Catalytic reactor

Abstract

There is provided a catalytic reactor device for facilitating an endothermic reaction of a reactant, the catalytic reactor device comprising: a burner for generating heat; a catalytic reactor for facilitating the endothermic reaction, wherein the heat generated by the burner is used to drive the endothermic reaction; wherein the catalytic reactor comprises one or more reactor elements arranged around a perimeter of the burner, wherein each reactor element comprises a flow structure configured to allow a flow of the reactant through the flow structure, wherein the flow structure extends along an axial direction of the burner and is arranged for heat exchange with the burner.

Description

[0001] CATALYTIC REACTOR

[0002] TECH N ICAL FI ELD

[0003] The present invention relates to a catalytic reactor, and in particular to a catalytic reactor for ammonia cracking, and to methods of performing endothermic reactions and / or cracking ammonia using the same.

[0004] BACKG ROU N D

[0005] Hydrogen is widely regarded as an important part of future energy solutions and chemical industries, offering a clean and sustainable alternative to fossil fuels. As a clean energy source, hydrogen emits only water when combusted or used in fuel cells, resulting in zero carbon emissions. Being the most abundant element in the universe and possessing a high energy content per unit mass, hydrogen serves as an efficient energy carrier. It can be employed in fuel cells for electricity generation, used as a fuel for transportation, and function as a vital feedstock in various industrial processes.

[0006] However, despite its advantages, the utilization of hydrogen presents notable challenges. Storing and distributing hydrogen in liquid form requires either high- pressure containment or extremely low temperatures, both of which are energy-intensive and costly. Additionally, heat leakage during storage and distribution can cause "boil-off," leading to significant hydrogen loss through evaporation. Establishing the necessary infrastructure for widespread hydrogen adoption also entails substantial financial investment. Moreover, hydrogen's highly flammable nature necessitates stringent safety measures during handling and storage.

[0007] Given these challenges, ammonia (NH3) is increasingly recognized as a promising hydrogen carrier due to its advantages in storage, transport, and energy density. Ammonia offers an alternative means of storing and transporting hydrogen, enabling efficient distribution from production regions to end-use locations. When using ammonia as a hydrogen carrier, the hydrogen must first be released by cracking the ammonia before being utilized as fuel in gas turbines, fuel cells, or as feedstock for industrial processes. This process, known as ammonia cracking, involves the catalytic decomposition of ammonia into its constituent elements, hydrogen and nitrogen.

[0008] As ammonia cracking is an endothermic reaction, it requires an external heat source to proceed. Existing methods either provide direct heat input to the process or couple it with an exothermic reaction to supply the necessary energy for cracking. However, known reactors and devices for performing ammonia cracking are bulky, require high pressure, have low combustion temperature, require a lot of catalyst material, or any other of a number of drawbacks.

[0009] Embodiments of the present invention thus seek to provide enhanced ammonia cracking reactors, devices, methods and other implementations that improve their performance in ammonia cracking (and other catalytic reactions) as well as providing new functionality and methods.

[0010] SU M MARY

[0011] The invention is defined by the appended independent claims. Additional features and advantages of the concepts disclosed herein are set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the described technologies. The features and advantages of the concepts may be realized and obtained by means of the instruments and combinations particularly pointed out in the appended claims. These and other features of the described technologies will become more fully apparent from the following description and appended claims, or may be learned by the practice of the disclosed concepts as set forth herein.

[0012] An objective of the present invention is to provide a catalytic reactor with superior heat transfer capacity and a very compact design. It is another objective is to provide a catalytic reactor for efficient cracking of ammonia.

[0013] In a first aspect, there is provided a catalytic reactor device for facilitating an endothermic reaction of a reactant, the catalytic reactor device comprising: a burner for generating heat; a catalytic reactor for facilitating the endothermic reaction, wherein the heat generated by the burner is used to drive the endothermic reaction; wherein the catalytic reactor comprises one or more reactor elements arranged around a perimeter of the burner, wherein each reactor element comprises a flow structure configured to allow a flow of the reactant through the flow structure, wherein the flow structure extends along an axial direction of the burner and is arranged for heat exchange with the burner. In some embodiments, the reactor elements and / or the flow structures may be arranged differently, so long as they can facilitate the endothermic reaction using heat transferred from the burner.

[0014] The catalytic reactor device according to the first aspect has a reduced size allowing the reactor to be placed even in small spaces. There is also an improved heat transfer capability between the burner to the catalytic reactor. Thus, the endothermic reaction can be performed at high temperature increasing the conversion efficiency of the reaction and reducing the amount of catalyst material required.

