Novel electrochemical reactor design

Abstract

The present invention relates to an electrochemical reactor comprising at least one fuel inlet in fluid connection with a fuel chamber located inside the electrochemical reactor, at least one product outlet in fluid connection with a product chamber located inside the electrochemical reactor wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed in a spiral shape around a reinforced reactor chamber of the electrochemical reactor, and wherein the at least one electrochemical membrane comprises at least one high temperature proton exchange membrane.

Description

[0001] Technical field of the invention

[0002] The present invention relates to a novel electrochemical reactor design. In particular, the present invention relates to a novel electrochemical membrane design and layout for an electrochemical reactor with or without an enhanced reactor (e.g., a Taylor-Couette reactor (TCR)) that can be surrounded by an electrochemical reactor having a specially designed electrochemical membrane mounted in, for example, a toroidal cylindrical box. Background of the Invention

[0004] An electrochemical reactor includes one or more electrochemical membranes within which are electrochemical cells that require a supply of electrical energy to initiate and maintain one or more chemical reactions to facilitate the function of the electrochemical reactor.

[0005] There are many types of electrochemical reactors, but they all consist of an anode, a cathode, and an electrolyte that allows ions (usually positively charged hydrogen ions (H + )) moves between the two sides of the electrochemical membrane. At the anode, the catalyst causes the fuel to undergo a reaction to produce ions (H + ) and an oxidation reaction of electrons. The ions move from the anode to the cathode through the electrolyte. At the same time, electrons flow from the anode to the cathode, completing the external circuit of the DC power supply.

[0006] To fully and successfully disrupt the energy industry, conventional electrochemical reactors face various challenges as the capacity of electrochemical reactors as well as their durability, effectiveness, and productivity are difficult to increase.

[0007] Accordingly, improved electrochemical reactor designs would be advantageous, and in particular more efficient, reproducible, durable and / or reliable electrochemical reactors with increased lifetime and productivity would be advantageous. SUMMARY OF THE INVENTION

[0009] The object of the present invention is therefore to provide a novel electrochemical reactor design.

[0010] In particular, the object of the present invention is to provide a new electrochemical reactor design which solves the above-mentioned problems of the prior art in terms of effectiveness, durability, reliability, lifetime and productivity as well as lower maintenance and manufacturing costs.

[0011] Therefore, one aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed around the fuel chamber of the electrochemical reactor in a spiral shape, concentric shape, radial shape or disc shape.

[0012] Another aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed in a spiral shape, concentric shape, radial shape or disc shape around the fuel chamber of the electrochemical reactor, and wherein at least one electrochemical membrane includes at least one high-temperature proton exchange membrane.

[0013] Another aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel provided to the fuel chamber moves substantially in a radial direction relative to the longitudinal direction of the electrochemical membrane and / or wherein the product moves substantially in a longitudinal direction of the longitudinal direction of the electrochemical membrane.

[0014] Another aspect of the invention relates to an intensified reactor, such as a Taylor-Couette reactor (TCR), comprising an energy unit and an intensified reaction chamber surrounded by an electrochemical reactor jacket, the intensified reaction chamber comprising at least one fuel inlet and at least one hydrogen outlet (H2) for gasification reaction products connected to the fuel chamber fluid inside the electrochemical reactor. 2 - outlet); wherein the electrochemical reaction chamber comprises an electrochemical membrane separating at least one fuel inlet and at least one hydrogen outlet.

[0015] Yet another aspect of the present invention relates to an enhanced reactor, such as a Taylor-Couette reactor (TCR), comprising an energy unit and an enhanced reaction chamber surrounded by an electrochemical reactor jacket, the enhanced reaction chamber comprising at least one fuel inlet and at least one hydrogen outlet (H2) for gasification reaction products connected to a fuel chamber fluidly disposed inside the electrochemical reactor. 2- outlet); wherein the electrochemical reaction chamber comprises an inner ring (in which an enhanced reactor, such as a Taylor-Couette reactor (TCR) can be placed) and an electrochemical membrane according to the present invention.

[0016] Another aspect of the present invention relates to an electrochemical reactor comprising an electrochemical membrane and at least one fuel inlet fluidly connected to a spiral flow path (6) and a fuel chamber located inside the electrochemical reactor, and at least one product outlet fluidly connected to a product chamber located inside the electrochemical reactor, wherein the fuel provided to the fuel chamber moves substantially in a radial direction relative to the longitudinal direction of the electrochemical membrane and / or wherein the product moves substantially in a longitudinal direction of the longitudinal direction of the electrochemical membrane, and wherein at least one electrochemical membrane can be at least one high-temperature proton exchange membrane.

[0017] A further aspect of the present invention relates to the use of an electrochemical reactor according to the present invention for converting a hydrocarbon composition at least partially into a hydrocarbon containing hydrogen (H 2 ) in an electrochemical reactor with or without an enhanced reactor according to the present invention, such as a Taylor-Couette reactor (TCR).

[0018] Another aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane.

[0019] Another aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane includes at least two layers, and wherein the gap between the at least two layers of the electrochemical membrane defines the product chamber.

[0020] Another aspect of the present invention relates to a box comprising one or more box elements, wherein one or more box elements include an electrochemical reactor, the electrochemical reactor including at least one fuel inlet connected to the fluid of a fuel chamber located inside the electrochemical reactor, and at least one product outlet connected to the fluid of a product chamber located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane.

[0021] Even further aspects of the present invention relate to a box comprising one or more box elements, wherein one or more of the box elements comprises an electrochemical reactor, the electrochemical reactor comprising at least one fuel inlet fluidly connected to a fuel chamber located inside the electrochemical reactor, and at least one product outlet fluidly connected to a product chamber located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein at least one electrochemical membrane comprises at least one high-temperature proton exchange membrane.

[0022] Even further aspects of the present invention relate to an electrochemical reactor comprising at least one fuel inlet fluidly connected to a fuel chamber located within the electrochemical reactor, and at least one product outlet fluidly connected to a product chamber located within the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane comprises at least one corrugated layer, such as at least two corrugated layers, for example at least three corrugated layers, such as at least four corrugated layers, for example at least five corrugated layers, such as at least six corrugated layers. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] FIG. 1 shows a spiral electrochemical membrane formed in a single spiral around an enhanced reactor (e.g., a Taylor-Couette reactor (TCR)) according to the present invention,

[0025] FIG. 2 shows an electrochemical membrane comprising two corrugated layers forming a fuel chamber and a product chamber,

[0026] Figure 3 An electrochemical membrane is shown, the electrochemical membrane comprising a corrugated layer and a top non-corrugated layer and a bottom non-corrugated layer, and a fuel chamber and a flow path are present above the top non-corrugated layer and below the bottom non-corrugated layer, and a product chamber is present between the non-corrugated layers, and

[0027] Figure 4 An electrochemical membrane is shown, the electrochemical membrane comprising two corrugated layers and a top non-corrugated layer and a bottom non-corrugated layer, and a fuel chamber and a flow path are present above the top non-corrugated layer and below the bottom non-corrugated layer, and a product chamber is present between the non-corrugated layers,

[0028] Figure 5 It shows that Figure 4 The same 4-layer electrochemical membrane is shown, further illustrating the hot spot in the top non-corrugated layer.

[0029] FIG. 6 shows various Archimedean spiral structures suitable for use in the present invention, ranging from spiral structures comprising a single spiral to spiral structures comprising multiple simultaneous spirals originating from the same radius, such as 3 simultaneous spirals, to 7 spirals and 20 spiral structures.

[0030] Figure 7 An example of the construction of an electrochemical membrane formed around a reinforced reactor, such as a Taylor-Couette Reactor (TCR), in the center of a spiral is shown.

[0031] Figure 8 An example of simultaneous 3D printed construction of an electrochemical membrane in the center of a spiral surrounding an enhanced reactor, such as a Taylor-Couette Reactor (TCR), is shown.

[0032] Fig. 9 An example of a cassette in the form of a radial star electrochemical reactor mounted around a central intensified reactor, such as a Taylor-Couette reactor (TCR), is shown.

[0033] Fig.10 An example of a cassette in the form of a disc electrochemical reactor mounted around a central intensified reactor, such as a Taylor-Couette reactor (TCR), is shown.

[0034] The present invention will now be described in more detail below. DETAILED DESCRIPTION OF THE INVENTION

[0036] The inventors of the present invention have discovered various methods to increase the surface area of ​​the electrochemical membrane of the electrochemical reactor of the present invention, allowing for increased reactivity of the electrochemical membrane, increased productivity and increased durability and increased effectiveness during use.

[0037] Therefore, one aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed around the fuel chamber of the electrochemical reactor in a spiral shape, concentric shape, radial shape or disc shape.

[0038] Another aspect of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed in a spiral shape, concentric shape, radial shape or disc shape around the fuel chamber of the electrochemical reactor, and wherein at least one electrochemical membrane includes at least one high-temperature proton exchange membrane.

[0039] An even further preferred embodiment of the present invention relates to an electrochemical reactor comprising at least one fuel inlet fluidly connected to a fuel chamber located inside the electrochemical reactor, at least one product outlet fluidly connected to a product chamber located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed in a spiral shape, concentric shape, radial shape or disc shape in a box installed around the enhanced reactor chamber of the electrochemical reactor. The main function of the electrochemical reactor according to the present invention can be to serve as an electrochemical hydrogen separator.

[0040] Another preferred embodiment of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed in a spiral shape, concentric shape, radial shape or disc shape in a box installed around an enhanced reactor chamber of the electrochemical reactor, and wherein at least one electrochemical membrane includes at least one high-temperature proton exchange membrane.

[0041] In an embodiment of the present invention, the electrochemical membrane may have a circular cross-sectional area, a substantially circular cross-sectional area or an elliptical cross-sectional area. Preferably, the cross-sectional area may be relative to the longitudinal direction of the electrochemical membrane.

[0042] Preferably, the circular cross-sectional area, substantially circular cross-sectional area or elliptical cross-sectional area of ​​the electrochemical membrane may comprise an inner ring and an outer ring. The inner ring may be connected to the outer ring by a spiral path, a concentric path, a radial path or a complex path.

[0043] The electrochemical membrane may be folded or printed in a spiral shape, a concentric shape, a radial shape, or a disk shape in a cassette mounted around the cross-sectional area of ​​the enhanced reactor chamber of the electrochemical reactor.

