55°C, the kinetics and rate of degradation are greatly improved.

The VHBM process described in patent application EP3642321 aims to control the different stages of the process. This process integrates the hydrolysis and acidogenesis stages in a first compartment, then the acetogenesis stage in a second compartment, then the methanogenesis stage in one or two compartments, then the methanogenesis stage in a final compartment. hydromethanization consisting of reducing the CO2 of the biogas using endogenous hydrogen produced in hydrolysis, which can be supplemented by exogenous hydrogen produced on site by water electrolysis or steam reforming.

Hydrolysis generates a process of decomposition of complex organic matter into simple compounds, soluble by several groups of hydrolytic bacteria and produces a gas essentially composed of CO2 and hydrogen which will be advantageously used in the hydromethanization process. It promotes enzymatic activity and substrate solubility.

Acidogenesis takes place in the same compartment as hydrolysis. Substrates are organic wastes that are metabolized into fermentation products, alcohols, organic acids, CO2 and hydrogen.

Acetogenesis transforms the products resulting from the acidogenic phase by acetogenic bacteria. The metabolism of these bacteria is mainly oriented towards the production of acetate.

Methanogenesis transforms acetate, hydrogen and carbon dioxide into methane in two ways:

• Acetoclast methanogenesis: acetate + H2 → CO2 + CH4
• Hydrogenophilic methanogenesis: CO2 + 4 H2 → CH4 + 2 H20

The 1st compartment (1) for thermo-enzymatic hydrolysis maintained at a hyperthermophilic temperature, of the order of approximately 70°C, is sized for an average hydraulic residence time of 2 to 3 days, in order to hydrolyze the material organic and produce volatile fatty acids and thus promote a pH of around 5.5. This makes it possible to have a pH of around 7 to 7.5 in the following stages of methanization and to maintain at the end of the process a substrate with a pH lower than 8 in order to avoid the production of gases inhibiting methanogenesis, such as H2S.

The 2nd and 3rd methanogenesis compartment (2) are sized for a hydraulic residence time of between 9 and 12 days, said residence time being able to be adapted by the filling level of the tanks.

A final hydromethanization compartment (3) contains a bacterial support. In this compartment, the biogas containing hydrogen which was produced in the hydrolysis compartment (1) is recycled. The biogas is introduced through microporous ramps located on the floor of the compartment. The volume of the compartment is sized so that the hydraulic residence time is around 24 hours.

Compartmentalization of the fermenter is essential to respect the stages of the hydro-methanization process. It makes it possible, in particular, to control the evolution of the pH during the process. The pH must be regulated according to the fermentation stage, in particular by regulating the partial pressure of carbon dioxide in the gas sky of the last hydromethanization compartment (3).

According to one implementation of the invention, the device according to the invention consists of prefabricated panels, which are mounted on the installation site of the device, said prefabricated panels including reservations for receiving and fixing the equipment, in particular the devices measurement and control, and being equipped with a nesting system (consisting of a male edge and a female edge), this makes it possible to eliminate thermal bridges.

For the purposes of the invention, the term "reservations" means elements integrated into the panels making it possible to connect them together and to fix the equipment on these panels, in particular the equipment making it possible to measure pressures, flow rates in particular of gas, or to check the pressure gas injectors on the panels making up the floors.

Advantageously, these prefabricated panels are insulating panels.

These panels are manufactured in the factory and then transported to the assembly site.

According to one implementation of the invention, the device is made up of prefabricated panels having dimensions allowing their transport by truck or train, that is to say meeting the standards and templates established by road and rail regulations.

Preferably, these dimensions are of the order of:

- width: between 1.60 m and 2.10 m;

- useful height: between 1.90 m and 3 m;

- length: less than 16 meters.

The interlocking of these panels makes it possible to meet the dimensions of the fermenter, both in the width and length directions.

According to a particular implementation, in the first hydrolysis compartment (1) of the device, the pH is regulated to approximately 5.5, thanks to the hyperthermophilic temperature.

Controlling the pH avoids the production of inhibitory gases in methanogenesis. It is necessary to emphasize the importance of the compartmentalization of fermenters allowing them to operate at different temperatures and to preserve the bacterial flora adapted to the compartment.

The control of the system takes into account the solubility differential between carbon dioxide and dihydrogen. The solubility of carbon dioxide depends on its undersaturation in the fermentation supporting substrate and the regulation of the partial pressure in the gas sky to maintain equilibrium as the solubilized carbon dioxide is reduced by hydrogen to produce methane.

Biogas production technologies are most often based on installations that economically require significant quantities of substrate to be transported to the methanization site, which generates significant fermentation volumes and the collection of substrates from numerous production sites.

