EP3325692B1 - Procédé et réacteur de réduction électrochimique de dioxyde de carbone - Google Patents

Procédé et réacteur de réduction électrochimique de dioxyde de carbone Download PDF

Info

Publication number
EP3325692B1
EP3325692B1 EP16757367.4A EP16757367A EP3325692B1 EP 3325692 B1 EP3325692 B1 EP 3325692B1 EP 16757367 A EP16757367 A EP 16757367A EP 3325692 B1 EP3325692 B1 EP 3325692B1
Authority
EP
European Patent Office
Prior art keywords
carbon dioxide
cathode
anode
compartment
separator
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.)
Active
Application number
EP16757367.4A
Other languages
German (de)
English (en)
Other versions
EP3325692A1 (fr
Inventor
Robert Christiaan Franciscus DE KLER
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.)
Coval Energy Ventures BV
Original Assignee
Coval Energy Ventures BV
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 Coval Energy Ventures BV filed Critical Coval Energy Ventures BV
Publication of EP3325692A1 publication Critical patent/EP3325692A1/fr
Application granted granted Critical
Publication of EP3325692B1 publication Critical patent/EP3325692B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms

Definitions

  • the invention is directed to a method for electrochemically reducing carbon dioxide, and to an electrochemical reactor.
  • One possible way of mitigating carbon dioxide emissions is to convert carbon dioxide into economically valuable materials, such as fuels and industrial chemicals. If the carbon dioxide is converted using energy from renewable sources, both mitigation of carbon dioxide emissions and conversion of renewable energy into a chemical form that can be stored for later use will be possible.
  • An interesting alternative conversion process involves the electrochemical reduction of carbon dioxide. Toxic or hazardous reducing agents are then replaced by clean electrons. In this case, the high thermodynamic stability of carbon dioxide is by-passed by a simple one-electron reduction at an electrode, leading to in situ generation of reactive intermediates. Often, room temperature conditions are sufficient, considering that the energy of the electrons is determined by the applied voltage. Since the electrochemical reduction takes place on a cathode surface, the need for complex homogeneous organometallic catalysts is minimised. Furthermore, electricity will be increasingly of renewable origin in the future, making organic electro-synthesis a promising technology for environmentally friendly chemical processes.
  • the electrochemical reduction of carbon dioxide can be applied for the synthesis of fuels like formic acid, methanol or methane. This allows storage of electric energy from periodic sustainable origin, like solar or wind energy.
  • Electro-synthesis is typically carried out in an electrochemical reactor connected to an external voltage or current source.
  • the electrochemical reactors can be categorised into undivided and divided cells.
  • a divided cell has a cathode compartment with a cathode, an anode compartment with an anode, and an interface (or divider or separator) between cathode compartment and anode compartment.
  • the interface in a divided cell functions as a separator. It is a barrier for specific species while allowing the transport of other species.
  • the separator controls the flow of ions between the two compartments. In particular, the separator may selectively allow the transport of cations from the anode compartment into the cathode compartment while simultaneously preventing the transport of anions in the opposite direction.
  • the separator may selectively allow the transport of anions from the cathode compartment into the anode compartment while preventing the transport of cations in the opposite direction.
  • control over ion flow provides a means to enhance or enforce the desired reaction chemistry to occur in the fluids contained in the individual compartments with respective electrodes, and increase the current efficiency by preventing the cycling of species by sequential oxidation and reduction.
  • the electrochemical reduction of carbon dioxide is a promising application in the field of electrochemistry.
  • materials can be produced including formic acid, formates, carbon monoxide, hydrogen, syngas, methanol, methane, and propane.
  • Products and process efficiencies depend amongst others on cell configuration, cathode material, surface area of the electrode, porosity of the electrode, catalyst, electrolyte (anolyte as well as catholyte) participating in reaction chemistry or acting as pH buffer, and process conditions like temperature, pressure, applied fluid flow, (over)potential, etc.
  • a conventional configuration in the electrochemical reduction of carbon dioxide comprises a divided cell with a cation exchange membrane (proton exchange membrane or cation membrane) separating an aqueous anolyte and catholyte.
  • Protons from water splitting
  • /or cations from the specific anolyte transfer to the cathode compartment where they react with the reduced carbon dioxide.
  • Products formed are retained in the cathode compartment, while typically oxygen evolves at the anode.
  • US-A-2008/0 223 727 describes a continuous co-current electrochemical reduction of carbon dioxide using a catholyte mixture with a specific volume ratio of carbon dioxide gas and liquid catholyte solvent.
  • a fuel like hydrogen is fed as a gas to the anode compartment.
  • the protons produced by direct splitting of the hydrogen fuel at the anode, transfer through the cation exchange membrane to react with the reduced carbon dioxide as in the previously mentioned configuration.
  • an anion exchange membrane is employed as separator.
  • the reduction of carbon dioxide at the cathode under wet conditions leads to the production of hydroxide ions that transfer through the anion exchange membrane and react with a hydrogen fuel at the anode to produce water.
  • the product of the carbon dioxide reduction is retained in the cathode compartment.
  • Bipolar membrane technology is relatively unexplored and finds an increasing number of applications in electro-catalytic membrane reactors ( Balster et al., Chemical Engineering and Processing 2004, 43, 1115-1127 ).
  • a bipolar membrane is catalytically active and may contribute to electrochemical conversions.
  • Bipolar membranes are known to be part of electro-dialysis stack design, and are configured together with anion and cation exchange membranes.
  • a bipolar membrane is a synthetic membrane comprising two oppositely charged ion-exchanging layers in contact with each other. The bipolar membrane may be considered the combination of a cation exchange membrane and an anion exchange membrane. By this arrangement of charged layers, the bipolar membrane is not effective in transporting either cations or anions across the full width of the membrane, and is to be distinguished from the ion selective membranes employed in the conventional electrochemical reduction of carbon dioxide.
