Gas-solid co-current downflow fluidised bed reactor with homogeneous flow

Abstract

The invention relates to a device and a process for gas-solid co-current downflow fluidised bed catalytic cracking comprising / using: a pipeline (1) suitable for carrying a downflow (4) of catalyst particles; a mixing chamber (2) connected to the pipeline (1) and suitable for being fed by the pipeline with a downflow, the mixing chamber comprising an inner wall and at least one first injector (5) of hydrocarbon feed (6); a gas-solid co-current downflow fluidised bed reactor (3) connected to the mixing chamber and suitable for being fed by the mixing chamber with a mixture comprising catalyst particles and hydrocarbon feed, the downflow gas-solid co-current fluidised bed reactor comprising an inner wall, wherein the inner wall of the mixing chamber and / or of the downflow gas-solid co-current fluidised bed reactor comprises one or more obstacles (9).

Description

[0001] Homogeneous downward flow gas-solid cocurrent fluidized bed reactor.

[0002] Technical field

[0003] The invention relates to the field of refining and petrochemistry and to processes and units for the chemical transformation of petroleum products, in particular hydrocarbon cuts, by Fluid Catalytic Cracking (FCC) for the production of light olefins (i.e., olefins comprising between 2 and 4 carbon atoms), and more particularly ethylene and propylene, and also aromatics (e.g. BTX), and more particularly paraxylene.

[0004] Prior art

[0005] The invention is part of the improvement of the design of the established flow zone of downward gas-solid co-current fluidized bed reactors ("downer" or "down flow reactor" according to English terminology), hereinafter called downward flow reactors, used for example for high severity catalytic cracking (HS-FCC).

[0006] Ethylene, Propylene, Butene, Butadiene and aromatics such as Benzene, Toluene and Xylene (BTX) represent the basic products for the petrochemical industry. These products are generally obtained by catalytic reforming and / or thermal cracking (steam cracking) of hydrocarbons such as naphtha, kerosene or diesel. These compounds are also obtained by fluidized catalytic cracking (FCC) of hydrocarbons, such as a Vacuum Gas Oil (VGO) and / or a residue (under vacuum or atmospheric) from the distillation of hydrocarbons and / or naphtha, diesel, and complete crudes.

[0007] The high severity catalytic cracking (HS-FCC) process aims to increase propylene and ethylene yields through high temperature reaction conditions, very short contact times (eg ~1 s), high ratios between the mass flow rate C of catalyst and the mass flow rate O of feedstock (C / O).

[0008] The disadvantages associated with a conventional FCC reactor with a rising gas-solid co-current fluidized bed (riser) such as back-mixing and catalyst accumulation near the wall, resulting in overcracking of hydrocarbons and excessive formation of coke, hydrogen, methane and ethane, do not allow the production of olefins to be promoted under high severity conditions. i In order to overcome these disadvantages, the HS-FCC process uses a downward flow reactor, where the catalyst and feedstock are set in motion under the effect of gravity with a flow approaching that of a plug flow. The downward gas-solid flow in a reactor avoids back-mixing and overcracking of the products, while the use of high C / O ratios ensures the predominance of catalytic reactions.High temperature favors the formation of reaction intermediates such as light olefins while a controlled and short contact time avoids side reactions which are responsible for the consumption of such intermediates.

[0009] On the other hand, downward gas-solid flow presents several major technological challenges, one of which is the flow and mixing in the steady-flow section of the reactor. Indeed, the catalyst flow in a downward flow reactor, especially at high solid mass fluxes (e.g., between 400-800 kg / m 2s), is characterized by a flat solid concentration profile in the central zone and an annular zone in the vicinity of the wall where the particle concentration and flux are higher. This segregation is the result of low gas velocity conditions at the wall (no-slip condition) which produces a low drag force on the particles resulting in agglomeration phenomena ("clustering" according to English terminology) between the particles. This phenomenon is well described in the literature (Zhu et al., The Canadian Journal of Chemical Engineering, Volume 73 (1995), pp. 662-677; Sun et al., Powder Technology, Vol. 370 (2020), pp. 184-196). On the other hand, this segregation leads to a lower catalyst concentration in the center of the reactor, thus reducing the reaction rates and the overall performance obtained at the reactor outlet.

[0010] Patent FR 2 753 453 B1 describes a downward flow cracking reactor comprising a contact zone between the hydrocarbons and the catalyst, consisting of: a mixing chamber of maximum section S2, placed in communication with means for supplying regenerated catalyst via an upper orifice defining a catalyst passage section S1; and a reaction zone of maximum section S4, placed in communication with the mixing chamber via an intermediate orifice of section S3, reactor in which the ratios S2 / S1 and S2 / S3 are between 1.5 and 8.

