Reactor-heat exchanger or cylindrical heat exchanger between at least one first and a second fluid

Abstract

A heat exchanger reactor or heat exchanger comprising: - a main body (1) having, on at least one axial portion thereof, a general cylindrical shape of revolution about a central axis (Y), said body (1) comprising: A primary circuit comprising a plurality of primary layers (10) each comprising at least one primary channel (12), A secondary circuit (25) comprising a plurality of secondary layers (20) each comprising at least one secondary channel (22), said secondary channel (22) extending longitudinally in a radial direction towards the lateral wall (4) of the body (1) and, A plurality of isthmuses (30), the primary and secondary layers, separated by isthmuses, being distributed according to a plurality of sectors (40) of which at least one sector (40) comprises a primary layer extending radially along a non-rectilinear primary extension axis (Yp),and a secondary sheet extending along a non-rectilinear secondary extension axis (Ys). Figure for the abbreviation: Figure 1,

Description

Title of the invention: Heat exchanger reactor or cylindrical heat exchanger between at least one first and a second fluid. Technical field

[0001] The present invention relates to the field of heat exchanger reactors intended for carrying out reactions, whether endothermic or exothermic. The invention also relates to the field of heat exchangers.

[0002] The invention finds applications in a wide range of processes involving endothermic or exothermic reactions, particularly those that are strongly endothermic or exothermic. These processes may include reactions whose kinetics are optimized by the addition of catalysts, whether homogeneous or heterogeneous and in a fixed bed.

[0003] This invention is particularly relevant in the context of the energy transition and green chemistry.

[0004] Indeed, the energy transition requires the production of energy molecules via low-carbon emission processes. In this context, synthetic molecules composed of hydrogen, nitrogen or carbon oxides play a crucial role.

[0005] To synthesize these molecules, precise temperature control is essential, particularly in highly exothermic reactions such as the hydrogenation of carbon and nitrogen oxides, as well as in endothermic reactions, for example, the reverse water-gas shift reaction. These processes also require high levels of conversion and selectivity, which necessitates high temperature and pressure conditions. To ensure profitability, it is crucial to intensify the reactions to maximize volumetric production while maintaining high conversion rates of reactants to final products.

[0006] Optimal temperature control is also essential for the quality of syntheses (in particular to limit the formation of undesirable by-products) and to prolong the life of catalysts, which are often essential to accelerate chemical reactions.

[0007] Finally, the transition to greener chemistry is central to reducing the environmental footprint of processes. From this perspective, the shift from batch processes to continuous synthesis processes is widely recognized as a fundamental step towards more environmentally friendly chemistry. This change often requires mastering thermally intense reactions, demanding high-pressure conditions to optimize reaction intensity and efficiency.

[0008] The use of heat exchanger reactors proves to be a particularly effective solution for achieving the aforementioned objectives. Technological background

[0009] The field of heat exchanger reactors, or heat exchangers, is well documented in the literature and known to those skilled in the art. These devices allow for optimal management of heat exchange, whether or not it originates from chemical reactions requiring rigorous thermal control, and this under exothermic or endothermic conditions.

[0010] Although simple architectures exist, they are not suitable for demanding chemical reactions, particularly those of heterogeneous catalytic syntheses. These reactions require precise thermal management, especially when the catalyst has low thermal conductivity. When the reactions involve gaseous phases, thermal management becomes even more complex due to the low thermal properties of the gas streams (density, thermal conductivity). Inadequate thermal management in a heat exchanger reduces the efficiency of heat exchange. In a reactor-heat exchanger, this can cause hot spots for exothermic reactions or cold spots for endothermic reactions. These imbalances affect conversion rates and selectivity.

[0011] In the case of hot spots, this can lead to the degradation of the catalyst due to aging, and, in some situations, safety risks related to a runaway reaction, not thermally controlled.

[0012] To control high-flux heat exchange, particularly in the intensification of endothermic or exothermic chemical reactions, those skilled in the art may opt for so-called "structured" or "millistructured" heat exchanger reactors.

[0013] This heat exchanger reactor structure comprises layers of reactive channels and layers of heat transfer fluid channels. It allows for optimal management of heat exchange between the two aforementioned layers. The walls have a limited thickness, adapted to manufacturability and pressure resistance. This configuration is optimal when the dimensions remain constant in the active zone of the heat exchanger reactor.

[0014] A person skilled in the art adjusts the dimensions of the reactive channels to reduce the thermal gradient between the wall and the center of the channels. The dimensions of the heat transfer channels are particularly critical for maximizing the heat transfer coefficient. Thermal efficiency is key, with high Reynolds numbers being a primary objective. These systems must also allow for sufficient flow to ensure optimal thermal capacity. Furthermore, the distance between the reactive and heat transfer channels plays a crucial role in the optimal sizing of the reactor-heat exchanger.

[0015] A common approach for the architecture of structured heat exchanger reactors is inspired by plate heat exchangers.

[0016] In the literature, several documents describe channel arrangements or methods for implementing them in reactors, often of parallelepiped shape. For example, the following patents can be cited: JP5890380; US10737234; US9441777; US8721974; US9283561; US7247276; US9302243; EP1908514; EP1474237; WO2007112945.

[0017] US patent 6989134 describes relevant prior art concerning the design of microchannel reactors, the design of which is mainly parallelepiped-shaped.

[0018] Patent EP3488924B1 incorporates several concepts relating to reactors assembled by hot isostatic compaction, in particular the principle of stacking sheets carrying alternately reactive channels and heat transfer channels.

[0019] US patent 8383054 focuses on the arrangement of a heat exchanger reactor for strongly exothermic and endothermic reactions by diffusion welding, but only addresses parallelepiped designs.

[0020] Patent EP3802060 relates to a design accessible by additive manufacturing. Although it is a cylindrical design, the internal arrangement is primarily focused on heat exchange between two flows.

[0021] Other patents also address cylindrical-shaped reactor-exchangers, but their manufacturing processes, which are mainly based on mechanical assembly methods, limit the optimization of heat flux densities, which reduces the intensification of exothermic or endothermic reactions per unit volume of reactor.

[0022] In this category of prior art, we can cite US patent 7507387, which describes a cylindrical design created by fitting together two pieces engraved on their cylindrical surfaces in order to form the channels for the circulation of fluids.

[0023] US patent 4423022 presents an arrangement in a pressurized cylindrical tank, but the invention relates mainly to the integration of internal packings in said tank.

[0024] Patent EP1236506 is distinguished by the internal arrangement of a cylindrical reaction chamber, but it does not optimize the heat flow and the intensification of the volumetric reaction, contrary to the objectives of the present invention.

[0025] Finally, patent EP3603795 deals with the optimization of a cylindrical reactor-exchanger manufactured by additive manufacturing. However, this reactor, designed for a Operating in co-current or counter-current mode, it does not allow for precise temperature control in exothermic or endothermic reactions.

