• 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 relates to a reactor (1) with a radial bed, comprising an enclosure provided with a reaction zone (10) moving bed of catalysts. The reactor further comprises inside the reaction zone (10): at least two distribution tubes (9) of the charge, each distribution tube (9) of the charge having a first end (11) in communication with the feed inlet means and a closed second end (12), the dispensing tubes (9) extending substantially vertically and are adapted to allow the feed to pass into the reaction zone (10) and retain the catalysts; and at least two collection tubes (13) of the effluent, each collection tube having a first end (14) in communication with the outlet means of the effluent and a second end (15) closed, the collector (13) extending substantially vertically and are designed to allow passage of the effluent into the collection tube (13) and retain the catalysts.
    公开号:FR3020968A1
    申请号:FR1454384
    申请日:2014-05-16
    公开日:2015-11-20
    发明作者:Frederic Bazer-Bachi；Fabrice Deleau；Alexandre Pagot
    申请人:IFP Energies Nouvelles IFPEN；
    IPC主号:
    专利说明:

    [0001] The present invention relates to the field of reactors for carrying out catalytic reactions in which the catalyst bed is mobile and in which there is a radial circulation of the charge to be treated from the periphery of the enclosure towards the center or from the center of the enclosure to its periphery. In the context of the invention, the term "radial" is used to describe the flow of reactants through a catalytic bed that is generally mobile in a set of directions corresponding to radii oriented from the periphery to the center or from the center to the periphery. . The present invention applies in particular to a radial flow of a reagent in gaseous form.
    [0002] STATE OF THE ART The unit most representative of this type of flow is a regenerative reforming unit of gasoline type hydrocarbon cuts that can be defined as having a distillation range of between 80 and 250 ° C. Some of these radial-bed units, including regenerative reforming, use a so-called moving bed catalyst flow, ie a slow gravitational flow of the catalyst particles confined in the annular enclosure bounded by an external grid and an inner wall (for example an inner grid) corresponding to the central collector which recovers the reaction effluents. The charge is generally introduced through the outer periphery of the annular bed and passes through the catalytic bed substantially perpendicular to the vertical direction of flow of the latter. The reaction effluents are then recovered in the central collector. The catalytic bed is thus limited on the inner side by an internal grid retaining the catalyst and on the outer side, either by another grid of the same type as the inner grid, or by a device consisting of an assembly of grid elements in the form of shells. The inner and outer grids are porous so as to allow the passage of the charge in the annular catalytic bed on the side of the outer grate, and the passage of the reaction effluents in the central collector on the inner grate side. In the state of the art, patent application FR 2948580 discloses a radial bed reactor in which the outer gate is replaced by a plurality of vertical distribution tubes immersed within the catalytic bed in the vicinity of the wall of the chamber. reactor. Such an assembly has a high mechanical strength which thus makes it possible to limit the buckling phenomena and thus to reduce the immobilization time of the reactor related to the repair and / or replacement of said grids.
    [0003] These reactors according to the prior art have a drawback related to the fact that a significant part of the volume is occupied by these internals (grid and central collector). In some cases, it may happen that the catalytic volume occupies only about 50% of the total volume of the enclosure.
    [0004] An object of the invention is to propose a novel concept of moving catalyst bed reactor with radial circulation for which the catalytic volume is optimized so as to improve the capacity of the reactor for the same useful volume of reactor, and therefore of to increase the charge rate that is likely to be treated in the reactor.
    [0005] SUMMARY OF THE INVENTION For this purpose, there is provided a reactor extending along a vertical axis, comprising: an enclosure provided with a moving bed catalyst catalyst; at least one inlet means for a charge situated above the reaction zone; at least one outlet means for an effluent produced by the catalytic reaction, located below the reaction zone; at least one catalyst inlet means capable of introducing the catalyst into an upper part of the reaction zone; at least one outlet means for the catalyst opening into a lower part of the reaction zone; The reactor further comprises within the reaction zone: at least two charge distribution tubes, each charge distribution tube having a first end in communication with the charge input means and a second closed end, the distribution pipes extending substantially vertically and are designed to allow the passage of the charge in the reaction zone and retain the catalysts; and at least two effluent collection tubes, each collection tube having a first end in communication with the outlet means of the effluent and a second closed end, the collection tubes extending substantially vertically and are designed to allow the passage of the effluent in the collection tube and retain the catalysts.
