Fixed bed tube reactor with a dressing room

Description

TECHNICAL FIELD

[0001] The present invention relates to the general field of heat exchanger reactors, and more particularly to the field of catalytic heat exchanger reactors using a solid catalyst, especially in powder form, and intended for the implementation of endothermic or mainly exothermic catalytic reactions.

[0002] Such reactions can be used, in particular, for the synthesis of fuels, for example, liquid fuels such as methanol (MeOH), or gaseous fuels such as methane or synthetic natural gas (SNG), dimethyl ether (DME), hydrocarbons, or olefins, obtained from hydrogen and carbon oxides or from synthesis gas comprising a mixture of hydrogen and carbon oxides. They can also be used for the generation of hydrogen from methane, the synthesis of ammonia from hydrogen and nitrogen, or the hydrogenation and dehydrogenation reactions involving hydrogen and liquid organic hydrogen carriers (LOHCs).

[0003] The invention can thus be particularly applied to highly exothermic reactions, such as the methanation (or more generally, the production of hydrocarbons or hydrogenation reactions) of carbon monoxide or carbon dioxide in the presence of hydrogen. It can also be applied to reactions such as the Fischer-Tropsch reaction, the wet or dry reforming of methane or other hydrocarbons, or oxidation or dehydrogenation reactions. The invention can also be used as a heat exchanger for applications, particularly those involving gas, that require frequent maintenance, for example, due to corrosion or fouling, among other things.

[0004] The invention thus proposes a fixed-bed tubular reactor capable of implementing, in particular, exothermic organic synthesis processes. PREVIOUS STATE OF THE ART

[0005] Catalytic reactors using solid catalysts are widely used for the synthesis of organic compounds such as synthetic fuels or fuels including natural gas substitutes (NGS), dimethyl ether, methanol, hydrocarbons or olefins.

[0006] In the context of hydrocarbon production, or more generally for hydrogenation reactions, from hydrogen and carbon monoxide, the equilibria involved, or hereafter referred to as the main reactions, are generically as follows: n CO + 2 n + 1 H 2 ⇔ C n H 2 n + 2 + n H 2 O n CO 2 + 3 n + 1 H 2 ⇔ C n H 2 n + 2 + 2 n H 2 O X + n H 2 ⇔ − X H 2 n −

[0007] The equilibrium described by the third equation (Eq.3) concerns liquid organic hydrogen carrier (LOHC) molecules. It is a reversible reaction, therefore occurring successively in exothermic and then endothermic sequences. These various reactions are well documented from a thermochemical perspective. They potentially give rise to side reactions (for example, WGS (Water-Gas Shift), RWGS (Reverse Water-Gas Shift), Boudouard formation, etc.) known to those skilled in the art but not described here.

[0008] The species involved in these main reactions and the side reactions are called "reactants" for the species entering the reactor, and "products" for the species produced by the main and side reactions. Furthermore, "reactive fluids" refers to all the species involved in these reactions. These reactions are all associated with specific thermodynamic conditions, pressure, and temperature, which are preferred based on the desired performance: it is generally advantageous to operate at high pressure, and it is also necessary to properly manage the exothermicity of these reactions by removing heat from the reaction zone. This ensures the conversion rate, selectivity, and catalyst lifetime, among other factors. Other features, discussed later, are also of interest.

[0009] Many catalytic reactor architectures used in industry for the thermal control and management of endothermic or exothermic chemical reactions are already known. The main types of heat exchanger reactors known for exothermic reactions are described below.

[0010] First, the simplest catalytic reactor technology is the so-called "fixed-bed" reactor. In cascaded adiabatic fixed-bed reactors, exothermicity is generally managed by diluting the reactants at the inlet of the first reaction stage, for example, by recirculating the products, and by using heat exchangers to cool the reactant-product mixture between the different reactors. This architecture has the advantage of simple construction but requires the use of gas recyclers to limit the temperature rise and necessitates the use of high-temperature stable catalysts. These reactors are typically used as centralized units operating in steady state.

[0011] Fluidized bed heat exchanger reactors also exist. Such reactors were developed to address the problem of heat transfer in fixed beds. These reactors offer the advantage of good thermal homogeneity within the reactor, which avoids hot spots, but require, for equivalent power output, a larger reactor volume than plug flow fixed beds. In these reactors, the catalyst is in the form of fine particles whose attrition must be controlled. Furthermore, the fluidization of the particles necessitates limiting the ranges of gas flow variation, making these reactors less flexible with regard to intermittent operation.