[0011] US Patents 10,889,768 B2 and US Patents 10,767,117 B2 describe systems and methods for producing petrochemical products (e.g. ethylene and other olefins), from hydrocarbon feedstocks (e.g. crude oil), in high severity fluid catalytic cracking (HS-FCC) units.

[0012] US Patent Application 2022 / 0016589 A1 describes a downflow reactor comprising annular distribution and mixing baffles. Summary of the Invention

[0013] In the context described above, a first object of the present invention is to overcome the problems of the prior art and to provide a device for fluidized bed catalytic cracking with descending gas-solid cocurrent with homogeneous catalyst flow, i.e., in which the solid concentration in the cross-section of the reactor is substantially uniform. Indeed, the device according to the invention makes it possible to obtain a homogeneous catalyst concentration between the central zone and the annular zone (i.e., in the proximity of the wall) of the descending gas-solid cocurrent reactor.

[0014] A second object of the present invention is to provide a device for downward gas-solid co-current fluidized bed catalytic cracking in which the solid concentration is increased in charge injection zones of the mixing chamber.

[0015] According to a first aspect, the aforementioned objects, as well as other advantages, are obtained by a device for catalytic cracking in a descending gas-solid co-current fluidized bed comprising, from top to bottom: a pipe adapted to transport a descending flow of catalyst particles; a mixing chamber connected to the pipe and adapted to be supplied by the pipe in a descending flow, the mixing chamber comprising an inner wall and at least one first hydrocarbon feed injector; a descending gas-solid co-current fluidized bed reactor connected to the mixing chamber and adapted to be supplied by the mixing chamber with a mixture comprising catalyst particles and hydrocarbon feed, the descending gas-solid co-current fluidized bed reactor comprising an inner wall;wherein the inner wall of the mixing chamber and / or the descending gas-solid co-current fluidized bed reactor comprises one or more discontinuous obstacles.;

[0016] Advantageously, the plurality of obstacles is adapted to homogenize the concentration of catalyst particles. Advantageously, the obstacles are adapted to deflect (the trajectory) of the catalyst particles towards the interior of the mixing chamber and / or the descending gas-solid co-current fluidized bed reactor, and / or towards the feed injection zones (i.e., near the first hydrocarbon feed injector).

[0017] According to one or more embodiments, the obstacles are adapted to distribute catalyst particles substantially towards the interior of the mixing chamber and / or the descending gas-solid co-current fluidized bed reactor. According to one or more embodiments, the obstacles comprise an upper surface that is oblique and descends inwardly, i.e., towards the center of the reactor.

[0018] According to one or more embodiments, the obstacles are adapted to prevent the accumulation of catalyst particles on the obstacles.

[0019] According to one or more embodiments, the obstacles are adapted to distribute catalyst particles along the wall of the mixing chamber.

[0020] According to one or more embodiments, the obstacles comprise a laterally descending, oblique upper surface.

[0021] According to one or more embodiments, the obstacles are in the shape of a prism, cylinder, pyramid, cone, and / or truncated cone.

[0022] According to one or more embodiments, obstacles are arranged in the mixing chamber upstream of the at least one first injector.

[0023] According to one or more embodiments, obstacles are arranged in the downflow reactor at an axial distance Hi from the mixing chamber of between 0*L and 0.9*L, L being the length of the downflow gas-solid co-current fluidized bed reactor.

[0024] According to one or more embodiments, the device comprises at least one row of obstacles arranged at a predetermined height from the inner wall of the mixing chamber and / or the downflow reactor.

[0025] According to one or more embodiments, the perimeter of the internal wall of the mixing chamber and / or the downflow reactor, occupied by the row of obstacles, is between 15% and 80%.

[0026] According to one or more embodiments, the row of obstacles reduces the passage section of the internal wall of the mixing chamber and / or the downflow reactor by 1% to 35% and preferably by 5% to 20%.

[0027] According to one or more embodiments, the row of obstacles in the mixing chamber comprises between 2 and 24 obstacles, and / or the row of obstacles in the downflow reactor comprises between 2 and 24 obstacles.