[0044] Preferably, the spiral shape is an open-ended spiral shape.An open-ended spiral may be a spiral wherein when starting closest to the central portion, for radial movement in the spiral, preferably in a direction away from the starting portion (from the inner ring), the distance from the central portion may increase.

[0045] The central part of the spiral electrochemical membrane and the starting part of the spiral electrochemical membrane may be the same or different. Preferably, the central part of the spiral electrochemical membrane and the starting part of the spiral electrochemical membrane may be different.

[0046] In an embodiment of the present invention, the fuel chamber of the electrochemical reactor may be disposed in a spiral shape between overlapping spiral electrochemical membranes. Preferably, the spiral electrochemical membranes may overlap without contacting.

[0047] Preferably, the spiral shape of the electrochemical membrane may be in the shape of an Archimedean spiral. The Archimedean spiral may have the property that any straight line extending from the original position through the spiral structure may intersect with the continuous turns of the spiral. The intersection of the continuous turns of the spiral may be arranged at a position with a constant or substantially constant separation distance.

[0048] In an embodiment of the present invention, the electrochemical membrane may be provided with one or more non-conductive radial flow spacers to prevent the electrochemical membrane from contacting itself during electrical operation to avoid electrical shorting of the electrochemical process and also to provide a mechanically resilient flow path for any residual fuel (such as a hydrocarbon composition) and gasification reaction products as they travel from the inner ring to the outer ring. Preferably, the spacers may be provided circumferentially (at longitudinal intervals) along the helical length of the electrochemical membrane.

[0049] The spiral may start at any radial distance from the central region.

[0050] Preferably, the spiral may be an Archimedean spiral.

[0051] To further increase the volume throughput of fuel and gasification gas in the electrochemical reactor, the number of flow paths for fuel and gasification gas can be increased. Multiple spirals can be used, in particular Archimedean multiple spirals can be suitable, where the spirals start at intervals of X degree arc - this depends on the number of spirals included.

[0052] The use of multiple spirals can be used to reduce the measured length of each spiral (per cross-sectional area), and thereby reduce the residence time of the gas or fluid (per spiral). In addition, the use of multiple spirals can increase the gas or fluid rate throughput because each shorter spiral will produce lower pressure losses and provide multiple flow paths, increasing the total flow cross-sectional area.

[0053] In an embodiment of the present invention, the radial length of the electrochemical membrane may preferably be greater than the longitudinal length of the electrochemical membrane. Preferably, the radial length of the electrochemical membrane may be at least 10% greater than the longitudinal length of the electrochemical membrane, such as at least 25%, for example at least 50%, such as at least 75%, for example at least 100%, such as at least 150%, for example at least 200%, such as at least 250%, for example at least 300%, such as at least 400%, for example at least 500%, such as at least 600%, for example at least 700%. A flow path may involve the distance that the fuel and / or gasification reaction product moves from the inner ring to the outer ring along the spiral flow path between and defined by the electrochemical membrane surface.

[0054] In an embodiment of the present invention, the spiral electrochemical membrane may include a single spiral electrochemical membrane or a plurality of electrochemical membrane spirals. Preferably, a plurality of electrochemical membrane spirals may include 2 spirals, such as 3 spirals, for example 5 spirals, such as 7 spirals, for example 10 spirals, such as 15 spirals, for example 20 spirals.

[0055] The fuel chamber may provide a radial flow of fuel relative to the longitudinal direction of the electrochemical membrane. Preferably, the fuel and gasification reaction products entering the electrochemical reactor and the electrochemical membrane flow path may move in a radial direction, preferably following and being bounded by the spiral electrochemical membrane, and from an inner ring of an adjacent enhanced reactor (e.g., a Taylor-Couette reactor (TCR)) of the electrochemical reactor to an outer ring of the electrochemical reactor.

[0056] In the electrochemical reactor according to the invention, the fuel chamber may be mounted in a spiral shape, a concentric shape, a radial shape or a disk shape around the inner ring of the electrochemical reactor, preferably guided and bounded by at least one electrochemical membrane.

[0057] In an embodiment of the present invention, the electrochemical reactor comprises:

[0058] (i) An electrochemical membrane folded in a spiral shape, concentric shape, radial shape or disk shape around an inner ring of an electrochemical reactor;

[0059] as well as

[0060] (ii) A fuel chamber installed in a spiral shape, concentric shape, radial shape or disk shape around the inner ring of the electrochemical reactor.

[0061] In other embodiments of the present invention, the space between consecutive electrochemical membranes of a spiral-shaped, concentric-shaped, radial-shaped, or disk-shaped electrochemical membrane may constitute a fuel chamber and a flow path for residual fuel and reaction products.

[0062] By providing these spiral, concentric, radial or disk-shaped structural paths, radial flow continuity of, for example, residual fuel and / or gasification reaction products from the inner ring to the outer ring of the electrochemical membrane can be provided, resulting in improved separation, conversion rate and productivity.

[0063] The electrochemical membrane may include a spiral, concentric, radial or disc-shaped electrochemical membrane, wherein the fuel introduced into the fuel inlet and / or the formed gasification reaction product moves from the inner ring to the outer ring along the membrane surface of these shapes. Preferably, the movement of the fuel and / or the formed gasification reaction product may be in a radial direction relative to the longitudinal direction of the electrochemical membrane.

[0064] During this movement along the electrochemical membrane from the inner ring to the outer ring, the concentration of the gasification reaction products can increase and the concentration of the added fuel can decrease as the fuel can be converted to gasification reaction products and the resulting products can be removed and transferred to the product chamber.

[0065] In an embodiment of the present invention, the gasification reaction product may be a gasification reaction product gas. The gasification reaction product gas may be in a supercritical fluid phase condition.

[0066] In a further embodiment of the present invention, the product collected in the product chamber may be moved in the longitudinal direction of the electrochemical membrane to the product outlet.

[0067] Preferably, the movement of the fuel and / or formed gasification reaction products may be in a radial direction relative to the longitudinal direction of the electrochemical membrane, and the products collected in the product chamber may move in the longitudinal direction of the electrochemical membrane to the product outlet.

[0068] In embodiments of the present invention, the spiral, concentric, radial or disk-shaped electrochemical membrane may have a length that extends through the entire length or a portion of the length (both longitudinally and radially) of the fuel chamber of the electrochemical reactor.

[0069] The electrochemical reactor according to the invention may comprise a waste material outlet.

[0070] The waste material outlet may be fluidly connected to the outer ring of the electrochemical membrane.

[0071] Preferably, the waste material may include water, pollutants, unconverted hydrocarbons, methane (CH 4 ), carbon dioxide (CO 2 ), carbon monoxide (CO) and the like.

[0072] Electrochemical membranes according to the present invention may allow the transport of molecules, atoms and / or ions from a fuel compartment to a product compartment.

[0073] In an embodiment of the present invention, the electrochemical membrane according to the present invention can allow the transport of hydrogen ions (H) from a hydrogen donor in a fuel chamber. + ) to form hydrogen (H 2 ). Hydrogen ions can be separated from the hydrogen donor in the fuel chamber at the anode. Hydrogen ions (H + ) can then be transported through the electrolyte and at the cathode on the product compartment within the electrochemical membrane, the hydrogen ions (H + ) accepts an electron to form a hydrogen atom, which can then be allowed to combine with another hydrogen atom to form hydrogen gas (H 2 ), hydrogen (H 2 ) can be captured in the product chamber.

[0074] Preferably, the spiral membrane may be in the form of an Archimedean spiral.

[0075] In an embodiment of the present invention, the electrochemical membrane may be provided with an anode, and preferably, the anode may face the fuel chamber.

[0076] In a further embodiment of the invention, the electrochemical membrane may be provided with a cathode, preferably the cathode may face the product chamber.

[0077] The electrochemical membrane according to the present invention may include two or more electrochemical cells, wherein one or more electrochemical cells are formed in a corrugated layer to produce and contain a plurality of parallel product chambers and / or fuel chambers. The corrugated layer provided with several anodes may face the fuel chamber, and the cathode may face the product chamber. The reverse arrangement may also be performed.

[0078] The at least one electrochemical membrane may comprise an anode and a cathode. Preferably, the at least one electrochemical membrane may comprise an electrolyte.

[0079] In an embodiment of the present invention, the electrochemical membrane may be a proton conducting electrochemical membrane.

[0080] Electrochemical membranes with proton conduction may involve acidic electrolytes (e.g. (H + )) is transported through an electrochemical electrolyte, which is placed between two porous electrodes and is formed by, for example, a proton-conducting metal oxide layer.

[0081] In the electrochemical reactor according to the present invention, hydrogen (H) 2 can be oxidized on the anode side of the electrochemical membrane, hydrogen (H 2 ) can be oxidized to protons (H + ), proton (H + ) are then conducted through the electrolyte until they eventually recombine with the electrons to reform hydrogen atoms, which recombine with other hydrogen atoms to produce hydrogen gas (H) at the cathode. 2 ).

[0082] Proton (H + ) must move through the electrolyte, and therefore, an electrochemical membrane material with predominantly proton conductivity at high temperatures may be required as the electrolyte.

[0083] Preferably, the electrochemical membranes and electrolytes according to the present invention may have high redox stability, preferably accompanied by high mechanical and thermal stability as well as high durability and optimal operation.

[0084] The electrochemical reactor and structure provided by the present invention can provide a method for producing one or more hydrocarbons (e.g., CH 4 ) to produce high-purity hydrogen for a variety of applications while capturing greenhouse gases such as CO 2 and / or CO), capturing greenhouse gases can be identified as a major benefit with significant environmental and climate relevance.

[0085] The reaction of the fuel can include several stages:

[0086] - Phase I may include fossil fuels (e.g. hydrocarbons, methane, natural gas, biogas, shale gas or gasified coal) such as with CO 2 , air or H 2 O is partially oxidized to produce synthesis gas (CO, CO 2 and H 2 );

[0087] - Stage II may include the water gas shift reaction (WGSR) to react water (H 2 O) converts carbon monoxide (CO) from syngas into carbon dioxide (CO 2 ) and more hydrogen (H 2 );

[0088] - Stage III may comprise the CO removal by an electrochemical membrane according to the invention, such as a mixed proton-electron conducting (MPEC) membrane 2 / H 2 Electrochemical separation.

[0089] In embodiments of the present invention, electrochemical membrane materials having mixed proton-electron conductivity and significant chemical stability under reducing and hydrothermal conditions may be preferred.

[0090] In further embodiments of the present invention, at least one electrochemical membrane between the fuel chamber and / or the product chamber may comprise at least one layer, wherein at least one layer may be a corrugated layer.