[0012] Another heat exchanger reactor technology involves reactors in which the chemical reaction takes place within a reactive channel continuously cooled by an external heat transfer fluid. Most of these reactors are shell-and-tube type, with the reaction occurring in reaction tubes cooled peripherally by a heat transfer bath. The reactive gases flow axially through the tubes, which contain a catalyst, for example, in powder form.

[0013] Combining heat exchanger reactors of the same or different types within the same unit can also be considered in order to improve the conversion, flexibility or utilization of recovered heat.

[0014] Managing the thermal constraints exerted on reactors begins with addressing the need for thermal control. This can take various forms, as outlined in the previous technological solutions. These include off-reactor solutions such as staging the overall conversion, with intermediate cooling and / or dilution and / or condensation; and in-reactor solutions such as the evolution towards the concept of heat exchanger reactors, the intensification of heat exchange, the reduction of reactive channel sizes (millistructuring), the integration of 3D conductive structures for thermal homogenization, and the staggering of reagent injections to distribute energy deposition.

[0015] Regarding the lifespan of catalysts, it should be noted that exothermic reactions generate a large amount of heat, which can lead to the formation of hot spots. This results in local degradation of the catalyst and a reduction in the overall conversion performance of the reactor / catalyst system. In other words, the degradation of the solid catalyst can lead to its deactivation and a decrease in the conversion rate of the chemical species present. The selectivity of the reactions involved is also affected.

[0016] Furthermore, certain hydrogenation reactions highly useful to industry, such as methanol synthesis or the Fischer-Tropsch reaction, as described by the preceding equations Eq. 1 to Eq. 3, are balanced and, under commonly used thermodynamic conditions, have low to moderate conversion rates. An interesting strategy then consists of incorporating permselective membranes onto one or more walls of the reaction channels, thereby removing a produced species, typically water, from the reaction medium. This unbalances the reaction and increases its productivity. The advantage of such a process has been demonstrated experimentally and theoretically. Innovations can focus on two main elements: the membranes themselves and the methods of integrating them into the reactors.

[0017] In the conventional heat exchanger reactor design with the catalyst located within the tubes, one of the challenges with shell-and-tube technologies is controlling the areas that become hotter due to the exothermic reaction. This phenomenon necessitates intense cooling of the tubes across their entire surface, whereas at any given time, only a small portion of this surface requires intensive cooling, for example, for the injection and axial circulation of reactants. A consequence of this is an oversizing of the thermal fluid flow rate.

[0018] To overcome these problems, an arrangement has been proposed that distributes the reactants along the entire length of the tubes. This solution allows for better temperature homogeneity throughout the reactor. In this regard, documents US 3,758,279 A, ​​US 4,374,094 A, EP 0 560 157 A1, and US 2,997,374 A propose heat exchanger reactors that implement reactant distribution from an annular distribution space. Specifically, these heat exchanger reactors, generally cylindrical in shape, comprise, arranged coaxially from the outside of the reactor, a tube, the annular distribution space, a catalyst charge, and a collection space. These solutions constitute the standard for cooling in shell-and-tube reactors, meaning that tube cooling is controlled solely by the flow in the shell.

[0019] These arrangements are not entirely satisfactory. The presence of the annular distribution space around the catalyst charge limits heat transfer from the catalyst to the tube, rendering the cooling systems generally considered inefficient. It remains possible, however, to insert heat-conducting elements into the reactor. Such a solution, however, is incompatible with reactors containing small-diameter tubes.

[0020] Conversely, document CN 103990420 A proposes the use of an insert with a distribution chamber and a collection chamber, positioned in the center of a tube and defining, together with the tube, an annular space housing the solid catalyst. However, the arrangement proposed in this document does not allow for homogeneous temperature distribution within the annular space. More specifically, this arrangement does not allow for an optimal temperature profile within the solid catalyst.

[0021] There figure 1US patent 8,961,909 A represents another example of a shell-and-tube reactor. This reactor is equipped with an injection tube immersed in a bed of catalytic powder, along which perforations are made. These perforations are arranged to ensure the injection of the reactive gas at different levels of the catalytic powder bed, thus limiting the formation of hot spots within the bed. However, this reactor is not entirely satisfactory. Indeed, to ensure its cooling, this reactor requires the implementation of multiple circulation circuits for a heat transfer fluid, which significantly increases its complexity.