[0015] Optionally, the flow structure of each reactor element comprises a first flow structure element and a second flow structure element, wherein the first flow structure element is configured to allow a flow of the reactant in a first axial direction, and wherein the second flow structure element is configured to allow a flow of the reactant in a second and opposite axial direction. The reactant inlet, the air inlet, and / or the mixer are accordingly located at the same end of the device simplifying installation and reducing space requirements.

[0016] Optionally, the first flow structure element is arranged radially closer to the burner than the second flow structure element. The heat transfer is accordingly greater to the first element than to the second element increasing the efficiency of the device and the catalytic reaction.

[0017] Optionally, the first flow structure element is arranged for heat exchange with the burner, and / or provided with a catalyst, and / or configured to facilitate the endothermic reaction.

[0018] Optionally, the second flow structure element is arranged for heat exchange with the burner so as to pre-heat the reactant. A temperature in the reactor (where the endothermic reaction is performed) can accordingly be increased, thus improving the conversion efficiency of the reaction and reducing the amount of catalyst material required.

[0019] Optionally, the first and / or second flow structure element comprises a pipe. The pipe shape has a large surface area allowing large heat transfer from the burner. The pipe may be made of metal or other thermally conductive material.

[0020] Optionally, the burner is a catalytic burner configured to perform a combustion reaction so as to generate the heat. The combustion reaction may also be referred to as an exothermic reaction. Accordingly, no external heat input is required, or at least the external heat input may be reduced.

[0021] Optionally, the catalytic burner comprises: a burner inlet for receiving one or more combustion reactants used in the combustion reaction, and a burner outlet for expelling one or more combustion products resulting from the combustion reaction, wherein optionally the burner outlet is arranged to allow a radial flow of the combustion products, optionally wherein the radial flow is across the one or more flow structures so as to provide the heat exchange. Optionally, the heat exchange between the burner and the one or more flow structures is provided via the combustion products leaving the burner outlet. The inventors have found such arrangements to further improve the heat transfer capabilities while further reducing the size of the reactor device.

[0022] Optionally, an outlet of the one or more flow structures is connected to the burner inlet. Thus, a product of the endothermic reaction may be used as fuel in the combustion reaction.

[0023] In a second aspect, there is provided a method of performing an endothermic reaction of a reactant, the method comprising: generating heat in a burner; provide a flow of reactant through one or more flow structures of one or more reactor elements arranged around a perimeter of the burner and extending along an axial direction of the burner; transferring heat from the burner to the reactant flowing through the one or more flow structures; and performing the endothermic reaction in the one or more flow structures using the heat transferred from the burner.

[0024] Optionally, the step of generating heat comprises performing an exothermic reaction, optionally wherein the exothermic reaction comprises reacting hydrogen with oxygen.

[0025] Optionally, the step of transferring heat from the burner comprises: providing a radial flow of combustion products from the exothermic reaction across the one or more flow structures, and transferring heat from the combustion products to the one or more flow structures.

[0026] Optionally, the method further comprises providing a flow of one or more products from the endothermic reaction to the burner, wherein the or more products from the endothermic reaction is used in the exothermic reaction in the burner.

[0027] Optionally, the step of providing a flow of reactant comprises providing a flow of reactant in a first axial direction in a first flow structure element of the flow structure, and providing a flow of reactant in a second and opposite axial direction in a second flow structure element of the flow structure, wherein optionally the endothermic reaction is performed in the first flow structure element, wherein optionally the method further comprises pre-heating the reactant in the second flow structure element using heat generated by the burner.

[0028] Optionally, the reactant is ammonia. Optionally the endothermic reaction is an ammonia cracking reaction.

[0029] BRI EF DESCRIPTION OF TH E DRAWINGS

[0030] In order to best describe the manner in which the above-described embodiments are implemented, as well as define other advantages and features of the disclosure, a more particular description is provided below and is illustrated in the appended drawings. Understanding that these drawings depict only exemplary embodiments of the invention and are not therefore to be considered to be limiting in scope, the examples will be described and explained with additional specificity and detail through the use of the accompanying drawings in which:

[0031] Fig. 1a is a flow diagram of a catalytic reactor according to embodiments;

[0032] Fig. 1 b is a flow diagram of a catalytic reactor according to embodiments;

[0033] Fig. 2a is a schematic cross-sectional view of a catalytic reactor according to embodiments;

[0034] Fig. 2b is a schematic perspective view of a catalytic reactor according to embodiments;

[0035] Fig. 2c is a detail view of a reactor element in a catalytic reactor according to embodiments; and Fig. 3 is a flowchart of a method of performing an endothermic reaction according to embodiments.

[0036] Further, in the figures like reference characters designate like or corresponding parts throughout the several figures. The first digit in the reference character denotes the first figure in which the corresponding element or part appears.

[0037] DETAI LED DESCRIPTION

[0038] Various embodiments of the disclosed methods and arrangements are discussed in detail below. While specific implementations are discussed, it should be understood that this is done for illustration purposes only. A person skilled in the relevant art will recognize that other components, configurations, and steps may be used without parting from the spirit and scope of the claimed invention.

