• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention a reactor (1) with radial circulation of gaseous fluid comprising: • an outer envelope (2) defining an enclosure extending along a vertical main axis comprising at least one catalytic zone (12) containing N fixed beds of catalyst ( 26,27) staggered along the vertical principal axis, N being an integer greater than or equal to 2, wherein the catalyst of each fixed bed has a different composition and wherein for each fixed bed the void ratio and or the average equivalent diameter of the catalyst are different; Input means of a gaseous fluid; Means for withdrawing a reaction effluent; • a collection assembly (8) of the reaction effluent disposed adjacent to the catalytic zone, a vertical collection assembly (8) of a gaseous fluid disposed adjacent to the catalytic zone; and wherein the collection assembly comprises N zones, each zone being associated with a fixed bed of the catalytic zone and in which at least two adjacent zones have different porosities which is a function of the void ratio and / or the average equivalent diameter catalyst of the fixed bed to create a homogeneous distribution of gaseous fluid velocities over the height of the catalytic zone and wherein at least two adjacent zones have different porosities.
    公开号:FR3033264A1
    申请号:FR1551833
    申请日:2015-03-05
    公开日:2016-09-09
    发明作者:Frederic Bazer-Bachi；Cecile Plais；Eric Sanchez
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] The present invention relates to a reactor for conducting catalytic conversion reactions of a hydrocarbon feedstock which is in the gas phase and with a movement of the feedstock through a catalytic bed in a set of directions corresponding to spokes oriented from the periphery towards the center or from the center of the reactor towards its periphery. The present invention also relates to a process for the catalytic treatment of a hydrocarbon feedstock using such a reactor. State of the art Catalytic bed reactors with a radial circulation of the gaseous charge are known in the field of refining. In particular, such reactors are used to carry out catalytic reforming reactions which aims to convert C7-C10 paraffinic and C7-C10 naphthenic compounds to aromatic compounds with the associated production of hydrogen. The catalytic conversion is generally carried out at high temperature, of the order of 500 ° C., at an average pressure of between 1 and 2.5 MPa and in the presence of a specific reforming catalyst so as to produce a high-index reformate. octane rich in aromatic compounds that can serve as a fuel base. Currently the reforming units in radial bed use so-called regenerative processes which operate by continuous withdrawal and regeneration of the catalyst which is then recycled into the process. For example, document FR 2 064 274 describes a reforming process using a radial flow reactor comprising two stepped catalytic beds arranged in series. The catalytic system is introduced at the top of the reactor and flows by gravity and is withdrawn at the bottom of the reactor to be treated in a regeneration unit and then recycled after regeneration at the top of the reactor. In operation, the catalyst and the hydrocarbon feed are fed continuously to the top of the reactor. The catalyst particles descend through the reactor in the form of two annular catalyst beds which are delimited by two spaced cylindrical grids (or sieves). The gaseous charge of hydrocarbons is sent in a descending stream and radially, for example from the periphery to the center of the reactor, through the first catalytic bed and a first effluent is recovered which is collected in a cylindrical collection space delimited by a cylindrical sieve (which is designated by the term "collection tube"). The effluent withdrawn from the collection space is reheated and returned in a downward and radial direction through the second annular catalyst bed disposed below the first catalyst bed. The spent catalyst is removed from the reactor by means of draw legs located at the bottom of the reactor and then sent to a catalyst regeneration unit 3033264 for treatment. At the end of the treatment, the regenerated catalyst is transferred to a storage hopper which serves to feed the reactor with catalyst. Thus the so-called multi-catalytic catalyst continuous-flow regeneration systems employ a single type of catalyst which travels in the form of an uninterrupted column of particles through the reactor from its top to the bottom. The constraints related to mobile radial bed technology are multiple. In particular, the gas velocities at the crossing of the catalytic bed are limited to: - avoid cavitation at the entrance of the bed - avoid blocking the catalyst at its output against the internal grid, also called "pinning" in English - reduce losses load (function of speed and bed thickness). Thus, radial reactors in a moving bed do not make it possible to use several types of catalysts for carrying out different catalytic reactions.