[0026] Generally, those skilled in the art can manufacture these heat exchanger reactors or heat exchangers by various methods, such as brazing parts with fusion of an intermediate material, localized welding (by electron beam, laser, TIG, etc.), or localized heating (by induction, thixotropic welding). More specifically, there is prior art relating to heat exchangers or heat exchanger reactors manufactured by diffusion welding, without melting the material. This diffusion welding, obtained by hot isostatic pressing (HIP) or hot uniaxial pressing (HUP) for certain designs, ensures the joining of the bonding zones with metallurgical continuity. This guarantees high thermal performance (absence of hot spots at material continuities) and optimal mechanical performance.The resulting assembly can be considered a single piece, without thermally affected areas or solidified molten zones that could create stress concentrations or singularities (bubbles, inclusions), thus avoiding differentials in mechanical behavior and fracture initiation points. Among the relevant patents already mentioned, we can also cite patents FR2879489, FR2936179, FR2949699, FR2950551, FR2955039, FR2989158, and FR3005499.

[0027] There is a need to further improve heat exchanger reactors, in particular to better manage the intense heat fluxes, generated by exothermic or endothermic reactions, under high pressure and temperature conditions. Summary of the invention

[0028] The invention aims to achieve this objective, and relates to a heat exchanger reactor or heat exchanger between at least a first and a second fluid comprising: - a main body, in particular a single piece or consisting of a set of plates having a sealing joint between two plates, having, on at least an axial portion thereof, a general cylindrical shape of revolution around a central axis, said body comprising: • A primary circuit for the circulation of the first fluid comprising a plurality of primary layers, each of the primary layers comprising at least one primary channel arranged to be traversed by the first fluid, said primary channel extending longitudinally along an axial direction of the body, • A secondary circuit, not connected to the primary circuit, intended for the circulation of the second fluid, comprising a plurality of secondary layers, each of the secondary layers being arranged between two successive primary layers and comprising at least one secondary channel arranged to be traversed by the second fluid, said secondary channel extending longitudinally in a radial direction towards the lateral wall of the body and, • A plurality of isthmuses, each arranged between successive primary and secondary layers, so as to obtain an alternation of primary layers, secondary layers, and isthmuses in a circumferential direction around the body, The primary and secondary nappes, separated by isthmuses, are distributed according to a plurality of successive sectors of number R with R>1, each sector comprising an alternation of two successive primary and secondary nappes and two isthmuses, with one of the isthmuses separating the two successive primary and secondary nappes, at least one sector of the plurality of sectors, called the "curvilinear sector", comprising • a primary sheet extending radially towards the lateral wall of the body along a non-rectilinear primary extension axis, and • a secondary sheet extending radially towards the lateral wall (4) of the body along a non-rectilinear secondary extension axis.

[0029] The invention applies both to the design of heat exchanger reactors and to the manufacture of heat exchangers dedicated exclusively to heat exchange. Thus, within the scope of the invention, the term "heat exchanger reactor" encompasses both a heat exchanger reactor and a pure heat exchanger.

[0030] The heat exchanger reactor according to the invention has several advantages.

[0031] First, compared with shaped heat exchanger reactors This parallelepiped-shaped structure exhibits high resistance to high pressures. Indeed, its cylindrical geometry of revolution allows for a relatively uniform distribution of forces around the wall of the cylindrical body. This makes such a geometry structurally more robust than the flat or angular shapes typical of parallelepiped geometries, which tend to concentrate stresses at certain points and experience significant deformation at others.

[0032] Advantageously, the heat exchanger reactor according to the invention is capable of withstanding particularly high pressures, well above 100 bar. Such a characteristic is useful for industrial applications, where heat exchanger reactors are often subjected to high-pressure conditions, particularly in heat transfer processes or chemical reactions requiring a pressurized environment to improve efficiency and reaction rates.

[0033] Furthermore, the presence of curved sectors, as claimed, offers a significant thermal advantage while maintaining the compactness of the reactor-exchanger. These curved sectors are arranged to optimize the use of the internal volume, maximizing the functional areas of the reactor-exchanger. Indeed, the primary and secondary layers have non-straight portions in their radial extension towards the lateral wall of the body. This reduces the amount of material not directly involved in heat exchange or chemical reactions. In particular, by shaping the primary and secondary layers to extend radially along a non-straight path, the space and material that would otherwise be present without fulfilling an active function in the process are minimized. The efficiency of heat exchange is thus improved.

[0034] Also, the design of the primary and secondary layers as claimed makes it possible to retain the mechanical advantages of the cylindrical shape while optimizing the thermal and chemical functions, and this without compromising the compactness of the exchanger, excessively.

[0035] The metal reduction required for the reactor-exchanger functions gives the manufactured products low thermal inertia. This characteristic facilitates direct control of the chemical reaction or heat exchange, even in the event of fluctuations in the inputs, for example, those associated with renewable energy sources. This avoids the need for costly buffer devices, often used to stabilize the fluctuations experienced by reactor-exchangers found in renewable energy sources related to electricity (solar or wind for hydrogen production), or related to the production of syngas by biological decomposition, gasification, or pyrogasification of organic waste.

[0036] The reactor-exchanger according to the invention is adapted to accommodate and control various types of reactions, whether exothermic or endothermic chemical reactions, or catalytic reactions, whether they involve homogeneous or heterogeneous catalysis. In the context of heterogeneous catalysis, the catalyst can be attached to the channel walls or placed inside the channels of the primary circuit in solid form, whether structured or unstructured.

[0037] The reactor-exchanger according to the invention is also suitable for chemical synthesis processes, particularly in the fields of synthetic fuels, fine chemicals and specialty chemicals.

[0038] For synthetic fuels, the invention applies to catalyzed chemical reactions requiring high pressure. These conditions are necessary to increase the synthesis yield. For example, it applies to the synthesis of methanol from CO or CO2 and hydrogen. It also applies to the production of ammonia from nitrogen and hydrogen. The invention also allows for a Improved control of the synthesis temperature. This is essential for limiting co-products or optimizing desired fractions. For example, this proves useful in the Fischer-Tropsch synthesis from CO and hydrogen.

[0039] The invention is also useful in intermediate chemical reactions integrated into complex transformation processes, where precise control of heat exchange and operating temperature under high pressure is desired. This includes, for example, reforming or partial oxidation reactions of hydrocarbons, the gas-water shift reaction (or its inverse), and hydrocracking processes.

[0040] In the field of chemical synthesis, the invention is particularly beneficial for the hydrogenation of liquids, an area offering vast opportunities for improvement. These reactions, carried out under high pressure, improve process safety by reducing the amount of reactants present at any given time, accelerate reaction kinetics under pressure, and optimize selectivity through control of residence time and temperature. Furthermore, it is applicable to reactions requiring extreme conditions, such as oxidation reactions in supercritical water, which have strong potential for effluent treatment, particularly for effluents containing persistent pollutants such as PFAS.