[0039] Hereinafter, certain embodiments will be described more fully with reference to the accompanying drawings. It will be apparent to those skilled in the art that various modifications and variations can be made without departing from the inventive concept. Other embodiments will be apparent to those skilled in the art from consideration of the specification and practice disclosed herein. It is to be understood that elements and materials may be substituted for those illustrated and described herein, parts and processes may be reversed or omitted, certain features may be utilized independently, and embodiments or features of embodiments may be combined, all as would be apparent to the skilled person in the art.

[0040] The embodiments herein are provided by way of example so that this disclosure will be thorough and complete, and will fully convey the scope of the inventive concept, and that the claims be construed as encompassing all modifications, equivalents and alternatives of the present inventive concept which are apparent to those skilled in the art to which the inventive concept pertains. If nothing else is stated, different embodiments may be combined with each other.

[0041] Although reference may be made to directions (e.g. left, right, up, down, upper, lower) as shown in the figures, it will be appreciated that these references are purely for illustrative purposes, and that embodiments are not limited to such directions.

[0042] The following definitions are means to aid in the description and understanding of the defined terms in the context of the present specification. The definitions are not meant to limit the defined terms to less than is described throughout this specification. Such definitions are means to encompass technical and grammatical equivalents.

[0043] As used herein, the term “catalyst” refers to a material that promotes a chemical reaction. The term “catalyst” includes, but is not limited to, a catalyst or catalysts capable of promoting combustion reactions, reforming reactions, cracking reactions (such as ammonia cracking reactions), and the like whether used as base catalyst(s) and / or additive catalyst(s). The catalyst, in the context of this application, can include, but is not limited to, nickel, iron, cobalt, iron cobalt, ruthenium, vanadium, palladium, rhodium, platinum, and the like, as well as various combinations thereof.

[0044] As used herein, the term “cracking” refers to a process or processes by which ammonia or other composite molecule is decomposed into its constituent components, in the case of ammonia into hydrogen and nitrogen, over at least one catalyst.

[0045] Fig. 1 a shows a catalytic reactor device 100 according to embodiments. The catalytic reactor device 100 is configured to facilitate a catalytic reaction involving a reactant. In particular, the catalytic reactor device 100 facilitates an endothermic reaction of the reactant, e.g. to produce one or more reaction products.

[0046] The catalytic reactor device 100 comprises a reactor 101 configured to facilitate an endothermic reaction (involving the reactant) and a burner 102 configured to generate heat.

[0047] The burner 102 may generate heat through an exothermic reaction, typically involving a combustion reaction of one or more fuels (or other reactants) together with air. As a result, a hot combustion gas or fluid will leave the burner 102. In some embodiments, the burner 102 may comprise a catalyst for facilitating the exothermic reaction.

[0048] The reactor 101 , on the other hand, facilitates an endothermic reaction, which may be a reforming reaction and / or a cracking reaction. The reactor 101 may, in the case of a cracking reaction, also be referred to as a cracker. The reactor 101 preferably comprises a catalyst to facilitate or drive the endothermic reaction.

[0049] The catalytic reactor device 100 is configured to couple the burner 102 with the reactor 101 so as to allow heat generated by the burner 102 to be used to drive the endothermic reaction in the reactor 101. Hence, the catalytic reactor device 100 can facilitate the endothermic reaction in the reactor 101 without any external heat input.

[0050] The catalytic reactor device 100 is accordingly arranged to allow heat transfer from the burner 102 (or the hot combustion fluid or gas leaving the burner 102) to the reactor 101 (or a reactant flowing through the reactor 101) so as to drive the endothermic reaction in the reactor 101. This may be achieved by the reactor 101 having a first heat transfer interface 103 allowing heat to be transferred from the burner 102 (or the hot combustion fluid) to the reactant flowing through the reactor 101. For example, the first heat transfer interface 103 may comprise a wall section of the reactor 101 (or a reactor element of the reactor 101 as will described later) being made of a thermally conductive material which is on one side exposed to the burner 102 (or the hot combustion fluid) and on another side exposed to the reactant 101.

[0051] The catalytic reactor device 100 may further comprise a pre-heater 104 configured to preheat the reactant before the endothermic reaction is performed in the reactor 101. The pre-heater 104 may be arranged such that heat may be transferred to the pre-heater 104 from the burner 102 (or the combustion fluid). In particular, the pre-heater 104 may comprise a second heat transfer interface 105, which may be substantially similar to the first heat transfer interface 103.

