EP4526422A1 - Anlage und verfahren zur herstellung von biomethan - Google Patents

Anlage und verfahren zur herstellung von biomethan

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Publication number
EP4526422A1
EP4526422A1 EP23726333.0A EP23726333A EP4526422A1 EP 4526422 A1 EP4526422 A1 EP 4526422A1 EP 23726333 A EP23726333 A EP 23726333A EP 4526422 A1 EP4526422 A1 EP 4526422A1
Authority
EP
European Patent Office
Prior art keywords
unit
biogas
biomethane
retentate
catalytic reaction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP23726333.0A
Other languages
English (en)
French (fr)
Inventor
Solène VALENTIN
François BARRAUD
Daniel Gary
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP4526422A1 publication Critical patent/EP4526422A1/de
Pending legal-status Critical Current

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    • 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
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    • B01D53/225—Multiple stage diffusion
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    • B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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Definitions

  • the present invention relates to an installation and process for producing biomethane.
  • the invention relates more particularly to an installation for producing deoxygenated biomethane having an oxygen concentration lower than a determined threshold, in particular lower than 100 ppm, from biogas, as well as a corresponding process.
  • Biogas is the gas produced during the degradation of organic matter in the absence of oxygen (anaerobic fermentation) also called methanization. This may be a natural deterioration observed in marshes or household waste dumps.
  • the production of biogas can also result from the methanization of waste in a dedicated reactor, the conditions of which are controlled. This reactor is called a methanizer or digester, then in a post-digester, similar to the digester and allowing the methanization reaction to be taken further.
  • Biomass is any group of organic materials that can be transformed into energy through this methanization process, for example sewage treatment plant sludge, manure/slurry, agricultural residues, and food waste.
  • Biogas mainly contains methane (CH 4 ) and carbon dioxide (CO 2 ) in varying proportions depending on the method of production and the substrate but can also contain, in smaller proportions, water and nitrogen. , hydrogen sulphide (H 2 S), oxygen, as well as other organic compounds, in trace amounts, including H 2 S, between 10 and 50,000 ppmv.
  • CH 4 methane
  • CO 2 carbon dioxide
  • H 2 S hydrogen sulphide
  • oxygen oxygen
  • trace amounts including H 2 S, between 10 and 50,000 ppmv.
  • biogas contains (in mole or volume) on dry gas, from 30 to 75% methane, from 15 to 60% carbon dioxide. , 0 to 15% nitrogen, 0 to 5% oxygen and trace compounds such as sulfur, chlorine, halogen and volatile organic compounds (VOCs).
  • Biogas can be valorized in different ways. It can, after light treatment, be recycled near the production site to provide heat, electricity or a mixture of the two (cogeneration); the high carbon dioxide content reduces its calorific value, increases compression and transport costs and limits the economic interest of its recovery for this local use.
  • Biomethane thus complements natural gas resources with a renewable part produced in the heart of the territories; it can be used for exactly the same uses as natural gas of fossil origin. It can supply a natural gas network, a filling station for vehicles, it can also be liquefied to be stored in the form of liquid natural gas (bioLNG).
  • bioLNG liquid natural gas
  • deoxygenation systems There are deoxygenation systems.
  • the catalytic deoxygenation of argon is usually carried out at low temperature, for example below 200°C and the deoxygenation of methane or biogas by catalysis is carried out at higher temperature, for example above 200°C.
  • the biogas passes through a bed of activated carbon eliminating so-called poisonous impurities such as sulfur (H 2 S, C 2 H 6 S, COS, etc.). If these carbons are not replaced in time, or if they fail, these impurities can become poisons in a catalytic deoxygenation system.
  • poisonous impurities such as sulfur (H 2 S, C 2 H 6 S, COS, etc.). If these carbons are not replaced in time, or if they fail, these impurities can become poisons in a catalytic deoxygenation system.
  • This invention provides a catalytic reactor in the biogas purification procedure to significantly remove the oxygen present in the biomethane.
  • Such an installation makes it possible to achieve ultrapurification of the biogas, by reducing the O 2 content present in the biomethane to a level below 100 ppm, in particular below 1 ppm.