[0041] The invention can be used in heat exchange contexts without mass transfer, particularly when the geometry of the channels must be adapted to the rheology of the fluids. This includes non-Newtonian fluids requiring heat exchange under pressure to raise or lower their temperature, using a heat transfer fluid. Body

[0042] The body of the reactor-exchanger advantageously corresponds to the component in which chemical reactions and / or heat exchanges take place.

[0043] The body may have said cylindrical shape of revolution over its entire total height.

[0044] Alternatively, the body may comprise, on at least two distinct axial portions, a cylindrical shape of revolution around the central axis, each portion having a different maximum diameter.

[0045] Preferably, the cylindrical body comprises two bases, in particular delimited by closing flanges, connected by a cylindrical side wall. The bases preferably have a substantially circular contour.

[0046] The primary and secondary circuits, as well as the isthmuses, are preferably arranged at least partially within the space delimited by the bases and the side wall.

[0047] Preferably, the cylindrical body has a total height, measured along its central axis, of less than 10 m, better less than 5 m, even better less than 2 m, for example less than 1 m.

[0048] Preferably, the cylindrical body has a maximum diameter De, measured in particular at one of its bases, of less than 5 m, better less than 2 m, for example less than 1 m.

[0049] Preferably, this maximum diameter is kept constant over the entire height of the body, that is to say along its total height. In other words, the body is a cylinder of revolution about the central axis.

[0050] The body can be made up of a stack of plates forming a complete body.

[0051] The body can be a single piece. In other words, the body corresponds to a single piece of a single unit, which includes the aforementioned primary and secondary channels.

[0052] Preferably, the one-piece body is made of a single material having a homogeneous composition throughout the entire body, generally a single metal or a single metal alloy. The body may also be made of several materials, either, for example, to select the most suitable material locally, for reasons of mechanical strength or chemical compatibility, or, for example, to ensure a seal between two successive metal plates, in which case the material chosen will be of the elastomer or graphite type.

[0053] The one-piece body can in particular be produced by machining a succession of one-piece parts initially without cutouts, the assembly of which makes it possible to form the channels.

[0054] Alternatively, the one-piece body is manufactured by additive manufacturing, in particular from powder or molten wire, using different melting processes, such as electron beam, laser, induction or plasma.

[0055] Alternatively, the one-piece body can be obtained by assembling and diffusion welding several parts, in order to form a single unitary part corresponding to the body. Sectors

[0056] By "sector" is meant a subdivision of the body delimiting a distinct zone of the body, comprising at least the group formed by the successive primary and secondary nappes as well as the isthmus separating them, and an isthmus adjacent to this group, located before or after it, in a given circumferential direction.

[0057] Preferably, each sector has a height identical to the total height of the body.

[0058] Preferably, each sector is adjacent to two neighboring sectors located on either side of it. Preferably, each sector is in direct contact with said neighboring sectors. The sector may be delimited, on one side, by the isthmus of one of its sectors neighbors, and, on the other hand, by one of the aquifers, primary or secondary, of the other neighboring sector.

[0059] Curvilinear sector

[0060] As previously stated, the body comprises at least one curvilinear sector whose primary and secondary layers each extend radially along a non-rectilinear axis.

[0061] The terms "radially," "radial direction," "radially," or "radial direction" are used in this application to designate a direction from the central axis of the body to its outer lateral wall. It should be emphasized that an element, such as an axis, segment, portion, or sheet extending radially, or in the radial direction, does not necessarily imply a straight trajectory equivalent to that of the radial axis of the body. This trajectory may be non-straight; for example, it may be curved and exhibit a deviation from the radial axis of the body, taking, for example, the form of a monotonic curve or a combination of curves of varying monotonicity.

[0062] The radial axis of the body, on the other hand, is a straight line perpendicular to the central axis of the body.

[0063] By "axis of extension" is meant the axis along which the sheet extends from an internal position in the body towards the lateral wall of the body

[0064] By "non-straight axis of extension," we mean an axis comprising at least one non-straight portion. This means that the axis of extension undergoes a change of direction at this portion. This change may be gradual, with a curved portion, or more pronounced, with a sharp break in slope, such as a right angle. The non-straight portion may also consist of a combination of curves and straight segments.

[0065] Preferably, the axes of extension of the primary and secondary nappes of the curvilinear sector are respectively curved.

[0066] By "curved extension axis" is meant a continuous and differentiable line, devoid of any discontinuity, along its entire path. In other words, the extension axis follows a smooth and regular path, without breaks or mathematical irregularities. Preferably, the curved extension axis is devoid of inflection. The absence of inflection means that the curvature of the axis maintains a constant sign throughout its path. In other words, the axis never changes its concavity (for example, it remains entirely convex or entirely concave), thus guaranteeing a uniform direction of curvature along its entire path.

[0067] Preferably, the primary and secondary extension axes have a substantially identical curvature.

[0068] By "axes exhibiting identical curvature," we mean spatially distinct (non-superimposed) axes whose curvature variation along their respective trajectories is identical. The two curved axes preferably have the same instantaneous radius of curvature.

[0069] This allows for maintaining a constant distance between the primary and secondary layers of the curved section. Maintaining this distance between the layers ensures uniformity of heat exchange and distributed stresses, thus guaranteeing an optimum. Indeed, this constant distance between the layers can contribute to better fluid circulation and more regular heat transfer, which is beneficial for maintaining homogeneous reaction or heat exchange conditions. Furthermore, a constant distance helps to avoid excessive mechanical stresses on the layers due to variations in pressure or temperature.

[0070] Preferably, the curvature of the primary and secondary extension axes is variable as a function of the radial distance, i.e. with respect to the central axis of the body, the primary and secondary extension axes each comprising, for example, a succession of arcs of circles.

[0071] Preferably, the tangent to each of the primary and secondary extension axes at a given point K forms a non-zero angle of inclination with respect to a radial axis of the body passing through this point K, this angle of inclination increasing progressively as the radial distance of the point with respect to the central axis of the body increases; in other words, the angle of inclination is advantageously an increasing function of the radial distance. The primary and secondary extension axes can thus take on a shape substantially similar to a volute.

[0072] Alternatively, the primary and secondary extension axes may each have a constant curvature. For example, this curvature may form an arc of a circle, concave or convex inwards.

[0073] Preferably, all sectors of said plurality of sectors being identical and each having the same width, the body comprising R curvilinear sectors. Each sector advantageously incorporates at least one of the characteristics described above in connection with the curvilinear sector. The body can thus exhibit symmetry around its central axis.

[0074] Preferably, said width lm is defined according to the following formula: lin - lp + ls + 2 x where lp, ls and f represent respectively the widths of the primary, secondary, and isthmuses of said sector.

[0075] Preferably, each sector extends radially from a non-zero radial distance, said radial distance being identical for all sectors. Thus, the starting point of the sectors is advantageously located on the lateral wall of a cylinder concentric with the body, with a diameter strictly smaller than the diameter of the body. This allows for the creation of a central housing inside the body, which can be used, for example, for fluid distribution or the mechanical fixing of closure flanges.