[0052] The pre-heater 104 may be arranged to receive a flow of reactant from a reactant inlet 106. After having passed through the pre-heater 104, the reactant may be configured to flow to the reactor 101 . In other words, the pre-heater 104 may be arranged before (i.e. upstream of) the reactor 101 in the direction of flow of the reactant.

[0053] It will be appreciated however, that in some embodiments the pre-heater 104 may be omitted, in which case the only heat transfer to the reactant may be performed in the reactor 101.

[0054] The catalytic reactor device 100 may further comprise a mixer 107 for mixing the fuel and air involved in the combustion process in the burner 102. The mixer 107 may be arranged before (i.e. upstream of) the burner 102. The mixer 107 may be arranged to receive air and fuel from an air inlet 108 and a fuel inlet 109 respectively, and to effectively mix the air and fuel to achieve an efficient combustion process in the burner 102. After having passed through the mixer 107, the air-fuel mixture is configured to flow to the burner 102. In other words, the mixer 107 is arranged upstream of the burner 102 in the direction of flow of the air-fuel mixture.

[0055] The flow of fluids through the catalytic reactor device 100 will now be described with reference to Fig. 1a. It is noted that in Fig. 1a solid lines indicate a flow fluid on a combustion side of the catalytic reactor device 100 (including air, fuel, air-fuel mixture and / or hot combustion products resulting from the combustion of the air-fuel mixture in the burner 102), and dotted lines indicate a fluid flow on the reactant side of the catalytic reactor device 100 (including the reactant and / or products resulting from the endothermic reaction in the reactor 101).

[0056] Starting with the combustion side, an air and fuel is received at the mixer 107 and mixed to obtain an air-fuel mixture. The air-fuel mixture then flows into the burner 102 where the mixture is combusted, optionally using a catalyst to promote the combustion process. Because the combustion reaction in the burner 102 is exothermic, the combustion products at an outlet of the burner 102 have a higher temperature than the air-fuel mixture at an inlet to the burner 102. The hot combustion products (typically in gas form) then flows over or across the first heat transfer interface 103 at the reactor 101 so as to allow heat to be transferred to the reactant flowing through the reactor 101. At the same time, the combustion gas is cooled down. The slightly cooler combustion products then flow over or across the second heat transfer interface 105 at the pre-heater 104 so as to allow heat to be transferred to the reactant flowing through the pre-heater 104. The further cooled combustion products then exit the catalytic reactor device 100 through the exhaust 110.

[0057] Turning to the reactant side, the reactant enters the catalytic reactor device 100 at the reactant inlet 106 and flows into the pre-heater 104 where it is heated by the slightly cooled combustion products flowing over or across the second heat transfer interface 105. As a result, the reactant is pre-heated. The pre-heated reactant then flows into the reactor 101 where it undergoes the endothermic reaction using heat transferred from the hot combustion products. The resultant product(s) then exits the system through a reactor outlet.

[0058] It is noted that in the embodiment shown in Fig. 1 a, the reactant side flow is isolated from (i.e. not in fluid communication or mixed with) the combustion side flow.

[0059] Although the burner 102 has generally been described as generating heat through an exothermic reaction, it will be appreciated that embodiments also include burners 102 configured to generate heat in other ways, such as via one or more heat generating elements (e.g. electrically powered heat generating elements configured to convert electrical power to heat), or the like.

[0060] Fig. 1 b shows a catalytic reactor device 100 where the fuel comprises one or more products resulting from the endothermic reaction in the reactor 101. Accordingly, the catalytic reactor device 100 may not rely on a separate fuel input, but rather utilise one or more product from the endothermic reaction to perform the combustion reaction. In other words, the product from the endothermic reaction in the reactor 101 is used as fuel in the burner 102. In some embodiments, such a configuration may be combined with an additional fuel input, e.g. if the amount of fuel required exceeds the amount of product(s) produced in the endothermic reaction.

[0061] In Fig. 1 b, solid lines indicates a flow of air, dotted lines indicate a flow of reactant (or products resulting from the endothermic reaction of the reactant), and dash-dot lines indicate a flow of a mix of air and the products resulting from the endothermic reaction of the reactant.

[0062] As seen by the lines and arrows in Fig. 1 b, the processes and flows are substantially similar to those described in relation to Fig. 1 b, apart from that the products from the endothermic reaction in the reactor 101 flows into the mixer 107 where they are mixed with air, and thereafter, the mixture flows into the burner 102 where it is combusted.

[0063] The catalytic reactor device 100 shown in Fig. 1 b is particularly advantageous for ammonia cracking, i.e. where the reactant is ammonia, and the endothermic reaction is an ammonia cracking reaction.

[0064] Ammonia cracking is the reversed reaction in the Haber-Bosch process where ammonia is produced. In particular, ammonia cracking is the reaction occurring when ammonia is decomposed into hydrogen and nitrogen according to the following chemical formula: NH31.5 H2+ 0.5 N2.