[0028] According to one or more embodiments, the radial position of the obstacles of an obstacle row is in a separation space between the radial position of two adjacent obstacles of an adjacent obstacle row. According to a second aspect, the aforementioned objects, as well as other advantages, are obtained by a method for downward gas-solid co-current fluidized bed catalytic cracking comprising the following steps: transporting a downward flow of catalyst particles in a conduit; feeding a mixing chamber through the conduit with the downward flow, the mixing chamber comprising an inner wall and at least one first hydrocarbon feed injector; feeding a downward gas-solid co-current fluidized bed reactor through the mixing chamber with a mixture comprising catalyst particles and hydrocarbon feed, the downward gas-solid co-current fluidized bed reactor comprising an inner wall;and at least partially cracking the hydrocarbon feedstock in the presence of the catalyst particles in the descending gas-solid co-current fluidized bed reactor, to produce an effluent comprising at least partially coked catalyst and gaseous cracking products, wherein the inner wall of the mixing chamber and / or the descending gas-solid co-current fluidized bed reactor comprises a plurality of obstacles.;

[0029] Other characteristics and advantages of the invention of the aforementioned aspects will appear on reading the description below and non-limiting examples of embodiments, with reference to the figures appended and described below.

[0030] List of figures

[0031] Figure 1 shows an FCC device according to one or more embodiments of the present invention comprising obstacles for homogenization of the catalyst flow.

[0032] Figure 2 shows 3D views of an FCC device according to one or more embodiments of the present invention comprising a plurality of rows of obstacles for homogenizing the catalyst flow.

[0033] Figure 3 shows 3D views of a diagram A of a reference FCC device, and a diagram B of an FCC device according to one or more embodiments of the present invention comprising three rows of the obstacles.

[0034] Figure 4 shows 3D views of diagrams A and B of the time-averaged catalyst volume fraction in the reference FCC device of Figure 3, and in the inventive FCC device of Figure 3, respectively. Figure 5 shows the radial profiles A and B of the solid fraction and the solid mass flux at 2.8 m below the injectors of the reference FCC device of Figure 3, and the inventive FCC device of Figure 3, respectively.

[0035] Detailed description of the invention

[0036] Embodiments according to the foregoing aspects will now be described in detail. In the following detailed description, numerous specific details are set forth in order to provide a more thorough understanding of the device and method according to the present invention. However, it will be apparent to those skilled in the art that the device may be implemented without these specific details. In other instances, well-known features have not been described in detail to avoid unnecessarily complicating the description.

[0037] In this specification, the term "comprise" is synonymous with (means the same as) "comprise", "include" and "contain", and is inclusive or open and does not exclude other elements not recited. It is understood that the term "comprise" includes the exclusive and closed term "consist". Furthermore, in this specification, the terms "essentially" or "substantially" or "about" correspond to an approximation of ± 10%, preferably ± 5%, very preferably ± 1%.

[0038] The invention relates to a fluidized bed catalytic cracking device and method for the chemical transformation of petroleum products (FCC), used for example for high severity catalytic cracking (HS-FCC).

[0039] An FCC unit typically processes a heavy cut from the vacuum distillation unit such as vacuum gas oil or vacuum residue, or atmospheric residue, alone or in a mixture. An FCC unit can also process lighter cuts such as gasoline or diesel cuts, alone or in a mixture. It is also possible to process a mixture of light and heavy cuts, or a complete crude. In order to increase propylene and ethylene yields by using high-severity reaction conditions (high temperature, very short contact times, high C / O ratios between the catalyst flow C and the feed O flow), catalytic cracking devices and processes typically use a downflow reactor (hereinafter referred to as a downflow reactor).

[0040] However, downward gas-solid flow presents several technological challenges, including achieving homogeneous flow and mixing in the established flow section of the downflow reactor. In order to overcome these drawbacks, improvements to the downflow reactor technology described in patent FR 2 753 453 B1 have been identified, to address the challenge presented above through the use of obstacles that can be inserted into the mixing chamber or downstream of the mixing chamber, i.e., in the downflow reactor.

[0041] The device according to the invention

[0042] Referring to Figure 1, the device according to one or more embodiments of the present invention comprises from top to bottom: a conduit 1; a mixing chamber 2; and a downflow reactor 3.

[0043] Line 1 is adapted to supply mixing chamber 2 with solid catalyst (particles). Line 1 mainly transports solid, as well as a fluidization gas entrained by the descending solid. Line 1 has a flow like a feed column ("standpipe" according to English terminology) well known to those skilled in the art.

[0044] The mixing chamber 2 connected to the pipe 1, comprises a side / vertical wall defining a central / vertical axis Z, and is adapted to feed the downflow reactor 3 with a mixture comprising catalyst particles, a hydrocarbon feedstock and optionally a diluent.