Small methanization installations based on nearby fermentable substrates exist on an extensive basis, with basic methanization technology in an isolated tank where new substrate is introduced every day, while keeping a base of the tank to preserve the bacteria. methanogens. Fermentation volumes are large, but the rate of degradation of organic matter is limited.

The production of biomethane with a high methane rate of more than 90% requires CO2 purification from the produced biogas containing around 50% to 60% methane.

VHBM technology, Visco-Hydro-Bio-Metha, allows the thick material in fermentation to be transported until it is extracted from the fermenter, in piston or semi-piston mode, while preserving the appropriate bacterial flora at each stage. This involves controlling the transfer of the fermenting substrate from one compartment to another.

The substrate is introduced at a sufficient dry matter level (15% dry matter for example), in order to avoid too rapid liquid and solid phase separation, which would require too frequent stirring and the destabilization of the bacterial flora. . A higher concentration rate of organic matter allows more biogas to be produced per volume of fermenter.

According to one implementation of the invention, the device comprises means making it possible to renew each day approximately a third of the bacterial support present in the hydromethanization compartment (3), made of digestate depleted in biodegradable organic matter.

Said means are in particular means making it possible to extract each day a third of the useful volume from the last methanization compartment to introduce it into an annexed fermentation tank, this making it possible to deplete the digestate of biodegradable organic matter, and means for reintroducing the equivalent of organic matter very depleted in biodegradable organic matter.

The renewal of the substrate supporting the hydromethanization in the hydromethanization compartment (3) for approximately 1/3 per day makes it possible to provide the nitrogen and trace elements necessary for the development and renewal of bacteria, particularly hydrogenophiles.

In synthesis, hydromethanization requires:

• To have a bacterial support made of digestate low in biodegradable organic matter
• To renew this support by approximately a third per day to provide the nitrogen necessary for the renewal of hydrogenophilic bacteria to reduce CO2 with H2 to produce methane.
• That the system be thick to avoid separation of liquid and solid phases. The proposed mixing system is adapted to a thick substrate, called viscous, an intermediate state between the dry route and the liquid route.
• A system for stirring a thick material adapted to the particularity of a gas flow which widens as it rises and leaves the lower part of the substrate to be stirred outside the stirring movement.
• Regulation of pH by managing partial pressure.

We know that the viscosity of a substrate decreases with increasing temperature and decreasing pH, in particular thanks to the influence of thermo-enzymatic hydrolysis at around 70°C. We know that an acidic pH around 5.5 in hyperthermophilic fermentation promotes the production of hydrogen necessary for hydrogenotrophic methanization. We know that the pH of the environment decreases with the increase in soluble carbon dioxide. Calculating and controlling the partial pressure of CO2 contributes to the proper functioning of the system. pH regulation allows the system to be maintained in a pH range favorable to bacterial activity and the avoidance of the carbonate form which precipitates.

This regulation is made possible by the compartmentalization of the fermenter, the control of transfers from one compartment to another, the biochemical exchanges between the aqueous and soluble phases of the metabolites introduced and produced, the dissolution and solubilization of the elements in water. free.

The effectiveness of the system depends on the convergence between the control of viscosity, the control of temperatures, pH and the partial pressure of carbon dioxide.

The balance of the fermentation system depends in particular:

• Managing the transfer from one compartment to another compatible with maintaining the biochemical balances of the methanization and hydromethanization stages.
• The subdivision of the fermenter into stirring sectors necessary for mixing a thick substrate in large fermentation volumes. The pressure loss due to friction on the walls promotes the settling of higher density elements. Which gradually reduces the useful fermentation volume.

- Regulation of the pH in a range favorable to methanogenic activity between 6.8 and 7.3 for example, thanks in particular to the dissolution of carbon dioxide in the fermentation substrate. When we double the partial pressure of CO2 we see a decrease in pH of around 0.3 units. Controlling the pH makes it possible, in particular, to avoid the carbonate form which precipitates.

- The evacuation of mineralized nitrogen and salts produced. Their progressive concentration is accompanied by an increase in pH with, in particular, the formation of ammonia, a potentially toxic element of methanogenesis.

By increasing the total pressure and partial pressure of each gas component in the gas sky, their solubility is increased.

The pH is partially regulated by controlling the hydraulic residence time.

The endogenous dihydrogen necessary for the reduction of CO2 in biogas is produced at a hyperthermophilic temperature of around 70°C in the first hydrolysis and acidogenesis compartment. This temperature, which is not very favorable for methanogenesis, allows a pH of around 5.5 to be obtained. The solubility differential between CO2 and H2 is reduced by the interplay of pressures and thanks to the biochemical form of carbon dioxide depending on pH.