[0091] By providing an electrochemical membrane comprising at least one corrugated layer, the surface area available for allowing molecules, atoms and / or ions to be transported from the fuel chamber to the product chamber can be increased, resulting in improved utilization and / or productivity of the electrochemical membrane and electrochemical reactor. Adding further enhanced continuous strips of anode and cathode along each of the corrugated groove ridges can reduce hot spots by helping to maintain an evenly distributed current density within the electrochemical layer.

[0092] The corrugated layer according to the invention may comprise one or two outer layers, and a plurality of grooves producing a corrugated structure. In a multi-layer type of corrugated layer, one or more intermediate layers may be inserted, for example, between the grooves of two layers. The effect of the corrugated layer may depend on the number of outer / intermediate layers and the number of grooves.

[0093] By increasing the number of intermediate layers, stacked grooves can be provided, resulting in increased structural integrity and durability of the electrochemical membrane. Instead of (or in addition to) adding one or more intermediate layers in the electrochemical membrane, two, for example single-sided corrugated layers can be placed together with contact sites at the grooves or at least part of the grooves of the corrugated layers.

[0094] The single-sided corrugated layer includes a layer of grooves attached to a fuel permeable material or a gas permeable material or a material similar to the electrochemical membrane used in the corrugated layer.

[0095] The size of the grooves of the corrugated layer may be as small as possible to provide the largest possible cumulative surface area, but not so small as to prevent or hinder access to the fuel material.

[0096] Preferably, the size (height) of the grooves of the corrugated layer may be in the range of 0.5 mm - 10 mm, such as in the range of 1 mm - 8 mm, for example in the range of 1.5 mm - 6 mm, such as in the range of 2 mm - 5 mm, for example in the range of 3 mm - 4 mm.

[0097] In an embodiment of the present invention, the electrochemical membrane may include a single corrugated layer, a double corrugated layer, a triple corrugated layer, or a quadruple corrugated layer. The corrugated layer may be provided with more than four layers; however, the number of corrugated layers may be provided according to the purpose, required durability, application, and accessibility of the electrochemical reactor.

[0098] In a preferred embodiment of the present invention, the layers of the electrochemical membrane may include an anode, an electrolyte, and a cathode.

[0099] Increasing the number of corrugated layers of the electrochemical membrane can also provide higher rigidity, higher mechanical strength, and thus a reduced risk of mechanical damage to the electrochemical membrane and electrochemical reactor. This can also reduce the risk of product production losses and increase productivity through increased electrochemical membrane life.

[0100] The grooves may be provided in different shapes. In an embodiment, the grooves of the corrugated layer may be wavy; in a sawtooth shape; in a circular shape; or crenellated.

[0101] When the electrochemical membrane comprises 2 or more layers, at least one layer may be corrugated.

[0102] In an embodiment of the present invention, the electrochemical membrane comprises a two-layer structure. Preferably, the two-layer structure comprises two corrugated layers of the electrochemical membrane.

[0103] In yet another embodiment of the present invention, the electrochemical membrane comprises a three-layer structure. The three-layer structure may include at least one corrugated layer, such as at least two corrugated layers, for example three corrugated layers. In order to save space in the electrochemical membrane, it may be preferred that the three-layer structure may include a corrugated layer and two straight or substantially straight layers in either side of the corrugated layer. This will also provide built-in operational redundancy for the product chamber of one layer in one direction.

[0104] In another embodiment of the present invention, the electrochemical membrane comprises a four-layer structure. The four-layer structure may include at least two corrugated layers, such as at least three corrugated layers, for example four corrugated layers. Preferably, the four-layer structure may include two corrugated layers facing each other and combined at the top of the groove, and two straight or substantially straight layers in either side of the two corrugated layers. This can also provide built-in operational redundancy for the product chamber of one layer in two directions.

[0105] When two corrugated layers face each other and are combined, the two corrugated layers may be separated by a product permeable element.

[0106] One advantage of having three or more layers in the electrochemical membrane, such as having four or more layers in the membrane, may be that such an electrochemical membrane may provide built-in operational redundancy for the product chamber and result in a significant reduction in vulnerability to indirect damage due to the formation of hot spot holes or tares in the electrochemical membrane, such as due to localized thermal damage on the electrochemical membrane. These hot spots may result in mixing of fuel and product, whereby the product stream may be contaminated. Increased mechanical stability, durability, and reliability may extend life and reduce replacement frequency, and reduce overall operating costs.

[0107] A preferred embodiment of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane.

[0108] Another preferred embodiment of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein at least one electrochemical membrane includes at least two layers, and wherein the gap between the at least two layers of the electrochemical membrane defines the product chamber.

[0109] Another preferred embodiment of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane includes at least one corrugated layer, such as at least two corrugated layers, for example at least three corrugated layers, such as at least four corrugated layers, for example at least five corrugated layers, such as at least six corrugated layers.

[0110] In an embodiment of the present invention, at least one electrochemical membrane may be folded or printed in a spiral shape, a concentric shape, a radial shape, or a disk shape in a box surrounding the enhanced reactor chamber.

[0111] In further embodiments of the present invention, the at least one electrochemical membrane may comprise at least two layers, and wherein a gap between the at least two layers of the at least one electrochemical membrane defines a product chamber.

[0112] Preferably, the at least two layers may include a contact site combining the at least two layers in a portion of at least one electrochemical membrane.

[0113] Gaps between at least two layers of at least one electrochemical membrane and between contact sites combining at least two layers in a portion of at least one electrochemical membrane may define a product chamber.

[0114] In yet another embodiment of the present invention, at least one electrochemical membrane may comprise at least one corrugated layer, such as at least two corrugated layers, for example at least three corrugated layers, such as at least four corrugated layers, for example at least five corrugated layers, such as at least six corrugated layers.

[0115] In embodiments of the present invention, the center of the electrochemical reactor may include an intensified reactor or portion thereof, such as a Taylor-Couette reactor (TCR) or portion thereof.

[0116] The electrochemical reactor and the enhanced reactor (e.g., Taylor-Couette reactor (TCR)) may preferably be two separate items, which may be combined to improve hydrogen production by including the enhanced reactor (e.g., Taylor-Couette reactor (TCR)) within the electrochemical reactor (preferably in the center of the electrochemical reactor).

[0117] Preferably, the centre of the electrochemical reactor comprises a Taylor-Couette reactor (TCR) or a portion thereof.

[0118] A portion of an intensified reactor (e.g., a Taylor-Couette reactor (TCR)) can involve a rotating central portion of an intensified reactor (e.g., a Taylor-Couette reactor (TCR)), which can be the portion that generates an intensified reactor (e.g., a Taylor-Couette reactor (TCR)) flow in a fuel provided in a fuel chamber.

[0119] Preferably, the electrochemical reactor comprises a core portion, which comprises an enhanced reactor, such as a Taylor-Couette reactor (TCR). An enhanced reactor, such as a Taylor-Couette reactor (TCR), may be surrounded by a fuel chamber. The fuel chamber may be surrounded by one or more electrochemical membranes according to the present invention. One or more electrochemical membranes according to the present invention may each contain a product chamber, or two or more product chambers may be formed by at least two layers in each electrochemical membrane. An enhanced reactor (such as a Taylor-Couette reactor (TCR)), a fuel chamber, one or more electrochemical membranes, and a product chamber may be surrounded by a housing that maintains and protects the active part of the electrochemical reactor.

[0120] A tonic reactor, such as a Taylor-Couette reactor (TCR), may be fluidly connected to the inner ring of the electrochemical membrane and / or in fluid contact with the fuel chamber of the electrochemical membrane.

[0121] In a preferred embodiment, the present invention relates to an electrochemical reactor comprising an enhanced reactor, such as a Taylor-Couette reactor (TCR), and an electrochemical membrane according to the present invention.

[0122] The electrochemical reactor according to the present invention with or without (preferably with) an enhanced reactor (such as a Taylor-Couette reactor (TCR)) may preferably be suitable for converting a fuel (such as with or without carbon dioxide (CO 2 ) into a hydrocarbon composition comprising hydrogen (H 2 )'s composition.

[0123] Preferably, the fuel is hydrogen (H 2 ) or the device for gasification can be accomplished with an enhanced reactor, such as a Taylor-Couette reactor (TCR), which is arranged in the center of the electrochemical membrane according to the invention.

[0124] A Taylor-Couette Reactor (TCR) may be a device that has been designed to utilize Taylor-Couette flow, which allows many flow regimes and conditions to occur and chemical transformations to occur with precise control of various reactor characteristics.

[0125] An intensified reactor, such as a Taylor-Couette reactor (TCR), may consist of a cassette shell, into which a first (rotating) inner cylinder may be inserted, such that a first annular gap may be formed.

[0126] The cartridge housing may contain one or more electrochemical membranes of the invention.

[0127] A preferred embodiment of the present invention relates to an enhanced reactor, such as a Taylor-Couette reactor (TCR), comprising an energy unit and an enhanced reaction chamber surrounded by an electrochemical reactor shell, the enhanced reaction chamber comprising at least one fuel inlet and at least one hydrogen outlet (H 2 - outlet), for example at least one hydrogen outlet (H) for gasification reaction products connected to a fuel chamber fluidly located inside the electrochemical reactor 2 - outlet); wherein the electrochemical reaction chamber comprises an electrochemical membrane according to the present invention.

[0128] Another preferred embodiment of the present invention relates to an enhanced reactor, such as a Taylor-Couette reactor (TCR), comprising an energy unit and an enhanced reaction chamber surrounded by an electrochemical reactor shell, the enhanced reaction chamber comprising at least one fuel inlet and at least one hydrogen outlet (H 2 - outlet), for example at least one hydrogen outlet (H) for gasification reaction products connected to a fuel chamber fluidly located inside the electrochemical reactor 2 - outlet); wherein the electrochemical reaction chamber comprises an electrochemical membrane separating at least one fuel inlet and at least one hydrogen outlet.

[0129] The electrochemical reactor may preferably comprise at least one outlet for waste materials, in particular at least one outlet for carbon dioxide (CO 2 -exit).

[0130] A preferred embodiment of the present invention relates to an electrochemical reactor, which includes at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel provided to the fuel chamber moves substantially in a radial direction relative to the longitudinal direction of the electrochemical reactor and / or wherein the product moves substantially in a longitudinal direction of the longitudinal direction of the electrochemical reactor.