[0022] US patent 7,402,719 B2, specifically Figure 3a, discloses another example of a reactor designed to allow the staged injection of a reactant C for its reaction with a reactant A. This reactor comprises two layers (or channels) separated by a wall, designed to ensure the circulation of reactants A and C, respectively. The two layers are also in fluidic communication by means of a plurality of perforations in the wall separating them. These perforations are arranged to ensure progressive mixing of reactant C with reactant A. This progressive mixing helps to limit the formation of hot spots. However, the reactor's stacked layer design makes it somewhat inconsistent.

[0023] Furthermore, in the Applicant's patent application FR 3 103 714 A1, an insert-type device organizes an axial distribution of reactive gases in the tubes, a circulation of gases in the substantially orthoradial direction through a catalyst bed in an annular space defined by the inner wall of a tube and the outer wall of the insert, and an axial collection of the produced gases.

[0024] There is still a need to improve these types of reactors, and in particular to equip such shell and tube reactors with an alternative fluid circulation system to improve cooling. DESCRIPTION OF THE INVENTION

[0025] The invention therefore aims to remedy at least partially the needs mentioned above and the drawbacks related to prior art achievements.

[0026] The invention aims in particular to provide a fixed-bed tubular reactor that allows for a more uniform distribution of reactants within the solid catalyst, a more homogeneous distribution of the heat flux generated within the solid catalyst, and improved cooling management. Furthermore, the invention seeks to provide a tubular reactor for which reliability and lifespan (of the catalysts) are improved compared to known prior art reactors, and which allows for optimization (increased) the gas transit time through the fixed bed of catalytic powder.

[0027] The invention thus relates, according to one of its aspects, to a fixed-bed tubular reactor extending, along a longitudinal axis, between a first end and a second end, said reactor comprising a bed of catalytic powder confined in an annular space delimited by an outer wall of a hollow tube and an inner wall of a hollow insert arranged coaxially in the hollow tube, the hollow insert comprising at least one distribution chamber and at least one collection chamber, separated from each other by at least one first separating wall, said at least one distribution chamber and said at least one collection chamber comprising, respectively, a gas inlet opening at the first end and a gas outlet opening at the second end,characterized in that the reactor further comprises at least one booster chamber separated from said at least one distribution chamber and said at least one collection chamber by at least one first separating wall, said at least one booster chamber comprising an inlet orifice for at least one booster fluid, separate from the gases circulating in said at least one distribution chamber and in said at least one collection chamber, at the first end and an outlet orifice for said at least one booster fluid at the second end.

[0028] Thanks to the invention, it is possible to improve the cooling of the reaction zone (reactants, reaction products, and catalysts) by enabling this zone to be cooled through internal and external circulation of a heat transfer fluid, which is beneficial for all hydrogenation reactions, for example. The overall performance of the reactor (conversion rate and reaction selectivity) will be improved by the greater temperature uniformity resulting from the application of the invention.

[0029] The reactor according to the invention may further include one or more of the following characteristics taken individually or in any possible technical combinations.

[0030] Each of the said at least one distribution chamber, at least one collection chamber and at least one supplementary chamber may be delimited by a section of the internal wall and two first separating walls.

[0031] Furthermore, the reactor may include at the first end and at the second end, respectively, a distributor space and a collector space between which the hollow insert is disposed.

[0032] In addition, the tube and the insert may be held by at least two retaining tube plates respectively at the first and second ends, at least one of said at least two retaining tube plates, in particular all the retaining tube plates, comprising an inlet or outlet conduit respectively fluidically connected to an inlet or outlet port for makeup fluid and formed in said at least one of said at least two retaining tube plates, to permit in particular lateral admission and / or extraction of makeup fluid.

[0033] The axial lengths of the tube and the insert may be different, with the axial length of the tube being notably shorter than the axial length of the insert.

[0034] Alternatively, the tube and the insert can be held by at least two retaining tube plates respectively at the first and second ends, and at least one inlet or outlet conduit respectively fluidically connected to an inlet or outlet port for makeup fluid can be located respectively in the distributor space and in the collector space, outside of said at least two retaining tube plates, to allow in particular a lateral admission and / or extraction of makeup fluid.

[0035] Alternatively, the tube and the insert may be held by at least two retaining tube plates respectively at the first and second ends, and said inlet orifice and said outlet orifice of said at least one makeup fluid may be formed respectively in the upper and lower ends of the insert to allow respectively a supply from the distributor space and an extraction from the collector space, the reactor further comprising at least one lateral gas supply duct and at least one lateral gas extraction duct.

[0036] Said at least one lateral supply duct and the supply of make-up fluid to the distributor space on the one hand, and said at least one lateral extraction duct and the extraction of make-up fluid from the collector space on the other hand, may be separated by a sealed separation plate.