  • problems associated with the conventional electrochemical processes include low availability of gaseous reactant at atmospheric pressure, substantial over potentials at the electrodes (stack), a high internal resistance to overcome (low power density), co-transport of anolyte with protons through cation exchange membrane and competitive reaction of these with the anion in the cathode compartment and a requirement for a secondary chemical conversion outside the main electrochemical reactor, low water dissociation rate, difficulties in achieving full conversion of a liquid and a gaseous reactant in a single pass through an electrochemical reactor operated in continuous mode, integrity of a thin membrane during pressurisation or depressurisation in particular with a gaseous phase on one side and a liquid phase on the other side.
  • Objective of the invention is to overcome one or more of these problems faced in the prior art.
  • the invention is directed to a method for electrochemically reducing carbon dioxide, comprising
  • the separator participates in the intended reaction chemistry instead of only transferring either cations or anions as being state of the art in carbon dioxide electrochemical reduction employing a cation exchange membrane or an anion exchange membrane, respectively.
  • the method of the invention advantageously allows for high electric power density, low voltage over-potentials and a low internal resistance for electricity/electric current, a reactive layer with potential high services for direct gas/dense phase and liquid/supercritical phase conversion of carbon dioxide, a tremendously increased dissociation rate of water into H + and OH - in the separator as compared to the equilibrium dissociation rate of water, production of OH - at the internal interface in the membrane as compared to production at the anode, versatility to operate the electrochemical reactor in continuous, as well as in semi-continuous or batch mode, and prevention of mechanical rupture or leakage of the membrane during start up or shut down of the reactor.
  • the separator can comprise (or consist of) a bipolar membrane, a charge-mosaic membrane, or a layered mixture of anion and cation exchange resins.
  • a bipolar membrane is defined as a synthetic membrane comprising two oppositely charged ion-exchanging layers in contact with each other.
  • a charge-mosaic membrane is defined as a membrane having a charge structure comprised of cation-exchange domains and anion-exchange domains which are alternately aligned and each of which penetrates the membrane from one side to the other side.
  • the separator may also be a permeable layer confining a mixture of a cation exchange resin and an anion exchange resin.
  • the separator comprises or consists of a bipolar membrane.
  • the separator may be in direct electrical contact with the cathode and/or anode of the electrochemical reactor.
  • the separator may be in indirect electrical contact with the cathode and/or anode of the electrochemical reactor via an electrically conductive liquid, such as an electrolyte, or more specifically a catholyte or anolyte.
  • the method of the invention may be performed in various embodiments that allow reduction of carbon dioxide using different configurations of the electrochemical reactor.
  • water can be split at the separator, thereby producing OH - ions and H + ions.
  • the feed with carbon dioxide (which can be present in different forms such as carbon dioxide, carbonic acid, bicarbonate, carbonate, etc .) can be reduced in the cathode compartment while consuming the H + ions, and the OH - ions can be oxidised in the anode compartment between to produce water.
  • the separator preferably comprises a cation exchange layer and an anion exchange layer in contact with each other at a junction, wherein the cation exchange layer faces the cathode and the anion exchange layer faces the anode.
  • This configuration may be represented by the following overall reactions.
  • the net result of these three reactions is: CO 2 + H 2 O ⁇ HCOOH + 1 ⁇ 2 O 2 (4)
  • This exemplary configuration is shown in figure 1 , wherein an electrochemical reactor 100 comprises a cathode compartment 110, a separator 120, and an anode compartment 130.
  • carbon dioxide can be reduced in the cathode compartment (where the carbon dioxide can be present in different forms such as carbon dioxide, carbonic acid, bicarbonate, carbonate, etc .) , thereby producing OH - ions.
  • water can be oxidised to produce H + ions.
  • the OH - ions and H + ions can be recombined at the separator, thereby producing water.
  • the separator preferably comprises a cation exchange layer and an anion exchange layer in contact with each other at a junction, wherein the anode exchange layer faces the cathode and the cation exchange layer faces the anode.
  • This configuration may be represented by the following overall reactions.
  • the net result of these three reactions is: CO 2 + H 2 O ⁇ HCOOH + 1 ⁇ 2 O 2 (4)
  • This exemplary configuration is shown in figure 2 , wherein an electrochemical reactor 100 comprises a cathode compartment 210, a separator 220, and an anode compartment 230.
  • the separator comprises a cation exchange layer and an anion exchange layer in contact with each other at a junction, wherein the cation exchange layer faces the cathode and the anion exchange layer faces the anode.
  • the separator comprises a cation exchange layer and an anion exchange layer in contact with each other at a junction, wherein the anion exchange layer faces the cathode and the cation exchange layer faces the anode.
  • the electrochemical reactor can advantageously be free of liquid electrolyte, such as catholyte and/or anolyte.
  • the electrochemical reactor is free of catholyte.
  • the cathode and bipolar membrane can be in direct contact in order to minimise electrical resistance.
  • Carbon dioxide can, for example be supplied as dense gas to the cathode compartment, and water may be supplied either to the cathode compartment or to the anode compartment in the appropriate amount to wet the cathode and anode structure thereby forming a reactive layer.
  • the absence of liquid electrolyte is highly preferred, as the presence of liquid electrolyte can lead to the production of undesirable by-products.
  • the method may be operated continuously, semi-continuously, or in batch. It is preferred to perform the method of the invention in a continuous mode.
  • the method of the invention further comprises releasing oxygen from the anode compartment, and collecting reduced carbon dioxide product or product mixture from the cathode compartment.