[0131] Another preferred embodiment of the present invention relates to an electrochemical reactor comprising an electrochemical membrane and at least one fuel inlet fluidly connected to a spiral flow path (6) and a fuel chamber located inside the electrochemical reactor, and at least one product outlet fluidly connected to a product chamber located inside the electrochemical reactor, wherein the fuel provided to the fuel chamber moves substantially in a radial direction relative to the longitudinal direction of the electrochemical membrane and / or wherein the product moves substantially in a longitudinal direction of the longitudinal direction of the electrochemical membrane, and wherein at least one electrochemical membrane can be at least one high-temperature proton exchange membrane.

[0132] Preferably, the fuel chamber and the product chamber may be separated by at least one electrochemical membrane.

[0133] In embodiments of the invention, the substantially radial direction may be substantially perpendicular to the substantially longitudinal direction.

[0134] The terms "substantially in radial direction" and / or "substantially in longitudinal direction" refer to movement directed primarily in radial or longitudinal direction, respectively, but may include longitudinal helical rotation of radial flow spacers to extend flow path helicity for improved fuel contact / residence time.

[0135] Preferably, the "substantially radial direction"; the "substantially vertical direction" and / or the "substantially longitudinal direction" may deviate from the radial direction, the vertical direction and / or the longitudinal direction by at most 20%; such as at most 15%, for example at most 10%, for example at most 5%, for example at most 2%, for example at most 1%.

[0136] Preferably, the fuel is a hydrocarbon composition. The hydrocarbon composition may comprise a hydrocarbon liquid or gas, such as methane (CH 4 ), biogas, water (H 2 O), carbon dioxide (CO 2 ), carbon monoxide (CO) and pollutants.

[0137] In the context of the present invention, the term "radial" refers to movement along a radius at a certain distance from the center of the electrochemical reactor, which distance may increase as the fuel (or gasification reaction product) moves from the inner ring of the electrochemical membrane to the outer ring of the electrochemical membrane (e.g., moving in a spiral direction, concentric direction, or radial direction).

[0138] Preferably, the product disposed in the product chamber and received at the product outlet may be hydrogen (H 2 ).

[0139] A preferred embodiment of the present invention relates to an electrochemical reactor according to the invention, a cartridge according to the invention with or without an enhanced reactor, such as a Taylor-Couette reactor (TCR) according to the invention, for at least partially converting a hydrocarbon composition into a hydrocarbon containing hydrogen (H 2 )'s composition.

[0140] Hydrocarbon compositions obtained from underground reservoirs (or introduced at the surface; as in the geothermal well option) can be fuels according to the present invention, and it is well known worldwide that there is an interest in reducing or even avoiding these potent greenhouse gas components and reaction products from these fuels such as carbon dioxide (CO 2 ) and methane (CH 4 ) emissions into the atmosphere, reducing serious environmental problems and the impact on global warming.

[0141] Therefore, there is an interest in finding more environmentally friendly alternative energy sources or alternative utilization of existing energy sources, such as fuels or hydrocarbon compositions, in a more climate-friendly manner. Intensified reactors according to the invention, such as Taylor-Couette reactors (TCR) and electrochemical membranes are solutions for such improved utilization, where the energy source can be fully or partially enriched with hydrogen (H 2 ) is provided in the form of a composition which is fully or partially enriched with hydrogen (H 2 ) can be produced in an efficient, productive and environmentally friendly and climate-friendly manner.

[0142] The intensified reactor according to the present invention may preferably be a Taylor-Couette reactor (TCR).

[0143] In an embodiment of the present invention, the enhanced reactor chamber of the electrochemical reactor may further include at least one water inlet (H 2 O-inlet) and / or at least one air inlet (O 2 - inlet). When an electrochemical reactor with or without an intensification reactor (such as a Taylor-Couette reactor (TCR)) can be used to convert carbon dioxide (CO 2 ) is injected into the reservoir, preferably at least one water inlet (H 2 O-inlet) and / or at least one air inlet (O 2 - inlet). This can lead to the production of further energy, in particular hydrogen (H 2 ):

[0144] -Boudouard reaction, in which hydrocarbon feed and carbon dioxide (CO 2 ) to provide a source of carbon monoxide other than hydrogen, and / or

[0145] - Autothermal reforming (ATR), wherein the synthesis gas (containing hydrogen (H 2 ) and carbon monoxide (CO)) can be partially oxidized by a hydrocarbon feed such as methane (CH 4 ) or biogas) and carbon dioxide (CO 2 ) and / or water (H 2 O) and / or oxygen, and / or

[0146] - Steam methane reforming (SMR), where the synthesis gas (containing hydrogen (H 2 ) and carbon monoxide (CO)) can be reacted with hydrocarbons and water (H 2 O) to produce, and / or

[0147] - Water Gas Shift Reaction (WGSR), in which carbon monoxide (CO) is reacted with water (H 2 O) is converted to provide hydrogen (H 2 ).

[0148] The at least one product outlet may be at least one hydrogen outlet (H 2 -exit).

[0149] In addition to at least one hydrogen outlet (H 2 In addition to the outlet, the electrochemical reactor according to the present invention may also include at least one carbon dioxide outlet (CO 2 - export). Found CO 2 - The outlet may be connected to the outer ring of the electrochemical membrane and may also be considered a product with value (eg, carbon credits).

[0150] Preferably, at least one hydrogen outlet (H 2 - outlet) can be connected to at least one fuel inlet and / or at least one carbon dioxide outlet (CO - outlet) by the electrochemical membrane according to the invention. 2 -export) separated.

[0151] In an embodiment of the present invention, at least one electrochemical membrane can separate hydrogen (H2) from a hydrocarbon composition, nitrogen, carbon monoxide, water and / or carbon dioxide mixture by an electrochemical separation process. 2 ). The electrochemical separation method may apply an electric current to at least one electrochemical membrane, and hydrogen may be electrochemically dissociated on a catalyst at the anode, transported across a hydrated proton exchange material, and then recovered at a catalytic cathode.

[0152] The membrane (electrochemical membrane) according to the invention may be a proton exchange membrane.

[0153] In the present context, the terms "electrochemical membrane" and "membrane" are used interchangeably.

[0154] In a further embodiment of the present invention, at least one electrochemical membrane according to the present invention may comprise at least one proton exchange material.

[0155] Preferably, the at least one electrochemical membrane comprises at least one high temperature proton exchange membrane as described herein.

[0156] In an embodiment of the present invention, the high temperature exchange membrane may be operated, may be capable of operating, may be suitable for operating at a temperature above 100°C, such as above 200°C, for example above 300°C, such as above 400°C, for example above 500°C, such as above 600°C, for example above 700°C, such as above 800°C, for example above 900°C, such as above 1000°C, for example above 1100°C, such as above 1200°C, for example in the range of 100°C-1200°C, for example in the range of 500°C-1000°C, such as in the range of 650°C-850°C, such as in the range of 675°C-800°C, for example in the range of 700°C-750°C.

[0157] The proton exchange membrane may be a solid oxide proton exchange membrane. Preferably, the proton exchange membrane may be a high temperature solid oxide proton exchange membrane.

[0158] The at least one proton exchange material may be selected from the group consisting of: an electrochemical hydrogen separator (EHS); a protonic ceramic electrochemical cell (PCEC); a solid oxide electrolyzer (SOEC); a hybrid solid oxide electrolyzer (H-SOEC); a proton exchange membrane (PEM); or a combination thereof.

[0159] A fuel, such as a hydrocarbon composition, preferably in combination with water, may be delivered from at least one fuel inlet to a fuel chamber where the hydrocarbon composition (along with optional, externally sourced, surface injected carbon dioxide CO) is fed to the fuel chamber. 2 ) can be converted into different reaction products, including hydrogen (H 2 The generated hydrogen (H 2 ) can then be electrochemically transferred through at least one electrochemical membrane, preferably a proton exchange material, to the hydrogen outlet (H 2 -exit).

[0160] Various reactions may occur in the fuel chamber and the enhanced reactor chamber, in particular, preferably providing gasification of the introduced hydrocarbon composition, resulting in hydrogen (H 2 ) is formed. The hydrogen produced (H2 ) can then be electrochemically transferred through at least one electrochemical membrane to at least one product outlet, such as a hydrogen outlet (H 2 -exit).

[0161] It may be necessary to supply energy to an enhanced reactor (e.g., a Taylor-Couette reactor (TCR)) to provide the necessary rotation of a central element that produces, for example, a Taylor-Couette flow, an ignition source for the reaction (to provide the minimum activation energy required to initiate the chemical reaction (after which the net exothermic reaction can self-propagate within the reactor)) and (if necessary) to promote the electrolysis reaction in the electrochemical reactor. The energy applied can come entirely or partially from the geological environment or the chemical reaction itself or mechanically, for example via heat transfer within the tool, a heat recovery system (HERS), a turboexpander, a turbogenerator, etc. or a combination of the above. However, in order to provide and ensure sufficient energy to the enhanced reactor (e.g., a Taylor-Couette reactor (TCR)) and the electrochemical membrane, energy can be provided from an external source via a cable or fluid injection if necessary. The external source can preferably be obtained from wind energy, solar energy and the like.

[0162] In embodiments of the present invention, the electrochemical reactor may include means for supplying energy or power to the electrochemical reactor.

[0163] In further embodiments of the invention, the electrochemical reactor may comprise means for connecting electrical cables.

[0164] The cable can provide power and energy, at least initially, for starting and / or running a process, such as a gasification and electrochemical process. During operation, the process can generate enough power and energy to support the process, and it may become unnecessary to supply power and energy, and the process may even generate excess energy that can be exported to the surface.

[0165] Without being bound by theory, it is believed that the pressure and / or temperature in subterranean operation of an electrochemical reactor according to the present invention may contribute so much energy to the process that excess energy may be created which may then be exported.

[0166] The cable may also provide a means of exporting energy if / when the electrochemical reactor provides excess energy.

[0167] A preferred embodiment of the present invention relates to a method for recovering hydrogen (H) from a fluid or gas from an underground reservoir. 2) composition, the system comprising a processing rig, the processing rig comprising an electrochemical reactor with or without an enhanced reactor, the electrochemical reactor converting the hydrocarbon composition at least partially into a gas comprising hydrogen (H 2 ) composition, wherein the system also includes a method for separating hydrogen from the reaction product and providing CO 2 Carbon capture utilisation and storage (CCUS) installations.