[0037] In addition, a sealing gasket can be placed between the insert and each of the sealed separating plates.

[0038] Furthermore, the flow of said at least one makeup fluid may be carried out in a co-current or counter-current manner to the flow of gases in said at least one distribution and collection chamber.

[0039] If necessary, the catalytic powder can be retained in the annular space by a fibrous material seal at each end of the annular space.

[0040] Advantageously, said at least one make-up fluid may be a heat transfer fluid, in particular a cooling fluid.

[0041] Furthermore, the insert can be a single piece.

[0042] Furthermore, the invention also relates, according to another of its objects, to the use of a tubular reactor as defined above, characterized in that it implements endothermic or exothermic reactions for the synthesis of fuels and combustibles.

[0043] In particular, the annular space can allow a hydrogenation reaction and said at least one booster chamber can allow a dehydrogenation reaction, or vice versa. BRIEF DESCRIPTION OF THE DRAWINGS

[0044] The invention will be better understood upon reading the detailed description that follows, the non-limiting examples of its implementation, and upon examination of the schematic and partial figures in the attached drawing, on which: there figure 1is a schematic representation of a fixed-bed tubular reactor according to the invention, along a cross-sectional plane passing through the longitudinal axis of the reactor, in particular along the longitudinal cross-sectional plane PP of the figure 2 allowing visualization of a collection chamber and a distribution chamber, the figure 2 is a cross-sectional view along a transverse plane, or normal section, perpendicular to the longitudinal axis of the tubular reactor of the figure 1 , there figure 3 is a schematic representation of the tubular reactor of figures 1 and 2 according to the longitudinal section plane P'P' of the figure 2 allowing visualization of two auxiliary chambers, supplied by lateral inlet and outlet ports, the figure 4 is a view similar to that of the figure 1 illustrating the use of seals to retain the catalyst, the figure 5 is a view similar to that of the figure 3illustrating the use of seals to retain the catalyst, the figure 6 is a schematic representation of another example of a tubular reactor according to the invention, from a view similar to that of the figure 1 , there figure 7 is a view similar to that of the figure 3 for the reactor of the figure 6 , there figure 8 is yet another schematic representation of another example of a tubular reactor according to the invention, from a view similar to that of the figure 1 , there figure 9 is a view similar to that of the figure 3 for the reactor of the figure 8 , THE Figures 10 And 11 are views, in axial section respectively along planes PP and P'P' with reference to the figure 2 , of a plurality of tubular reactors similar to that of the figures 1 to 5 , located inside a grille, and the figure 12 is a view, in axial section along the plane P'P' with reference to the figure 2, of a plurality of tubular reactors similar to that of the figures 6 And 7 located inside a grille.

[0045] Throughout these figures, identical references may designate identical or analogous elements.

[0046] Furthermore, the different parts represented in the figures are not necessarily shown on a uniform scale, in order to make the figures more legible. DETAILED DESCRIPTION OF SPECIFIC IMPLEMENTATION METHODS

[0047] The present invention relates to a tubular heat exchanger reactor with a fixed catalytic powder bed. In particular, the catalytic powder bed is confined within an annular space delimited by a wall, referred to as the outer wall, of a hollow tube and another wall, referred to as the inner wall, of a hollow insert housed coaxially within said tube. The catalytic powder bed may, in particular, comprise a catalyst in granular form.

[0048] Thus, at figures 1 and 2An example of the embodiment of a fixed-bed tubular reactor according to the present invention can be seen. It should be noted that on these figures 1 and 2 , as well as in all the figures described subsequently, the arrows F represent the direction of gas flow. Furthermore, the arrows F', notably visible on the figures 3 , 5 , 7 , 9 And 11 , represent the direction of flow of the makeup fluid.

[0049] The tubular reactor 1 according to the present invention comprises an external hollow tube 10 extending along a longitudinal axis XX' between a first end 11 and a second end 12. The hollow tube 10 may have rotational symmetry about the longitudinal axis XX'. It is therefore understood that the longitudinal axis XX' may be an axis of revolution of the hollow tube 10.

[0050] The hollow tube 10 may be made of a metal, including steel, aluminum alloy, copper alloy, nickel alloy, and others. The diameter of the hollow tube 10 may be between 5 mm and 100 mm. The wall, referred to as the outer wall 15, forming the hollow tube 10 may have a thickness between 0.5 mm and 10 mm. The hollow tube 10 may have a length between 10 times and 200 times the diameter of its inner surface.