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[0086] The R-number of curvilinear sectors is advantageously chosen to optimize the performance of the reactor-exchanger. In particular, the R-number of curvilinear sectors can be determined to maximize the internal volume of the primary channels in the primary circuit layers. The number R of curvilinear sectors and the width lm of each sector are preferably related by the following equation: & _ corresponds to the distance radial from the starting point of the sectors. Preferably, the angle of inclination ai at a point K on the corresponding extension axis is defined by the following equation: a,- = cos*1 Where corresponds to the radial distance from point K, the angle of inclination. 2 In other words, the distance dK corresponds to the instantaneous diameter of the body at the point K, that is to say the diameter of the cylinder concentric with the body and whose lateral wall includes said point K. Preferably, the angle of inclination ai fulfills the following condition: This helps to avoid the overlap of curvilinear sectors. Advantageously, for each curvilinear sector, with reference to a cylindrical coordinate system, the points (r,0) defining the geometric locus of the primary and / or secondary nappes of this sector are determined by the following iterative relations: rN+l = rN+pxcosai ^v+1 “ + With [ Dt fr0~ 2 U = 0 where rN+i represents the radial coordinate of the next point KN+[ after an iterative step p in the radial direction, with respect to the previous coordinate rN of the point KN: this value rN+[ is obtained by adding to the initial radial coordinate rN the product of a step p and the cosine of the angle of inclination afau point Kn+i with dxN+l ~ dN + p; 0v+i is the angular coordinate of the next point Kn+i after an iterative step p, relative to the previous angular coordinate #;v of point KN: this value is calculated by adding to the initial point 6^ the product of the step p and the sine of the angle of inclination ai, calculated from the instantaneous diameter dx; 0, is the angle increment corresponding to the projection of the step p inclined at an angle a; along the direction 0 at a distance dK from the center of the cylinder. 2

[0087] / \ “Idll | # |

[0088] The step size p can be constant or variable.

[0089] In embodiments, the step p corresponds to the distance separating the sections, in particular transverse, of two successive primary channels of the primary aquifer of the curvilinear sector.

[0090] Alternatively, the step p can correspond to the spatial resolution of the primary sheet of the curvilinear sector. Primary circuit

[0091] The first fluid can circulate within the primary circuit at a pressure greater than 500 bars.

[0092] Primary channel

[0093] As mentioned previously, the primary channel extends longitudinally along an axial direction of the body.

[0094] It should be noted that the terms "axially," "axial direction," or "axial direction" are used in this application to designate a direction from the first base of the body to the second base. It should be emphasized that an element, such as an axis, segment, portion, or sheet extending axially, or in the axial direction, does not necessarily imply a rectilinear trajectory equivalent to that of a straight line parallel to the central axis of the body. This trajectory may be non-rectilinear, for example, curved.

[0095] Preferably, each primary channel has an elongated shape and extends axially along a straight longitudinal axis parallel to the central axis of the body. Also, the first fluid advantageously follows straight trajectories within the primary channels parallel to the central axis of the body.

[0096] Alternatively, the primary channel extends axially in a non-rectilinear manner, so that the first fluid takes a more complex axial path within the corresponding primary layer for better mixing and increased heat exchange in the primary circuit.

[0097] The primary channel may have a longitudinal axis having any shape allowing the aforementioned non-rectilinear arrangement.

[0098] For example, the longitudinal axis can follow a curved trajectory, such as helical, in particular around an axis parallel to the central axis of the body.

[0099] The longitudinal axis can still follow a segmented straight axial trajectory, consisting, along the axial direction, of several successive straight portions connected by abrupt transitions or plateaus.

[0100] The primary channel may have a rounded cross-section, such as oblong or circular.

[0101] Alternatively, the primary channel may have a cross-section of polygonal shape, for example square, rectangular or even rhombus.

[0102] In certain embodiments, the primary channel has, at at least two different points on its longitudinal axis, cross-sections of different shapes and / or dimensions.

[0103] The primary channel may have a smooth inner wall.

[0104] Alternatively, the primary channel has a partially rough inner wall, being provided for example with undulations, protuberances or baffles.

[0105] The primary channel of the primary aquifer can have a length between 20% and 100% of the total height of the body.

[0106] The primary channel may open onto at least one of the two bases of the body, preferably onto both bases of said body.

[0107] Primary layer

[0108] The primary aquifer may comprise a number of primary channels between 1 and 1,000, preferably between 1 and 500.

[0109] The primary channels of the primary sheet may have the same length. In this embodiment, each primary channel opens onto both bases of the body.

[0110] Alternatively, at least two primary channels of the primary aquifer have a different length.

[0111] The primary channels of the primary aquifer may have an identical shape.

[0112] Alternatively, at least two primary channels of the primary aquifer may present different shapes and different sections but retaining the key characteristics, including the width of the channels, the length according to the radial direction varying, better, the hydraulic diameter, or the Reynolds number, or better still the geometric characteristics which impact the heat exchange coefficient at the wall.

[0113] The primary circuit may include a number of primary layers greater than 1, in particular between 1 and 1,000, better between 2 and 100.

[0114] Preferably, the primary circuit comprises several primary layers.

[0115] At least one primary layer, preferably each primary layer, comprises a plurality of primary channels arranged along its primary extension axis. This increases the mechanical strength of the cylindrical body at high pressures.

[0116] Preferably, the primary channels of said primary aquifer are spaced apart from each other, in particular at equal distances, the space between them being occupied, preferably, by the isthmuses of the corresponding sector.

[0117] In some embodiments, the primary channels of said primary layer are substantially cylindrical in shape, their number preferably being given by 2⁻¹⁰, where n is a non-zero integer. The use of cylindrical primary channels makes it possible to increase the number of channels per layer. Furthermore, cylindrical primary channels offer the advantage of a geometry that allows, for example, increased pressure resistance, the search for a piston-type fluid flow mode in the primary circuit, or the integration of specific inserts. This cylindrical configuration also presents favorable conditions for particular chemical reactions, especially those involving two-phase flows.

[0118] In embodiments, the primary channels of said primary aquifer are substantially oblong, said channels adopting for example a shape substantially similar to that of a bean, their number preferably being given by 2”, where n is a non-zero integer.

[0119] Alternatively or in addition, at least one primary layer, or even each primary layer, comprises a single primary channel extending radially towards the lateral wall along the primary extension axis of the latter. In such an embodiment, the single primary channel may incorporate indentations to increase the perimeter of said primary channel. Also, according to this configuration, the single primary channel presents an increased exchange surface area with the adjacent secondary layers.

[0120] Within the primary layer, the primary channels can be connected in series, in parallel or in mixed series and parallel mode.