[0168] In the present context, the term "processing unit" may refer to a collection of surface and downhole equipment that receives a flowing stream of hydrocarbon composition (from the surface or a geological reservoir) entering the wellbore and CO from an external source at the surface. 2 The surface equipment may include processes that facilitate separation (into components), chemical or physical processing, compression or additional pumping of the hydrocarbon composition and its components for storage, further processing or export and sale.

[0169] The electrochemical reactor of the present invention can be used on the ground or in a wellbore. Preferably, the reactor can be used in a wellbore.

[0170] In an embodiment of the present invention, the electrochemical reactor may be placed in a wellbore at a vertical depth substantially equal to that of a hydrocarbon reservoir or geothermal reservoir, wherein the exhaust gas (e.g., CO 2 The exhaust gas) can be pumped into a hydrocarbon reservoir or a geothermal reservoir.

[0171] Preferably, by providing CO 2 The carbon capture device captures carbon dioxide (CO 2 ) may include CO naturally occurring in hydrocarbon compositions 2 or by converting the hydrocarbon composition at least partially into a gas comprising hydrogen (H 2 ) and the CO produced 2 , and / or CO introduced from an external source and injected from the ground 2 .

[0172] In an embodiment of the present invention, the carbon dioxide (CO 2 ) (from hydrocarbon compositions, hydrocarbons converted to hydrogen and / or introduced from external sources and injected from the surface) may also contain carbon monoxide (CO).

[0173] Preferably, hydrogen (H 2 ) may be a composition comprising hydrogen (H 2 ) of an organic composition.

[0174] According to the present invention, a fuel, such as a hydrocarbon composition, can be at least partially converted into a gas comprising hydrogen (H 2The term "at least partially" may relate to at least 1% (w / w) of the hydrocarbon composition being convertible into a hydrocarbon composition comprising hydrogen (H 2 ) composition, for example, at least 5% (w / w) of the hydrocarbon composition can be converted into hydrogen (H 2 ), such as at least 10% (w / w) of the hydrocarbon composition, for example 20% (w / w) of the hydrocarbon composition, such as at least 30% (w / w) of the hydrocarbon composition, for example 40% (w / w) of the hydrocarbon composition, such as at least 50% (w / w) of the hydrocarbon composition, for example 60% (w / w) of the hydrocarbon composition, such as at least 70% (w / w) of the hydrocarbon composition, for example 80% (w / w) of the hydrocarbon composition, such as at least 90% (w / w) of the hydrocarbon composition, for example 95% (w / w) of the hydrocarbon composition, such as at least 97% (w / w) of the hydrocarbon composition, for example 99% (w / w) of the hydrocarbon composition can be converted into a hydrocarbon gas comprising hydrogen (H 2 )'s composition.

[0175] The effect of an electrochemical membrane with or without (preferably with) an enhanced reactor according to the present invention (e.g., a Taylor-Couette reactor (TCR)) can be enhanced by:

[0176] - Separate geothermal heating (processing in the ground);

[0177] - geothermal heating in combination with heat pumps and / or heat exchangers (underground, above ground or above ground treatment); or

[0178] - geothermal heating combined with electric heating (underground treatment or above-ground or above-ground treatment);

[0179] - introduction of catalyst materials;

[0180] - Separate geological pore pressure (processed underground);

[0181] - a combination of geological pore pressure and the temperature combinations listed above; or

[0182] - Externally supplied, surface injected carbon monoxide (CO) and / or carbon dioxide (CO 2 );

[0183] - Improved electrolyte chemistry within the electrochemical membrane layer of the electrochemical reactor;

[0184] - Heat energy recovery system (HERS), combined heat and power system (CHP), turbo expander, turbo generator or similar.

[0185] Preferably, the reactor according to the invention operates in underground conditions.

[0186] Preferably, the reactor can convert the hydrocarbon composition at least partially into a hydrocarbon containing hydrogen (H 2 )'s composition.

[0187] The electrochemical reactor according to the invention, preferably with an enhanced reactor, such as a Taylor-Couette reactor (TCR), may comprise a reactor for converting, for example, carbon monoxide (CO) and / or carbon dioxide (CO 2 ) is injected into the reservoir. Carbon monoxide (CO) and / or carbon dioxide (CO 2 ) injection into underground reservoirs can be carried out via:

[0188] - and for obtaining hydrogen (H 2 ) is the same well as the well of

[0189] - and for obtaining hydrogen (H 2 ) is different from the well used to obtain hydrogen (H 2 ) is in fluid communication with a well; or

[0190] - wells entering the reservoir, where hydrogen (H 2 ) no longer occurs or has ever occurred.

[0191] Preferably, the carbon monoxide (CO) and / or carbon dioxide (CO) undergoing carbon capture 2 The method may be used to convert a hydrocarbon composition at least partially into a gas comprising hydrogen (H 2 ) composition produced by the device of carbon monoxide (CO) and / or carbon dioxide (CO 2 ).

[0192] In an embodiment of the present invention, carbon monoxide (CO) and / or carbon dioxide (CO) 2 Carbon monoxide (CO) and / or carbon dioxide (CO) may be contained in the hydrocarbon composition and may also be provided or may be derived from an external source. 2 ) and for converting a hydrocarbon composition at least partially into a gas comprising hydrogen (H 2 ) composition produced by the device of carbon monoxide (CO) and / or carbon dioxide (CO 2 ) combination.

[0193] Preferably, hydrogen (H 2 ) can be obtained from the product outlet and can be enriched with (H 2 ).

[0194] In an embodiment of the present invention, hydrogen (H 2 ) comprises at least 1% (w / w) hydrogen (H 2 ), such as at least 5% (w / w) hydrogen (H2 ), such as at least 10% (w / w), for example at least 15% (w / w), such as at least 20% (w / w), for example at least 25% (w / w), such as at least 30% (w / w), for example at least 40% (w / w), such as at least 50% (w / w), for example at least 60% (w / w), such as at least 70% (w / w), for example at least 80% (w / w), such as at least 85% (w / w), for example at least 90% (w / w), such as at least 95% (w / w), for example at least 98% (w / w) of hydrogen (H 2 ).

[0195] In embodiments of the invention, the reservoir may contain water, and the water may be at least partially converted into a hydrocarbon composition comprising hydrogen (H 2 ) is formed during the composition.

[0196] Electrolysis according to the present invention may also occur in combination with elevated subterranean temperatures and pressures to improve the conversion of fuels (e.g., hydrocarbon compositions) to hydrogen (H 2 ) of the composition.

[0197] Preferably, the electrochemical reactor with or without the enhanced reactor according to the present invention can be placed at least 100 meters TVD underground, such as at least 150 meters TVD underground, for example at least 250 meters TVD underground, such as at least 500 meters TVD underground, for example at least 750 meters TVD underground, such as at least 1000 meters TVD underground, for example at least 1500 meters TVD underground, such as at least 2000 meters TVD underground, for example at least 2500 meters TVD underground, such as at least 5000 meters TVD underground, for example at least 7500 meters TVD underground, such as at least 10,000 meters TVD underground, for example at least 12,500 meters TVD underground, such as at least 15,000 meters TVD underground.

[0198] In embodiments of the invention, an electrochemical reactor with or without an enhanced reactor may be at least 100 meters below the treatment device, such as at least 150 meters below the treatment device, for example at least 250 meters below the treatment device, such as at least 500 meters TVD below the treatment device, for example at least 750 meters TVD below the treatment device, such as at least 1000 meters TVD below the treatment device, for example at least 1500 meters TVD below the treatment device, such as at least 2000 meters TVD below the treatment device, for example at least 2500 meters TVD below the treatment device, such as at least 5000 meters TVD below the treatment device, for example at least 7500 meters TVD below the treatment device, such as at least 10,000 meters TVD below the treatment device, for example at least 12,500 meters TVD below the treatment device, such as at least 15,000 meters TVD below the treatment device.

[0199] Carbon capture according to the present invention may involve the removal of carbon monoxide (CO) and / or carbon dioxide (CO) originally present in a hydrocarbon composition or produced during the conversion of a hydrocarbon composition (or a portion thereof) into a hydrogen composition. 2 ) is the process of capturing carbon monoxide (CO) and / or carbon dioxide (CO) before it enters the atmosphere.

[0200] Carbon capture may include carbon monoxide (CO) and / or carbon dioxide (CO 2 ), of which carbon monoxide (CO) and / or carbon dioxide (CO 2 ) may not originate from a reservoir or hydrocarbon composition, but may be provided from the surface, for example from the atmosphere, by carbon capture above ground, or from any external CO 2 Market sources or industrial supplies.

[0201] It may be operationally or commercially advantageous to treat waste gases (e.g., CO 2 or CO) into an adjacent geological reservoir or formation (or vertically below or above the hydrocarbon reservoir) in the same or a different well or wellbore.

[0202] The electrochemical reactor according to the present invention may be used in geothermal processes, wherein hydrocarbon compositions may be injected from the ground.

[0203] Preferably, carbon monoxide (CO) and / or carbon dioxide (CO) originally present in the hydrocarbon composition or generated during the conversion of the hydrocarbon composition (or a portion thereof), or provided from an external supply source. 2 ) may be transported to and stored in the same reservoir as that from which the gasified hydrocarbon composition is obtained, or may be transported and stored in a different reservoir or geological formation via the same or different wells or wellbores. Preferably, the carbon dioxide (CO ) initially present in the hydrocarbon composition or generated during the conversion of the hydrocarbon composition (or a portion thereof), or provided from an external supply source 2 ) can be stored in the same reservoir via the same or different wellbores.

[0204] In a preferred embodiment of the invention, the electrochemical reactor with the electrochemical membrane may be placed underground during operation. Preferably, the electrochemical reactor with the electrochemical membrane may be placed in a subterranean wellbore. Preferably, the electrochemical reactor with the electrochemical membrane may not be placed in a reservoir, except that it remains in a wellbore that is drilled in, along, or through the reservoir and is placed at an equivalent vertical depth of the reservoir.

[0205] Preferably, underground refers to the depth of the reactor below the surface of the earth and below the sea floor.

[0206] The location of the reactor may preferably be at least 100 meters TVD underground, such as at least 150 meters TVD underground, for example at least 250 meters TVD underground, such as at least 500 meters TVD underground, for example at least 750 meters TVD underground, such as at least 1000 meters TVD underground, for example at least 1500 meters TVD underground, such as at least 2000 meters TVD underground, for example at least 2500 meters TVD underground, such as at least 5000 meters TVD underground, for example at least 7500 meters TVD underground, such as at least 10,000 meters TVD underground, for example at least 12,500 meters TVD underground, such as at least 15,000 meters TVD underground.