[0051] The tubular reactor 1 also includes a hollow insert 20, which extends along the longitudinal axis XX' and is generally cylindrical in shape. The hollow insert 20 is housed coaxially within the volume of the hollow tube 10. Specifically, the insert 20 also includes a wall, referred to as the inner wall 21, which may be gas-permeable, and which, together with the outer wall 15, defines an annular space 30. This annular space 30 is filled with a catalytic powder and is the site of the conversion reactions of reactive gases that may pass through the tubular reactor 1. The annular space 30 may have a thickness, defined as the distance between the outer wall 15 and the inner wall 21, of between 2% and 20% of the diameter of the inner surface of the hollow tube 10. The hollow insert 20 may be a single piece.The hollow insert 20 can, for example, be made of stainless steel, notably by brazing methods, or of aluminum, notably by extrusion or additive manufacturing methods (for example, a 3D printing process), or even of polymers for certain low-temperature reactions. The various openings of the hollow insert 20 can be made during the insert's manufacture and / or machined subsequently.

[0052] The hollow insert 20 also includes at least one distribution chamber 40 and at least one collection chamber 50. Here, for the sake of simplicity, only one distribution chamber 40 with a single injection point and one collection chamber 50 are shown, but this choice is not exhaustive. In particular, the hollow insert 20 may include between 1 and 4 distribution chambers 40, and between 1 and 4 collection chambers 50.

[0053] Said at least one distribution chamber 40 and said at least one collection chamber 50 are advantageously arranged alternately, and extend over the entire length of the hollow insert 20.

[0054] Advantageously, the hollow insert 20 also includes at least one additional chamber 100 organizing the axial circulation of an additional fluid, here two additional chambers 100, but the invention is not limited on the number of additional chambers and additional fluids.

[0055] Thus, we find successively by observing a plane in section normal to the axis XX' of the hollow tube 10, as visible on the figure 2a first auxiliary chamber 100, said at least one collection chamber 50, a second auxiliary chamber 100 and said at least one distribution chamber 40. Said at least one collection chamber 50, said at least one distribution chamber 40 and the auxiliary chambers 100 are further separated from each other by first separating walls 60. It is therefore understood that a distribution chamber 40 is delimited by two separating walls 60 and a section of the internal wall 21. Equivalently, a collection chamber 50 is also delimited by two first separating walls 60 and another section of the internal wall 21. Equivalently again, an auxiliary chamber 100 is separated by two first separating walls 60 and yet another section of the internal wall 21.

[0056] Furthermore, the first separating walls 60 extend along the entire length of the hollow insert 20 within the volume defined by the hollow tube 10, and are arranged to prevent any direct passage of gas from one chamber to the other. For example, the first separating walls 60 form planes passing through the longitudinal axis XX'.

[0057] In particular, the first two separating walls 60 of a distribution chamber 40 may have a generally elongated shape and extend along the longitudinal axis XX' from the first end 11 to the second end 12. In particular, the first two separating walls 60 of a distribution chamber 40 may have a common side coinciding with the longitudinal axis XX'.

[0058] Furthermore, reactor 1 may include, at the first end 11 of the hollow insert 20, a distribution space 42, or inlet plenum, through which one or more reactive gases may be admitted into the distribution chamber 40 via an inlet opening. Similarly, reactor 1 may include, at the second end 12 of the hollow insert 20, a collector space 51, or outlet plenum, through which one or more gases may be discharged via an outlet opening.

[0059] Furthermore, the distribution chamber 40 is sealed at the second end 12, and the collection chamber 50 is sealed at the first end 11.

[0060] The inner wall 21 may further include at least one distributing opening and at least one collecting opening, respectively allowing the distribution of a gas that can be admitted through the inlet opening at the level of the inlet plenum 42 into a distribution compartment towards the annular space 30, and the collection of the gas distributed in the annular space 30 by the collection chamber 50.

[0061] The hollow tube 10 is advantageously held by two tubular retaining plates 33, each of which includes a first watertight fixing system 34 for the hollow tube 10 to each retaining plate 33. Similarly, the hollow insert 20 is advantageously held by the two retaining plates 33, each of which includes a second watertight fixing system 35 for the hollow insert 20 to each retaining plate 33. Separating walls 36 are also present in each of the retaining plates 33, between which the hollow tube 10 and the hollow insert 20 are contained.