Dihydrogen, the lightest gas, to be solubilized must be diffused by diffusion ramps which prevent its coalescence and its evacuation into the gas sky.

According to one implementation of the invention, the device comprises diversion plates distributed over all the floors of each compartment, which allow the injection of compressed biogas.

According to another implementation of the invention, the device comprises means for reintroducing the biogas produced in the hydrolysis (1) and methanization (2) compartments into the last hydromethanization compartment (3).

Said means are in particular diffusion ramps integrated into the floor receiving the recirculated and superpressed biogas and diffused through a multitude of micro holes.

According to one implementation of the invention, the device comprises means for adjusting the partial pressure of carbon dioxide in the closed gas sky of the last hydromethanization compartment (3) receiving the recirculated biogas, composed in particular of CH4, CO2 and hydrogen, to which exogenous hydrogen is optionally added.

Said means are in particular a device for measuring the partial pressure of the gases CH4, CO2 and H2, in the hydromethanization compartment, integrating the measurement of the composition of the gas, coupled to a volume calculator of the gaseous sky making it possible to adjust the volume of exogenous hydrogen added to reduce the CO2 of the biogas by endogenous and exogenous hydrogen into methane according to the ratio C02 + 4 H2 = CH4 + 2 H20.

The reduction of carbon dioxide by dihydrogen can only be effective if the substrate in which the gases dissolve is homogeneous, therefore regularly homogenized by mixing with compressed gas or any other suitable means.

The entire hydromethanization process is controlled by a control-command system which integrates the monitoring of the pH, the calculation of the partial pressure of the CO2, the pressure in the gas sky necessary to promote the solubilization of the CO2 and in particular facilitate its reduction by endogenous hydrogen produced in hydrolysis and exogenous hydrogen to directly produce biomethane.

More specifically, the device according to the invention comprises a control system (command) which integrates the measured or evaluated data of production of gas, hydrogen, CO2, which regulates the pressures in the gas sky, in particular of the last compartment hydromethanization (3), which regulates transfers from one compartment to another and the renewal rate of the digestate supporting hydromethanization, which calculates and optimizes the partial pressure of the compartments by controlling the regulation valves on the gas outlets and which adjusts the flow rates, duration and frequency of agitation and homogenization of the substrate in each compartment.

DESCRIPTION OF FIGURES

Micro-Hydro-Métha-Plaques or MHMP device – Representation of a basic module

There represents the basic module of the MHMCV device which can be multiplied by as many modules as available substrates. It reveals 5 compartments with a total volume of 87 m3 and a useful volume of around 61 m3. Compartment (1) is intended for hydrolysis; the compartments (2) are the methanization compartments; and compartment (3) is intended for hydromethanization.

The arrow (a) indicates the place of introduction of the substrate; the arrow (c) indicates the direction of passage of the substrate from one compartment to another; the arrow (d) the place of exit of the substrate. The circles in compartment (1) represent the brewing nozzles. The arrows inside the device represent the path of the substrate within the device. The squares crossed by the arrows represent the transfer valves from one compartment to another.

The assembly of the whole is made from prefabricated panels which have been delivered.

For example :

The basic module has a total volume of 87 m3, for a useful volume of 61 m3.

The filling rate is approximately of the order of 70%, i.e.: 61 m3

Dimensions of the panels:

Width: 1.98, Height: 2.81, Total length: 15.56 m.

This is subdivided into five compartments:

- 1st hydrolysis compartment: Length: 2.78 m, height: 2.81 m, width: 1.98 m, i.e. total volume of: 15.4 m3

- 2°, 3°, 4° methanization compartment:

Width: 1.98 m, height: 2.81 m Total length: 11.67 m (3 x 3.89 m) or: 65 m3

• 5th hydromethanization compartment:

Length: 1.11 m, Height: 2.81 m, Width: 1.98 m Is: 6.20 m3

Micro-Hydro-Métha-Plaques or MHMP device – Representation of two coupled basic modules

Only the width of the device is doubled in two basic modules.

Width: 3.96, Height: 2.81 m, Total length: 15.56 m

Total volume: 173 m3. Useful volume: 121 m3.

Compartment (1) is intended for hydrolysis; the compartments (2) are the methanization compartments; and compartment (3) is intended for hydromethanization.

The arrow (a) indicates the place of introduction of the substrate; the arrow (c) indicates the direction of passage of the substrate from one compartment to another; the arrow (d) the place of exit of the substrate. The arrows inside the device represent the path of the substrate within the device. The squares crossed by the arrows represent the transfer valves from one compartment to another.