  • the reduced carbon dioxide product or product mixture can comprise one or more components from a group of molecules referred to as platform chemicals, such as alkanes, alkenes, syngas, carboxylic acids, alcohols, including diols, aldehydes, and ketones. More specifically, the carbon dioxide product or product mixture can comprise one or more components selected from the group consisting of carbon monoxide, hydrogen, syngas, formic acid, a formate, methanol, acetaldehyde, methane, and ethane. Preferably, the reduced carbon dioxide or product mixture comprises one or more selected from the group consisting of methanol, formic acid, a formate, and acetaldehyde. Accordingly, the method can involve the conversion of carbon dioxide into one or more of these compounds. In a preferred embodiment, the method comprises the conversion of carbon dioxide to formic acid. The product that is obtained may be controlled by varying the applied voltage.
  • platform chemicals such as alkanes, alkenes, syngas, carboxylic acids, alcohols
  • a water feed is introduced into the anode compartment.
  • This water feed may be supplied in liquid form, in vapour form or in gaseous form.
  • the water feed comprises at least water, but may further comprise other components such as one or more selected from the group consisting of pH control agents, conductivity control agents, and reactivity inhibitors. It is also possible that the water feed is water.
  • the water feed is a feed that has water as main component.
  • a carbon dioxide feed is introduced into the cathode compartment.
  • This carbon dioxide feed may be supplied in one of the following phase, as a supercritical phase, in a liquid phase, in a dense phase, in a vapour phase or in a gaseous phase.
  • the carbon dioxide feed is in a dense phase.
  • dense phase carbon dioxide refers to carbon dioxide in either liquid form or supercritical form.
  • the carbon dioxide itself may be liquid, or it may be a solute in a liquid solvent, such as water.
  • the carbon dioxide feed comprises at least carbon dioxide, but may further comprise other components, such as one or more selected from the group consisting of water droplets, aerosols, pH control agents, conductivity control agents, and compounds for mediated electrochemical conversion.
  • the carbon dioxide feed is a feed that has carbon dioxide as main component.
  • the carbon dioxide feed comprises a majority of carbon dioxide and a minority of water.
  • the carbon dioxide feed is pre-conditioned in a dedicated vessel to obtain high concentrations of reactive species (CO 2 , carbonic acid, bicarbonate, and carbonate) for carbon dioxide reduction.
  • the carbon dioxide feed is suitably pre-conditioned in terms of pressure, temperature, and pH, and preferably consists of a mixture of carbon dioxide and water with an excess of carbon dioxide.
  • the carbon dioxide is preferably fed to the reactor in a dense phase and water is preferably partly solubilised in the dense carbon dioxide phase, whereby the dense phase carbon dioxide will be highly concentrated with ionic reactive species.
  • reactive species are formed by a reaction between water and the carbon dioxide during the pre-conditioning step, and (additional) ionic reactive species can be formed during the contacting in the electrochemical reactor of the dense phase carbon dioxide with the membrane where the membrane is saturated with water.
  • the pressure of the carbon dioxide feed is preferably 20 bara or more, such as 30 bara or more, even more preferably 50 bara or more, and most preferably 60 bara or more. Usually, the pressure of the carbon dioxide feed will not exceed 200 bara. More preferably, the pressure of the carbon dioxide feed will be 150 bara or less, even more preferably 100 bara or less, and most preferably 80 bara or less.
  • the carbon dioxide feed may have a density of 10-1000 kg/m 3 , preferably a density of 100-980 kg/m 3 , and more preferably a density of 600-960 kg/m 3 .
  • Both water feed and carbon dioxide feed may be introduced into the electrochemical reactor continuously or intermittently. It is also possible to introduce the water feed and carbon dioxide feed into the electrochemical reactor in a batch wise fashion.
  • This oxygen can be released from the anode compartment via an anode compartment outlet. It is preferred that the rate of introducing the carbon dioxide feed and the rate of releasing the oxygen is monitored and controlled. This may be realised, for instance, by releasing oxygen when the absolute pressure thereof is 0.2 bar or more higher than the pressure of the carbon dioxide feed, preferably 0.3-1.0 bar higher than the pressure of the carbon dioxide feed, and more preferably 0.4-0.8 bar higher than the pressure of the carbon dioxide feed. This control can advantageously prevent mechanical damages by avoiding large pressure differences in the system.
  • the pressure difference between the anode and the cathode compartment i.e. the pressure difference over the membrane
  • the oxygen maybe released, for instance, when the pressure difference between the anode and the cathode compartment is 0.2 bar or more, preferably in the range of 0.2-1.0 bar pressure difference, and more preferably in the range of 0.3-0.8 bar pressure difference.
  • This control of the feeding and the release of the various streams can be achieved, by an advanced pressure control system, employing pressure transducers, pressure transmitters, pressure controllers, and pressure differential transducers.
  • the carbon dioxide feed can be fed to the electrochemical reactor at a fixed pressure (e.g . in the range of 20-100 bara), thereby guaranteeing an automatic supplementation of this reactant. Fluctuations in the water feed can be damped by using, for example, an expansion chamber, pusher bellows, etc.
  • a (pre)conditioning step is included for both the water feed stream and the carbon dioxide feed stream.
  • a pressurised, thermostatic vessel or hydraulic accumulator is employed to assure stable pressure and temperature levels for the feed streams.
  • a basic process flow diagram of the main process steps including the most relevant instrumentation for pressure control is depicted in figure 3 .
  • the water feed supplied at the anode can be in direct contact with the produced gaseous oxygen.
  • the pressure thereof can be at an absolute pressure with a set-point for a control valve to release oxygen slightly higher than the carbon dioxide feed pressure, for example 0.5 bar higher than the carbon dioxide feed pressure.
  • the pressure difference over the membrane and the pressure difference between the various streams will not exceed the pressure of the operational window.
  • the pressure difference over the membrane should be in the range of 0.3-0.8 bar.
  • the command signal for the valve can be derived from a sensor that monitors an absolute pressure.
  • the liquid reactants contact the pressure hull of the vessel.
  • a sensor may be employed that monitors a pressure differential between the carbon dioxide feed and released oxygen and controls and overrules the absolute pressure signal command.
  • the pressure differential signal can affect the operation of a valve connected to the cathode compartment inlet to adjust the rate of carbon dioxide feed introduction and a valve at the anode compartment outlet to adjust the rate of oxygen release.