[0062] According to an advantageous aspect illustrated in figures 4 And 5The catalytic powder is retained in the annular space 30 by a seal 31, for example made of fibrous material, at each end of the annular space 30. Since the seal 31 is made of fibrous material, it is necessarily porous and therefore permeable to reactive gases. The fibrous material may, in this respect, comprise at least one of the following: glass fiber, ceramic fiber, metal fiber, carbon fiber, or polymer fiber.

[0063] The seal 31 can be in the form of a braid, a sheath, a cord, or simply consist of a filling of fibrous material. The fibrous material is advantageously a thermal insulator and has a thermal conductivity substantially equivalent to that of the catalyst used (0.2 W / m / K to 10 W / m / K).

[0064] There figure 3 allows visualization, in axial section according to the plane P'P' of the figure 2, the booster chambers 100 described previously. Each booster chamber 100 is supplied by a lateral inlet port 110, located near the end 11 of the hollow tube 10, this inlet port 110 being supplied by a lateral inlet conduit 111 formed in the upper retaining plate 33.

[0065] Similarly, each makeup chamber 100 has a lateral outlet 112, located near the end 12 of the hollow tube 10, this outlet 112 being fluidically connected to a lateral outlet conduit 113 formed in the lower retaining plate 33. In this way, a makeup fluid F' can be admitted by circulation into the retaining tube plates 33.

[0066] Advantageously, the invention thus makes it possible to extend the thermalization capacities of reactor 1, in particular to allow the management and circulation of make-up fluids, including utility or reactive fluids, in addition to the reactants and reaction products, for example according to equations Eq. 1 and / or Eq. 2 described previously.

[0067] The geometry of the hollow insert 20 and the geometry of the hollow external tube 10 are defined so as to allow separate feeding of the distribution chambers 40 and make-up chamber 100, and separate outlets of the collection chambers 50 and make-up chamber 100.

[0068] In the example of implementation of the figures 1 to 5The hollow tube 10 and the hollow insert 20 have different axial lengths, the hollow tube 10 being shorter than the hollow insert 20, and the supply and discharge of the makeup fluid is carried out through a retaining plate 33, via conduits 111 and 113. Furthermore, the flow of the makeup fluid F' is directed axially and co-currently with the gas circulation. However, a counter-current design may also be advantageous.

[0069] In the example of implementation of the figures 6 And 7 The supply of the auxiliary chambers 100 is ensured by means of dedicated conduits located in the inlet plenums 42 and outlet plenums 51, and no longer by means of conduits machined in retaining plates 33.

[0070] More specifically, as seen on the figure 7, a lateral inlet conduit 111, for the admission of makeup fluid F', is located along the upper retaining plate 33, outside of it, in the upper part of reactor 1. Similarly, a lateral outlet conduit 112, for the extraction of makeup fluid F', is located along the lower retaining plate 33, outside of it, in the lower part of reactor 1.

[0071] Thus, the supply and discharge of the makeup fluid F' are ensured by conduits 111, 112 constructed outside the retaining tube sheets 33, and providing a leak-proof connection with the outside of the inlet 41 and outlet 51 plenums. Furthermore, the flow of the makeup fluid F' is directed axially and in a co-current manner with the gas circulation. However, a counter-current design may also be advantageous.

[0072] In the example of implementation of the figures 7 and 8The supply of the auxiliary chambers 100 is ensured by means of additional connections in the inlet plenum 42 and outlet plenum 51.

[0073] More specifically, as seen on the figure 7 The supply and extraction of the makeup fluid F' are ensured by the upper and lower ends of the hollow insert 20. The reactive fluids F are then introduced laterally via lateral reactive fluid inlet 140 and outlet 141 channels, as shown in the figure 9 The airtight separation between the makeup fluids F' and the reactive fluids F is ensured by means of removable separation plates 105, introduced into the inlet and outlet plenums, and arranged each around the hollow insert 20. A sealing gasket 106 is then placed between each separation plate 105 and the hollow insert 20.

[0074] Advantageously, the methods of implementation of figures 5 and 6 on the one hand, and of the figures 7 and 8 On the other hand, they allow for the creation of a tubular plate and tube assembly close to classic designs.

[0075] THE Figures 10 And 11 are an illustration of the implementation of a plurality of tubular reactors 1 conforming to the invention, and in particular according to the variant of figures 1 to 5 Similarly, the figure 12 is an illustration of the implementation of a plurality of tubular reactors 1 conforming to the invention according to the variant of figures 6 And 7 .

[0076] This implementation includes in particular four tubes 1 arranged parallel to each other in a shell C. The tubular support plates 33 allow the tubes 1 to be held in place, and provide a space for the circulation of a heat transfer fluid intended for the cooling of the tubes 1, by means of heat transfer fluid supply and evacuation systems 120.