[0207] Preferably, the subsurface may involve hydrocarbon drilling or geothermal drilling.

[0208] In an embodiment of the present invention, the hydrocarbon composition produces a gas comprising hydrogen (H 2 )'s composition may include gasifying the hydrocarbon composition at a high temperature.

[0209] Depending on the vertical depth of the electrochemical reactor placed in the wellbore, some or all of the fluids and gases may naturally enter their supercritical fluid phases due to the hydrostatic or geothermal temperatures and pressures present in the wellbore. The supercritical phase of the fluid may further enhance the gasification process and reduce the energy required to process the hydrocarbon composition.

[0210] At shallower depths, supercritical conditions may also be induced or artificially created within the tool by techniques in which the internal pressure within the tool may be increased via applied surface pressure, flow restrictions that induce back pressure, weighted annular fluids, or a combination of these.

[0211] The hydrocarbon composition produces a gas comprising hydrogen (H 2 ) of the composition, such as a gasification process, may require a large amount of heat.

[0212] In an embodiment of the present invention, when provided to the fuel chamber, the fuel converts to hydrogen (H 2 ) can include at least one gasification process. The gasification process can be an initial gasification process, preferably in an enhanced reactor such as a Taylor-Couette reactor (TCR). Before the reaction products enter the electrochemical reactor, the gasification process is also called indirect internal reforming (IIR).

[0213] The continuous electrochemical reaction can transfer hydrogen from the reaction product concentration within the flow path to the product chamber and dynamically reduce the hydrogen concentration in the flow path. This simultaneous and spontaneous transfer and removal of hydrogen can reduce the hydrogen concentration along the flow path, which can then bias the chemical equilibrium of the gasification chemical reaction to produce more hydrogen in the flow path concentration, increasing the production and accumulation of hydrogen transferred to the product chamber.

[0214] The electrochemical reactor according to the present invention can convert the fuel into a gas containing carbon dioxide (CO 2 ) or carbon monoxide (CO). The composition comprising carbon dioxide (CO 2 ) or carbon monoxide (CO) can generate revenue streams and storage for collection and capture at waste outlets. 2 The initiation of the composition of carbon monoxide (CO) or carbon monoxide (CO) may include at least one gasification process, preferably in an enhanced reactor.

[0215] Transferring hydrogen from the gasification reaction products to a product compartment via an electrochemical membrane, such as within a spiral electrochemical membrane path, can increase the concentration of waste products within the path. Water and waste gases such as CO 2 or CO can thus be obtained in an increased concentration at at least one waste material outlet, allowing the discharge or collection of concentrated waste gases such as CO 2 or CO for revenue stream or capture purposes. If operational optimization requires, products (hydrogen) and waste (e.g. CO 2 The flow streams of CO and CO can also be exchanged or interchanged.

[0216] A large amount of heat may be required to drive the hydrocarbon composition to produce hydrogen (H 2 ) of the composition, such as a gasification process, can be above the minimum chemical reaction activation energy and can be in the range of 100°C-1200°C, for example in the range of 500°C-1000°C, such as in the range of 650°C-850°C, such as in the range of 675°C-775°C, for example about 700°C.

[0217] Any residual fuel and gasification reaction products may also undergo direct internal reforming (DIR) or further gasification within the electrochemical reactor to produce hydrogen (H 2 ).

[0218] In an embodiment of the present invention, the performance of the electrochemical reactor can be further improved by the wellbore pressure, which can depend on various parameters, such as the depth of the wellbore (or the depth of the reactor in the wellbore), the specific underground reservoir, the location of the underground reservoir; different rock types surrounding the underground reservoir and / or the wellbore, different fluid / gas contents, geological structures and / or formation thicknesses, etc.

[0219] Geothermal heating and / or geological pore pressure can be used as an energy source or significant energy contribution to heat and accelerate the hydrocarbon composition to contain hydrogen (H 2 ) chemical reaction of the composition, such as gasification process, leads to a significant reduction in production energy costs. Geological temperature and pore pressure can also be used as energy source to make part of the reaction composition supercritical (such as CO 2 , H 2 and H 2 O) transformation, increasing the speed, energy and efficiency of the reaction.

[0220] Geothermal heating and / or geological pore pressure can come from geothermal energy and is energy from the Earth's interior. Geothermal energy is thought to originate from the formation of the planets and from the radioactive decay of matter. The high temperatures and pressures within the Earth's interior can cause some rocks to melt, and the solid mantle to behave plastically, causing parts of the mantle to convect upward because it is lighter than the surrounding rock and the temperature at the core-mantle boundary can reach over 4000°C.

[0221] Geothermal heating and / or geological pore pressure, for example using water from hot springs, has been used for bathing since the Paleolithic era and for space heating since Roman times, however more recently geothermal power (the term used for electricity generated from geothermal energy) has become more important. It is estimated that the Earth's geothermal resources are theoretically sufficient to meet humanity's energy needs, although currently only a small portion is being profitably exploited, usually in areas close to tectonic plate boundaries.

[0222] When recovering water from a water reservoir, recovering hydrocarbon compositions from a gas reservoir, or recovering hydrocarbon compositions from an oil reservoir, the depth of the reservoir can determine the temperature, pressure, and geothermal energy. Generally, the deeper the reservoir is below the earth's surface, the higher the geothermal energy and the higher the temperature, although geological anomalies do exist where higher temperatures and pressures are found at shallower depths than predicted by normal geological gradients.

[0223] Therefore, the inventors of the present invention surprisingly found a method for utilizing geothermal energy to produce a gas containing hydrogen (H 2 ) composition. 2 ) can be preferably produced with potent greenhouse gases (GHG) such as carbon dioxide (CO 2 ) and / or methane (CH 4 ) emissions and discharges. This can be achieved by increasing the amount of methane (CH 4 ) (e.g. biogas or biomethane), carbon monoxide (CO) and / or carbon dioxide (CO 2 ) can be further improved by ground injection.

[0224] This improvement can be achieved by an electrochemical reactor with or without (preferably with) an enhanced reactor according to the present invention.

[0225] In embodiments of the invention, the underground reservoir may be a liquid hydrocarbon reservoir, such as an oil reservoir (underground oil reservoir), a gaseous hydrocarbon reservoir, such as a gas or condensate reservoir (underground gas reservoir) or a geothermal reservoir (underground geothermal reservoir).

[0226] Preferably, the electrochemical reactor with or without the enhanced reactor according to the present invention may be suitable for recovering products, in particular hydrogen compositions (H 2 -composition). Preferably, the underground reservoir may be a liquid hydrocarbon reservoir, such as an oil reservoir (underground oil reservoir), a gaseous hydrocarbon reservoir, such as a gas or condensate reservoir (underground gas reservoir) or a geothermal reservoir (underground geothermal reservoir).

[0227] The intensified reactor according to the present invention may comprise a rotating energy unit. The rotating unit may preferably rotate around a central axis of the reactor. In an embodiment of the present invention, the electrochemical reactor may comprise an intensified reactor, such as a Taylor-Couette reactor (TCR).

[0228] The energy unit may be supplied to an enhanced reactor, such as a Taylor-Couette reactor (TCR), and / or an electrochemical membrane of the present invention.

[0229] In an embodiment of the invention, an enhanced reactor, such as a Taylor-Couette reactor (TCR), may provide a rotation in the range of 100rpm-30,000rpm, such as in the range of 500rpm-8,000rpm; for example in the range of 1,000rpm-6,000rpm; such as in the range of 1500rpm-5,000rpm; for example in the range of 2,000rpm-4,000rpm; such as in the range of 2500rpm-3,500rpm; for example at about 3,000rpm.

[0230] The inventors of the present invention have found that by providing the electrochemical reactor according to the present invention as a cartridge comprising one or more cartridge elements according to the present invention, scalability, repairability, maintainability, sustainability and / or cost can be significantly improved. The cartridge configuration can allow for sequential / piecewise repair or replacement, field repair or replacement, resulting in less downtime, less material waste and higher productivity.

[0231] A preferred embodiment of the present invention relates to a box comprising one or more box elements, wherein one or more box elements include an electrochemical reactor, the electrochemical reactor including at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane.

[0232] Another preferred embodiment of the present invention relates to a box comprising one or more box elements, wherein the one or more box elements include an electrochemical reactor, the electrochemical reactor including at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein at least one electrochemical membrane includes at least one high-temperature proton exchange membrane.

[0233] The product chamber may be located inside the electrochemical membrane.

[0234] Preferably, the membrane separating the fuel chamber and the product chamber may comprise at least one electrochemical reactor layer.

[0235] In an embodiment of the invention, the fuel chamber may include at least one waste / exhaust outlet fluidly connected to the outer ring.

[0236] In the context of the present invention, the term "box" may refer to a container or box that holds an electrochemical membrane of an electrochemical membrane shape and / or electrochemical membrane structure according to the present invention, provides a fuel chamber and is ready to receive an enhanced reactor, such as a Taylor-Couette reactor (TCR), and is then ready for use.

[0237] In an embodiment of the present invention, one or more box elements may be one or more annular cylindrical box elements.

[0238] The box according to the present invention may include multiple box elements, such as 2 or more box elements, for example 3 or more box elements, such as 5 or more box elements, for example 7 or more box elements, such as 10 or more box elements, for example 12 or more box elements, such as 15 or more box elements, for example 20 or more box elements, such as 25 or more box elements, for example 50 or more box elements, such as 75 or more box elements, for example 100 or more box elements.

[0239] In embodiments of the invention, one or more annular cylindrical boxes may be provided with a central aperture for receiving a fortified reactor, such as a Taylor-Couette Reactor (TCR).

[0240] In further embodiments of the present invention, a fuel chamber may be formed between an interior space formed between a cartridge and a enhanced reactor, such as a Taylor-Couette Reactor (TCR).

[0241] When the box comprises a plurality of box elements, the box elements may be stacked on top of each other, thereby providing a central hole through the box comprising the plurality of box elements.

[0242] The central hole of the box or one or more annular cylindrical box elements can form an enhanced reactor chamber and can allow the insertion of an enhanced reactor, such as a Taylor-Couette reactor (TCR). When an enhanced reactor (such as a Taylor-Couette reactor (TCR)) can be inserted into the central hole of the annular cylindrical box, a fuel chamber can be formed between the outer surface of the enhanced reactor (such as a Taylor-Couette reactor (TCR)) and the inner ring of the electrochemical membrane.