    [0002] An object of the invention is to provide a radial bed reactor which comprises at least one fixed catalytic bed consisting of several layers of catalyst, for which the pressure drop is controlled so that the gaseous feed is distributed homogeneously over the height of the catalytic zone.
    [0003] The reactor according to the invention may be derived from a remodeling (or "revamping" according to the English terminology) of a radial reactor with a fixed catalytic bed in which the central collector has been replaced by a collection assembly described herein. -Dessous. SUMMARY OF THE INVENTION The present invention thus relates to a reactor with a radial circulation of gaseous fluid, comprising: an outer envelope defining an enclosure extending along a vertical main axis comprising at least one catalytic zone containing N fixed catalyst beds arranged in staged manner along the vertical principal axis, 30 N being an integer greater than or equal to 2, in which the catalysts of two adjacent fixed beds are of different compositions and in which two adjacent fixed beds have a void ratio and / or a average equivalent diameter of the different catalyst; input means for a gaseous fluid; Means for withdrawing a reaction effluent; A vertical collection assembly for the reaction effluent disposed adjacent to the catalytic zone; and wherein the collection assembly comprises N zones, each zone being associated with a fixed bed of the catalytic zone and in which at least two adjacent zones have different porosities which is a function of the void ratio and / or the equivalent diameter means of the catalyst of the fixed bed in order to create a homogeneous distribution of the gaseous fluid velocities over the height of the catalytic zone. According to one embodiment, the collection assembly comprises a vertical cylindrical grid permeable to gaseous fluid and impermeable to catalysts and the grid comprises N zones, each zone being associated with a fixed bed of the catalytic zone and in which at least two adjacent areas have different porosities. According to another embodiment, the collection assembly comprises a vertical cylindrical grid permeable to gaseous fluid and impervious to catalysts and a gas-permeable vertical cylindrical tube supported by said grid and disposed concentrically with respect to said grid. The cylindrical tube comprises N zones, each zone being associated with a fixed bed of the catalytic zone and in which at least two adjacent zones have different porosities which are a function of the void ratio and / or the average equivalent diameter of the bed catalyst. fixed. Preferably, each zone of the cylindrical tube has through holes and wherein the number and / or size of the through holes are different from one zone to another. Preferably, the grid is formed by a plurality of vertical wires spaced from each other and secured to a plurality of horizontal support rings and the cylindrical tube is integral with the horizontal support rings. The catalytic zone may be of annular shape defined between a cylindrical outer sieve and a cylindrical internal sieve placed at a distance from the outer sieve, the sieves being permeable to the gaseous fluid and impervious to the catalysts. According to one embodiment, the outer screen consists of an assembly of shell-shaped ducts permeable to gaseous fluid and impervious to catalysts. According to a particular embodiment, the outer sieve of the catalytic zone is constituted by the collection assembly and said reactor is configured to operate with the gaseous fluid flowing in upward or downward movement and in one direction. radial centrifugal. Alternatively, the internal sieve of the catalytic zone is constituted by the collection assembly and the said reactor is configured to operate with the gaseous fluid flowing in ascending or descending motion and in a centripetal radial direction. The present invention also relates to a process for converting a gaseous hydrocarbon feedstock using a reactor according to the invention, comprising the following 10 stages: the gaseous hydrocarbon feedstock is continuously fed into a catalytic bed contained in the reactor; the hydrocarbon feedthrough radially crossing the catalytic beds is brought into contact with the catalysts so as to produce a gaseous effluent; and said effluent is withdrawn after passing through the collection assembly. The conversion reaction may be selected from catalytic reforming, skeletal isomerization of olefins, metathesis for propylene production, oligocracking.