[0121] Preferably, the primary layer includes at least one fluid inlet, located at one of the distal ends of at least one of its primary channels, allowing the first fluid to be conveyed along the primary channel(s) in an axial direction of the cylindrical body and at least one fluid outlet located at one of the distal ends of at least one of its channels, allowing the first fluid to be evacuated.

[0122] In the context of a reactor-exchanger, the primary circuit can be used for the circulation of a reaction medium. Secondary circuit

[0123] The secondary circuit can be used for the circulation of a heat transfer fluid ensuring thermal regulation of the reaction medium of the primary circuit.

[0124] The secondary circuit is arranged so that the second fluid can circulate within it at a pressure of 1 bar to more than 1,000 bars and in particular from 1 to 100 bars.

[0125] In embodiments, the alternating arrangement of the primary and secondary layers allows for a crossflow arrangement, that is to say, the first fluid will flow in a primary layer along a mainly axial trajectory and the second fluid will flow in the secondary layer along a mainly radial trajectory.

[0126] The secondary channel may have a cross-section whose largest dimension is between 1 mm and the axial length of the reactor-exchanger body and in particular between 2 mm and 50 mm.

[0127] The secondary channel may have a rounded cross-section, such as oblong or circular.

[0128] Alternatively, the secondary channel may have a cross-section of polygonal shape, for example square, rectangular or even rhombus.

[0129] In embodiments, the secondary channel is arranged to be traversed by the second fluid in a single direction, for example from the inside out or vice versa.

[0130] In some embodiments, the secondary channel is arranged to allow the second fluid to flow in at least two different directions. For example, the secondary circuit may include a first channel for conveying the fluid radially in a first direction from its inlet, and a second channel for directing the fluid radially in a second direction, preferably opposite to the first direction, towards its outlet. The path of the second fluid in the secondary channel can thus follow a general U-shaped trajectory. When the fluid enters the secondary channel, it first follows the first channel in the first direction, then changes direction to follow the second channel in the second direction.

[0131] Each secondary aquifer may have a number of secondary channels between 1 and 10,000, preferably between 2 and 500.

[0132] Each secondary channel may include a single secondary channel.

[0133] Alternatively, the secondary layer comprises a plurality of secondary channels, in particular aligned successively along an axis parallel to the central axis of the cylindrical body.

[0134] In some embodiments, the secondary channels of the secondary layer are arranged axially along an axis parallel to the central axis of the body, with a constant spacing between them.

[0135] Alternatively, this spacing is variable.

[0136] Fluid distribution network

[0137] The secondary circuit may further include a fluid distribution network to convey the second fluid to the secondary aquifer(s).

[0138] Preferably, the distribution network includes at least one distribution conduit to convey the second fluid to the secondary aquifers.

[0139] Preferably, the distribution network comprises several distribution conduits, each arranged to distribute the second fluid into one or more secondary aquifers.

[0140] Advantageously, the distribution network comprises several distribution conduits, each specifically arranged to distribute the second fluid into a corresponding secondary aquifer. In other words, each conduit is dedicated to supplying a single secondary aquifer.

[0141] In certain embodiments, the distribution conduit(s) extend axially, in particular along a straight longitudinal axis parallel to the central axis of the cylindrical body.

[0142] Preferably, the distribution conduits are arranged around the central axis of the cylindrical body, equidistant from it.

[0143] In embodiments, the distribution conduit(s) are arranged in the central housing within the cylindrical body at a radial distance less than Di / 2.

[0144] In embodiments, the distribution conduit(s) are arranged around the periphery of the cylindrical body, in particular at a radial distance between Di / 2 and Dc / 2.

[0145] The distribution conduits can be arranged alternately in the central housing and around the periphery of the cylindrical body.

[0146] The distribution conduit(s) may have a length, measured along their longitudinal axis, of between 10% and 100% of the total height of the body.

[0147] The distribution conduit(s) may have a cross-section whose largest dimension is less than 0.75 Di.

[0148] The distribution conduit(s) may have a rounded cross-section, in particular oblong or circular, or polygonal.

[0149] Collection network

[0150] In some embodiments, the secondary circuit includes a collection network to recover the second fluid from the secondary aquifers.

[0151] Preferably, the collection network includes at least one collection conduit arranged to collect the second fluid from secondary aquifers.

[0152] Preferably, the collection network comprises a plurality of collection conduits, each arranged to collect the second fluid from one or more secondary aquifers.

[0153] Advantageously, the collection network comprises several collection conduits, each specifically arranged to collect the second fluid from a corresponding secondary aquifer.

[0154] In certain embodiments, the collection conduit(s) extend axially, in particular along a straight longitudinal axis parallel to the central axis of the cylindrical body.

[0155] Preferably, the collection conduit(s) are disposed in the aforementioned central housing.

[0156] Preferably, the collection conduits are arranged around the central axis of the cylindrical body, equidistant from it.

[0157] The collection conduit(s) may be arranged at a radial distance of less than Di / 2.

[0158] The collection conduit(s) can be arranged at a radial distance between Di / 2 and Dc / 2.

[0159] The collection channels can be arranged alternately in the central housing and on the periphery of the cylindrical body.

[0160] The collection distribution conduits may have a length between 0.1% and 100% of the total body height.

[0161] Distribution and / or collection conduits may have a cross-section whose largest dimension is less than 5 times Di

[0162] Said cross-section may be rounded, in particular oblong or circular, or polygonal.

[0163] The collection conduits can be arranged alternately with the distribution conduits around the central axis of the cylindrical body, in particular at an equal distance from it.

[0164] Each secondary channel can be connected to successive distribution and collection conduits, following this alternation of conduits.

[0165] In some embodiments, the collection conduits may be axially offset relative to the distribution conduits. Preferably, the distribution conduits open onto one of the bases of the cylindrical body, while the collection conduits open onto the other base of the cylindrical body.

[0166] In embodiments, the distribution conduit(s) are arranged in the central housing of the cylindrical body while the collection channel(s) are arranged on the periphery of the cylindrical body, or vice versa.

[0167] The distribution and collection networks may include, for at least one secondary aquifer, at least one common conduit, said common conduit serving for example to collect the second fluid from a first group of channels of the secondary aquifer and to convey this fluid to a second separate group of channels within the same aquifer. Isthmus

[0168] Advantageously, the isthmuses of the curvilinear sector(s) have a constant width, identical for both isthmuses. This width can be between 0.05 mm and 50 mm, and preferably between 0.1 mm and 30 mm.

[0169] Preferably, each of the isthmuses of the curvilinear sector extends radially along a curvature identical to that of the primary and secondary nappes.

[0170] The reactor-exchanger may include a plurality of filter elements arranged at the inlet of the primary and / or secondary layers. These elements allow the free flow of fluids while retaining particles. They thus serve to prevent the deposition of fluid-carried particles in the primary and secondary circuit layers, thereby reducing the risk of clogging. Furthermore, for chemical reactions catalyzed by a fixed-bed catalyst, these filters can be particularly advantageous for containing the catalyst within the primary circuit layers.