[0045] The downflow reactor 3 is connected to the mixing chamber 2 and is adapted to at least partially crack the hydrocarbon feedstock in the presence of the catalyst particles to produce an effluent comprising at least partially coked catalyst and gaseous cracking products, and optionally unconverted vaporized feedstock.

[0046] Specifically, with reference to Figure 1, the pipe 1 supplies the mixing chamber 2 with a descending flow 4 of (hot) catalyst particles, the mixing chamber 2 comprising one or more first injectors 5 of hydrocarbon feedstock 6. According to one or more embodiments, the first injector(s) 5 is adapted to inject diluent (e.g. water vapor) with the feedstock. According to one or more embodiments, the mixing chamber 2 comprises one or more second injectors 7 of diluent 8. In the mixing chamber 2, the descending flow 4 comes into contact with the hydrocarbon feedstock 6 atomized using the first injector(s) 5 and optionally with diluent 8, introduced for example by the second injector(s) 7. Advantageously, the injection of diluent 8 makes it possible to reduce the partial pressure of the hydrocarbon feedstock and to reduce secondary reactions.Advantageously, the injection of diluent 8 makes it possible to improve the atomization of the hydrocarbon feedstock 6. According to one or more embodiments, the diluent 8 is chosen from the group consisting of water vapor, nitrogen, CO2, light hydrocarbons (e.g. C1-C5 compounds), combustion fumes. According to one or more embodiments, the diluent 8 comprises or consists of water vapor.

[0047] According to one or more embodiments, the pipe 1 is of constant cross-section geometry, such as cylindrical, square, rectangular or hexagonal, or of variable cross-section, such as a truncated pyramid or cone, or a combination of the different geometric shapes. According to one or more embodiments, the pipe 1 is of cylindrical shape and optionally of variable diameter. According to one or more embodiments, the pipe 1 is of at least partially frustoconical shape. According to one or more embodiments, the pipe 1 comprises (in the direction of flow of the solid catalyst): a cylindrical section, for example the diameter of which is chosen to obtain a solid flow of 100 to 800 kg / (m 2 s) and preferably between 300 and 600 kg / (m 2s); a truncated section (called a narrowing section) adjacent to the mixing chamber 2, the diameter of which decreases, for example in order to achieve a solid flow, without taking into account the internals, between 400 and 2000 kg / (m 2 s) and preferably between 700 and 1500 kg / (m 2 s); and optionally a second cylindrical section, for example whose diameter is chosen to obtain a solid flow, without taking into account the internals, between 400 and 2000 kg / (m 2 s) and preferably between 700 and 1500 kg / (m 2 s).

[0048] According to one or more embodiments, the mixing chamber 2 is of constant cross-section geometry, such as cylindrical, square, rectangular or hexagonal, or of variable cross-section, such as a truncated pyramid or cone, or a combination of the different geometric shapes. According to one or more embodiments, the mixing chamber 2 is of cylindrical shape and optionally of variable diameter. According to one or more embodiments, the mixing chamber 2 is of at least partially frustoconical shape. According to one or more embodiments, the mixing chamber 2 comprises an upper limit of cross-section S1 connecting the mixing chamber 2 to the pipe 1 and a lower limit of cross-section S2 connecting the mixing chamber 2 to the downflow reactor 3, the ratio S1 / S2 being less than 0.9 and preferably less than 0.7. According to one or more embodiments, the ratio S1 / S2 is between 0.4 and 0.9, preferably between 0.5 and 0.7.

[0049] According to one or more embodiments, the mixing chamber 2 comprises between 2 and 12 first injectors 5, preferably between 3 and 8 first injectors 5.

[0050] According to one or more embodiments, the mixing chamber 2 comprises between 2 and 12 second injectors 7, preferably between 3 and 8 second injectors 7. According to one or more embodiments, the injectors 5 and / or 7 are inclined upwards or downwards or are substantially arranged horizontally.

[0051] According to one or more embodiments, the injectors 5 and / or 7 are inclined upwards, for example with an angle of between 10° and 45° relative to the horizontal.

[0052] With reference to Figure 1, according to one or more embodiments, first injectors 5 and / or second injectors 7 are arranged in one or more horizontal rows, i.e., perpendicular to the central / vertical axis Z of the mixing chamber 2. According to one or more embodiments, second injectors 7 are arranged below (eg a row) first injectors 5. According to one or more embodiments, second injectors 7 are arranged between two rows of first injectors 5.

[0053] According to one or more embodiments, the radial position of the second injectors 7 is in a separation space between the adjacent radial positions of two first injectors 5. According to one or more embodiments, the second injectors 7 are positioned substantially at half the separation angle of two first injectors 5.