    [0004] DETAILED DESCRIPTION OF THE INVENTION The other features and advantages of the invention will appear on reading the following description, which is given solely by way of illustration and is not restrictive, and to which are appended: FIG. perspective view with a partial section of a radial flow and moving bed reactor according to the prior art; - Figure 2 is a sectional view along a plane parallel to the vertical axis of a reactor according to the invention; - Figure 3 is a sectional view along a plane parallel to the vertical axis of a reactor according to the invention; FIG. 4 is a detailed sectional view along a plane perpendicular to the vertical axis of a collection assembly according to the invention; - Figure 5 is a plan view of a cylindrical tube of a collection assembly according to the invention.
    [0005] Referring to Figure 1, a radial flow reactor 1 according to the prior art is externally in the form of a cylinder forming a cylindrical chamber 2 extending along a vertical axis of symmetry AX. The enclosure 2 comprises in its upper part a first orifice 3 and in its lower part a second orifice 4. The orifices 3 and 4 are intended respectively for the inlet and the outlet of a fluid passing through the reactor 1. It should be noted that the respective functions of the orifices 3 and 4 can be reversed, that is to say that the orifice 4 serves as a fluid inlet orifice and the orifice 3 is an outlet orifice of the reaction effluent. Inside this cylindrical reservoir is arranged a catalytic bed 7 having the shape of a vertical cylindrical ring limited on the inner side by a collection assembly 8 central retaining the catalyst and the outer side by a grid called "external" 5 either of the same type as the inner grid of the collection assembly 8, or by a device consisting of an assembly of shell-shaped grid members 6 extending longitudinally, as shown in FIG. 1. These grid elements 6-shaped shells forming ducts are also known by the English name of "scallops". These ducts 6 are held by the tank and generally plated on the inner face of the enclosure, parallel to the axis AX. The shell-shaped grid members 6 are in direct communication with the first port 3 via their upper end to receive a charge gas stream. The gas flow diffuses through the perforated wall of the ducts 6, 20 to cross the catalytic bed 7 by converging radially toward the center of the reactor 1. The charge is thus brought into contact with the catalyst in order to undergo chemical transformations, for example a catalytic reforming reaction, and produce an effluent from the reaction. The reaction effluent is then collected by the central collection assembly 8 which is in communication with the second port 4 of the reactor. The collection assembly 8 comprises a cylindrical grid 9 and a cylindrical tube 10 disposed in the space circumscribed by the cylindrical grid 9. The grid 9 which acts as a sieve is designed so as to be permeable to the gaseous fluid and impermeable to gases. catalyst particles. The cylindrical tube 10, permeable to the gaseous fluid is perforated and thus comprises through holes. In operation, the gaseous fluid introduced into the first orifice 3 is distributed over the height of the reactor and then passes radially through the "external" gate 5, then crosses radially through the catalytic bed 7 where it is brought into contact with the catalyst in order to produce an effluent which is subsequently collected by the assembly 8 and discharged through the second orifice 4. Such a so-called "moving bed radial" reactor operates with a continuous gravity flow of catalyst in the annular catalytic bed 7. The reactor 1 comprises and further means for introducing the catalyst 11 into the annular catalytic bed, arranged in an upper part of the reactor and catalyst withdrawal means 11 'which are arranged in a lower part of the reactor. It should be noted that a so-called "fixed bed radial" reactor does not generally comprise means for introducing catalyst 11 or means for withdrawing catalyst 11 '.