[0171] The invention also relates to the use of the heat exchanger reactor according to the invention, for hydrogenation reactions of fluids, in particular in the presence of a fixed bed catalyst.

[0172] The fluid can be a gas. The exchange reactor according to the invention can be used for the synthesis of methane, methanol or synthetic hydrocarbons from CO or CO2 and hydrogen.

[0173] The reactor-exchanger according to the invention can be used for the production of ammonia from nitrogen and hydrogen or its reverse decomposition reaction.

[0174] The fluid can be a liquid.

[0175] The fluid may also be in a supercritical state Brief description of the figures

[0176] The following description, with reference to the accompanying drawings, given by way of non-limiting examples, will clearly explain what the invention consists of and how it can be implemented. Regarding the accompanying figures:

[0177] [Fig-1] The [Fig. 1] represents a main body of a heat exchanger reactor or heat exchanger according to the invention;

[0178] [Fig.2] Fig.2 represents in isolation the secondary circuit, in perspective view, of the heat exchanger reactor or heat exchanger of [Fig.1],

[0179] [Fig.3] [Fig.3] is a detail of [Fig.2],

[0180] [Fig.4] The [Fig.4] is a cross-section and schematic of a first variant of the heat exchanger reactor or heat exchanger of the [Fig.1];

[0181] [Fig.5] Fig.5 is a curve showing the evolution of the primary circuit volume as a function of the number of sectors,

[0182] [Fig.6] The [Fig.6] represents in isolation the primary and secondary circuits of a main body of a heat exchanger reactor or heat exchanger according to a second variant of the invention;

[0183] [Fig.7] The [Fig.7] is a detail of the [Fig.6];

[0184] [Fig.8] The [Fig.8] is a longitudinal and schematic section of the reactor-heat exchanger body or heat exchanger of the [Fig.6];

[0185] [Fig.9] The [Fig.9] is a cross-section of a heat exchanger reactor body or heat exchanger according to a third variant of the invention;

[0186] [Fig. 10] The [Fig. 10] is a cross-section of a reactor-heat exchanger body or heat exchanger according to a fourth embodiment of the invention; and

[0187] [Fig. 11] The [Fig. 11] is an example of a sector according to the invention. Description of method(s) of implementation

[0188] In the figures, and unless otherwise specified, identical elements shall bear the same reference numerals.

[0189] Figure 1 illustrates a main body 1 of a reactor-exchanger according to the invention. The main body 1 is a single-piece elongated part, generally made of a single metal or metal alloy.

[0190] The main body 1 may also consist of a stack of pieces of a single metal, a metal alloy, or alternating metals. An elastomer or graphite-type material may be inserted between each metal piece.

[0191] As illustrated, the body 1 has a substantially cylindrical shape of revolution about a central axis Y. This cylindrical body 1 comprises two bases 2 of circular contour 2 delimited by closing flanges 6. The cylindrical body 1 further has a cylindrical side wall 4 connecting said bases 2, thus forming a closed structure that delimits the internal space of the body 1. The dimensions of the cylindrical body 1 can vary depending on the intended application. For example, its total height H, measured along the Y-axis, can be less than 10 m, while its maximum diameter De can be less than 5 m.

[0192] The cylindrical body 1 comprises a primary circuit for the circulation of at least one first fluid, which may be a reaction fluid in a chemical process. This primary circuit comprises a plurality of elongated primary channels 12 extending axially along a longitudinal axis, which, in this example, is straight and parallel to the central axis Y of the body 1. As illustrated, each primary channel opens onto the two bases 2 of the body 1. In the illustrated example, the supply of the primary channels 12 with the first fluid and the collection of this fluid take place at the distal ends of the primary channels 12, that is to say at the bases of the cylindrical body 1.

[0193] The primary channels 12 are distributed along several primary layers 10. In the illustrated example, each primary layer 10 comprises three primary channels 12, aligned successively in the radial direction of the cylindrical body 1. As shown in [Fig. 1], the primary channels of the same layer 10 are spaced apart by a non-zero distance e. Each primary layer 10 extends radially from a non-zero radial distance Di / 2 along a non-straight primary extension axis Yp. The radial distance Di / 2 mentioned is identical for all the primary layers 10. Thus, the starting point of the primary layers is located on the lateral wall of a cylinder concentric with the body 1, of diameter Di. As illustrated in [Fig. 1], the primary extension axis Yp is curved.

[0194] In the illustrated example, the primary channels 12 of each primary layer 10 are substantially oblong, each having opposite lateral faces with identical concavity. In this example, the primary channels 12 thus adopt a shape substantially similar to that of a bean. The number of primary channels per layer 10 is given by 2⁻¹⁰, where n is a non-zero integer.

[0195] Alternatively, the primary channels 12 are arranged in direct contact to form the primary layer 10, as illustrated in Figure 4. In this embodiment, the primary channels 12 of each primary layer are substantially cylindrical in revolution. Similar to the oblong mode, the number of primary channels per layer 10 is given by 2⁻¹⁰, where n is a non-zero integer.

[0196] The cylindrical body 1 also includes a secondary circuit 25 for the circulation of a second fluid, used for example as a heat transfer fluid. This second fluid notably allows the temperature of the reaction medium in the primary circuit to be regulated by transferring heat between the heat transfer fluid and the reaction fluid of the primary circuit.

[0197] In the illustrated example, the secondary circuit 25 comprises several secondary channels 22, distributed in secondary layers 20. Each secondary layer 20 is positioned between two successive primary layers 10 and comprises a predetermined number of secondary channels 22, arranged in succession along an axis parallel to the central axis Y of the cylindrical body 1. In the illustrated example, the number of secondary channels 22 in each layer 20 is greater than 5, in particular greater than 10.

[0198] Each secondary layer 20 extends radially, from a radial distance equal to Di / 2 along a curved extension axis Ys. The starting point of the secondary layers is located on the lateral wall of the cylinder of diameter Di.

[0199] In the illustrated example, the secondary channels 20 are elongated in shape and extend radially along a longitudinal axis parallel to the secondary extension axis Ys.

[0200] The secondary circuit 25 further comprises a distribution network 50 of the second fluid in the secondary layers 20.

[0201] In the illustrated example, the distribution network 50 comprises a plurality of distribution conduits 52 arranged to convey the second fluid to the secondary aquifers 20. As shown in Figures 2 and 3, each distribution conduit 52 is specifically arranged to distribute the second fluid into a corresponding secondary aquifer 20.

[0202] The distribution conduits 52 are elongated and extend axially, parallel to the central axis Y of the cylindrical body. They are arranged in a central cylindrical housing, formed inside the cylindrical body 1.

[0203] As shown in particular in [Fig.3], the central housing 5 has a central axis coinciding with the central axis Y of the cylindrical body and a diameter less than Di. In this example, the distribution conduits 52 are arranged within the housing around the central axis Y of the cylindrical body 1, at equidistant points from it.