  • biogas we mean raw biogas or the flow of raw biogas leaving a biogas production unit, in particular a digester, containing, in mole or volume, from 30 to 75% methane, from 15 to 60 % carbon dioxide, as well as at least one of: water, nitrogen, hydrogen sulfide, oxygen, and/or volatile organic compounds (VOCs).
  • a digester containing, in mole or volume, from 30 to 75% methane, from 15 to 60 % carbon dioxide, as well as at least one of: water, nitrogen, hydrogen sulfide, oxygen, and/or volatile organic compounds (VOCs).
  • VOCs volatile organic compounds
  • deoxygenated biogas we mean indifferently the biogas or the flow of biogas leaving the catalytic reaction unit after the deoxygenation step.
  • biomethane we mean indifferently biomethane and the flow of biomethane leaving the biogas purification unit, or purified biogas, comprising by molar mass or by volume, for example less than 5% of carbon dioxide and less than 1% of oxygen (volume and molar quantity being equivalent in the case where the ideal gas equation is used).
  • deoxygenated biomethane we mean indifferently biomethane and the flow of biomethane leaving the catalytic reaction unit after the deoxygenation step.
  • partially purified biogas we mean the biogas being purified to eliminate or reduce the level of impurities and/or carbon dioxide or the biogas taken from the purification unit, enriched in methane compared to the biogas and enriched in carbon dioxide compared to biomethane.
  • a partially purified biogas is for example a first retentate leaving the first membrane separation unit.
  • partially purified deoxygenated biogas we mean indifferently the partially purified biogas and the stream of partially purified biogas or a first retentate leaving the catalytic reaction unit after the deoxygenation step.
  • guard bed we mean a bed of protective particles aimed at trapping so-called poisonous impurities, such as sulfur, chlorine, halogen, or VOCs, likely to be contained in biogas or biomethane or the partially purified biogas to enter the catalytic reaction unit.
  • the invention may also relate to any alternative device or method comprising any combination of the characteristics above or below.
  • FIG. 1 represents a schematic and partial view illustrating a fourth embodiment of the structure and operation of an installation according to the invention.
  • FIG. 1 represents a schematic and partial view illustrating a fifth embodiment of the structure and operation of an installation according to the invention.
  • FIG. 1 represents a schematic and partial view illustrating a sixth embodiment of the structure and operation of an installation according to the invention.
  • FIG. 1 represents a schematic and partial view illustrating an example of structure and operation of a catalytic reactor which can be used within the installation according to the invention.
  • the installation shown in is an example of a biomethane production device 10.
  • the installation comprises a fluid circuit comprising an upstream end intended to be connected to a biogas source, for example the outlet of a biogas production unit, a particular digester, to receive a flow of biogas 1 and a downstream end configured to supply biomethane 10.
  • the installation comprises, between its upstream and downstream ends, a biogas purification unit 5, in particular a carbon dioxide separation unit, capable and configured to produce biomethane 9 whose essential (majority) component is methane ( CH 4 ) and further comprising, in molar or volume, less than 5% CO 2 and less than 1% O 2 , in particular less than 3% CO 2 and less than 0.7% O 2 .
  • the installation may include, upstream of the purification unit 5, a heat exchanger to adjust the temperature of the gas flow supplying the purification unit 5.
  • the purification unit 5 may comprise a PSA type unit and/or a washing type unit, in particular an absorption treatment unit by means of a washing column and/or a membrane permeation treatment unit comprising, for example, at least two separation units per membrane.
  • the membrane permeation processing unit may include three or four (or more) membrane separation units.
  • Each membrane separation unit may include one or more membranes connected in parallel.
  • the membrane permeation treatment unit comprises three membrane separation units, of which the first membrane separation unit and the second membrane separation unit are arranged in series in the circuit. The first membrane separation unit and the third membrane separation unit are connected in parallel.
  • One of the flows coming from the second membrane separation unit and/or one of the flows coming from the third membrane separation unit can be recycled to supply the membrane permeation treatment unit.
  • the installation may include at least one pressure control member such as one or more proportional valves and/or or at least one temperature control unit such as heat exchanger(s).