    [0006] A reactor according to the invention, according to a first embodiment, is shown in Figure 2 which is a sectional view along a plane parallel to the vertical axis of the reactor. The reactor 1 comprises a catalytic zone 12 which includes two catalytic beds 13, 14 of fixed bed type, annular, that is to say radial. The two fixed catalytic beds 13, 14 are stacked vertically one above the other and separated by a plate having the shape of a ring or any other means of separation. Alternatively, when the ratio of the average equivalent diameters of the catalysts composing two adjacent catalytic beds is less than a factor of 4, it is conceivable to stack the catalytic beds so that the upper catalytic bed is directly supported by the lower catalytic bed. In the context of the invention, a reactor can of course comprise a catalytic zone having N catalytic beds, with N being an integer greater than or equal to 2. The catalytic zone is of annular shape and is delimited by an external sieve 16 of cylindrical shape and an internal sieve 17 of cylindrical shape also placed at a distance from the outer screen 16. Preferably, the two sieves 16, 17 are arranged concentrically and centrally with respect to the casing 2 of the reactor 1. The reactor of FIG. 2 thus comprises three main spaces: a substantially external annular space 18 delimited by the casing 2 and the external cylindrical sieve 16 and a solid plate 21 arranged at the lower end of the annular space external 18 and secured to the lower ends of the outer sieve 16 and inner 17 and the envelope 2; a substantially annular space delimiting the catalytic zone 12, defined by the external cylindrical sieve 16 and internal sieve 17; a substantially cylindrical space 19 delimited by the internal cylindrical sieve 17 and a solid plate 20 disposed at the upper end of the space 19 and secured to the upper ends of the outer and inner sieves 16. In the example of FIG. 2, the internal sieve is a collection assembly according to the invention whose structure is detailed below with reference to FIGS. 4 and 5. Thus, the cylindrical space 19, delimited by the collection assembly, is a collection space 35 which is in communication with the discharge port 4 of the effluent.
    [0007] The reactor of FIG. 2 is configured to operate with a centripetal radial flow of gaseous fluid. In operation, the hydrocarbon feedstock is introduced into the reactor 1 via the orifice 3 located in the upper part of the casing 2 and is distributed in the outer annular space 18. The hydrocarbon feedstock passes through the sieve 5 external 16 and radially diffuses in the annular space 12 through the catalytic beds 13 and 14 and wherein it is contacted with the catalysts to produce an effluent. The effluent diffuses through the internal cylindrical sieve 17 (or collection assembly) and then confined in the collection space 19 from where it is discharged as a product outside the reactor through the orifice 4 located at the bottom of the reactor.
    [0008] According to the invention, the catalyst beds 13, 14 comprise a catalyst whose composition is different. For example, when the catalysts consist of a metal filler deposited on a support, the catalysts of the catalytic beds may have a support of different composition and / or have a different metallic composition and / or contain a different amount of metals and / or may have a different specific surface.
    [0009] Thus, with the reactor according to the invention, the hydrocarbon feedstock can be treated with two different catalysts in order to undergo different chemical transformations depending on the height of the catalytic zone. According to the invention, the catalytic zone can of course comprise N different catalysts with N greater than or equal to 2.
    [0010] Furthermore, according to the invention, the catalytic beds 13, 14 have a void fraction and / or a mean equivalent diameter of the catalyst particles which are different, ie the relative difference of the void ratios is at least 0.5%, preferably at least 1% and the relative difference of the average equivalent diameters is at least 5%, preferably at least 10%.
    [0011] According to an alternative embodiment of FIG. 2, the external sieve 16 may be replaced by a set of ducts (or "scallop" according to the English terminology) as mentioned above. FIG. 3 shows another embodiment of the reactor according to the invention which differs from that of FIG. 2 in the arrangement of the collection assembly. In the case presented, the external cylindrical sieve 16 is formed by the collection assembly. The reactor of Figure 3 is, as shown, configured to work with an upward flow of gaseous fluid and in a centrifugal radial direction (i.e. from the center to the periphery of the reactor). The hydrocarbon feed is thus sent through the bottom of the reactor via the orifice 4 35 and is distributed in the cylindrical space 19. The hydrocarbon feedstock then diffuses 3033264 8 through the annular space (or catalytic zone) By passing through the inner screen 17. During its radial passage in the annular zone 12, the hydrocarbon feedstock comes into contact with the fixed bed catalysts 13 and 14 to produce an effluent. The effluent diffuses through the outer cylindrical screen 16 (or collection assembly) and is then confined in the outer annular space 18 (collection space) from which it is discharged, as a product, out of the reactor. by the orifice 3 located at the top of the reactor 2. It is of course possible to decline the reactor according to the invention, so that it operates with a downward flow of the gaseous fluid and in a centrifugal radial direction (that is, ie from the center to the periphery of the reactor) or even with an upward radial flow of the gaseous fluid and in a centripetal radial direction (that is from the periphery to the center of the reactor). According to the invention, the reactor comprises a collection assembly of the effluent produced by the catalytic reaction which takes place within each fixed catalyst bed of the catalytic zone. The collection assembly 8 is configured and placed with respect to the catalytic beds so as to collect said gaseous effluent after the radial passage of the catalytic beds and includes N zones associated respectively with the N fixed catalytic beds. According to the invention, two adjacent zones have different porosities which are adapted to the void ratio and / or the average equivalent diameter of the catalyst of the fixed bed.