  • the discharge rate of the reduced carbon dioxide product or product mixture may be controlled using a control valve connected to the cathode compartment outlet.
  • the pressure in the electrochemical reactor is 20 bara or more, preferably 30 bara or more, even more preferably 50 bara or more, and most preferably 60 bara or more. Usually, the pressure in the electrochemical reactor will not exceed 200 bara. More preferably, the pressure in the electrochemical reactor will be 150 bara or less, even more preferably 100 bara or less, and most preferably 80 bara or less.
  • an overpressure is maintained in the anode compartment with respect to the cathode compartment.
  • the separator divides the reactor in two compartments, wherein the anode compartment suitably contains a liquid phase (such as an aqueous liquid), while the cathode compartment suitably contains a gaseous phase (such as a carbon dioxide gas).
  • the liquid phase is difficult to compress, while the gaseous phase can be more easily compressed.
  • Possible pressure fluctuations that may occur in the system could lead to transport of the liquid through the membrane in the direction of the gaseous phase.
  • this overpressure can facilitate the diffusion of H + ions in the bipolar membrane.
  • the over-pressure can, for example, be in the range of 0.2-0.5 bar, such as 0.3-0.4 bar.
  • the reduced carbon dioxide product or product mixture can be further purified after being collected using one or more of the state of the art separation methods, such as distillation, absorption or membrane separation.
  • Such purification may comprise one or more from the group of membrane separations consisting of ultrafiltration, nanofiltration, pervaporation, vapour permeation, and membrane distillation.
  • Such purification methods can be based on the difference in molecular size and/or affinity for a membrane material.
  • the method comprises a step wherein the reduced carbon dioxide product or product mixture is subjected to dehydration.
  • dehydration may, for instance, involve dehydration of methanol and/or acetaldehyde.
  • the residual or permeate of a purification step of the reduced carbon dioxide product or product mixture can optionally be recycled to the carbon dioxide feed, optionally after recompression.
  • the temperature in the electrochemical reactor during the method of the invention is preferably 20 °C or less, and may be even cooler, such as 10 °C or less, or even 5 °C or less.
  • the temperature will normally not be below 0 °C.
  • Such relatively low temperatures can be achieved by active cooling of the electrochemical reactor and/or by introducing low temperature water feed and/or low temperature carbon dioxide feed ( e.g . by active cooling of the feed).
  • the reduced carbon dioxide product or product mixture can be collected. This may be accomplished by removing reduced carbon dioxide product or product mixture from the cathode compartment via a cathode compartment outlet. Such outlet is typically located at the bottom of the cathode compartment. The product or product mixture can then suitably be collected in a separate volume, before optionally being processed further.
  • the electrical potential between the anode and the cathode can be applied using an external power supply that is connected to the electrodes (anode and cathode).
  • the electrical potential should be sufficient to drive the reaction, and more in particular for the cathode to reduce carbon dioxide into a reduced carbon dioxide product or product mixture.
  • the invention is directed to an electrochemical reactor, preferably for performing a method as described herein, said reactor comprising an anode compartment separated from a cathode compartment by a separator, wherein said cathode compartment is in contact with a cathode and said anode compartment is in contact with an anode, said anode compartment comprising an anode compartment inlet for feeding water and an anode compartment outlet for releasing oxygen, said cathode compartment comprising a cathode compartment inlet for feeding carbon dioxide and a cathode compartment outlet for collecting reduced carbon dioxide product or product mixture, wherein said separator is selected from the group consisting of a bipolar membrane, a charge-mosaic membrane, and a layered mixture of anion and cation exchange resins, said electrochemical reactor being configured to operate at a pressure of 2.0 MPa (20 bara) or more.
  • the cathode and/or the anode may be embedded in the separator.
  • the cathode and/or anode may be embedded in one of the ion exchange layers of the bipolar membrane.
  • the cathode is preferably embedded in one of the ion exchange layers, and the anode is embedded in the other ion exchange layer.
  • the separator preferably comprises a cation exchange layer and an anion exchange layer.
  • the separator can then be oriented in the electrochemical reactor such that the cation exchange layer faces the cathode and the anion exchange layer faces the anode.
  • the separator can be oriented in the electrochemical reactor such that the anion exchange layer faces the cathode and the cation exchange layer faces the anode.
  • the electrochemical reactor is configured to operate at a pressure of 20 bara or more, more preferably 30 bara or more, even more preferably 50 bara or more, such as 60 bara or more.
  • the pressure in the electrochemical reactor will not exceed 200 bara.
  • the pressure in the electrochemical reactor is preferably 150 bara or less, more preferably 100 bara or less, such as 80 bara or less.
  • the separator may be mechanically supported on at least one side. It is also possible to mechanically confine the separator between two mechanical supports.
  • the reactor can further be mechanically supported by a holder, which may hold the mechanical support.
  • the reactor can suitably further comprise a water feed line, a carbon dioxide feed line, an oxygen release line, and a reduced carbon dioxide product collection line.
  • the water feed line is then connected to the anode compartment inlet
  • the carbon dioxide feed line is then connected to the cathode compartment inlet
  • the oxygen release line is then connected to the anode compartment outlet
  • the reduced carbon dioxide product collection line is then connected to the cathode compartment outlet.
  • the oxygen release line and/or the anode compartment inlet comprises a pressure valve which is operably linked to a pressure sensor for measuring the pressure difference between the carbon dioxide feed line and the oxygen release line.
  • the carbon dioxide feed line and/or the cathode compartment inlet may comprise a pressure valve which is operably linked to a pressure sensor for measuring the pressure difference between the carbon dioxide feed line and the oxygen release line.
  • the pressure valve at the oxygen release side may further be operably linked to a pressure sensor for measuring the absolute pressure in the oxygen release line.