    [0006] The present invention thus relates to a catalytic conversion reactor with a radial diffusion of the gaseous and slow gravity flow of catalyst which includes a plurality of substantially vertical charge distribution tubes immersed within the catalytic bed and in wherein the central effluent collection tube is replaced by a plurality of substantially vertical effluent collection tubes immersed in the catalyst bed. The term "substantially vertical" means that the tubes may have an inclination of between 0 and 150 relative to the vertical central axis of the reactor.
    [0007] Such a reactor internal configuration indeed makes it possible to obtain a catalytic volume gain for the same useful volume of the given reactor, thus to increase the flow rate of the feedstock to be treated and consequently the capacity of the reactor to the iso-volume of the reactor. reactor. In other words, it is possible to envisage treating a same feed rate with a reactor according to the invention whose dimensions are smaller compared with those of a reactor of the prior art. Preferably, the number of charge distribution tubes is greater than or equal to four and the number of collection tubes of the effluent is greater than or equal to four.
    [0008] The field of application of the reactor according to the invention comprises the catalytic reforming of gasolines, the skeletal isomerization of various olefinic cuts at 04, 05, or the metathesis process for the production of propylene for example. This process list is not exhaustive and the present invention can be applied to any type of catalytic process with a radial flow of a gaseous charge.
    [0009] According to one embodiment, the feed inlet means comprises an inlet tube in communication with an orifice formed in the shell of the reactor. Preferably the outlet means of the effluent comprises at least one outlet tube in communication with an orifice formed in the shell of the reactor. According to a preferred embodiment, the catalyst inlet means and the catalyst discharge means comprise at least one tube open at the ends and in communication with an orifice formed in the shell of the reactor.
    [0010] In a preferred embodiment, the catalyst inlet means comprises a plurality of tubes, each in communication with an orifice formed in the reactor shell.
    [0011] In an advantageous embodiment from the point of view of robustness, the reactor comprises a first upper plate integral with the shell and the charge distribution tubes are supported by the first plate and each of the distribution tubes of the charge is in position. communicating with an orifice formed in said first tray. In this embodiment, preferably the catalyst inlet means comprises a plurality of tubes which are also supported by the first tray and each tube is in communication with an orifice formed in the first tray. For example, the first plate is of frustoconical and preferably frustoconical shape of inverted cone, that is to say that the apex of the cone is directed towards the second end of the reactor (the bottom of the reactor). The upper deck is further designed to be gas and catalyst tight.
    [0012] According to a preferred embodiment, the reactor further comprises a second lower plate integral with the calandria and the reaction zone is between the first and second trays. The collection tubes are supported by the second tray and each collection tube is in communication with an orifice formed in the second tray. The bottom plate is designed to be gas and catalyst tight. In this embodiment the catalyst outlet means may comprise a plurality of catalyst outlet tubes which are supported by the second tray and each of the catalyst outlet tubes is in communication with an orifice formed in the second tray and with a orifice formed in the shell.
    [0013] In a preferred embodiment, the first tray and the second tray are adapted to close the second ends of the effluent collecting tubes and the second ends of the feed distribution tubes, respectively.
    [0014] Advantageously, the distribution and / or collection tubes of the effluent are removably fixed in the reactor. According to one aspect of the invention, the distribution and collection tubes are arranged, in a plane perpendicular to the vertical axis, in a plurality of rows of tubes. In one embodiment, each tube line consists of either dispensing tubes or collection tubes and the tube lines are arranged such that a line of collection tubes is disposed adjacent to a line formed distribution tubes. According to another embodiment, each line of tubes alternately comprises a dispensing tube and a collection tube. When the tube network comprises lines of tubes, the tubes of two adjacent lines may be arranged vis-a-vis, i.e. in a so-called "square" pitch. Alternatively, when the tube network comprises lines of tubes, the tubes of two adjacent lines are shifted, i.e. in a so-called "triangular" pitch. According to an alternative embodiment, the dispensing and collecting tubes are arranged in a plane perpendicular to the vertical axis, forming a plurality of concentric rows and in which a row consisting of collection tubes is arranged in an adjacent manner. one row consisting of distribution tubes. According to another embodiment, the distribution and collection tubes are arranged, in a plane perpendicular to the vertical axis, in a plurality of concentric rows and each row of tubes comprises a plurality of distribution tubes and collection tubes. . According to an advantageous embodiment in terms of optimizing the use of the catalytic volume, a portion of the collection and / or distribution tubes are contiguous to the reactor shell. According to a particular embodiment, a part of the collection and / or distribution tubes is an integral part of the reactor shell. Collection and dispensing tubes may be of circular, ellipsoidal, lenticular or quadrilateral (e.g., square, rectangular or diamond) section. When the effluent collection or effluent collection tube is of circular section, it has a distribution or collection area of opening angle a. The distribution angle α or collection is generally between 30 ° and 360 °, and preferably between 1800 and 3600. When the section of the distribution pipes of the load and / or collection of the effluent is not circular in shape, the peripheral extent of the collection or distribution surface of the tubes is preferably at least 50% the total peripheral extent of the outer section of said tube. Preferably the distribution and collection area (or distribution or collection surface) respectively of the feed distribution and effluent collection tubes extends over most of the vertical length of the tube. By major part means a portion corresponding to at least 80% of the vertical length of the tube, and preferably at least 90% of said length.