[0065] When the catalytic reactor device 100 is used for ammonia cracking, a flow of ammonia is provided at the reactant inlet 106. The ammonia flows through the preheater 104 where it is pre-heated. The ammonia then flows through the reactor 101 where it is “cracked”, i.e. at least partially decomposed into its constituent components, hydrogen and nitrogen, using heat from the burner 102. The hydrogen and nitrogen, together with any remaining ammonia, then flows into the mixer 107 where it is mixed with air. The mixture flows into the burner 102 where the hydrogen reacts with oxygen in the air in an exothermic reaction producing water (typically in the form of steam due to the heat generated in the exothermic reaction). The hot combustion products then flow across the first heat transfer interface 103 at the reactor 101 and thereafter across the second heat transfer interface 105 at the preheater 104 to exchange heat to the reactant therein. The cooled down combustion products then exit the catalytic reactor device 100 through the exhaust 110. Note that not all the hydrogen (resulting from the ammonia cracking reaction) is combusted in the burner 102, thus resulting in a net production of hydrogen.

[0066] Figs. 2a to 2c show schematic views of the catalytic reactor device 100. In particular, Fig. 2a shows a cross-sectional view of the catalytic reactor device 100 where only half of the device is shown because it is (rotationally) symmetric around the axial axis A-A, while Fig. 2b shows a perspective view of the catalytic reactor device 100, and Fig. 2c shows a detailed schematic view of a reactor element of the catalytic reactor device 100.

[0067] The catalytic reactor device 100 shown in Figs. 2a to 2c corresponds to the device of Fig. 1 b (i.e. without a separate fuel input). However, the teachings of Figs. 2a to 2c and the corresponding description may equally be applied to the catalytic reactor device of Fig. 1a with a separate fuel input with appropriate modifications that will be within the capabilities of the skilled person.

[0068] As shown in Figs. 2a and 2b, the burner 102 is centrally arranged in the catalytic reactor device 100. The burner 102 may be cylindrical or substantially cylindrical as shown, although it will be appreciated that other burner shapes, such as cuboid shapes, are within the scope of the inventive concept.

[0069] The burner 102 may comprise an inlet 201 located at a first axial end of the burner 102. The second axial end of the burner 102 may be closed. The outlet 202 of the burner 102 may be provided at a perimeter of the burner 102, such as a circumferential portion of the burner 102 in the case of a cylindrical burner. In particular, the burner outlet 202 may be arranged such that the outlet flow from the burner 102 is substantially in a radial outwards direction. The burner outlet 202 may extend around substantially the entire perimeter of the burner 102. The burner outlet 202 may also extend along a substantial axial portion, such as substantially the entire axial length of the burner 102.

[0070] The burner 102 is surrounded by a one or more reactor elements 203 forming the reactor 101. In other words, the reactor 101 may comprise one or more reactor elements 203 arranged around a perimeter or circumference of the burner 102. By positioning the reactor element(s) 203 around the perimeter of the burner 102 (or at least a portion of the perimeter with the burner outlet 202), the combustion products leaving the burner 102 through the burner outlet 202 will flow across the reactor elements 203.

[0071] The reactor element(s) 203 extend in an axial direction of the burner 102, e.g. to cover an axial portion where the burner outlet 202 is provided. Preferably, the reactor element(s) 203 extend along the entire axial length of the burner 102.

[0072] For example, a plurality of reactor elements 203 may be provided around the perimeter. The plurality of reactor elements 203 may comprise at least 5 reactor elements, optionally at least 10 reactor elements, optionally at least 25 reactor elements, optionally at least 40 reactor elements, optionally at least 60 reactor elements, optionally at least 100 reactor elements, to provide a large heat transfer area. It will be appreciated that the number of reactor elements 203 may be determined in dependence on the size of the burner 102 and / or catalytic reactor device 100, which allows the device to have great scalability.

[0073] The plurality of reactor elements 203 may be spaced apart so as to allow the combustion products leaving the burner 102 to flow between the reactor elements 203 in order to exit the catalytic reactor device 100. For example, the plurality of reactor elements 203 may be evenly spaced around the perimeter of the burner 102.

[0074] Each reactor element 203 may be formed by a flow structure 204 configured to allow a flow of reactant therethrough and in an axial direction of the burner 102. The flow structures 204 may each be formed of one or more pipes (as shown in Figs. 2a to 2c) or any other channel(s) or structure(s) capable of allowing the afore-mentioned flow of reactant.

[0075] The flow structure(s) 204 may be made from thermally conductive material, preferably metal, to allow heat transfer from the combustion products leaving the burner 102 to the reactant flowing through the flow structure 204.