  • the invention is directed to a electrochemical reaction module, comprising two or more electrochemical reactors as described herein in parallel.
  • a stack of repeat units (300) as shown in figure 4a may be placed in a high pressure reaction vessel as shown in figure 4b .
  • the repeat unit (300) shown in figure 4a contains a bipolar membrane (100) confined between two constructive parts of similar design that form the cathode compartment and the anode compartment, respectively.
  • Each part consists of a holder (320) for conductive mechanical support (310).
  • the cathode compartment has a port (330) opening to a common cathode feed volume.
  • the anode compartment has a port (340) opening to a common anode feed volume.
  • Figure 4b shows a stack of the repeat units (300) in a high pressure reaction vessel.
  • the high pressure vessel consists of two parts.
  • the upper part (420) is only a cover and can be removed for access to the electrodes and membranes.
  • the lower part (410) supports the stack of cathode-bipolar membrane-anode repeat units, which physically separates the cathode compartment of the reactor vessel at the bottom of the reactor vessel from the anode compartment of the reactor vessel at the top of the reactor vessel.
  • the lower part has two entry ports; one for the cathode feed (430), for example carbon dioxide at high pressure, and for the anode feed (440), for example water.
  • the lower part has two exit ports; one for the reaction product(s) at the cathode side (450), and one for the anode side (460).
  • the tubing connected to entry and exit ports can be brought to the desired level inside the high-pressure electrochemical reactor vessel.
  • the lower part of the reactor vessel also contains the connection ports to a differential pressure sensing device (470). Albeit not show, it is clear that pressure sensing devices for sensing cathode compartment pressure and/or anode compartment pressure can be mounted on the lower part of the reactor vessel.
  • a number of such high pressure reaction vessels may, for instance, be operated in parallel.
  • An example thereof is shown in figure 3 .
  • water (1) and carbon dioxide (2) feeds are fed to respectively the anode and the cathode chambers of the high pressure reaction vessel.
  • the product mixture (3) is collected at the bottom of the reaction and is purified in a separation unit.
  • the product (4) (here formic acid), leaves the system.
  • Oxygen (5) evolves at the anode and leaves the system as a gas from the anode chamber.
  • the permeate of the separation unit (10) is recompressed and recycled into the dense carbon dioxide feed stream (2).
  • the reactor (500) contains a bipolar membrane (100) in a cylindrical configuration.
  • the bipolar membrane has a mechanical support (510). This mechanical support allows a dense gas phase reactant (e.g . carbon dioxide, or carbon dioxide plus water vapour at high pressure) to pass from the cathode compartment.
  • the product is collected in to the cathode compartment volume (530).
  • a conductive screen (520) At the other side of the bipolar membrane is a conductive screen (520) that allows a liquid phase reactant (such as water or water plus electrolyte) to pass from the anode compartment.
  • the anode chamber is in open contact with the common anode chamber volume (540).
  • a stack of these electrochemical reactors (500) may be placed in a high pressure reaction vessel, for example in a similar fashion as shown in figure 4b , or as a single unit in a high pressure tube, the aggregate being a tube-in-tube electrochemical reactor.
  • a high pressure electrochemical cell was designed in order to have optimal dimensions for the reactor. This is, in particular, relevant for the volume of the electrolyte compartments, the surface area of the membrane, and the surface area of the electrodes.
  • the operating conditions are, typically, in the range of 1-100 bar and temperatures are in the range of 5-50 °C.
  • the use of a high pressure, dense phase mixture of carbon dioxide and water has as main advantage that high concentrations of ionic, reactive species especially, bicarbonate (HCO 3 - ) and carbonate (CO 3 2- ) will be formed.
  • the presence of the ionic carbonate species (HCO 3 - and CO 3 2- ) avoids the need of using an additional electrolyte solution. More specifically, in the proposed reactor configuration there is no need to use a catholyte and/or anolyte solution.
  • Table 1 shows the amount of CO 2 (concentration of CO 2 per litre) when CO 2 is solubilised in water up to a pressure of 10 bar. In this case the CO 2 concentration is also referred to as the CO 2 solubility.
  • Table 2 shows the maximum amount (concentration of CO 2 per litre) that can be achieved at the given conditions in the case where a small amount of water is added to a CO 2 dense phase. For the two situations a temperature of 20 °C is taken, which might require some cooling of the reactor.
  • Table 1 Concentration of CO 2 for different conditions, starting with an aqueous solution.
  • a relatively small reaction volume can be used, as compared to the conventional electrochemical cells that employ an electrolyte solution.
  • the typical conditions that are applied are atmospheric pressures, and as a result the mass-based ratio of the reactant CO 2 , to be consumed in the reduction reaction, to the water (in the electrolyte solution) is well below unity.
  • the mass-based CO 2 to water ratio is in the order of 0.001-0.005 (1 to 5 g CO 2 per litre water). While in the case of starting with a dense phase CO 2 , the envisaged CO 2 to water (mass-based) ratio will be close to unity, based on densities and operation above 50 bar and temperatures below 20 °C.
  • a small reaction volume assures a small(er) distance between the electrodes and the bipolar membrane, with as main result a minimal resistance for the electrical current, and the optimal (minimum) ratio of reaction volume to electrode surface area also assures a high current density. Furthermore, because of the difference in density between the dense CO 2 phase and the liquid formic acid phase, with a density of formic acid of 1.22 kg/l there will be a separation of the product from the reactants.
  • the use of the bipolar membrane will assure a high flux of (only) protons (hydrogen ions, H + ions) across the membrane into the dense CO 2 phase.
  • the use of the bipolar membrane for the water splitting, into OH - and H + is an essential step for high selective reduction of carbon dioxide, with a bipolar membrane only hydrogen ions will flow into the dense CO 2 phase with the bicarbonate and carbonate ions. Again, the absence of additional ions that are normally exchanged across ion exchange membranes used in electro-catalytic reduction of CO 2 will assure no unwanted side reactions.
  • the reactor configuration is ideally suited for the production of formic acid, by providing flexible operation to achieve the required and selected over-potential for carbon dioxide reduction, according to the following reactions/steps:

Claims (15)

  1. Procédé pour réduire par voie électrochimique du dioxyde de carbone, comprenant :
    a) l'introduction, dans un compartiment anodique d'un réacteur électrochimique, d'une alimentation en eau, ledit compartiment anodique comprenant une anode ;
    b) l'introduction, dans un compartiment cathodique d'un réacteur électrochimique, d'une charge de dioxyde de carbone, dans lequel la charge en dioxyde de carbone contient du dioxyde de carbone comme composant principal, ledit compartiment cathodique comprenant une cathode ;
    c) l'application dans le réacteur électrochimique d'un potentiel électrique entre l'anode et la cathode suffisant pour que la cathode réduise le dioxyde de carbone en dérivé ou mélange de dérivés du dioxyde de carbone réduits,
    dans lequel ledit compartiment anodique est séparé dudit compartiment cathodique par un séparateur comprenant une membrane bipolaire, une membrane de charge mosaïque ou un mélange de couches de résines échangeuses d'anions et de cations, et dans laquelle la pression dans le réacteur électrochimique est de 2,0 MPa (20 barra) ou plus.
  2. Procédé selon la revendication 1, dans lequel la charge de dioxyde de carbone est préconditionnée en termes d'une ou plusieurs conditions choisies dans le groupe constitué par la pression, la température et le pH, de préférence en termes de chacun de ceux-ci, plus préférablement la charge de dioxyde de carbone est préconditionnée sous une forme choisie dans le groupe constitué par le dioxyde de carbone, l'acide carbonique, le bicarbonate et le carbonate.
  3. Procédé selon la revendication 1 ou 2, dans lequel la charge de dioxyde de carbone comprend une majorité de dioxyde de carbone et une minorité d'eau.
  4. Procédé selon l'une quelconque des revendications 1 à 3, dans lequel la charge de dioxyde de carbone
    - est supérieure à la pression atmosphérique, de préférence la charge de dioxyde de carbone présente une pression de 2,0 MPa (20 bara) ou plus, de préférence de 3,0 MPa (30 bara) ou plus, plus préférablement de 5,0 MPa (50 bara) ou plus, tels que 6,0 MPa (60 bara) ou plus, et/ou
    - présente une densité de 10-1000 kg/m3, de préférence 100-980 kg/m3, plus préférablement 600-960 kg/m3.
  5. Procédé selon l'une quelconque des revendications 1 à 4, dans lequel ledit réacteur électrochimique est exempt d'électrolyte liquide.
  6. Procédé selon l'une quelconque des revendications 1 à 5, ledit procédé comprenant
    - la décomposition de l'eau au niveau du séparateur, produisant ainsi des ions OH- et des ions H+,
    - la réduction du dioxyde de carbone dans le compartiment cathodique, de façon à consommer ainsi lesdits ions H+, et
    - l'oxydation desdits ions OH- dans le compartiment anodique pour produire de l'eau,
    dans lequel ledit séparateur comprend de préférence une couche d'échange de cations et une couche d'échange d'anions en contact l'une avec l'autre à leur jonction, et dans lequel la couche d'échange de cations fait face à la cathode et la couche d'échange d'anions fait face à l'anode.
  7. Procédé selon l'une quelconque des revendications 1 à 6, ledit procédé comprenant
    - la réduction du dioxyde de carbone dans le compartiment cathodique, produisant ainsi des ions OH-, et
    - l'oxydation de l'eau dans le compartiment anodique pour produire des ions H+, et
    - la recombinaison dudit OH- des ions et des ions H+ au niveau du séparateur pour produire de l'eau,
    dans lequel ledit séparateur comprend de préférence une couche d'échange de cations et une couche d'échange d'anions en contact l'une avec l'autre au niveau d'une jonction, et dans lequel la couche d'échange d'anions fait face à la cathode et la couche d'échange de cations fait face à l'anode.
  8. Procédé selon l'une quelconque des revendications 1 à 7, dans lequel la charge de dioxyde de carbone est sous la forme d'une phase supercritique, d'une phase dense, d'une phase liquide ou d'une phase gazeuse.
  9. Procédé selon l'une quelconque des revendications 1 à 8, dans lequel ledit procédé fonctionne en continu et comprend
    - la libération d'oxygène depuis le compartiment anodique, et
    - la collecte des dérivés de dioxyde de carbone réduits ou d'un mélange de tels dérivés depuis ledit compartiment cathodique.
  10. Procédé selon l'une quelconque des revendications 1 à 9, dans lequel ledit procédé implique la conversion du dioxyde de carbone en
    - une ou plusieurs molécules de plate-forme choisies dans le groupe consistant en gaz de synthèse, alcanes, alcènes, alcools comprenant des diols, acides carboxyliques, aldéhydes, et les cétones; et/ou
    - un ou plusieurs des dérivés choisis dans le groupe constitué par le monoxyde de carbone, l'hydrogène, le gaz de synthèse, l'acide formique, un formiate, le méthanol, l'acétaldéhyde, le méthane et l'éthane.
  11. Procédé selon l'une quelconque des revendications 1 à 10, dans lequel une surpression est maintenue dans le compartiment anodique par rapport au compartiment cathodique, de préférence ladite surpression, indiquée comme une différence de pression, est comprise dans la plage de 0,03-0,05 MPa (0,3 -0,5 bar), plus préférablement dans la plage de 0,02-0,04 MPa (0,2-0,4 bar).
  12. Réacteur électrochimique, de préférence pour mettre en œuvre un procédé selon l'une quelconque des revendications 1 à 11, ledit réacteur comprenant un compartiment anodique séparé d'un compartiment cathodique par un séparateur, dans lequel ledit compartiment cathodique est en contact avec une cathode et ledit compartiment anodique est en contact avec une anode, ledit compartiment anodique comprenant une entrée de compartiment anodique pour l'alimentation en eau et une sortie de compartiment anodique pour libérer de l'oxygène, ledit compartiment cathodique comprenant une entrée de compartiment cathodique pour l'alimentation en dioxyde de carbone, et une sortie de compartiment cathodique pour collecter un dérivé de dioxyde de carbone réduit ou un mélange de tels dérivés,
    dans lequel ledit séparateur est choisi dans le groupe constitué d'une membrane bipolaire, d'une membrane de charges mosaïque et d'un mélange de couches de résines échangeuses d'anions et de cations,
    ledit réacteur électrochimique étant configuré pour fonctionner à une pression de 2,0 MPa (20 bara) ou plus, et dans lequel la cathode et/ou l'anode est/sont de préférence noyées dans le séparateur.
  13. Réacteur électrochimique selon la revendication 12, dans lequel le séparateur comprend une couche échangeuse de cations et une couche échangeuse d'anions et dans lequel le séparateur est orienté de telle sorte que la couche échangeuse de cations fait face à la cathode et la couche échangeuse d'anions fait face à l'anode,
    ou
    dans lequel le séparateur comprend une couche d'échange de cations et une couche d'échange d'anions et dans lequel le séparateur est orienté de telle sorte que la couche d'échange de cations fait face à l'anode et que la couche d'échange d'anions fait face à la cathode.
  14. Réacteur électrochimique selon la revendication 12 ou 13, dans lequel le séparateur est supporté mécaniquement sur au moins un côté, ou est confiné entre deux supports mécaniques.
  15. Réacteur électrochimique selon l'une quelconque des revendications 12 à 14, ledit réacteur comprenant en outre une ligne d'alimentation en eau, une ligne d'alimentation en dioxyde de carbone, une ligne de libération d'oxygène et une ligne de collecte de produits de dioxyde de carbone réduit, dans lequel la ligne de libération d'oxygène comprend une soupape de pression qui est fonctionnellement liée à un capteur de pression pour mesurer la différence de pression entre la conduite d'alimentation en dioxyde de carbone et la conduite de libération d'oxygène.
EP16757367.4A 2015-07-22 2016-07-21 Procédé et réacteur de réduction électrochimique de dioxyde de carbone Active EP3325692B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP15177809 2015-07-22
PCT/NL2016/050545 WO2017014635A1 (fr) 2015-07-22 2016-07-21 Procédé et réacteur permettant une réduction électrochimique du dioxyde de carbone