[0243] The intensified reactor may be a fluid oscillator.

[0244] Fluid oscillators can be based on the Coanda and / or Bernoulli effects.

[0245] Preferably, the fluid oscillator can be selected from an oscillating baffle reactor, an ejector device that induces hydrodynamic cavitation or allows pulsating flow by ultrasound or mechanical vibration, a static mixer reactor, a microreactor, an ejector loop reactor or a reactor based on Taylor-Couette flow (e.g., Taylor-Couette reactor, TCR). Preferably, the intensified reactor or fluid oscillator can be a reactor based on Taylor-Couette flow (particularly Taylor-Couette reactor, TCR).

[0246] In an embodiment of the present invention, at least one electrochemical membrane of the annular cylindrical cartridge may include a spiral membrane structure, a corrugated membrane structure, a concentric radial membrane structure, a radial star membrane structure, or a disk membrane structure.

[0247] The annular cylindrical box may include a spiral membrane structure or a concentric radial membrane structure, or a radial star membrane structure, or a disk membrane structure combined with a corrugated membrane structure.

[0248] The electrochemical membrane of the ring-shaped cylindrical case may include a single electrochemical membrane or a plurality of electrochemical membranes, wherein the plurality of electrochemical membranes may be arranged with one electrochemical membrane surrounding another electrochemical membrane with a radius increasing from the center of the ring-shaped cylindrical case.

[0249] In an embodiment of the present invention, the electrochemical membrane of the annular cylindrical box may include a spiral membrane structure in which the radius of the electrochemical membrane (relative to the center of the electrochemical membrane) continuously increases when moving along the electrochemical membrane when formed around the center of the annular cylindrical box.

[0250] In another embodiment of the present invention, the electrochemical membrane of the annular cylindrical box may include a concentric radial membrane structure, wherein cylindrical membranes with a constant but increasing radius (relative to the center of the electrochemical membrane) may be placed around each other, wherein the concentric radial membrane structure with the smallest radius closest to the center of the annular cylindrical box and the concentric radial membranes with a larger radius are arranged around as the radius increases.

[0251] The radial star-shaped electrochemical membrane structure may include several electrochemical membranes according to the present invention, preferably multiple individual electrochemical membranes are held by radial flow spacers. Multiple individual electrochemical membranes may be provided in various sizes to increase the total electrochemical membrane surface area as the radius increases from the center of the box. Preferably, the radial star-shaped electrochemical membrane structure is not provided as an annular box element. However, for ease of use and handling, the assembled star-shaped structure may be contained within an outer annular box housing. Fig. 9 An example of a radial star electrochemical membrane structure is shown.

[0252] The disc electrochemical membrane structure can allow easy replacement of cylindrical discs, easy to scale up or down, and easy to 3D print complex shapes during manufacturing. The electrochemical disc membrane structure can include an electrochemical membrane according to the present invention. The flow path size of the disc electrochemical membrane structure can be changed by height (straight, converging, diverging, wavy), width (straight, converging, diverging or wavy), obstacles in the channel (baffles, traps, spoiler columns, etc.), direction (spiral, straight, star-shaped, Z-shaped, leaf-shaped, etc.), cross-sectional shape (circular, semicircular, rectangular or triangular), cross-sectional shape (with or without sub-channels), flow path outlet (or dead end) and the number of inlets, suitable for adjusting the residence time (e.g., providing a long, medium or very short residence time for the membrane), and an even number of Archimedean spirals that make the cathode and anode offset relative to each other. The disc reactor can include multiple disc membranes stacked to a desired axial length. Fig.10 An example of a disc membrane structure is shown. Construction using 3D printing can be used to print the above complex flow paths.

[0253] The electrochemical membrane may preferably surround the fuel chamber of the electrochemical reactor.

[0254] It should be noted that embodiments and features described in the context of one aspect of the invention may also be applicable to other aspects of the invention.

[0255] The present invention will now be described in further detail in the following detailed description of the accompanying drawings.

[0256] Figure 1a shows a radial view of a spiral membrane (1) according to the invention, and Figure 1b It shows that Figure 1a A longitudinal view of a spiral electrochemical membrane (1) is shown.

[0257] Figure 1a and Figure 1b An example of a spiral electrochemical membrane (1) mounted around a rotating enhanced reactor (e.g., a Taylor-Couette reactor (TCR)) is shown, with the rotating enhanced reactor (2) located in the center of the spiral in the enhanced reaction chamber (24). The spiral electrochemical membrane (1) includes a fuel chamber (3). The fuel chamber (3) can extend from an inner ring (4) to an outer ring (5) along a flow path (6) formed by the spiral electrochemical membrane (1). The inner ring (4) contains both a fuel (such as a hydrocarbon composition) and reaction products from its gasification reaction within the inner ring (4). Any remaining fuel, such as a hydrocarbon composition and gasification gas, moves along the flow path (6) of the spiral electrochemical membrane (1) from the inner ring (4) toward the outer ring (5). The fuel, such as a hydrocarbon composition, can further react to produce hydrogen ions (H + ) and gasification gas. Hydrogen contained in the gasification reaction product reacts with the electrochemical membrane and is removed from the hydrocarbon composition flow path (6). The longer the hydrocarbon composition and the gasification reaction product move along the flow path (6), the lower the concentration of hydrocarbons in the flow path (6) and the higher the concentration of the remaining gasification gas, and the higher the concentration of hydrogen (H 2 ) is formed in the product chamber (10). Preferably, water and waste gases such as CO 2 or CO can be obtained at the outer ring (5). At least one waste material outlet (not shown) can be provided in fluid connection with the outer ring (5) to allow exhaust gases, such as CO, to be discharged or collected. 2 or CO.

[0258] When the fuel (hydrocarbon composition) and the gasification reaction products move from the inner ring (4) along the flow path (6), the anode (8) disposed on the outer surface of the spiral electrochemical membrane (1) (and also on the outer surface of the corrugated layer (18)) can generate hydrogen ions (protons, H + ), the hydrogen ions move through the electrolyte (7) within the corrugated layer (18) to the cathode (9) (the inner surface of the corrugated layer (18), which also serves as the surface of the product chamber (10)), where the hydrogen ions receive electrons and reform into hydrogen atoms, which then recombine with another hydrogen atom (H) and produce hydrogen gas (H) in the product chamber (10). 2 ).

[0259] Non-conductive radial flow spacers (15) are arranged circumferentially (at longitudinal intervals) along the helical length of the electrochemical membrane (1) to prevent the electrochemical membrane from contacting itself and to provide a flow path (6) for the fuel (e.g., hydrocarbon composition) and gasification reaction products as they travel from the inner ring (4) to the outer ring (5).

[0260] The spiral electrochemical membrane (1) shown in Figure 1 may or may not include an electrochemical membrane comprising a corrugated layer (18). The corrugated layer (18) may include a single corrugated layer, such as a double corrugated layer, for example a triple corrugated layer, such as a quadruple corrugated layer.

[0261] Figure 2: Figure 2a An electrochemical membrane (1) for an electrochemical reactor according to the invention is shown, which has two corrugated layers (18), and a view of how the membrane can be spiraled to form a spiral electrochemical membrane (1) according to the invention ( Figure 2b ), having a centrally placed intensified reactor such as a Taylor-Couette reactor (TCR) placed in an intensified reaction chamber (24). The corrugated layer (18) is provided with a plurality of anodes (8) facing the fuel chamber (3) and cathodes (9) facing the product chamber (10). An electrolyte (7) may be placed between the anodes (8) and the cathodes (9). Hydrogen (H 2 ) can be produced and stored in the product chamber (10) as described above. The fuel can be provided to the fuel chamber (3) for example via a fuel permeable liner (11) of the structure of the auxiliary electrochemical membrane (1). The liner (11) can be used as a layer of the corrugated layer (18) of the electrochemical membrane (1). The liner (11) / layer is provided with an anode (8), which is connected to the corrugated layer (18) on the fuel chamber side of the electrochemical membrane (1). The corrugated layer (18) is also provided with a cathode (9), which is connected to the gas permeable liner (13) on the product chamber side of the electrochemical membrane (1). A flow path (6) is formed on one or both sides of the electrochemical membrane (1).

[0262] Figure 3 A 3-layer electrochemical membrane (1) is shown, where two layers (12) (top and bottom) are straight, and one corrugated layer (18) is provided with an anode (8), an electrolyte (7) and a cathode (9) to promote hydrogen (H 2 ) is formed as previously described. The fuel chamber may be an area outside the top layer (12) and the bottom layer (12). A product chamber (10) is formed between the layer (12) and the corrugated layer (18). Fuel may be provided to the fuel chamber (3) surrounding the top layer (12) and the bottom layer (12), and a flow path (6) is formed on one or both sides of the electrochemical membrane (1).

[0263] Figure 4A 4-layer electrochemical membrane (1) is shown, wherein two layers (12) (a top layer (12) and a bottom layer (12)) are straight, and two corrugated layers (18) are disposed between the straight layers (12). The fuel chamber (3) may be an area outside the top layer (12) and the bottom layer (12), and a product chamber (10) is formed between the layer (12) and the corrugated layer (18). The two corrugated layers may be formed by allowing hydrogen (H 2 ) is separated by a gas permeable liner (13) for transferring from one product chamber (10) to another product chamber. The layer (12) and the corrugated layer (18) may be provided with an anode (8), an electrolyte (7) and a cathode (9) to promote hydrogen (H 2 ) is formed as previously described. A flow path (6) is formed on one or both sides of the electrochemical membrane (1).

[0264] Figure 5 It shows that Figure 4 A 4-layer electrochemical membrane is described and the diagram shows the advantage of multiple layers (12 / 18) in the electrochemical membrane, namely that the vulnerability to indirect damage, such as due to localized thermal damage on the electrochemical membrane (1), is significantly reduced due to the formation of hot spot holes (14) or scale in the layer (12) of the electrochemical membrane (1). These hot spots (14) may cause mixing of fuel and product, whereby the product stream may be contaminated. However, when operating with, for example, a 3-layer or 4-layer electrochemical membrane, the hot spots (14) in one layer may allow hydrogen (H 2 ) product moves to an adjacent product chamber (10). This therefore provides intentional built-in redundancy for durability, reliability, life and productivity, while improving mechanical strength and robustness to reduce the probability of tool failure events.