[0204] The secondary circuit 25 further comprises a collection network 60 for the second fluid from the secondary aquifers 20.

[0205] In the illustrated example, the collection network 60 comprises a plurality of collection conduits 62, each arranged to collect the second fluid from one or more secondary aquifers 20. As shown, each collection conduit 62 is specifically arranged to collect the second fluid from a corresponding secondary aquifer 20.

[0206] As can be seen in Figures 2 and 3, the collection conduits 62 extend parallel to the central axis of the cylindrical body, and are arranged in the central housing 5. The collection conduits 62 are arranged alternately with the distribution conduits 52 around the central axis Y of the cylindrical body, at an equal distance from it.

[0207] The distribution conduits 52 and collection conduits 62 can have respectively a length Ld and Le each between 0.1% and 100% of the total height of the body.

[0208] In the illustrated example, the collection ducts 62 are axially offset relative to the distribution ducts 52. Thus, in this configuration, the ducts of distribution 52 open onto one of the bases 2 of the cylindrical body 1, while the collection conduits 62 open onto the other base 2 of the cylindrical body 1.

[0209] In this example, the collection conduits 62 are sealed at one of their distal ends, at the level of a first face of the body 1, while the distribution conduits 52 are sealed at the distal end located at the second face opposite to the first.

[0210] In the example of Figures 2 and 3, each secondary channel 22 is connected to the successive distribution and collection conduits 62 by two ends 22a and 22b. In this configuration, each secondary channel 22 has a first channel 24 for conveying the second fluid radially in a first direction A, from its inlet at end 22a to the side wall 4 of the body 1, and a second channel 26 for directing the second fluid radially in an opposite direction B, to the corresponding collection conduit 62 via its end 22b. The path of the second fluid in the secondary channel 22 thus takes the form of a "U": it first follows the first channel 24 in direction A, then changes direction to follow the second channel 26 in the opposite direction B, before exiting through end 22b.

[0211] The cylindrical body 1 further comprises a plurality of isthmuses 30 arranged each between a successive primary layer 10 and secondary layer 20 so as to obtain an alternation of primary layers 10, secondary layers 20 and isthmuses in a circumferential direction F of the body 1. As illustrated, each isthmus extends radially towards the lateral wall 4 of the body along a curved extension axis Yi.

[0212] The aforementioned elements are distributed according to a plurality of distinct and successive sectors 40 in the circumferential direction F of the cylindrical body 1, an example of which is given in [Fig. 11]. As can be seen in [Fig. 4], each sector 40 comprises two successive primary 10 and secondary 20 layers and two isthmuses 30, with one of the isthmuses separating the two successive layers 10 and 20. In the example of Figures 1 to 3, the spaces e between the successive primary channels 12 of the same layer 10 are occupied by the isthmuses 30 of the corresponding sector 40.

[0213] As can be seen in this figure, each sector 40 is adjacent to two sectors 40 located on either side. This sector 40 is delimited, on the one hand, by the isthmus 30 of one of its adjacent sectors, and, on the other hand, by the secondary layer 20 of the other adjacent sector.

[0214] Each sector in the illustrated example comprises, in the counter-clockwise direction, a secondary aquifer 20, followed by a first isthmus 30, a primary aquifer 10 successive to the secondary aquifer 20, and then a second isthmus 30.

[0215] In the illustrated example, the sectors 40 are identical and have a curvilinear profile.

[0216] The curvilinear sectors 40 each have a width lm defined according to the following formula: lm = lp+1^ + 2x1^ where lp and ls represent respectively the widths of the primary and secondary layers, and lj is the width of each isthmus of the sector, measured between two primary 12 and secondary 22 channels of the corresponding successive layers 10 and 20. In the illustrated example, the width l is identical for the two isthmuses 30 of the curvilinear sector 40 as well as for all the isthmuses of the cylindrical body 1.

[0217] The number R of the curvilinear sectors 40 is determined to optimize the thermal performance of the heat exchanger. In the illustrated example, this number R is chosen to maximize the internal volume of the primary channels 10, as shown in [Fig. 5]. This figure illustrates a curve representing the relationship between the number R of sectors 40 and the optimal volume of the primary channels 12, highlighting an optimum for maximum thermal performance of the primary circuit.

[0218] The number R of sectors 40 and the width lm of each curvilinear sector 40 are related by the following equation: r* _ lm . i ~

[0219] For each curvilinear sector 40, the primary extension axis Yp and the secondary extension axis Ys have identical curvature. The extension axes Yi of the isthmuses 30 also have identical curvature to that of the axes Yp and Ys. This curvature varies according to the distance from the central axis of the cylindrical body. As can be seen in the figures, the tangent TK to each of the extension axes primary Yp and secondary Ys at a given point K form an angle of inclination ai; non-zero with respect to a radial axis XR of the cylindrical body 1 passing through this point K. This angle of inclination ai increases progressively as the radial distance of the point K with respect to the central axis Y of the cylindrical body 1 increases, in other words, the angle of inclination ai is an increasing function of the radial distance.

[0220] This angle of inclination aî is given by the following equation:

[0221] Where corresponds to the radial distance from point K. 2

[0222] In order to avoid the overlap of the curvilinear sectors 40, the angle of inclination ai preferably satisfies the following condition: a < |-an-i ).

[0223] For each curvilinear sector, with reference to a cylindrical coordinate system, the points (r,0) defining the geometric locus of the primary and / or secondary nappes of this sector are determined by the following iterative relations:

[0224]

[0225]

[0226]

[0227]

[0228]

[0229]

[0230]

[0231]

[0232]

[0233]

[0234] rN+i “ rN + PX OOS<7;- ®N+\~ ®N + ®î With [ -Pi r0~ 2 | 0o = O where rN+i represents the radial coordinate of the next point Kn+i after an iterative step p in the radial direction, with respect to the previous coordinate rN of the point KN: this value rN+i is obtained by adding to the initial radial coordinate rN the product of a step p and the cosine of the angle of inclination θ at the point Kn+i with dxN+i — dθ + p; and 0N+i is the angular coordinate of the next point Kn+i after an iterative step p, relative to the previous angular coordinate 0N of point KN: this value is calculated by adding to the initial point 0N the product of the step p and the sine of the angle of inclination ai, calculated from the instantaneous diameter dKn+i- 0i is the angle increment corresponding to the projection of the step p inclined at an angle a; along the direction 0 at a distance from the center of the cylinder. 0,- = tan' ............. The step p can correspond to the distance separating the sections, in particular transverse, of two successive primary channels 12 of the primary aquifer 10 of the curvilinear sector 40. Alternatively, the step size p can correspond to the spatial resolution of the primary layer 10 of the curvilinear sector 40. Figures 6 to 8 illustrate a heat exchanger reactor body according to a variant of the invention. In the illustrated embodiment, the distribution network 50 and collection network 60 comprise, for each secondary channel 20, a common conduit 72 arranged around the periphery of the cylindrical body. In the illustrated example, these networks comprise several common conduits 72, arranged around the central axis Y of the cylindrical body 1 at equidistant intervals from it. Each conduit 72 is arranged to collect the second fluid from a first group of secondary channels 20A of a secondary channel 20 and convey it, following the arrow Fl, to a second distinct group 20B within the same secondary channel 20. In this example, the two groups of secondary channels 20A and 20B are separated axially by a distance e2, greater than the distance e1 that separates two successive secondary channels 22 within the same group 20A or 20B. In this embodiment, the distribution network 50 comprises a plurality of distribution conduits 52, extending axially around the central axis Y and arranged in the central housing 5. These distribution conduits 52 have a length Ld less than half the total height H of the cylindrical body 1.