    [0012] In the context of the invention, the porosity of a zone is defined as being the ratio between the total permeable surface of said zone (i.e., the total area of the openings) and the total area developed by said zone. According to one embodiment, the collection assembly comprises a cylindrical grid acting as a sieve which is porous to the gas and impervious to catalysts of the catalytic beds and which comprises N zones associated respectively with the N fixed catalytic beds. For example, the grid is formed by an assembly of profiled metal wires arranged parallel to each other along the vertical axis and held together by a set of horizontal metal support rings welded to the vertical wires at any point in the vertical direction. contact with these. The arrangement of the vertical wires and the support rings define the openings of the grid. Thus the porosity of the grid areas can be controlled by varying the pitch between the vertical wires and the support rings. Alternatively, the grid can be obtained by assembling several grid elements of different porosities.
    [0013] According to another embodiment shown in FIG. 4, the collection assembly comprises a cylindrical grid of uniform porosity over its entire height, permeable to gas and impervious to catalyst catalysts and a porous cylindrical tube with gas which is supported by the cylindrical grid and arranged concentrically with respect to the grid. In this embodiment, the gas-porous cylindrical tube comprises N zones associated respectively with the N catalytic fixed beds and in which two adjacent zones have different porosities which are adapted to the void ratio and / or the average equivalent diameter of the catalyst of the bed. fixed. According to an alternative embodiment, the cylindrical tube 10 is made by assembling tubes of different porosity.
    [0014] FIG. 4 is a sectional view along a plane perpendicular to the vertical axis AX of the collection assembly 8, which details the configuration of a collection assembly 8. The grid 9 consists of a wire assembly shaped metal members 22 arranged parallel to each other along the vertical axis of the collection assembly. For example, the profile of the wires may be in V as shown in FIG. 4. However, the wires may have other shapes, such as for example having a circular cross-section. The vertical wires 22 have a first face 23 and a second opposite face 24. In the context of the invention, the first face 23 relates to the face which is in contact with the catalytic bed catalyst particles when the entire collection 8 is carried out in a radial reactor. The second face 24, which may be referred to as "back", corresponds to the face that is not in contact with the catalyst bed when the collection assembly is implemented in a radial reactor. The profiled wires 22 are held together by a set of horizontal metal support rings welded to the second face 24 of the vertical wires at any point of contact with the latter. The support rings 25 are preferably regularly arranged along the height 25 of the grid 9. Thanks to this arrangement of the vertical wires 22 and the support rings 25, the grid 9 has a perforated wall on its periphery. The arrangement of the wires 22 and the rings 25 is such that the openings formed are capable of allowing a gaseous fluid to diffuse while retaining the catalyst particles. The collection assembly 8 further comprises a cylindrical tube 10, pressed against said grid 30 9. Specifically, the tube 10 is secured, for example for welding or riveting, the "back" side of the profiled son 22 via the rings of support 25. As shown in FIGS. 2, 3 and 5, the cylindrical tube comprises two zones 26 and 27 with controlled porosity which are respectively associated with the catalytic beds 13 and 14 and whose height corresponds respectively to the heights of the catalytic beds 13 and 14 The cylindrical tube 3033264 can be obtained from a metal sheet which is wound or folded 360 °. According to an alternative embodiment, the cylindrical tube 10 is made by assembling tubes of different porosity. With reference to FIG. 5, the zones 26 and 27 of the cylindrical tube 10 comprise a plurality of through-holes 28 which allows the passage of the gaseous fluid which has diffused radially through the catalytic beds 13 and 14 and the grid 9. In the invention, the zones 26 and 27 of the cylindrical tube 10 have different porosities from each other. In the context of the invention, the porosity of