[0265] FIG. 6 schematically shows a spiral structure according to the invention for an electrochemical membrane. Figure 6a A single spiral is shown, preferably a single Archimedean spiral. In order to increase the volume throughput of the fuel and gasification gas in the electrochemical membrane, the number of flow paths (6) for the fuel and gasification gas can be increased, and multiple spirals can be used, wherein each spiral used provides a separate flow path (6). Preferably, the multiple spirals can be Archimedean multiple spirals, wherein the individual spirals each start at intervals of X degrees of arc [ Figure 6b ] - depends on the number of spirals included. An advantage of using multiple spirals can be to reduce the measured length of each spiral (per cross-sectional area) and thereby reduce the gas residence time (per spiral). In addition, the use of multiple spirals can increase the gas rate throughput because as each spiral flow path (6) is shorter, it provides lower pressure losses and the total cross-sectional area available for flow increases. (i.e., from one flow path (6) to multiple flow paths (6) that are open to flow from the inner ring (4) to the outer ring (5)).

[0266] A flow path (6) may involve the distance that the fuel and / or gasification gas moves from the inner ring along the spiral electrochemical membrane surface to the outer ring.

[0267] This flow path allows the electrochemical membrane to electrochemically screen valuable gasification reaction products from an enhanced reactor, such as a Taylor-Couette Reactor (TCR), into a separate flow stream for sale or capture.

[0268] In FIG6 , the spiral electrochemical membrane can be illustrated as a single spiral electrochemical membrane ( Figure 6a )、3 spiral electrochemical membrane ( Figure 6b )、7 spiral electrochemical membrane ( Figure 6c ) and 20 spiral electrochemical membranes ( Figure 6d ).

[0269] The Archimedean spiral allows multiple spirals to be initiated simultaneously from a central ring of an intensified reactor, such as a Taylor-Couette reactor (TCR), increasing volume throughput and reducing residence time and pressure drop within the spiral when necessary. The number of spirals is tailored to optimize the process.

[0270] Figure 7 An example of a configuration of an electrochemical membrane (1) mounted in the center of a spiral around an enhanced reactor (2), such as a Taylor-Couette reactor (TCR).

[0271] In step I, the cathode (9) can be prepared from cathode material as a series of capillaries that produce product chambers (10), and the capillaries can be connected to a series of product chambers. These capillaries act like pseudo-corrugations.

[0272] In step II, an electrolyte (7), such as a ceramic solid oxide coating, may be placed on the surface of the cathode (9) provided in step I.

[0273] In step III, a flexible insulator (16) may be placed to avoid contact between the anode (8) and cathode (9).

[0274] In step (IV), a coating of anode material may be placed on the electrolyte (7) provided in step II.

[0275] In step (V), the finished electrochemical membrane (1) comprises a series of capillaries having an electrolyte coating (7), the capillaries comprising a cathode (9) on the inside facing the product chamber (10) and an anode (8) on the outside facing the fuel chamber (3), wherein the cathode (9) and the anode (8) are separated by the electrolyte (7) and a flexible insulator (16).

[0276] The electrochemical membrane (1) provided can be installed in, for example, a ring-shaped cylindrical box and placed around a centrally placed enhanced reactor (2) (for example, a Taylor-Couette reactor (TCR)), and a spiral electrochemical membrane (1) is provided around the enhanced reactor (for example, a Taylor-Couette reactor (TCR)). The spiral electrochemical membrane (1) includes a fuel chamber (3). The fuel chamber (3) can extend from an inner ring (4) to an outer ring (5) along a flow path (6) formed by the spiral electrochemical membrane (1).

[0277] Non-conductive radial flow spacers (15) are arranged circumferentially (at longitudinal intervals) along the helical length of the electrochemical membrane (1) to prevent the electrochemical membrane from contacting itself and to provide a flow path (6) for the fuel (e.g., hydrocarbon composition) and gasification reaction products as they travel from the inner ring (4) to the outer ring (5).

[0278] Figure 8 An example of the construction of a spiral electrochemical membrane (1) with internal corrugations (18) is shown, which is printed around an enhanced reactor (2) (e.g., a Taylor-Couette reactor (TCR)) in the center of the spiral. The anode (8), electrolyte (7), and cathode (9) layers can be 3D printed onto a liner (11) simultaneously in a corrugated pattern using a multi-head printer (17), each printer having its own specific "ink" (e.g., ink of metal, electrolyte, and insulator) to be deposited. Radial flow spacers (15) of insulating material are printed on the liner at intervals circumferentially and perpendicular to the longitudinal product chamber (10) to maintain the flow path between the individual spiral electrochemical membrane (1) wraps. Printing is continued until the desired outer diameter is reached. The space inside the two corrugated layers (18) can form a product chamber (10), and a fuel chamber (3) is set outside the two corrugated layers (18). A permeable liner (13) can be set between the two corrugated layers (18).

[0279] Fig. 9 A cassette (19) in the form of a radial star reactor (20) is shown, the cassette (19) comprising a plurality of radial star membrane structures (21) comprising an electrochemical membrane according to the present invention. The plurality of radial star membrane structures (21) are individual electrochemical membranes held by radial flow spacers (15). Fig. 9 In the invention, a plurality of radial star-shaped membrane structures (21) are provided in various sizes to increase the total electrochemical membrane surface area as the radius increases from the center of the box (19). The box (19) is provided with a central hole for receiving an enhanced reactor (2) in the form of a Taylor-Couette reactor (TCR).

[0280] Fig.10A cassette (19) in the form of a cylindrical disc reactor (22) is shown, which may include a plurality of disc membranes (23) stacked to a desired axial length. The disc membrane structure (23) may preferably include an electrochemical membrane according to the invention. The cassette (19) is provided with a central aperture for receiving an enhanced reactor (2) in the form of a Taylor-Couette reactor (TCR).

[0281] Reference numerals

[0282] 1) Electrochemical reactor

[0283] 2) Enhanced reactors, such as Taylor-Couette reactors (TCR)

[0284] 3) Fuel chamber

[0285] 4) Inner ring

[0286] 5) Outer ring

[0287] 6) Flow path

[0288] 7) Electrolytes

[0289] 8) Anode

[0290] 9) Cathode

[0291] 10) Product Room

[0292] 11) Pad / layer

[0293] 12) Electrochemical membrane (including anode, electrolyte and cathode)

[0294] 13) Breathable lining

[0295] 14) Hotspot

[0296] 15) Radial flow spacers

[0297] 16) Flexible insulator

[0298] 17) 3D printing head (including various materials)

[0299] 18) Corrugated electrochemical membrane layer (including anode, electrolyte and cathode)

[0300] 19) Box

[0301] 20) Radial star reactor

[0302] 21) Radial star-shaped membrane structure

[0303] 22) Disc Reactor

[0304] 23) Disc membrane structure

[0305] 24) Strengthen the reaction chamber.

Claims

1. An electrochemical reactor, comprising at least one fuel inlet connected to a fuel chamber fluid located inside the electrochemical reactor, and at least one product outlet connected to a product chamber fluid located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane is folded or printed in a spiral shape around the fuel chamber of the electrochemical reactor, and wherein the at least one electrochemical membrane comprises at least one high-temperature proton exchange membrane.

2. An electrochemical reactor according to claim 1, wherein the electrochemical membrane is provided with an anode surface (8) facing the fuel chamber and the spiral flow path (6), and / or wherein the electrochemical membrane is provided with a cathode surface (9) facing the product chamber.

3. An electrochemical reactor according to any one of the preceding claims, wherein the electrochemical membrane is a proton conducting electrochemical membrane.

4. An electrochemical reactor according to any of the preceding claims, wherein the at least one electrochemical membrane between the fuel chamber and / or the product chamber can include at least one layer, wherein at least one layer can be a corrugated layer.

5. An electrochemical reactor according to any one of the preceding claims, wherein the centre of the electrochemical reactor comprises an intensified reactor or part thereof, such as a Taylor-Couette reactor (TCR) or part thereof.

6. An electrochemical reactor according to any one of the preceding claims, wherein when a fuel is provided to the fuel chamber, the conversion of the fuel into hydrogen (H2) in the product chamber comprises at least one gasification process.

7. An electrochemical reactor according to any one of the preceding claims, wherein the high temperature electrochemical membrane is capable of operating at a temperature above 100°C.

8. An electrochemical reactor according to any one of the preceding claims, wherein the electrochemical reactor comprises means for supplying energy or power to the electrochemical reactor.

9. A box comprising one or more box elements, wherein the one or more box elements comprise an electrochemical reactor, the electrochemical reactor comprising at least one fuel inlet fluidly connected to a fuel chamber located inside the electrochemical reactor, and at least one product outlet fluidly connected to a product chamber located inside the electrochemical reactor, wherein the fuel chamber and the product chamber are separated by at least one electrochemical membrane, wherein the at least one electrochemical membrane comprises at least one high-temperature proton exchange membrane.

10. The cartridge of claim 9, wherein the one or more cartridge elements are one or more annular cylindrical cartridge elements.

11. Cassette according to any of claims 9-10, wherein the cassette, in particular the one or more annular cylindrical cassette elements, is provided with a central hole for receiving an intensified reactor.

12. The cartridge of claim 11, wherein the fuel chamber is formed between an internal space formed between the cartridge and the enhanced reactor.

13. An enhanced reactor, such as a Taylor-Couette reactor (TCR), comprising an energy unit and an enhanced reaction chamber surrounded by an electrochemical reactor jacket, the enhanced reaction chamber comprising at least one fuel inlet and at least one hydrogen outlet (H2-outlet); wherein the electrochemical reaction chamber comprises an electrochemical membrane separating the at least one fuel inlet and the at least one hydrogen outlet.

14. An electrochemical reactor comprising an electrochemical membrane and at least one fuel inlet fluidly connected to a spiral flow path (6) and a fuel chamber located inside the electrochemical reactor, and at least one product outlet fluidly connected to a product chamber located inside the electrochemical reactor, wherein the fuel provided to the fuel chamber moves substantially in a radial direction relative to the longitudinal direction of the electrochemical membrane and / or wherein the product moves substantially in a longitudinal direction of the longitudinal direction of the electrochemical membrane, and wherein at least one electrochemical membrane can be at least one high-temperature proton exchange membrane.

15. An electrochemical reactor according to any one of claims 1 to 8 or claim 14, or a box according to any one of claims 9 to 12, or an enhanced reactor according to claim 13, such as a Taylor-Couette reactor (TCR), for at least partially converting a hydrocarbon composition into a composition comprising hydrogen (H2).

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