    [0015] According to the invention, the number of charge distribution tubes and effluent collection tubes and their dimensions are determined so that the average pressure drop of the collection tubes is equal to ± 20%, preferably ± 10% of the average pressure drop of the distribution tubes.
    [0016] DETAILED DESCRIPTION OF THE INVENTION The other features and advantages of the invention will appear on reading the description which will follow, given solely by way of illustration and without limitation, and to which are appended: FIG. overall assembly including a partial section of a reactor according to the invention; - Figure 2 is a cross-sectional view along the vertical axis of the reactor of Figure 1; FIG. 3 is a cross-sectional view along the vertical axis of a reactor according to the invention; - Figure 4 is a sectional view along a plane perpendicular to the vertical axis of the reactor showing a tube network according to a first distribution mode; - Figure 5 is a sectional view along a plane perpendicular to the vertical axis of the reactor showing a tube network according to a second distribution mode; - Figure 6 is a sectional view along a plane perpendicular to the vertical axis of the reactor showing an array of tubes according to a third distribution mode; FIG. 7 is a distribution graph of the residence times for a reactor according to the prior art and according to the invention.
    [0017] Generally, identical elements are denoted by the same references in the figures. FIG. 1 shows a radial flow catalytic reactor 1 according to the invention which is in the form of a cylinder, formed by a shell 2, delimiting a cylindrical enclosure which extends along a substantially vertical axis of symmetry (AZ ). The shell 2 comprises in its upper part a first orifice 3 and in its lower part a second orifice 4 which are respectively input means of the feedstock to be treated and effluent outlet means produced by the catalytic reaction. The shell 10 2 delimits an enclosure which contains a reaction zone 10. The first and second orifices 3,4, located respectively above and below the reaction zone 10, are surrounded by a tubing 5,6 which thus allows connecting the shell to a fluid inlet and outlet piping system. As indicated in FIG. 1, the upper portion of the shell 2 is traversed by a plurality of catalyst introduction tubes (also called a leg) 7 which open into the upper part of the enclosure and into the reaction zone 10. The calender further comprises a plurality of exhaust tubes (or withdrawal) 8 of the catalyst disposed in the lower part of the enclosure. The catalyst evacuation (or withdrawal) tubes 8 are immersed in the bottom of the reaction zone 10 and open out to the reactor 1. The catalyst which is distributed in the reaction zone 10 is in the form of particles. for example spherical diameter generally between 1 to 5 mm. Of course, the catalyst may take other forms such as for example cylindrical granules. According to the present invention, the reactor 1 comprises a plurality of charge distribution tubes 9 which open into the reaction zone 10. The charge distribution tubes 9 extend in the reaction zone 10 in a substantially vertical direction, preferably substantially parallel to the axis of symmetry AZ, and at least 80% of the height of the reaction zone 10. The charge distribution tubes 9 are open at their first end 11 which is in communication with the first orifice upper 3 of the reactor shell. As for the second lower end 12, it is closed so as to prevent the passage of the load by the second end. The charge distribution tubes 9 are designed to be gas permeable and impervious to the catalyst. The charge distribution tubes 9, which may be considered as filtration devices permitting the passage of the gaseous feedstock in the reaction zone 10 and preventing the passage of the catalyst from the reaction zone 10 into the distribution tube, may occur. for example in the form of a tube provided with openings whose size is smaller than the size of the catalyst particles or in the form of a "Johnson" type grid known to those skilled in the art. With reference to FIG. 1, the reactor 1 according to the invention further comprises a plurality of effluent collection tubes 13 (product of the catalytic reaction) immersed in the reaction zone 10 and which extend in a substantially direction vertical, preferably substantially parallel to the axis of symmetry (AZ). The collection tubes of the effluent 13 are open at a first end 14 which is in communication with the second orifice 4 (outlet of the effluent) formed in the shell while the second end 15 opposite the first end 14 is closed. The collection tubes 13 of the effluent are designed to be permeable to the reaction products (reaction effluent) and impervious to the catalyst. The collection tubes, which can be viewed as filtration devices allowing passage of the effluent from the reaction zone 10 into the collection tube and preventing passage of the catalyst from the reaction zone 10 into the collection tube, can present for example in the form of a tube formed of a sheet and provided with openings whose size is smaller than the size of the catalyst particles or in the form of a grid of the type "Johnson" known from the skilled person.