Publications (2)

Publication Number Publication Date
EP3325692A1 EP3325692A1 (fr) 2018-05-30
EP3325692B1 true EP3325692B1 (fr) 2020-09-16

Family

ID=53724030

Family Applications (1)

Application Number Title Priority Date Filing Date
EP16757367.4A Active EP3325692B1 (fr) 2015-07-22 2016-07-21 Procédé et réacteur de réduction électrochimique de dioxyde de carbone

Country Status (4)

Country Link
EP (1) EP3325692B1 (fr)
DK (1) DK3325692T3 (fr)
ES (1) ES2824158T3 (fr)
WO (1) WO2017014635A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL2031327B1 (en) * 2022-03-18 2023-09-29 Univ Delft Tech Carbon capture and conversion

Families Citing this family (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DK3453065T3 (da) 2016-05-03 2021-05-17 Opus 12 Incorporated Reaktor med avanceret arkitektur til elektrokemisk reduktion af cox
DE102017208610A1 (de) 2017-05-22 2018-11-22 Siemens Aktiengesellschaft Zwei-Membran-Aufbau zur elektrochemischen Reduktion von CO2
WO2019051609A1 (fr) * 2017-09-14 2019-03-21 The University Of British Columbia Systèmes et procédés de réduction électrochimique de dioxyde de carbone
DE102017223521A1 (de) * 2017-12-21 2019-06-27 Siemens Aktiengesellschaft Durchströmbare Anionentauscher-Füllungen für Elektrolytspalte in der CO2-Elektrolyse zur besseren räumlichen Verteilung der Gasentwicklung
JP7364313B2 (ja) 2018-01-22 2023-10-18 トゥエルブ ベネフィット コーポレーション 二酸化炭素リアクタ制御のための方法
CN111971418B (zh) 2018-04-13 2023-10-27 托普索公司 产生用于合成反应的包含co和co2的气体混合物的方法
KR20200142544A (ko) 2018-04-13 2020-12-22 할도르 토프쉐 에이/에스 하이드로포밀화 반응에서 사용하기 위한 합성 가스의 생성 방법
CA3098176A1 (fr) * 2018-04-25 2019-10-31 The University Of British Columbia Systemes et procedes de generation electrochimique de gaz de synthese et d'autres produits chimiques utiles
EP3574991A1 (fr) 2018-05-31 2019-12-04 Haldor Topsøe A/S Reformage à la vapeur chauffée par un chauffage à résistance
CA3105856A1 (fr) * 2018-07-10 2020-01-16 Saipem S.P.A. Procede et systeme de production de monoxyde de carbone et de dihydrogene a partir d'un gaz contenant du co2
CA3120748A1 (fr) 2018-11-28 2020-06-04 Opus 12 Incorporated Electrolyseur et procede d'utilisation
JP7204620B2 (ja) * 2019-09-17 2023-01-16 株式会社東芝 電気化学反応装置
BR112022010144A2 (pt) 2019-11-25 2022-09-06 Twelve Benefit Corp Conjunto de eletrodos de membrana para redução de cox
US11591700B2 (en) 2020-02-10 2023-02-28 Alliance For Sustainable Energy, Llc Electrolyzers for the reduction of carbon dioxide to formate
US20230151501A1 (en) * 2020-04-17 2023-05-18 The University Of British Columbia Electrolytic conversion of carbon-containing ions using porous metal electrodes
CN111910211B (zh) * 2020-06-22 2021-11-19 西安交通大学 一种连续流动光电催化co2还原反应系统
JP7247150B2 (ja) * 2020-09-02 2023-03-28 株式会社東芝 二酸化炭素電解装置および二酸化炭素電解方法
FR3131589A1 (fr) 2021-12-31 2023-07-07 Mickaël ARNOLD Procede de reduction electrochimique de co2 liquide ou supercritique
CN114672832A (zh) * 2022-01-27 2022-06-28 西安交通大学 一种可同时作流动和膜电极电解池的二氧化碳电解反应器
WO2024035474A1 (fr) 2022-08-12 2024-02-15 Twelve Benefit Corporation Production d'acide acétique