[0077] In the example of Figures 10 And11 , the distribution chamber(s) 40 are supplied directly from the inlet plenum 42 via reagent supply systems 125. Then, the evacuation of unconverted products and reagents is carried out in the outlet plenum 51 via extraction systems 126.

[0078] Here, the external tubes are shorter than the inserts 20, and the makeup fluid F' is distributed directly into the inserts 20 by conduits 111, 113 integrated into the tubular retaining plates 33.

[0079] In the example of the figure 12 The hollow inserts 20 are longer. The supply and extraction of the make-up fluid F' are carried out by a dedicated circuit of conduits 111, 113 located outside the retaining plates 33.

[0080] The tubular reactor 1 according to the present invention, and in particular the implementation of booster chambers 100 allowing the circulation of utility or reactive fluids, makes it possible to extend the thermalization capacities.

[0081] This configuration also addresses the issue of catalytic powder heating, particularly in granular catalyst form, and thus limits the formation of hot spots. The result is a more efficient and durable device. Furthermore, the arrangement of the catalytic powder within the annular space 30 facilitates its cooling. Example application:

[0082] Two numerical models were created based on the principle of the invention, using a cooling heat transfer fluid as the make-up fluid.

[0083] For these, a reactor supply at 3 bar and 250°C was assumed, a homogeneous heat exchange coefficient on the outside of the hollow tube 10 of 1500 W / m 2< / K with a reference temperature of 250°C, and a heat release in the porous matrix of 200 W of power.

[0084] A first simulation was conducted without internal circulation of the heat transfer fluid, and a second simulation with internal circulation of the heat transfer fluid, all other things being equal. The results are summarized in Table 1 below. Not only does the internal circulation of a makeup fluid, in this case a heat transfer fluid, within the makeup chambers 100 limit the temperature increase, but it also allows for better temperature homogeneity within the catalytic bed. Table 1 gas porous matrix (catalyst) heat transfer fluid (supplementary) average temperature (°C) maximum temperature (°C) average temperature (°C) maximum temperature (°C) Without 271 292 290 308 With 254 256 271 279

[0085] Of course, the invention is not limited to the examples of implementation that have just been described. Various modifications can be made to it by a person skilled in the art.

[0086] In particular, the number, and the respective angular arrangement, of the 100 auxiliary chambers, 50 collection chambers and 40 distribution chambers may vary.

[0087] The direction of flow of the makeup fluids F' in the makeup chambers 100 can vary.

[0088] The choice of location of the feeds and extractions, in particular at the end of insert 20 or by lateral tapping of insert 20, respectively of the make-up fluids F' and of reactants F may vary depending on the process.

[0089] The supply of the auxiliary chambers 100 may or may not be associated with the tubular plates 33.

[0090] The reactor 1 according to the invention may or may not include means for staged injection.

[0091] In the case where the 100 auxiliary chambers are used as cooling chambers, as in the previous examples, the efficiency of the system can be further improved by various manipulations aimed at intensifying heat exchanges and known to those skilled in the art, such as structuring, in particular micro-structuring, of surfaces, modifications of thermo-hydraulic regimes, among others.

[0092] In the event that the hollow insert 20 is the site of an endothermic reaction, the heat input could be provided by the heat transfer fluid, instead of the make-up fluid as the cooling fluid.

[0093] In particular, the auxiliary chambers 100 can be used to house a chemical reaction of the opposite nature to that located in the annular space 30, for example, a hydrogenation reaction versus a dehydrogenation reaction, for the purpose of energy integration. This latter reaction can, for example, be considered as taking place through a fixed bed.

[0094] Thus, for example, annular space 30 can be the site of a hydrogenation reaction of the type CO₂ + 4 H₂ → CH₄ + 2 H₂O (ΔH₂₉ = -165 kJ / mol), and the booster chambers 100 can be the site of a catalytic fixed-bed dehydrogenation reaction based on the GBL / BDO ("butyrolactone / butanediol") pair of liquid organic hydrogen carrier (LOHC) molecules of the type BDO → GBL + 2 H₂ (ΔH₂₉ = 31 kJ / mol H₂). The reaction enthalpies and operating conditions are compatible so that the energy required for dehydrogenation is supplied by the hydrogenation reaction.