[0076] In some embodiments, each flow structure 204 comprises a first flow structure element 204a and a second flow structure element 204b. The first flow structure element 204a may form the reactor 101 while the second flow structure element 204b may form the pre-heater 104. Accordingly, the second flow structure element 204b may be arranged between the reactant inlet 106 and the first flow structure element 204a, while the first flow structure element 204a is arranged between the second flow structure element 204b and the mixer 107. The reactant thus flows from the reactant inlet 106 into the second flow structure element 204b where it is pre-heated, after which it flows into the first flow structure element 204a where the reactant undergoes the endothermic reaction, after which the product(s) from said reaction enter the mixer 107 to be mixed with air.

[0077] The first flow structure element 204a is preferably arranged to allow a flow of reactant in a first axial direction (downwards in Fig. 2c) while the second flow structure element 204b is arranged to allow a flow in a second axial direction opposite to the first (upwards in Fig. 2c). The reactant inlet 106 may thus be located at the same axial end of the catalytic reactor device 100 as the air inlet 108, the flow structure outlet 205, and the mixer 107 allowing for a more compact design that can be conveniently installed even when space is limited.

[0078] The first flow structure element 204a (of each reactor element 203) may be arranged radially closer to the burner 102 than the second flow structure element 204b (of the same reactor element 203). Thus, as the hot combustion products leaves the burner 102, they will first exchange heat with the first flow structure element 204a (so as to drive the endothermic reaction) and thereafter flow to the second flow structure element 204b to exchange heat to preheat the reactant flowing therethrough.

[0079] In particular, the first flow structure elements 204a of all reactor elements 203 may be arranged at a first radial distance from the burner 102 while the second flow structure elements 204b may be arranged at a second radial distance, the second radial distance being larger than the first radial distance.

[0080] Each of the first and second flow structure elements 204 may be formed by a pipe or other channel. Each pair of first and second flow structure elements 204 may be connected at an axial end away from the reactant inlet 106.

[0081] Of course, embodiments also include the use of only one flow structure element 204 per reactor element 203, in which case the reactant inlet 106 may be provided at an opposite axial end to the mixer 107. In such a case, the pre-heater 104 of the catalytic reactor device 100 may be omitted, or arranged in another suitable way.

[0082] Embodiments also include other types of flow structures 204 than the above-described pipes. For example, in a catalytic reactor device 100 with only one reactor element 203, the flow structure 204 of that one reactor element 203 may be formed by one or more annular channels provided around the burner 102 and extending in an axial direction so as to allow a flow of reactant in an axial direction.

[0083] For example, if the reactor element has first and second flow structure elements 204a, 204b, the first flow structure element 204a may be formed by a first annular channel arranged closest to the burner 102, while the second flow structure element 204b may be formed by a second annular channel surrounding the first annular channel.

[0084] The annular channel(s) may be provided with a plurality of transverse radial channels extending therethrough to allow a transverse (i.e. radial) flow of the combustion products from the burner 102 without the combustion products coming into direct contact with the reactant.

[0085] Howsoever the flow structure(s) 204 are arranged, they may be provided with a catalyst to promote the endothermic reaction. In particular, at least the first flow structure element 204a (corresponding to the reactor 101) may be provided with a catalyst to promote the endothermic reaction. The catalyst may advantageously comprise ruthenium and / or nickel, although it will be appreciated that embodiments also include other catalysts, which may be selected in dependence on the specific endothermic reaction that is to be performed.

[0086] Fig. 3 shows a method of performing the endothermic reaction of a reactant, optionally using a catalytic reactor device 100 as previously described.

[0087] In step 301 , heat is generated in a burner 102. The heat may be generated by an exothermic reaction (optionally including combustion of hydrogen and oxygen), or by any other method of generating heat.

[0088] In step 303, a flow of reactant is provided through one or more flow structures 204. The flow structures 204 may be flow structures as previously described in relation to Figs. 2a to 2c. In particular, step 303 may comprise providing a flow of reactant in a first axial direction in a first flow structure element 204a, and providing a flow of reactant in a second and opposite axial direction in a second flow structure element 204b.

[0089] In step 305, heat is transferred from the burner 102 to the reactant flowing through the one or more flow structures 204. For example, heat may be transferred from one or more combustion products resulting from an exothermic reaction in the burner, e.g. after said products have exited the burner 102 and flow across the flow structure(s) 204.

[0090] Heat may be transferred to one or both of the first and second flow structure elements 204a, 204b. In particular, step 305 may comprise pre-heating the reactant in the second flow structure element 204b.

[0091] In step 307, the endothermic reaction is performed in the one or more flow structures 204 using the heat transferred from the burner 102. For example, the endothermic reaction may be performed in the first flow structure element 204a. The endothermic reaction may be an ammonia cracking reaction, and the reactant may accordingly be ammonia.