    [0018] Figure 2 is an internal view of the reactor of Figure 1, showing in detail the upper and lower parts of the reactor. It can be observed in FIG. 2 that the upper part of the reactor 1 is provided with an upper plate 16 integral with the calender 2. Thus the reservoir is divided into two zones, namely: a zone of confinement of the charge 17 located at above the upper plate 16, between the shell 2 and the upper plate 16; and - a reaction zone 10 located below the upper plate 16 and extending to the bottom of the reactor.
    [0019] The upper plate 16 is made of a material impervious to the catalyst particles and also to the gases circulating in the confinement zone 17 and the reaction zone 10.
    [0020] As shown in FIG. 2, the distribution tubes of the load 9 are supported by the upper plate 16 and pass through it so that their first free open end 11 opens into the confinement zone of the load 17. It is also noted that the legs Catalyst introduction 7 are supported by the upper plate 16 and are arranged in such a way that their free open end opens into the upper part of the reaction zone 10 located under the upper plate 16. FIG. 2 also shows that the upper plate 16 comprises an inverted truncated cone portion 18 (ie the top of the cone is directed towards the bottom of the reactor) whose circular base 10 has a diameter smaller than that of the enclosure and a circular skirt 19 which provides the connection from the frustoconical portion 18 to the calender 2. The circular skirt 19 is of descending slope towards the bottom of the reactor 1. It is also noted that the base of the is connected to the circular skirt 19 by means of an annular flat which is traversed by the distribution tubes 7 of the catalyst, the open end of which opens into the reaction zone 10. As indicated in FIG. 2, the skirt 19, sectional view, also comprises an annular portion 24 extending along the vertical axis and connected to the flattened portion 20. As can be seen in FIG. 2, the upper part of the reaction zone 10 thus comprises a first cylindrical annular zone extended by a second annular zone of essentially frustoconical section of greater dimension than the first annular zone. The catalyst which is introduced by the distribution legs 7 passes into the first cylindrical annular section and is dispersed in the second frustoconical annular zone. In the context of the invention and alternatively, the skirt 19 can extend in a substantially horizontal plane, that is to say perpendicular to the vertical axis (AZ). Of course, the upper plate 16 may take other configurations such as, for example, a disc which includes openings through which the catalyst distribution tubes and the charge distribution tubes pass. Still with reference to FIG. 2, in the reaction zone 10 located under the upper plate 16, effluent collection tubes 13 are arranged. The collection tubes 13 comprise a first open bottom end 14 which is in communication with the outlet 4 of the effluent and a second upper end 15 closed. Advantageously from a standpoint of mechanical maintenance, the second end 15 is fixed integrally to the upper plate 16 and preferably removably to allow easy replacement of the tube. In the embodiment shown in FIG. 2, the lower end 14 of the collection tubes 13 is fixed to the shell 2 by means of a central tube 21 forming an integral part of the shell 2 and which extends into a lower part of the reaction zone 10. Advantageously, in order to facilitate the mounting of the collection tubes 13 to the calender, the lower part of the collection tubes 13 is bent so as to fit the convex lower portion of the shell 2 of the reactor 1. An alternative embodiment of a reactor according to the invention is shown schematically in Figure 3 which is a cross-sectional view along a plane parallel to the axis of symmetry (AZ) of the reactor 1.