a zone of the tube is defined by the ratio between the total permeable surface of said zone (i.e. the total surface of the holes) and the total surface area developed by said zone. For example, if an area has a total developed area of 1 m2 and has 50 through holes of 1.12 cm radius, the porosity of said area is equal to: P = (50 x (7t x (1, 12.10-2) 2)) / (1) = 0.02 The porosity of the different zones of the cylindrical tube which are respectively associated with the catalytic beds can be regulated by means of parameters such as the through-hole density (ie ie the number of holes per m2 of area developed by the area) or the size of the through holes. According to the invention, the through-holes may be distributed over the surface of the zone with a regular pitch between the holes and forming a regular network, for example in a triangle or a square. It should be noted that in the context of the invention, the through holes may have a section of any shape, for example circular, triangle, square or rectangle. The collection assembly according to the invention therefore has an evolutionary porosity which makes it possible to adjust the overall pressure drop at the level of the collection assembly as a function of the vacuum level of the catalytic beds and / or the equivalent mean diameter of the catalysts that make up the catalytic beds. The porosity of the collection assembly will be adapted to create an individual pressure drop at each zone associated with a catalytic bed which allows the gaseous charge to be distributed homogeneously over the total height of the catalytic zone in order to avoid formation. preferred paths for the gaseous fluid.
    [0015] In the context of the invention, the vacuum ratio of a catalytic bed can be determined by measuring the pressure drop across this bed by applying the Ergun relationship, connecting the pressure drop to the density of the catalyst. catalytic bed. The void ratio can also be determined by measurements of the catalyst mass contained in a predefined volume, it being expected that the density of the catalytic grain is known.
    [0016] The average equivalent diameter of a catalyst particle can be determined by those skilled in the art from particle size analyzes performed on an average sample of particles. According to the invention, the rules for constructing a collection assembly will thus take into account, in particular, the fact that the pressure drop experienced by a gaseous feed that passes through a catalytic bed is all the more important that the void rate of said bed is weak (all things being equal). Likewise, the load loss wiped off by the gaseous feedstock in the catalytic bed also depends on granulometric parameters, for example the mean equivalent diameter of the particles that make up the bed. Generally, at equivalent loading rate of a catalytic bed and all things being equal, the pressure drop in said bed is all the more important that the average equivalent diameter of the particles is small. The person skilled in the art will also take into account the type of implementation of the reactor in which the collection assembly is placed. Indeed, in the case where the gaseous fluid circulates in an upward and radial movement, it undergoes a greater pressure drop at the head of the reactor in the case where the pressure drop in the distribution area of the load is not negligible. On the contrary, in the situation where the gaseous fluid moves in a downward radial movement, the pressure drop undergone is more marked at the bottom of the reactor than at the top of the reactor. Thus, in order to guarantee a uniform overall pressure drop over the height of the catalytic beds, account must also be taken of the arrangement along the vertical axis of the fixed catalytic beds and the type of implementation of the reactor.
    [0017] Preferably the pressure drop will be adjusted at the collection assembly so as to ensure a minimum pressure drop to ensure a good distribution of the gas along the collection assembly. The pressure losses of the different zones of the collection assembly are generally adjusted between 10 and 200 mbar, preferably between 20 and 100 mbar.
    [0018] It should be noted that in the context of the invention, when the catalytic zone comprises more than two fixed beds, then two adjacent fixed beds comprise catalysts of different compositions and have a void ratio and / or an average equivalent diameter of different catalyst.