  • the installation comprises at least one catalytic reaction unit 3 comprising at least one bed of at least one oxidation catalyst configured to deoxygenate the biogas before it enters the purification unit 5. That is to say that the catalytic reaction unit 3 comprising at least one bed of at least one oxidation catalyst is located upstream of the purification unit 5 to deoxygenate the biogas flow 1.
  • catalytic reaction unit 3 is configured to bring the biogas into contact with at least one bed of at least one oxidation catalyst of the catalytic reaction unit 3.
  • the oxidation catalyst is preferably an oxidation catalyst oxidation of methane.
  • This oxidation catalyst comprises a catalyst bed which may comprise particles of at least one precious metal, for example chosen from Pd, Pt and Rh.
  • precious metals for example chosen from Pd, Pt and Rh.
  • one or more of these precious metals is deposited on at least one oxide inorganic metallic, for example chosen from Al 2 O 3 , ZrO 2 , TiO 2 , ZnO, MgO and CaO, in particular chosen from Al 2 O 3 , ZrO 2 and TiO 2 .
  • the bed of the oxidation catalyst (in particular a methane oxidation catalyst) may comprise particles of at least one transition metal, for example chosen from Cu and Ni.
  • One or more of these metals is deposited on or mixed with at least one inorganic metal oxide, for example chosen from Al 2 O 3 , ZrO 2 and TiO 2 , ZnO, MgO and CaO, in particular chosen from ZnO, MgO and CaO.
  • inorganic metal oxide for example chosen from Al 2 O 3 , ZrO 2 and TiO 2 , ZnO, MgO and CaO, in particular chosen from ZnO, MgO and CaO.
  • the installation further comprises a compressor 2 upstream of the catalytic reaction unit 3.
  • this compressor could be placed downstream of the catalytic reaction unit 3.
  • Compressor 2 is a device or system configured to compress raw biogas 1 received from a biogas production unit upstream of the installation and/or pretreated biogas.
  • the compressor 2 may be a medium pressure compressor lubricated with oil or water or not, configured to increase the pressure and make it possible to effectively ensure the separation of carbon dioxide from methane in the purification unit 5.
  • An oil removal system can be placed downstream of the compressor 2 to avoid contamination of the purification unit 5 and/or the catalytic reaction unit 3 by oil.
  • the installation can comprise, in particular upstream of the compressor 2 and the catalytic reaction unit 3, a pretreatment unit 14 configured to eliminate at least part of the water and at least part of the water and /or hydrogen sulfide and/or VOCs present in biogas 1.
  • This pretreatment unit 14 may include a booster, a blower or a compressor to have sufficient pressure for the passage of the gas in the other stages and/or a drying unit by condensation of the water, in particular at 5°C, and/or at least one bed of activated carbons to preferentially remove hydrogen sulphide and VOCs.
  • the pretreatment unit 14 can be arranged starting with a drying unit configured to eliminate at least part of the water included in the raw biogas 1.
  • the raw biogas leaving the drying unit can then be received by a blower to achieve sufficient pressure for the passage of gas in the following stages.
  • the installation may comprise at least one hydrogen sulphide elimination unit, in particular two hydrogen sulphide elimination units, connected in parallel, whose activated carbon is selected to preferentially eliminate the hydrogen sulfide present in biogas 1.
  • the installation can also include a VOC elimination unit connected in series to the hydrogen sulfide elimination unit and whose activated carbon is selected to preferentially eliminate the VOCs present in biogas 1.
  • the installation may comprise, upstream of the catalytic reaction unit 3 and/or upstream of the purification unit 5, an impurity elimination unit 15 configured to eliminate at least one impurity chosen from sulfur, chlorinated, halogenated, and VOCs.
  • the impurity elimination unit 15 may comprise at least one guard bed comprising particles of at least one metal oxide of at least one metal chosen from transition metals.
  • the at least one guard bed comprises particles of at least one metal oxide, for example a metal peroxide, a transition metal oxide and/or a transition metal oxide doped with another transition metal.
  • the at least one guard bed comprises a mixture comprising at least one, two or more or all of the following oxides: zinc oxide, zinc oxide doped with copper, alumina, alumina doped with potassium, and manganese peroxide.
  • the removal of impurities in the impurity removal unit 15 is for example carried out at a temperature greater than or equal to 150°C, in particular between 150°C and 400°C, preferably between 300°C and 400°C.