    [0021] The reactor of Figure 3 comprises a first upper circular plate 16 and a second lower circular plate 22 integral with the calender 2. The second plate is made of a gas-tight material and catalyst. The reaction zone 10 in which the catalyst and the feed are confined is delimited by the volume of the enclosure comprised between the first and second trays 16, 22. In this embodiment, it will be noted that, advantageously, the second ends of the distribution tubes of the charge 9 and the collection tubes of the effluent 13 are closed respectively by the second plate 22 and by the first plate 16. Preferably said tubes are removably attached to said trays. The operating principle of the moving catalyst bed reactor according to the invention is now described with reference to FIG. 3. The gaseous hydrocarbon feedstock is sent into the reactor 1 through the upper orifice 3 via the feed pipe. injection 5 and fills the containment volume of the load 17 delimited by the calender and the upper plate 16. The charge is fed into the reaction zone 10 by means of the vertical distribution tubes 9 via the upper opening 11 opening into the zone The charge passes through the distribution tubes 9 and diffuses radially through the distribution tubes, permeable to gaseous fluid and impermeable to the catalyst particles, in the reaction zone 10. As for the catalyst, it is sent continuously in the reaction zone 10, via the tubes (or legs) for distributing the catalyst 7, the free end of which opens into the reaction zone 10, gravitarily at a relatively low speed (of the order of one meter per hour). The catalyst thus fills the reaction zone 10 and is moreover continuously withdrawn from the reaction zone 10 and discharged from the reactor via the catalyst outlet tubes (or legs) 8. The catalyst then distributes uniformly to occupying the volume of the reaction zone 10 comes into contact with the feedstock to carry out the catalytic conversion reaction and produce a reaction effluent. The reaction effluent is collected in the effluent collection tubes 13, permeable to the reaction effluent and impervious to the catalyst. As indicated by the arrows in solid lines in FIG. 3, the effluent diffuses radially through the collection tubes of the effluent 13 and is led through the lower plate 22 into a confinement space of the effluent 23 situated in below the lower plateau. The effluent is discharged from the reactor through the outlet of the effluent 4 through the outlet pipe 6 which is in communication with the confinement space 23 of the effluent.
    [0022] FIG. 4 illustrates a first exemplary mode of distribution of the collection tubes for the effluent 13 and the distribution of the charge 9 in the reactor. Referring to Figure 4, which is a sectional view along a plane perpendicular to the vertical axis of the reactor, the collection and distribution tubes are arranged in a network consisting of rows of tubes. In the example of FIG. 4, the network comprises a plurality of lines consisting of charge distribution tubes (E) and a plurality of lines consisting of collection tubes (S). A line consisting of collecting tubes is arranged with adjacent to a line of distribution tubes. FIG. 5 represents another mode of distribution of the effluent collection and charge distribution tubes in which the collection and distribution tubes are arranged forming a network of tube lines. The arrangement of Figure 5 is characterized in that each line of tubes alternately comprises a feed distribution tube (E) and an effluent collection tube (S).
    [0023] In the context of the invention and in the case where the tubes for collecting the effluent and for distributing the charge are distributed along lines, the tubes of two adjacent lines may be arranged either facing each other forming a square pitch, are offset by forming a triangular pitch as shown in Figure 4 or 5.
    [0024] According to another mode of distribution of the effluent collection tubes and the distribution of the charge represented in FIG. 6, the tubes are arranged on a plurality of approximately concentric rows alternately constituted by tubes for collecting the effluent (S). and charge distribution tubes (E). The term "approximately concentric" means that the centers of all the rows are contained in a circle centered on the center of the enclosure. It is also possible, in the case of a configuration in concentric rows of tubes, to successively alternate the effluent (S) and the load distribution tubes (E) in the same row of collection tubes. Preferably, when the charge distribution tubes and the effluent collection tubes are of circular section, they respectively have an angular diffusion sector and an angular collection sector whose opening angle a is generally understood. between 300 and 360 ° and preferably between 1800 and 3600. When the section of the feed distribution and / or effluent collection tubes is not circular in shape, the peripheral extent of the collection or distribution surface of the tubes is preferably at least 50 % of the total peripheral extent of the outer section of said tube. According to another particular characteristic of the present invention, the angular sector (or surface) of distribution and / or collection of the tubes is produced by means of a "Johnson" type grid. According to another embodiment, the sector (or surface) of distribution and / or collection of the tubes is achieved by means of orifices distributed in the wall of said sector, the diameter of the orifices being between 0.3 and 0.8 dp, dp denoting the minimum diameter of the catalyst grains. The term "minimum diameter" means the minimum distance measured between two opposite points taken from the catalyst. It should be noted that it is also possible to attach a portion of the tubes (effluent collection and / or load distribution) to the calender to maximize the useful catalytic volume of the reaction zone. According to another alternative, part of the tubes is an integral part of the calender. Still within the scope of the invention, the section of the tubes may be different from a circular section for example of square, rectangular, triangular or elliptical shape. In order to ensure a mechanical strength of the tubes, it is possible to further provide connecting means between the tubes, for example bars, secured to said tubes for example by welding. The support bars may advantageously be integral with the calender.