[0235] The collection network 60 further comprises collection conduits 62, arranged axially in continuity with the distribution conduits 52, from which they are separated by a distance e2. In the illustrated example, these collection conduits 62 have a length Le less than half the total height H of the cylindrical body 1, and are arranged to convey the second fluid from the secondary aquifers 20 of the second group 20B, in the direction indicated by arrow FL

[0236] The distribution and collection networks can adopt other configurations, as illustrated in Figures 9 and 10.

[0237] In the embodiments of Figures 9 and 10, the distribution conduits 52 are arranged in the central housing 5 of the body 1 while the collection channels 62 are arranged around the periphery of the body 1.

[0238] The invention is not limited to the examples just described.

Claims

1. Demands Heat exchanger reactor or heat exchanger between at least one first and a second fluid comprising: - a main body (1), in particular a single piece or consisting of a set of plates having a sealing joint between two plates, having, on at least an axial portion thereof, a general cylindrical shape of revolution around a central axis (Y), said body (1) comprising: • A primary circuit for the circulation of the first fluid comprising a plurality of primary layers (10), each of the primary layers (10) comprising at least one primary channel (12) arranged to be traversed by the first fluid, said primary channel (12) extending longitudinally along an axial direction of the body (1), • A secondary circuit (25) not connected to the primary circuit, intended for the circulation of the second fluid, comprising a plurality of secondary channels (20), each of the secondary channels (20) being arranged between two successive primary channels (10) and comprising at least one secondary channel (22) arranged to be traversed by the second fluid, said secondary channel (22) extending longitudinally in a radial direction towards a lateral wall (4) of the body (1) and, • A plurality of isthmuses (30), each arranged between a successive primary sheet (10) and secondary sheet (20), so as to obtain an alternation of primary sheets (10), secondary sheets (20) and isthmuses (30) in a circumferential direction of the body (1), The primary (10) and secondary (20) nappes, separated by isthmuses, are distributed according to a plurality of successive sectors (40) of number R with R>1, each sector (40) comprising an alternation of two successive primary (10) and secondary (20) nappes and two isthmuses (30), with one of the isthmuses separating the two successive primary and secondary nappes (10; 20), at least one sector (40) of the plurality of sectors, called the "curvilinear sector", comprising • a primary sheet (10) extending radially towards the lateral wall (4) of the body along a non-rectilinear primary extension axis (Yp), and • a secondary sheet (20) extending radially towards the lateral wall (4) of the body along a non-rectilinear secondary extension axis (Ys).

2. Heat exchanger reactor or heat exchanger according to claim 1, the primary (Yp) and secondary (Ys) extension axes being curved.

3. Heat exchanger reactor or heat exchanger according to claim 2, the primary (Yp) and secondary (Ys) extension axes having substantially identical curvature.

4. Heat exchanger reactor or heat exchanger according to any one of claims 2 and 3, the curvature of the primary (Yp) and secondary (Ys) extension axes being variable as a function of the distance from the central axis of the body, the primary and secondary extension axes each comprising, for example, a succession of arcs of circles.

5. Heat exchanger reactor or heat exchanger according to the preceding claim, the tangent to each of the primary (Yp) and secondary (Ys) extension axes at a given point K forming a non-zero angle of inclination (ai) with respect to a radial axis of the body passing through this point K, this angle of inclination (¾) increasing progressively as the radial distance of the point K with respect to the central axis (Y) of the body (1) increases.

6. Heat exchanger reactor or heat exchanger according to any one of the preceding claims, all sectors (40) of said plurality of sectors being identical and each having an identical width (1m), the body (1) comprising R curvilinear sectors.

7. Heat exchanger reactor or heat exchanger according to the preceding claim with connection to claim 5, the angle of inclination (¾) at a point K of the corresponding extension axis (Yp; Ys) being defined by the following equation: 1 / \ — COS 4 / 360 \ j \ 4 xsnii ^x^J / Where dK corresponds to the radial distance from point K, the instantaneous inclination angle 2 (¾) preferably fulfilling the following condition: J

8. Heat exchanger reactor or heat exchanger according to any one of the preceding claims, at least one primary layer (10), preferably all primary layers (10), comprising a plurality of primary channels (12) arranged along the primary extension axis (Yp), these channels (12) preferably being spaced apart from each other, in particular at equal distances, the space between them being occupied, preferably, by the isthmuses (30) of the corresponding sector (40).

9. Heat exchanger reactor or heat exchanger according to the preceding claim, the primary channels (12) of said primary layer being substantially cylindrical of revolution, their number being given by 2”, where n is a non-zero integer.

10. Claim-heat exchanger or heat exchanger according to claim 8, the primary channels of said primary layer being substantially oblong, each preferably having opposite lateral faces having an identical concavity, said channels adopting for example a shape substantially similar to that of a bean, their number being by reference given by 2", where n is a non-zero integer.

11. A heat exchanger reactor or heat exchanger according to any one of the preceding claims, the secondary circuit (25) further comprising: - a distribution network for conveying the second fluid to the secondary aquifers, preferably said network comprising at least one distribution conduit, preferably a plurality of distribution conduits, each being arranged to distribute the second fluid into one or more secondary aquifers, and - a collection network for recovering the second fluid from the secondary aquifers, preferably the collection network comprising at least one collection conduit, preferably a plurality of collection conduits arranged each to collect the second fluid from one or more secondary aquifers.

12. Heat exchanger reactor or heat exchanger according to the preceding claim, the collection ducts being arranged alternately with the distribution ducts around the central axis of the body(1).

13. Heat exchanger reactor or heat exchanger according to any one of claims 11 and 12, the distribution and collection networks comprising, for at least one secondary aquifer, at least one common conduit, said common conduit serving for example to collect the second fluid from a first group of channels of the secondary aquifer and to convey this fluid to a second separate group of channels within the same aquifer.

14. Heat exchanger reactor or heat exchanger according to any one of the preceding claims, said body being monobloc and obtained by additive manufacturing or by diffusion assembly and welding of several parts, to ultimately form a single piece of one block corresponding to said body.

15. Use of the heat exchanger reactor according to any one of the preceding claims, for the hydrogenation reactions of fluids, in particular in the presence of a fixed bed catalyst.

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