Diagram of a single compartment from plates prefabricated in the factory and assembled on site.

has. Introduction of the substrate. b. Gas outlet above the compartments.

vs. Regulated passage of the substrate from one compartment to another d. Substrate outlet.

The arrows inside the device represent the path of the substrate within the device. The squares crossed by the arrows represent the transfer valves from one compartment to another.

Schemes with double compartments and the transfer between these compartments.

has. Substrate introduction.

vs. Regulated passage of the substrate from one compartment to another d. Substrate outlet.

The arrows inside the device represent the path of the substrate within the device. The squares crossed by the arrows represent the transfer valves from one compartment to another.

EXAMPLES

Table 1 below shows all the numerical characteristics of the basic module illustrated on the .

Meters Meters Meters Volume TSH Length Height Width Flight. total m ³ / Useful flight Total 14 Days 15.56 2.81 1.98 87 / 61 Hydrolysis 3 Days 2.78 2.81 1.98 15/11 1st, 2nd, 3rd compartment 10 Days 11.67 2.81 1.98 65 / 45 Hydromethanization 1 Day 1.11 2.81 1.98 6 / 4.3

There represents the doubling of the installation by juxtaposing 2 modules.

Table 2 below indicates all the numerical characteristics of the module illustrated on the .

Meters Meters Meters Volume TSH Length Height Width Flight. total m ³ / Useful flight Total 14 Days 15.56 2.81 3.96 173 / 121 Hydrolysis 3 Days 2.78 2.81 3.96 31 / 22 1st, 2nd, 3rd compartment 10 Days 11.67 2.81 3.96 130 / 91 Hydromethanization 1 Day 1.11 2.81 3.96 12 / 8.6

Figures 3A and 3B represent:

• Compartments (1) (2) and (3) and the passage of the substrate regulated by transfer valves (squares crossed by the arrows), which only open once a day for example when loading with substrate new. These valves are thus closed during mixing of the compartments in order to avoid failure to control the flow between the compartments.
• The gas outlets (b) above the compartments ( )
• The pressurized gas inlet nozzles under the diversion plates represented by white circles in compartment (1) ( )
• The transfer of the substrate from one compartment to another in the direction indicated by the arrow c. ( and 3B)
• The passage of the substrate regulated by transfer valves. (squares crossed by the arrows). ( and 3B)

Table 3. SUBSTRATE ENERGY SIZING BALANCE.

This indicative assessment serves as a basis for specifying the process and the volume of micro-fermenters installed by assembling prefabricated plates in the factory.

Table 3 below presents the balance of substrate and energy consumed, as well as the production of biogas. MO: organic matter; MS: dry matter.

Substrate introduced. Biogas production Dilution Rate MO M ³ /t M ³ /d Tx CH4 M ³ CH4 T. Day M.S. T.MS MO rate T.MO 16% Gradient Degraded Gradient Biogas 2.40 25% 0.60 85% 0.51 3.75 70% 0.36 850 303 50% 152 CO2 CH4 M3 C02 net CH4 net CO2 Need H2 M ³ H2 M ³ H2 Red. CO2 M ³ CH4 M ³ CH4 Rate CO2 M3 bio- - 10% - 10% /day Endogenous Exogenous By H2 Supplement. /DAY CH4 Residual Methane 152 137 137 546 221 325 92% 126 262 96% 11 273

Volume of the basic fermenter estimated at 87 m3, useful volume of 61 m3 useful.

2.4 tonnes of substrate at 25% DM reduced to 16% DM as input after dilution with juice from the digestate and/or with water, i.e. 3.75 tonnes at 16% DM.

Based on an organic matter rate of 85%, a reduction rate of organic matter of 70% and a production of 850 m3 of biogas per tonne degraded, the biogas production is of the order of 304 m3/day (CH4: 152 m3, CO2: 152 m3). With 10% self-consumption and losses, we have 274 m3 of biogas composed of 137 m3 of CH4 and approximately 137 m3 of CO2. This self-consumption may seem low at first glance. But it relates to a gas production much higher than what we usually encounter.

The last hydromethanization compartment receives the recirculated biogas, composed of CH4, CO2 and H2, produced in the hydrolysis compartment at approximately 70°C, through microporous diffusion ramps installed on the floor of this last compartment .

The production of endogenous hydrogen in hydrolysis at 70°C is of the order of 221 m3. To produce biomethane with approximately 96% CH4, we need 546 m3 of hydrogen.