  • a heat exchanger or heater can be provided for this purpose, for example upstream of or in said impurity elimination unit 15.
  • the impurity removal unit 15 and the catalytic reaction unit 3 can be integrated into a single catalytic reactor. More particularly, the at least one guard bed and the at least one bed of at least one oxidation catalyst can be integrated into a single catalytic reactor. The reactor feed gas thus passes through the at least one guard bed, and then through the at least one oxidation catalyst.
  • the installation also preferably includes a pressure control valve 13 located in or downstream of the biogas purification unit 5.
  • the pressure control valve 13 is for example a valve of the proportional type and configured to control the pressure of the supply to the purification unit 5.
  • the opening/closing of this valve 13 makes it possible to adjust the pressure within the purification unit 5 and/or within the catalytic reaction unit 3.
  • the supply pressure of the purification unit 5 ensures the quality of the biomethane in terms of carbon dioxide.
  • the proportional valve 13 is closed (at least partially) and therefore the supply pressure of the purification unit 5 is increased, when the carbon dioxide level is higher than the required quality.
  • the proportional valve 13 is open (at least partially) and therefore the supply pressure of the purification unit 5 is reduced, when the carbon dioxide level is lower than the required quality.
  • the installation shown in is another example of a biomethane production device 10.
  • the embodiment of the is distinguished from that of the essentially in that the catalytic reaction unit 3 is integrated into the biogas purification unit 5, for example between different membrane separation units or stages when the purification unit is a membrane permeation treatment unit.
  • the installation shown in is another example of a biomethane production device 10 which differs from the previous examples in that the catalytic reaction unit 3 is located downstream of the purification unit 5.
  • the catalytic reaction unit 3 is configured to bring the biomethane obtained from the purification unit 5 into contact with at least one bed of at least one oxidation catalyst from the catalytic reaction unit 3.
  • the biomethane brought into contact with at least one bed of at least one oxidation catalyst of the catalytic reaction unit 3 comprises for example, in molar or volume, less than 5% CO 2 and less than 1% O 2 , in particular less than 3% CO 2 and less than 0.7% O 2 .
  • the installation may include a compressor 2 located upstream of the catalytic reaction unit 3 and/or upstream of the purification unit 5 and/or downstream of the purification unit 5.
  • the compressor 2 can be configured to compress the raw biogas 1 received directly from a biogas production unit upstream of the installation and/or the biomethane leaving the purification unit 5.
  • the installation may also include at least one heat exchanger or heater 17 configured to heat the at least one catalytic reaction unit 3 and/or the gas entering the catalytic reaction unit 3.
  • the at least one heat exchanger or heater 17 can be located upstream of the catalytic reaction unit 3 and configured to heat the feed gas of the catalytic reaction unit 3 for example by indirect contact with the gas produced by the catalytic reaction unit 3.
  • the installation may include a unit for controlling the temperature of the gas, in particular produced by the catalytic reaction unit 3, in order to ensure the quality of the gas leaving the catalytic reactor, in terms of oxygen content.
  • a temperature control unit can ensure the quality of the deoxygenated biomethane produced, in terms of oxygen content in the biomethane.
  • the temperature control unit comprises for example a heat exchanger 17 allowing indirect contact of the feed gas and the product gas of the catalytic reaction unit 3.
  • the temperature control unit may comprise a line by-pass 90 of the heat exchanger 17 including a valve 91, for example a proportional valve, in order to control/limit the flow of the feed gas which is circulated in the heat exchanger 17 before enter the catalytic reaction unit 3 and a controller 16, for example an automaton or a computer, comprising a microprocessor.
  • the controller 16 can be configured to control or limit the flow rate of the gas, for example produced by the catalytic reaction unit 3, which circulates in the heat exchanger 17 by opening the proportional valve 91 when the temperature of the gas produced is higher at the operating temperature for obtaining the correct oxygen content or the composition of the deoxygenated gas, in particular for obtaining the composition of the deoxygenated biomethane 10.
  • the operating temperature within the catalytic reaction unit 3 is in particular between 280°C and 450°C, preferably between 280°C and 390°C or between 380°C and 420°C.