    [0019] For example, a catalytic bed according to the invention may comprise two types of catalysts A and B which are arranged in fixed beds alternately: ABAB. Alternatively, a catalytic bed may comprise N fixed beds, each comprising a different catalyst. (N different catalysts A, B, C, etc.) and take an ABC type configuration. EXAMPLE The reforming of an average density charge of 2.8 kg.rn-3 and an average viscosity of 0.015 cP is carried out in a reactor having an external grid of 2400 mm in diameter and a central collector of diameter 1200 mm. for a total height of 10m. In this reactor, two catalytic beds of 5 m height are loaded. The first catalytic bed consists of a catalyst in the form of beads with a diameter of 3.5 mm, with a dense loading characterized by a vacuum of 38%. The second catalytic bed 15 consists of a catalyst in the form of extrudates with an equivalent diameter of 2 mm, with a dense loading characterized by a vacuum of 40%. According to the prior art, initially, the cylindrical tube installed on the collection zone is unchanged (perforations of circular section 7 mm in diameter, with a triangular pitch of 50 mm). Simulations of the flow of charge in this reactor, with COMSOL Multiphysics® software, have shown, for a mean superficial charge entry speed of 0.4 ms-1 in a centripetal direction, that output of the catalytic beds were different: 0.774 ms-1 output of the first bed, 0.826 ms-1 output of the second bed, 6.8% relative difference.
    [0020] According to the invention, two adapted perforated tubes have been installed in front of the catalytic beds: the first and second tubes respectively have holes of circular section of 6.8 mm and 7.3 mm in diameter, which are arranged with a not triangular 50 mm. The unbalance of the output speeds is greatly reduced: 0.800 m.s-1 at the output of the first bed, 0.801 m.s-1 at the output of the second bed, or 0.1% relative difference. The use of a tube having areas of different porosity depending on the catalytic bed thus makes it possible to standardize the average velocity field between the two catalytic beds and consequently to limit the formation of preferential paths 35 for the fluid. gaseous at the level of the fixed catalytic beds.
    权利要求:
    Claims (11)
    [0001]
    REVENDICATIONS1. Reactor (1) with radial circulation of gaseous fluid, comprising: - an outer envelope (2) defining an enclosure extending along a vertical main axis comprising at least one catalytic zone (12) containing N fixed catalyst beds (26,27) arranged in a staggered manner along the vertical principal axis, N being an integer greater than or equal to 2, in which the catalysts of two adjacent fixed beds are of different compositions and in which two adjacent fixed beds have a void ratio and / or a mean equivalent diameter of the different catalyst; input means for a gaseous fluid; - Tapping means of a reaction effluent; - A vertical collection assembly (8) of the reaction effluent disposed adjacent to the catalytic zone; and wherein the collection assembly comprises N zones, each zone being associated with a fixed bed of the catalytic zone and in which at least two adjacent zones have different porosities which is a function of the void ratio and / or the average equivalent diameter catalyst of the fixed bed to create a homogeneous distribution of gaseous fluid velocities over the height of the catalytic zone and wherein at least two adjacent zones have different porosities.
    [0002]
    2. Reactor according to claim 1, wherein the collection assembly comprises a vertical cylindrical grid (9) permeable to gaseous fluid and impermeable to catalysts and the grid comprises N zones, each zone being associated with a fixed bed of the catalytic zone. and wherein at least two adjacent areas have different porosities.
    [0003]
    Reactor according to claim 1, wherein the collection assembly comprises a vertical cylindrical grid (9) permeable to gaseous fluid and impermeable to catalysts and a vertical cylindrical tube permeable to gas (10) supported by said grid (9) and disposed concentrically with respect to said grid (9) and the cylindrical tube (10) comprises N zones, each zone being associated with a fixed bed of the catalytic zone and in which at least two adjacent zones have different porosities which is function vacuum rate and / or average equivalent diameter of the catalyst of the fixed bed. 3033264 14
    [0004]
    4. Reactor according to claim 3, wherein each zone of the cylindrical tube has through holes (28) and wherein the number and / or dimension of the through holes are different from one area to another.
    [0005]
    Reactor according to one of claims 2 to 4, wherein the grid (9) is formed by a plurality of vertical wires (22) spaced from each other and secured to a plurality of horizontal support rings (25). ) and the cylindrical tube (10) is integral with the horizontal support rings (25).