[0092] The endothermic reaction may be performed at a high temperature, such as above 700 degrees Celsius, optionally above 750 degrees Celsius, optionally above 800 degrees Celsius. Such high temperatures can be reached due to the design of the catalytic reactor device 100 according to embodiments and the efficient heat transfer capabilities from the burner to the reactor elements 203.

[0093] The products from the ammonia cracking reaction (or at least the hydrogen resulting therefrom) may be used in performing the exothermic reaction in step 301.

[0094] The various embodiments described above are provided by way of illustration only and should not be construed to limit the invention. For example, the principles herein may be applied to any catalytic process and / or endothermic reaction. Those skilled in the art will readily recognize various modifications and changes that may be made to the present invention without following the example embodiments and applications illustrated and described herein, and without departing from the scope of the present disclosure. Throughout this specification, the word “may” is used in a permissive sense (i.e. meaning having the potential to), rather than in the mandatory sense (i.e. meaning must).

[0095] Throughout this specification, the words “comprise”, “include”, and variations of the words, such as “comprising” and “comprises”, “including”, “includes”, do not exclude other elements or steps.

[0096] As used throughout this specification, the singular forms “a”, “an”, and “the”, include plural referents unless explicitly indicated otherwise. Thus, for example, reference to “an” element includes a combination of two or more elements, notwithstanding use of other terms and phrases for one or more elements, such as “one or more” or “at least one”.

[0097] The term “or” is, unless indicated otherwise, non-exclusive, i.e. encompassing both “and” and “or”. For example, the feature “A or B” includes feature “A”, feature “B” and feature “A and B”.

[0098] Unless otherwise indicated, statements that one value or action is “based on”, “in response to” and / or “in dependence on” another condition or value or action, encompass both instances in which the condition or value or action is the sole factor and instances where the condition or value or action is one factor among a plurality of factors.

[0099] Unless otherwise indicated, statements that “each” instance of some collection have some property should not be read to exclude cases where some otherwise identical or similar members of a larger collection do not have the property, i.e. each does not necessarily mean each and every.

[0100] Embodiments also include the following numbered clauses:

[0101] 1. A catalytic reactor device for facilitating an endothermic reaction of a reactant, the catalytic reactor device comprising: a burner for generating heat; a catalytic reactor for facilitating the endothermic reaction, wherein the heat generated by the burner is used to drive the endothermic reaction; wherein the catalytic reactor comprises one or more reactor elements arranged around a perimeter of the burner, wherein each reactor element comprises a flow structure configured to allow a flow of the reactant through the flow structure, wherein the flow structure extends along an axial direction of the burner and is arranged for heat exchange with the burner.

[0102] 2. The catalytic reactor device according to clause 1 , wherein the flow structure of each reactor element comprises a first flow structure element and a second flow structure element, wherein the first flow structure element is configured to allow a flow of the reactant in a first axial direction, and wherein the second flow structure element is configured to allow a flow of the reactant in a second and opposite axial direction. The catalytic reactor device according to clause 2, wherein the first flow structure element is arranged radially closer to the burner than the second flow structure element. The catalytic reactor device according to clause 2 or 3, wherein the first flow structure element is: arranged for heat exchange with the burner, and / or provided with a catalyst, and / or configured to facilitate the endothermic reaction. The catalytic reactor device according to any one of clauses 2 to 4, wherein the second flow structure element is arranged for heat exchange with the burner so as to pre-heat the reactant. The catalytic reactor device according to any one of clauses 2 to 5, wherein the first and / or second flow structure element comprises a pipe. The catalytic reactor device according to any preceding clause, wherein the burner is a catalytic burner configured to perform a combustion reaction so as to generate the heat. The catalytic reactor device according to clause 7, wherein the catalytic burner comprises: a burner inlet for receiving one or more combustion reactants used in the combustion reaction, and a burner outlet for expelling one or more combustion products resulting from the combustion reaction, wherein optionally the burner outlet is arranged to allow a radial flow of the combustion products, optionally wherein the radial flow is across the one or more flow structures so as to provide the heat exchange. The catalytic reactor device according to clause 8, wherein the heat exchange between the burner and the one or more flow structures is provided via the combustion products leaving the burner outlet. . The catalytic reactor device according to clause 8 or 9, wherein an outlet of the one or more flow structures is connected to the burner inlet. . A method of performing an endothermic reaction of a reactant, the method comprising: generating heat in a burner; provide a flow of reactant through one or more flow structures of one or more reactor elements arranged around a perimeter of the burner and extending along an axial direction of the burner; transferring heat from the burner to the reactant flowing through the one or more flow structures; and performing the endothermic reaction in the one or more flow structures using the heat transferred from the burner. The method according to clause 11, wherein the step of generating heat comprises performing an exothermic reaction, optionally wherein the exothermic reaction comprises reacting hydrogen with oxygen. The method according to clause 12, wherein the step of transferring heat from the burner comprises: providing a radial flow of combustion products from the exothermic reaction across the one or more flow structures, and transferring heat from the combustion products to the one or more flow structures. The method according to clause 12 or 13, wherein the method further comprises providing a flow of one or more products from the endothermic reaction to the burner, wherein the or more products from the endothermic reaction is used in the exothermic reaction in the burner. The method according to any one of clauses 11 to 14, wherein the step of providing a flow of reactant comprises providing a flow of reactant in a first axial direction in a first flow structure element of the flow structure, and providing a flow of reactant in a second and opposite axial direction in a second flow structure element of the flow structure, wherein optionally the endothermic reaction is performed in the first flow structure element, wherein optionally the method further comprises pre-heating the reactant in the second flow structure element using heat generated by the burner. The method according to any one of clauses 11 to 15, wherein the reactant is ammonia, and the endothermic reaction is an ammonia cracking reaction.