  • the installation may include an analyzer 18, for example an oxygen analyzer analyzing the gas flow in the circuit and whose measurement signal is sent to the controller 16.
  • an analyzer 18 for example an oxygen analyzer analyzing the gas flow in the circuit and whose measurement signal is sent to the controller 16.
  • the controller 16 proceeds to close the proportional valve 91 to obtain the increase in temperature via the heat exchanger 17.
  • the analyzer 18 is preferably located downstream of the purification unit 5 and the catalytic reaction unit 3.
  • the installation also preferably comprises a pressure control valve 13 located downstream of the biogas purification unit 5, and/or the catalytic reaction unit 3.
  • the pressure control valve 13 is for example a valve of the proportional type and configured to control the supply gas pressure of the purification unit 5.
  • the opening/closing of this valve 13 makes it possible to adjust the pressure within the purification unit 5 and/or at within the catalytic reaction unit 3.
  • the operating pressure within the catalytic reaction unit 3 can be maintained above atmospheric pressure, preferably between 5 and 20 bar, in particular between 8 and 15 bar.
  • the supply gas pressure of the purification unit 5 ensures the quality of the biomethane in terms of carbon dioxide content.
  • the supply gas pressure of the purification unit 5 is in particular between 8 and 15 barg.
  • the proportional valve 13 When the carbon dioxide level is higher than the required quality, for example higher than 3%, the proportional valve 13 is closed and therefore the supply pressure to the purification unit 5 is increased. This increases the efficiency of the purification of carbon dioxide within the purification unit 5. Conversely, when the level of carbon dioxide is lower than the required quality, for example lower than 2%, the proportional valve 13 is open at least partially and in reaction the supply pressure of the purification unit 5 is reduced.
  • the installation shown in is another example of a biomethane production device 10 which differs from the embodiment of the in that the purification unit 5 comprises three membrane separation units.
  • the catalytic reaction unit 3 is in particular located upstream of a first membrane separation unit 5a.
  • the first membrane separation unit 5a (or the first membrane separation stage) can be provided with several suitable parallel membranes and is configured to receive the biogas and provide a first permeate 6 and a first retentate 7.
  • the second membrane separation unit 5b (or the second membrane separation stage) can be provided with several suitable parallel membranes and is configured to receive the first retentate 7 and provide a second permeate 8 and a second retentate 9 also called biomethane.
  • the installation can also include, upstream of the second membrane separation unit 5b, a heat exchanger (not shown for the sake of simplification) configured to adjust the temperature of the gas flow entering the second membrane separation unit 5b. This heat exchanger ensures the quality of biomethane 9 in terms of carbon dioxide by increasing the selective permeation of carbon dioxide by reducing the temperature if necessary.
  • the third membrane separation unit 5c (or the third membrane separation stage) can be provided with several membranes in parallel and is capable and configured to receive the first permeate 6 and provide a third permeate 11 and a third retentate 12.
  • the first membrane separation unit 5a is able to receive the flow of compressed and deoxygenated biogas 1 leaving the catalytic reaction unit 3 and to provide a first permeate 6 enriched in carbon dioxide relative to the biogas 1 and a first retentate 7 enriched in methane compared to biogas 1.
  • the second permeate 8 and/or the third retentate 12 is recycled upstream of the compressor 2.
  • the pressure control valve 13 is located downstream of the second membrane separation unit 5b on the second retentate 9 which is the deoxygenated biomethane 10.
  • the installation can also include, downstream of the third retentate 12, a control valve configured to adjust the level of methane in the permeate 11 which is discharged to the vent and therefore limit the loss of methane.
  • the installation shown in is another example of a biomethane production device 10 which differs from that of the essentially in that the catalytic reaction unit 3, comprising at least one bed of at least one oxidation catalyst, is located downstream of the first membrane separation unit 5a and configured to deoxygenate the first retentate 7 before its entry into the second membrane separation unit 5b. That is to say that the deoxygenated gas flow, in particular the first deoxygenated retentate 7, leaving the catalytic reaction unit 3 is then received by the second membrane separation unit 5b to provide the second permeate 8 and the second retentate 9 which is deoxygenated biomethane 10.