    [0025] By way of nonlimiting example, a reactor according to the invention has the following characteristics: - Internal diameter of the reaction zone between 1.5 and 6 m - internal diameter of the tubes between 0.1 and 0.6 m - Distance between two adjacent tubes between 0.2 and 0.9 m The number of charge distribution tubes and effluent collection tubes and their dimensions are determined so that the average loss of pressure of the tubes of collection is equal to ± 20%, preferably within ± 10%, of the average head loss of the distribution tubes. It is possible to add a pressure drop generating element, for example a perforated grid, on the distribution or collection tubes in order to guarantee uniform distribution of the fluid over the entire height of the tubes.
    [0026] EXAMPLE The example described below compares residence time distributions (DIS) by simulation in reactors according to the prior art and according to the invention. It is thus possible to obtain for each of the two reactors a distribution of the residence times, which can be characterized in particular by the average residence time of the feedstock in the reactor, a variable directly correlated with the conversion of the feedstock. The reactor "according to the prior art" has an internal diameter of 2.8 m. The enclosure comprises a catalytic bed in the form of a vertical cylindrical ring limited on the inside by an inner cylindrical grid retaining the catalyst and on the outer side by a cylindrical grid of the same type as the inner grid. After passing through the catalytic bed, the reaction effluents are collected in a vertical cylindrical collector through the inner retaining grid of the catalyst. The external grid diameter is 2.4 m and the internal grid diameter is 0.9 m. The grids have an effective height of 9 m.
    [0027] In the reactor according to the invention, the outer and inner grids are replaced by tubes of diameter 0.19 m with a triangular pitch between the tubes of 0.52 m. The diameter is the same for collection tubes and distribution tubes. This reactor comprises nineteen tubes located in the catalytic bed and one equivalent of 7 tubes contiguous to the shell.
    [0028] Six of the tubes located in the bed and all the tubes attached to the shell are injection tubes (equivalent to 13 tubes). The remaining tubes (13 remaining in the catalytic bed) are collection tubes. Finally, the internal diameter of the reactor is always equal to 2.8 m and the effective height of the tubes is 9 m.
    [0029] For the simulation with the reactor according to the prior art, the nominal flow rate of the gaseous feedstock passing through the reactor is 120 t / h and assuming that the density of the feedstock is on average 1.8 kg / m 3 and with a viscosity of 2.10-5 Pa.s. The catalyst is assumed to be in the form of 2 mm diameter grain and with a grain void ratio of 41%. The same data are used for the simulation of the reactor according to the invention, with the exception of the charge flow rate which is increased by 38%. For each of the two reactors, the residence time distributions are obtained numerically with the COMSOL Multiphysics 4.2a software. The charge is sent to the reactor at time t = 0 and the charge rate is then maintained in time.
    [0030] The simulations show that the average pressure losses in the distribution tubes (10 mBar) and in the collection tubes (9 mBar) are indeed very close (difference of 10%).
    [0031] The DIS simulations also show that the average residence time of the feedstock in the reactor according to the prior art and according to the invention for which the nominal flow rate of the feed has been increased by 38% is identical (FIG. 7). In other words, for the same reactor size, the reactor according to the invention makes it possible to pass a charge flow increased by 38%, at iso conversion of the charge (same residence time). Thus, thanks to the reactor concept according to the invention it is possible to increase the reactor isovolume charge flow rate and thus to improve the productivity of the reactor.
    权利要求:
    Claims (16)
    [0001]
    REVENDICATIONS1. Reactor (1) extending along a vertical axis, comprising: - an enclosure provided with a moving bed catalyst bed (10); at least one inlet means of a charge situated above the reaction zone (10); at least one outlet means of an effluent produced by the catalytic reaction, situated below the reaction zone (10); at least one inlet means (7) for the catalyst capable of introducing the catalyst into an upper part of the reaction zone (10); at least one outlet means (8) for the catalyst opening into a lower part of the reaction zone (10); the reactor comprising inside the reaction zone (10): at least two distribution tubes (9) of the charge, each distribution tube (9) of the charge having a first end (11) in communication with the feed inlet means and a closed second end (12), the dispensing tubes (9) extending substantially vertically and are adapted to allow the load to pass into the reaction zone (10) and retain the catalysts; and at least two collection tubes (13) of the effluent, each collection tube having a first end (14) in communication with the outlet means of the effluent and a second end (15) closed, the collector (13) extending substantially vertically and are designed to allow passage of the effluent into the collection tube (13) and retain the catalysts.