    [0006]
    6. Reactor according to one of the preceding claims, wherein the catalytic zone is of annular shape defined by a cylindrical outer sieve (16) and a cylindrical inner sieve (17) placed at a distance from the outer sieve (16), the sieves being gas permeable and impervious to catalysts.
    [0007]
    7. Reactor according to claim 6, wherein the outer screen (16) is constituted by an assembly of shell-shaped ducts permeable to gaseous fluid and impermeable to catalysts. 15
    [0008]
    Reactor according to claim 6, wherein the outer sieve of the catalytic zone (12) is constituted by the collection assembly (8) and said reactor is configured to operate with the gaseous fluid flowing in an upward movement. or descending and in a centrifugal radial direction.
    [0009]
    The reactor of claim 6, wherein the inner screen (17) of the catalytic zone (12) is constituted by the collection assembly (8) and said reactor is configured to operate with the gaseous fluid flowing. in ascending or descending motion and in a centripetal radial direction.
    [0010]
    10. A process for converting a gaseous hydrocarbon feedstock using a reactor according to one of the preceding claims, comprising the following steps: - the gaseous hydrocarbon feedstock is continuously fed into a catalytic bed contained in the reactor; the hydrocarbon feedstock passing radially through the catalytic beds is brought into contact so as to produce a gaseous effluent; and said effluent is withdrawn after passing through the collection assembly.
    [0011]
    The process according to claim 10, wherein the conversion reaction is selected from catalytic reforming, skeletal isomerization of olefins, metathesis for propylene production, oligocracking.
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    EP3473335A1|2019-04-24|Removable basket for catalytic reactor
    FR2818559A1|2002-06-28|DEVICE FOR PROVIDING A SEPARATE INJECTION AND A HOMOGENEOUS DISTRIBUTION OF TWO FLUIDS
    FR3043575A1|2017-05-19|CATALYST REGENERATION ASSEMBLY
    FR3029429A1|2016-06-10|RADIAL BED REACTOR TO PERFORM LOW CATALYST QUANTITY
    同族专利:
    公开号 | 公开日
    FR3033264B1|2017-03-03|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP0218660B1|1985-04-16|1989-06-07|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Method and apparatus for the production of ozone|
    KR900000860B1|1985-04-26|1990-02-17|에어프로덕츠 앤드 케미칼스, 인코오포레이티드|Vertical type radical flow reactor and hydrocarbon treating operations using it|
    EP1818094A1|2006-02-13|2007-08-15|Ammonia Casale S.A.|Wall system for catalytic beds of synthesis reactors|
    FR2953738A1|2009-12-11|2011-06-17|Inst Francais Du Petrole|Unit for catalytic conversion of hydrocarbon fractions running in radial bed enclosed in annular region between outer cylindrical enclosure e.g. basket and inner cylindrical enclosure, where outer surface of basket comprises thread system|CN108018070A|2016-10-28|2018-05-11|中国石油化工股份有限公司|A kind of heavy oil feedstock fixed bed hydrogenation system|
    WO2020260029A1|2019-06-26|2020-12-30|IFP Energies Nouvelles|Reactor for the catalytic treatment of hydrocarbons with semi-continuous catalyst replacement|
    WO2021206916A1|2020-04-07|2021-10-14|Uop Llc|Processes for changing catalytic activity in a radial flow reforming reactor|
    法律状态:
    2016-03-08| PLFP| Fee payment|Year of fee payment: 2 |
    2016-09-09| PLSC| Search report ready|Effective date: 20160909 |
    2017-03-27| PLFP| Fee payment|Year of fee payment: 3 |
    2018-03-28| PLFP| Fee payment|Year of fee payment: 4 |
    2020-03-26| PLFP| Fee payment|Year of fee payment: 6 |
    2021-03-26| PLFP| Fee payment|Year of fee payment: 7 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1551833A|FR3033264B1|2015-03-05|2015-03-05|RADIAL REACTOR WITH FIXED CATALYTIC BEDS|FR1551833A| FR3033264B1|2015-03-05|2015-03-05|RADIAL REACTOR WITH FIXED CATALYTIC BEDS|
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