  • the deoxygenation step is carried out in the catalytic reaction unit 3 by bringing the first retentate 7 into contact with at least one bed of at least one oxidation catalyst of the unit catalytic reaction 3.
  • the installation can also include a gas temperature control unit as illustrated in in which an analyzer 18 is preferably located downstream of the first membrane separation unit 5a and the catalytic reaction unit 3.
  • a pressure control valve 13 is located downstream of the second membrane separation unit 5b on the second retentate 9 which is deoxygenated biomethane 10.
  • the installation can also include, downstream of the catalytic reaction unit 3 and upstream of the second membrane separation unit 5b, a heat exchanger (not shown for the sake of simplification) configured to adjust the temperature of the gas flow entering the second membrane separation unit 5b.
  • Said heat exchanger is preferably located downstream of the unit for controlling the temperature of the gas leaving the catalytic reactor 3 as described above with reference to the . This heat exchanger ensures the quality of biomethane 9 in terms of carbon dioxide by increasing the selective permeation of carbon dioxide by reducing the temperature if necessary.
  • the catalytic reaction unit 3 By placing the catalytic reaction unit 3 on the retentate 7 of the first membrane separation unit 5a, it is possible to limit the flow rate treated by the catalytic reaction unit 3 and to benefit from the second membrane unit 5b to separate the carbon dioxide produced in the catalytic reaction unit 3. Such a location of the catalytic reaction unit 3 is also advantageous because this catalytic reaction deoxygenation device produces water and CO 2 .
  • the second membrane separation stage 5b separates the water and the produced CO 2 in order to achieve the quality of biomethane required. No investment in additional equipment is necessary to achieve this quality of biomethane at the outlet of the second membrane separation stage 5b and there is no additional electricity consumption.
  • the gas treated by the catalytic oxidation in the catalytic reaction unit 3 still contains a significant CO 2 content.
  • This CO 2 inert during the reaction will be heated by exothermicity of the reaction and the maximum temperature reached to obtain the total conversion will be lower.
  • the installation shown in is another example of a biomethane production device 10 which differs from that of the essentially in that the catalytic reaction unit 3 is located downstream of the second membrane separation unit 5b. That is to say that the catalytic reaction unit 3 is capable and configured to receive the flow of compressed biomethane 9 which is the second retentate 9 (and comprises, by volume, for example less than 3% of CO 2 and less than 0.7% O 2 , in particular less than 3% CO 2 and less than 0.7% O 2 ).
  • This unit 3 comprises at least one guard bed and at least one bed of at least one oxidation catalyst, in particular a methane oxidation catalyst.
  • the catalytic elimination of oxygen is carried out in the presence of methane present in the gas flow, in particular in biomethane or biogas, and its impurity consisting of oxygen, at a temperature between 280°C and 450°C, preferably between 280°C and 390°C or between 380°C and 420°C.
  • the contact time or residence time (Ts) of the gas flow passing through the oxidation catalyst bed is between 1s and 2.6s, at a predetermined volume of catalysts and at a temperature between 280°C and 450°C , more particularly between 380°C and 420°C.
  • the gas flow in particular biogas or biomethane, can, before entering the catalytic reaction unit 3, pass through a heat exchanger 17 for reheating.
  • the deoxygenated gas flow is cooled.
  • this cooling can be carried out in the aforementioned reheating heat exchanger 17. That is to say that the flows before and after deoxygenation can be put into thermal exchange in the same exchanger 17, in particular counter-current.
  • the installation can also include an adsorber 19 configured to eliminate by-products of the oxidation reaction, carbon dioxide and water, possibly contained in the deoxygenated gas flow.
  • the gas flow leaving the adsorber 19 then supplies the purification unit 5 or to the next unit in the installation, for example the unit included in the purification unit 5, for example to the second separation unit by membrane, when the catalytic reaction unit 3 is integrated into the purification unit 5 or brought to the pressure control unit 13.
  • the structure and operation of the catalytic reaction unit 3 demonstrated in the can apply to the catalytic reaction unit of any of the has .
  • the present invention also relates to a process for producing deoxygenated biomethane 10 which can be implemented by the installation for producing deoxygenated biomethane 10 described above.

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