    [0002]
    2. Reactor according to claim 1, wherein the reactor (1) is formed of a calender (2) and the feed inlet means comprises an inlet tube (5) in communication with an orifice (3). formed in the shell (2).
    [0003]
    3. Reactor according to claims 1 or 2, wherein the reactor (1) is formed of a calender (2) and the outlet means of an effluent comprises an outlet tube (6) in communication with an orifice (4). ) formed in the shell (2).
    [0004]
    4. Reactor according to one of the preceding claims, wherein the reactor (1) is formed of a calender (2) and wherein the inlet means (7) of the catalyst and the outlet means (8) of the catalyst comprise at least one tube open at the ends and said tube (7,8) is in communication with an orifice formed in the shell (2).
    [0005]
    5. Reactor according to one of the preceding claims, wherein the reactor (1) is formed of a calender (2) and comprises a first upper plate (16) integral with the calender (2) and wherein the distribution tubes of the charge (9) are supported by the first plate (16) and each of the distribution tubes (9) of the charge and the catalyst inlet means (7) are respectively in communication with an orifice formed in the first plate higher (16).
    [0006]
    6. Reactor according to claim 5, wherein the first upper plate (16) is of frustoconical shape.
    [0007]
    7. Reactor according to one of claims 5 to 6, wherein the reactor further comprises a second lower plate (23) integral with the calender (2) and the reaction zone (10) being defined between the first and second trays and wherein the collection tubes (13) of the effluent are supported by the second lower plate (23) and each collection tubes (13) of the effluent and outlet means (8) of the catalyst are in communication with a orifice formed in the second lower plate (23).
    [0008]
    8. The reactor of claim 7, wherein the first upper plate (16) and the second lower plate (23) respectively seal the second ends (15) of the collection tubes (13) of the effluent and the second ends (12). ) distribution tubes (9) of the load.
    [0009]
    9. Reactor according to one of the preceding claims, wherein the distribution tubes (9) and collection (13) are arranged in a plane perpendicular to the vertical axis, in a plurality of rows of tubes, wherein each tube line consists of charge distribution tubes or effluent collection tubes in which a line consisting of effluent collection tubes (13) is disposed adjacent to a line of distribution tubes the load (9).
    [0010]
    10. Reactor according to one of claims 1 to 8, wherein the distribution tubes (9) and collection (13) are arranged in a plane perpendicular to the vertical axis, in a plurality of rows of tubes, in wherein each line of tubes alternately comprises a charge distribution tube (9) and an effluent collection tube (13).
    [0011]
    11. Reactor according to claims 9 or 10, wherein the tubes of two adjacent lines are arranged vis-à-vis forming a square pitch.
    [0012]
    12. Reactor according to claims 9 or 10, wherein the tubes of two adjacent lines are arranged in a staggered manner forming a triangular pitch. 15
    [0013]
    13. Reactor according to one of claims 1 to 8, wherein the distribution tubes (9) and collection (13) are arranged in a plane perpendicular to the vertical axis, on a plurality of concentric rows of tubes and wherein a row of effluent collection tubes (13) is disposed adjacent to a row of charge distribution tubes.
    [0014]
    14. Reactor according to one of claims 1 to 8, wherein the distribution tubes (9) and collection (13) are arranged in a plane perpendicular to the vertical axis, in a plurality of concentric rows of tubes and wherein each row of tubes comprises distribution tubes (9) and collection tubes (13).
    [0015]
    15. Reactor according to one of the preceding claims, wherein the distribution tubes and / or collection (9, 13) are contiguous to the calender (2) of the reactor. 30
    [0016]
    16. Reactor according to one of the preceding claims, wherein the collection tubes (13) and distribution (9) are circular, ellipsoidal or lenticular section or quadrilateral.