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2625656C (fr) 2005-10-13 2014-12-09 Mantra Energy Alternatives Ltd. Reduction electrochimique continue du dioxyde de carbone
US9145615B2 (en) * 2010-09-24 2015-09-29 Yumei Zhai Method and apparatus for the electrochemical reduction of carbon dioxide
US20130105304A1 (en) 2012-07-26 2013-05-02 Liquid Light, Inc. System and High Surface Area Electrodes for the Electrochemical Reduction of Carbon Dioxide
US9074290B2 (en) * 2012-07-31 2015-07-07 Gas Technology Institute Bipolar ion exchange membranes for batteries and other electrochemical devices
US9873951B2 (en) 2012-09-14 2018-01-23 Avantium Knowledge Centre B.V. High pressure electrochemical cell and process for the electrochemical reduction of carbon dioxide
CN102912374B (zh) 2012-10-24 2015-04-22 中国科学院大连化学物理研究所 一种以双极膜为隔膜的电化学还原co2电解池及其应用

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL2031327B1 (en) * 2022-03-18 2023-09-29 Univ Delft Tech Carbon capture and conversion
WO2023177298A3 (fr) * 2022-03-18 2024-04-04 Technische Universiteit Delft Capture et conversion de carbone

Also Published As

Publication number Publication date
WO2017014635A1 (fr) 2017-01-26
EP3325692A1 (fr) 2018-05-30
DK3325692T3 (da) 2020-10-19
ES2824158T3 (es) 2021-05-11

Similar Documents

Publication Publication Date Title
EP3325692B1 (fr) Procédé et réacteur de réduction électrochimique de dioxyde de carbone
Overa et al. Tandem and hybrid processes for carbon dioxide utilization
US20210047743A1 (en) Method for electrochemically reducing carbon dioxide
US8277631B2 (en) Methods and devices for the production of hydrocarbons from carbon and hydrogen sources
US11198942B2 (en) Electrolysis system for carbon dioxide
US20160215403A1 (en) Extraction of carbon dioxide and hydrogen from seawater and hydrocarbon production therefrom
AU2017209876B2 (en) Electrolysis system and method for electrochemical ethylene oxide production
EP3752660B1 (fr) Capture et conversion électrochimiques intégrées de dioxyde de carbone
EP4189143A2 (fr) Système et procédé de commande de réacteur à dioxyde de carbone
US11560633B2 (en) Electrochemical production of carbon monoxide and/or syngas
US20220362707A1 (en) Systems and methods for capturing carbon dioxide and regenerating a capture solution
Brunetti et al. CO2 conversion by membrane reactors
WO2019197514A1 (fr) Procédé de génération d'un gaz de synthèse destiné à être utilisé dans des réactions d'hydroformylation
CA3179888C (fr) Procede et appareil de regeneration electrochimique d'hydroxyde et de dioxyde de carbone
CN114787076A (zh) 储氢方法、氢气的制造方法及氢气制造系统
NL2031327B1 (en) Carbon capture and conversion
US20240018082A1 (en) Metal formate production
US11846034B1 (en) Carbon monoxide electrolyzers used with reverse water gas shift reactors for the conversion of carbon dioxide into added-value products
EP4079720A1 (fr) Production d'acide formique ou de formaldéhyde à partir de dioxyde de carbone
US20220063997A1 (en) Liquid phase reforming of oxygenates for hydrogen production
KR20240060020A (ko) 이산화탄소 전환시스템

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20180207

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20190305

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: GRANT OF PATENT IS INTENDED

INTG Intention to grant announced

Effective date: 20200515

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE PATENT HAS BEEN GRANTED

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 602016044148

Country of ref document: DE

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Ref country code: FI

Ref legal event code: FGE

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 1314250

Country of ref document: AT

Kind code of ref document: T

Effective date: 20201015

REG Reference to a national code

Ref country code: NO

Ref legal event code: T2

Effective date: 20200916

Ref country code: DK

Ref legal event code: T3

Effective date: 20201013

REG Reference to a national code

Ref country code: NL

Ref legal event code: FP

REG Reference to a national code

Ref country code: SE

Ref legal event code: TRGR

REG Reference to a national code

Ref country code: DE

Ref legal event code: R079

Ref document number: 602016044148

Country of ref document: DE

Free format text: PREVIOUS MAIN CLASS: C25B0003040000

Ipc: C25B0003250000

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20201217

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20201216

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210118

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2824158

Country of ref document: ES

Kind code of ref document: T3

Effective date: 20210511

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20210116

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 602016044148

Country of ref document: DE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20210617

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20210721

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20220621

Year of fee payment: 7

REG Reference to a national code

Ref country code: AT

Ref legal event code: UEP

Ref document number: 1314250

Country of ref document: AT

Kind code of ref document: T

Effective date: 20200916

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 20220720

Year of fee payment: 7

Ref country code: NO

Payment date: 20220725

Year of fee payment: 7

Ref country code: IT

Payment date: 20220726

Year of fee payment: 7

Ref country code: IE

Payment date: 20220721

Year of fee payment: 7

Ref country code: GB

Payment date: 20220721

Year of fee payment: 7

Ref country code: FI

Payment date: 20220721

Year of fee payment: 7

Ref country code: ES

Payment date: 20220928

Year of fee payment: 7

Ref country code: DK

Payment date: 20220725

Year of fee payment: 7

Ref country code: DE

Payment date: 20220720

Year of fee payment: 7

Ref country code: AT

Payment date: 20220721

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20220720

Year of fee payment: 7

Ref country code: BE

Payment date: 20220720

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20160721

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

REG Reference to a national code

Ref country code: NO

Ref legal event code: CHAD

Owner name: COVAL ENERGY VENTURES B.V., NL

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20231005

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20240123

Year of fee payment: 8

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IE

Payment date: 20240126

Year of fee payment: 8

Ref country code: ES

Payment date: 20240126

Year of fee payment: 8

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 20240129

Year of fee payment: 8

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20200916

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FI

Payment date: 20240126

Year of fee payment: 8

Ref country code: DE

Payment date: 20240126

Year of fee payment: 8

Ref country code: GB

Payment date: 20240126

Year of fee payment: 8

Ref country code: CH

Payment date: 20240125

Year of fee payment: 8