Claims

CLAI MS1. A catalytic reactor device for facilitating an endothermic reaction of a reactant, the catalytic reactor device comprising: a catalytic burner for performing a combustion reaction so as to generate heat, wherein the burner comprises a burner outlet for expelling one or more combustion products resulting from the combustion reaction; a catalytic reactor for facilitating the endothermic reaction, wherein the heat generated by the burner is used to drive the endothermic reaction; wherein the catalytic reactor comprises one or more reactor elements arranged around a perimeter of the burner, wherein each reactor element comprises a flow structure configured to allow a flow of the reactant through the flow structure, wherein the flow structure extends along an axial direction of the burner and is arranged for heat exchange with the burner; characterized in that the burner outlet is arranged to allow a radial flow of the one or more combustion products across the one or more flow structures so as to provide the heat exchange.

2. The catalytic reactor device according to claim 1 , wherein the flow structure of each reactor element comprises a first flow structure element and a second flow structure element, wherein the first flow structure element is configured to allow a flow of the reactant in a first axial direction, and wherein the second flow structure element is configured to allow a flow of the reactant in a second and opposite axial direction.

3. The catalytic reactor device according to claim 2, wherein the first flow structure element is arranged radially closer to the burner than the second flow structure element.

4. The catalytic reactor device according to claim 2 or 3, wherein the first flow structure element is: arranged for heat exchange with the burner, and / or provided with a catalyst, and / or configured to facilitate the endothermic reaction.

5. The catalytic reactor device according to any one of claims 2 to 4, wherein the second flow structure element is arranged for heat exchange with the burner so as to pre-heat the reactant.

6. The catalytic reactor device according to any one of claims 2 to 5, wherein the first and / or second flow structure element comprises a pipe.

7. The catalytic reactor device according to any preceding claim, wherein the catalytic burner further comprises: a burner inlet for receiving one or more combustion reactants used in the combustion reaction.

8. The catalytic reactor device according to any preceding claim, wherein the heat exchange between the burner and the one or more flow structures is provided via the combustion products leaving the burner outlet.

9. The catalytic reactor device according to claim 7, wherein an outlet of the one or more flow structures is connected to the burner inlet so as to facilitate a flow of at least part of the products from the endothermic reaction to the burner inlet.

10. The catalytic reactor device according to any preceding claim, wherein the burner outlet extends along at least half of the length of the flow structures, optionally along substantially the entire length of the flow structures.11 . A method of performing an endothermic reaction of a reactant, the method comprising: generating heat in a burner by performing a combustion reaction; provide a flow of reactant through one or more flow structures of one or more reactor elements arranged around a perimeter of the burner and extending along an axial direction of the burner; transferring heat from the burner to the reactant flowing through the one or more flow structures; and performing the endothermic reaction in the one or more flow structures using the heat transferred from the burner, characterized in that the step of transferring heat from the burner comprises providing a radial flow of combustion products from the combustion reaction across the one or more flow structures.

12. The method according to claim 11 , wherein the combustion reaction comprises reacting hydrogen with oxygen.

13. The method according to claim 11 or 12, wherein the method further comprises providing a flow of one or more products from the endothermic reaction to the burner, wherein the or more products from the endothermic reaction is used in the exothermic reaction in the burner.

14. The method according to any one of claims 11 to 13, wherein the step of providing a flow of reactant comprises providing a flow of reactant in a first axial direction in a first flow structure element of the flow structure, and providing a flow of reactant in a second and opposite axial direction in a sec- ond flow structure element of the flow structure, wherein optionally the endothermic reaction is performed in the first flow structure element, wherein optionally the method further comprises pre-heating the reactant in the second flow structure element using heat generated by the burner.

15. The method according to any one of claims 11 to 14, wherein the reactant is ammonia, and the endothermic reaction is an ammonia cracking reaction.

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