Claims

1. A fixed-bed tubular reactor (1) which extends, along a longitudinal axis (XX'), between a first end (11) and a second end (12), said reactor (1) comprising a bed of catalytic powder confined in an annular space (30) delimited by an external wall (15) of a hollow tube (10) and an internal wall (21) of a hollow insert (20) disposed coaxially in the hollow tube (10), the hollow insert (20) comprising at least one distribution chamber (40) and at least one collection chamber (50), separated from each other by at least one first separating wall (60), said at least one distribution chamber (40) and said at least one collection chamber (50) comprising, respectively, a gas admission opening (42) at the first end (11) and a gas evacuation opening (51) at the second end (12), characterised in that the reactor (1) further includes at least one supplemental chamber (100) separated from said at least one distribution chamber (40) and from said at least one collection chamber (50) by at least one first separating wall (60), said at least one supplemental chamber (100) comprising an inlet orifice (110) for at least one supplemental fluid (F'), distinct from the gases circulating in said at least one distribution chamber (40) and in said at least one collection chamber (50), at the first end (11) and an outlet orifice (112) of said at least one supplemental fluid (F') at the second end (12).

2. The reactor according to claim 1, characterised in that each of said at least one distribution chamber (40), at least one collection chamber (50) and at least one supplemental chamber (100) is delimited by a section of the internal wall (21) and two first separating walls (60).

3. The reactor according to claim 1 or 2, characterised in that it includes at the first end (11) and at the second end (12), respectively, a distributor space (42) and a collector space (51) between which the hollow insert (20) is disposed.

4. The reactor according to one of the preceding claims, characterised in that the tube (10) and the insert (20) are held by at least two tubular holding plates (33) respectively at the first (11) and second (12) ends, at least one of said at least two tubular holding plates (33), in particular all the tubular holding plates (33), including an inlet or outlet conduit (111, 113) respectively fluidly connected to a supplemental fluid (F') inlet (110) or outlet (112) orifice and formed in said at least one of said at least two tubular holding plates (33), in particular to allow lateral admission and / or extraction of supplemental fluid (F').

5. The reactor according to claim 4, characterised in that the axial lengths of the tube (10) and the insert (20) are different, the axial length of the tube (10) being in particular shorter than the axial length of the insert (20).

6. The reactor according to claim 3, characterised in that the tube (10) and the insert (20) are held by at least two tubular holding plates (33) respectively at the first (11) and second (12) ends, and in that at least one inlet or outlet conduit (111, 113) respectively fluidly connected to a supplemental fluid (F') inlet (110) or outlet (112) orifice is located respectively in the distributor space (42) and in the collector space (51), outside said at least two tubular holding plates (33), to allow in particular lateral admission and / or extraction of supplemental fluid (F').

7. The reactor according to claim 3, characterised in that the tube (10) and the insert (20) are held by at least two tubular holding plates (33) respectively at the first (11) and second (12) ends, and in that said inlet orifice (110) and said outlet orifice (113) of said at least one supplemental fluid (F') are respectively formed in the upper and lower ends of the insert (20) to respectively allow a supply from the distributor space (42) and an extraction from the collector space (51), the reactor (1) further comprising at least one lateral gas supply conduit (140) and at least one lateral gas extraction conduit (141).

8. The reactor according to claim 7, characterised in that said at least one lateral supply conduit (140) and the supply of supplemental fluid (F') to the distributor space (42) on the one hand, and said at least one lateral extraction conduit (141) and the extraction of supplemental fluid (F') from the collector space (51) on the other hand, are separated by a sealed separation plate (105).

9. The reactor according to claim 8, characterised in that a seal (106) is disposed between the insert (20) and each of the sealed separation plates (105).

10. The reactor according to any one of the preceding claims, characterised in that the flow of said at least one supplemental fluid (F') is carried out in a co-current or counter-current manner to the flow of gases in said at least one distribution (40) and collection (50) chamber.

11. The reactor according to any one of the preceding claims, characterised in that the catalytic powder is retained in the annular space (30) by a seal (31) made of fibrous material at each of the ends of the annular space (30).

12. The reactor according to any one of the preceding claims, characterised in that said at least one supplemental fluid (F') is a heat transfer fluid, in particular a cooling fluid.

13. The reactor according to any one of the preceding claims, characterised in that the insert (20) is a one-piece part.

14. A use of a tubular reactor (1) according to any one of the preceding claims, characterised in that it implements endothermic or exothermic reactions for the synthesis of fuels and combustibles.

15. The use according to claim 14, characterised in that the annular space (30) allows a hydrogenation reaction and in that said at least one supplemental chamber (100) allows a dehydrogenation reaction, or vice versa.