The remainder of around 325 m3 is produced on site by electrolysis or reforming.

On the basis of 4 m3 of H2 to reduce 1 m3 of CO2 and an efficiency of 92%, we produce 126 m3 of CH4 which added to the 137 m3 of methane net from the biogas makes a total of 263 m3 of methane. The residual CO2 of around 11 m3 gives a CH4 rate on biomethane of approximately 96%.

In this last compartment, the biogas thus produced containing methane, hydrogen and CO2 is recirculated at a flow rate equivalent to a hydraulic residence time of around 24 hours. The size of this last compartment is adapted to this duration. This compartment must be cooled to operate at approximately 35°C. This heat is advantageously used in preheating the hydrolysis compartment.

In this process, the CO2 of the biogas is reduced by endogenous hydrogen, possibly supplemented by exogenous hydrogen, on a bacterial support made of digestate poor in biodegradable organic matter, sufficiently renewed to provide the nitrogen necessary for the development of hydrogenophilic bacteria. producing methane according to the reaction C02+ 4 H2 = CH4 + 2 H2O.

The renewal of the substrate serving as bacterial support is renewed by a third per day. This makes it possible to provide the necessary nitrogen and the conservation of hydrogenophilic bacteria whose theoretical division speed is a few hours.

The volume production is 3.19 m3 of biomethane produced / m3 fermenter.

Table 4 below gives an example of operation of a device according to the invention:

FERMENTER VOLUME T. Day M.S. MO TSH MS rate Substrate Flight Flight Substrate 25% 85% Total Incoming Incoming Useful M3 Total 2.40 0.60 0.51 16 16% 3.75 60 86

The templates established by road and rail regulations are as follows (dimensions are in meters or cubic meters):

- SNCF WAGON:

Height/Width/Length/Tare/Volume

2.81 /1.98 /15.55 /18.6 /86.5

- Road template:

Width / Length / Road Train / Height

2.5 / 12 / 18 / 4.3

Claims (10)

Compartmental viscous micro-hydro-methanization device intended for the production of biomethane from organic waste, consisting of a compartmentalized fermenter constructed from prefabricated panels, characterized in that it comprises:

• A thermo-enzymatic hydrolysis compartment (1) maintained at a hyperthermophilic temperature, suitable for the destructuring of said organic waste and the production of hydrogen,
• At least two methanization compartments (2) maintained at a thermophilic temperature,
• A hydromethanization compartment (3), with a volume of the order of approximately 1/12 of the cumulative volume of compartments (1) and (2), containing a bacterial support made of digestate depleted in biodegradable organic matter suitable for renewal of hydrogenophilic bacteria, allowing the reduction of CO2 by hydrogen into methane.

Device according to claim 1, characterized in that said prefabricated panels are mounted on the installation site of the device, said prefabricated panels including reservations for receiving and fixing the equipment, in particular the measuring and control devices, and being provided with 'an interlocking system. Device according to claim 1 or 2, in which in the first hydrolysis compartment (1), the pH is regulated to approximately 5.5, thanks to the hyperthermophilic temperature. Device according to one of claims 1 to 3, comprising means for re-introducing the biogas produced in the hydrolysis (1) and methanization (2) compartments into the last hydromethanization compartment (3). Device according to one of claims 1 to 4, comprising means for adjusting the partial pressure of carbon dioxide in the closed gas sky of the last hydromethanization compartment (3) receiving the recirculated biogas, composed in particular of CH4, CO2 and hydrogen, to which exogenous hydrogen is optionally added. Device according to one of claims 1 to 5, comprising means for renewing each day a third of the bacterial support made of digestate depleted of organic matter in the hydromethanization compartment (3). Device according to one of claims 1 to 6, characterized in that it comprises diversion plates distributed over all the floors of each compartment, allowing the injection of compressed biogas. Device according to one of claims 1 to 7, characterized in that it comprises a control system which integrates the measured or evaluated data of production of gas, hydrogen, CO2, which regulates the pressures in the gas sky , in particular of the last hydromethanization compartment, which regulates transfers from one compartment to another and the renewal rate of the digestate supporting hydromethanation, which calculates and optimizes the partial pressure of the compartments by controlling the regulation valves on the gas outlets and which adjusts the flow rates, duration and frequency of agitation and homogenization of the substrate in each compartment. Device according to one of claims 1 to 8, characterized in that said prefabricated panels have dimensions allowing their transport by truck or train. Device according to claim 9, characterized in that said dimensions are of the order of:
- width: between 1.60 m and 2.10 m;
- useful height: between 1.90 m and 3 m;
- length less than 16 m.