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    同族专利:
    公开号 | 公开日
    KR102356416B1|2022-01-26|
    US9486767B2|2016-11-08|
    CN105080435A|2015-11-25|
    KR20150132021A|2015-11-25|
    TW201603881A|2016-02-01|
    BR102015010744B1|2020-11-03|
    TWI652111B|2019-03-01|
    BR102015010744A2|2015-12-29|
    FR3020968B1|2016-05-13|
    CN105080435B|2019-07-12|
    US20150328612A1|2015-11-19|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EP0693312A1|1994-07-22|1996-01-24|Institut Français du Pétrole|Improvement in moving bed enclosures|
    FR2948580A1|2009-07-29|2011-02-04|Inst Francais Du Petrole|DEVICE FOR DISTRIBUTING THE LOAD AND RECOVERING EFFLUENTS IN A RADIAL BED CATALYTIC REACTOR|
    FR2966751A1|2010-10-28|2012-05-04|IFP Energies Nouvelles|Radial bed reactor for regenerative reforming of species, skeletal isomerization, metathesis and oligocracking, comprises external cylindrical grid and coaxial internal cylindrical grid defining annular space containing catalyst bed|FR3060413A1|2016-12-15|2018-06-22|IFP Energies Nouvelles|METHOD FOR HYDROTREATING HEAVY LOADS IN MULTITUBULAR RADIAL REACTOR|
    CN111068590A|2018-10-22|2020-04-28|中国石油化工股份有限公司|Solid acid alkylation method|US2108087A|1935-11-09|1938-02-15|Houdry Process Corp|Apparatus for contact treatment of materials|
    US2893950A|1956-06-29|1959-07-07|Phillips Petroleum Co|Method and apparatus for feeding fluid reactants to a moving bed of solid contact particles|
    US5759242A|1996-07-23|1998-06-02|Praxair Technology, Inc.|Radial bed vaccum/pressure swing adsorber vessel|
    CA2451618A1|2001-06-25|2003-01-03|Jott Australia Pty Ltd|Fluid/solid interaction apparatus|
    JP4477432B2|2004-06-29|2010-06-09|東洋エンジニアリング株式会社|Reformer|
    FR2914395B1|2007-03-30|2009-11-20|Inst Francais Du Petrole|NEW COMPACT EXCHANGER REACTOR USING A POROUS BURNER|
    CN101279877B|2007-04-04|2011-07-20|中国石油化工股份有限公司|Method for increasing yield of ethylene and propone in conversion process of oxocompound|
    CN201186210Y|2008-07-22|2009-01-28|吕仲明|Vertical type water-cooling tube box type reactor|
    US8313561B2|2010-10-05|2012-11-20|Praxair Technology, Inc.|Radial bed vessels having uniform flow distribution|
    CN202570115U|2012-03-19|2012-12-05|南京天华化学工程有限公司|Radial reactor for moving bed|FR3054028B1|2016-07-15|2018-07-27|IFP Energies Nouvelles|CONTAINER OF A HEAT STORAGE AND RESTITUTION SYSTEM COMPRISING A DOUBLE CONCRETE WALL|
    CN107983270B|2016-10-27|2021-01-08|中国石油化工股份有限公司|Moving bed reactor, solid acid alkylation reaction system and solid acid alkylation reaction method|
    US10478794B1|2019-02-26|2019-11-19|Chevron Phillips Chemical Company Lp|Bi-modal radial flow reactor|
    CN111113677B|2020-01-04|2021-08-03|永丰上达建材实业有限公司|High-precision quantitative reaction system for A material and B material for concrete preparation|
    CN112023838A|2020-08-31|2020-12-04|江苏永大化工机械有限公司|Synthetic reactor for producing ethylene glycol from coal|
    法律状态:
    2015-04-29| PLFP| Fee payment|Year of fee payment: 2 |
    2015-11-20| PLSC| Publication of the preliminary search report|Effective date: 20151120 |
    2016-05-18| PLFP| Fee payment|Year of fee payment: 3 |
    2017-05-19| PLFP| Fee payment|Year of fee payment: 4 |
    2018-05-30| PLFP| Fee payment|Year of fee payment: 5 |
    2019-05-28| PLFP| Fee payment|Year of fee payment: 6 |
    2020-05-27| PLFP| Fee payment|Year of fee payment: 7 |
    2021-05-26| PLFP| Fee payment|Year of fee payment: 8 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1454384A|FR3020968B1|2014-05-16|2014-05-16|MULTITUBULAR RADIAL BED REACTOR|FR1454384A| FR3020968B1|2014-05-16|2014-05-16|MULTITUBULAR RADIAL BED REACTOR|
    BR102015010744-7A| BR102015010744B1|2014-05-16|2015-05-12|multitubular radial bed reactor|
    TW104115305A| TWI652111B|2014-05-16|2015-05-13|Multi-tube radial bed reactor|
    CN201510247588.5A| CN105080435B|2014-05-16|2015-05-15|Multitube radial bed reactor|
    KR1020150068030A| KR102356416B1|2014-05-16|2015-05-15|Multi-tube radial bed reactor|
    US14/712,965| US9486767B2|2014-05-16|2015-05-15|Multi-tube radial bed reactor|
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