[0054] With reference to Figures 2 and 3, according to one or more embodiments, at least one first injector 5 and / or at least one second injector 7 is rotated at an angle of between 0° and 45°, and preferably between 10° and 20°, relative to the radial direction of the diameter D of the mixing chamber 2, i.e., the projection of the axis of the injectors 7 onto a horizontal plane forms said angle, with the radial direction of the diameter D of the mixing chamber 2, which is perpendicular to the central / vertical axis Z.

[0055] With reference to Figure 1, the mixing chamber 2 feeds the downflow reactor 3 with a mixture of hydrocarbon feedstock 6, catalyst particles and optionally diluent 8. Advantageously, the hydrocarbon feedstock 6 and the catalyst particles give rise to the cracking reactions which complete each other in the downflow reactor 3 of a length L (along the central / vertical axis Z) to produce a hydrocarbon effluent comprising cracking products, spent catalyst and potentially a portion of the unreacted hydrocarbon feedstock. The length L of a downflow reactor 3 is typically between 2 m and 25 m.

[0056] According to one or more embodiments, the downflow reactor 3 is of constant cross-section geometry, such as cylindrical, square, rectangular or hexagonal, preferably cylindrical. According to one or more embodiments, the downflow reactor 3 is of cylindrical shape and optionally of variable diameter. According to one or more embodiments, the diameter of the downflow reactor 3 is defined such that the superficial velocity of the gas passing through it is between 2 m / s and 26 m / s, preferably between 6 m / s and 16 m / s. According to the invention, the inner wall of the mixing chamber 2 and / or of the downflow reactor 3 comprises one or more obstacles 9. Advantageously, the obstacles 9 are adapted to homogenize the concentration of catalyst particles. Specifically, the obstacles 9 make it possible to redistribute the catalyst particles which can accumulate close to the walls (egof mixing chamber 2 and downflow reactor 3).

[0057] According to the invention, the radial position of the at least one obstacle 9, on the inner wall of the mixing chamber 2 and / or the downflow reactor 3, is discontinuous. In the present application the term "discontinuous obstacle" means that the perimeter of the inner wall of the mixing chamber 2 and / or the downflow reactor 3, occupied by the obstacle 9, is less than 90%, preferably less than 80%, very preferably less than 70%. According to one or more embodiments, the perimeter of the inner wall of the mixing chamber 2 and / or the downflow reactor 3, occupied by the obstacle 9, is between 15% and 80%, preferably between 30% and 70%, very preferably between 40% and 60%. Thus the at least one obstacle 9 is not of continuous, i.e. annular, shape.

[0058] The obstacles 9 may be of various geometric shapes. According to one or more embodiments, the obstacles 9 are in the shape of a cube, a tetrahedron, a parallelepiped, a prism (e.g. a prism with a triangular, square, rectangular, hexagonal, circular or elliptical base), or a pyramid (e.g. a pyramid with a triangular, square, rectangular, hexagonal, circular or elliptical base), or a truncated cone, for example forming separate elements on the wall of the mixing chamber 2. According to one or more embodiments, the base is substantially perpendicular to the vertical axis Z.

[0059] According to one or more embodiments, the obstacles 9 are arranged to avoid the accumulation of catalyst particles on the obstacles 9. According to one or more embodiments, the obstacles 9 comprise a lower portion (lower end surface) wider than the upper portion (upper end surface).

[0060] According to one or more embodiments, the obstacles 9 are arranged to distribute the catalyst particles towards charge injection zones of the mixing chamber 2, zones more concentrated in hydrocarbons. According to one or more embodiments, the obstacles 9 comprise an upper surface that is oblique and descends laterally, i.e., along the wall of the mixing chamber 2.

[0061] According to one or more embodiments, the obstacles 9 are arranged to distribute the catalyst particles substantially inwards (e.g. towards the vertical axis Z), a zone more concentrated in hydrocarbons. According to one or more embodiments, the obstacles 9 comprise an upper surface that is oblique and descends from the outside towards the inside. According to one or more embodiments, obstacles 9 are arranged in the mixing chamber 2 upstream of the at least one first injector 5 of hydrocarbon feedstock 6 and / or of the at least one second injector 7 of diluent 8. Advantageously, the obstacles 9 make it possible to direct the catalyst particles towards the injectors and increase contact, in particular with the hydrocarbon feedstock 6. According to one or more embodiments, the radial position of the obstacles 9 in the mixing chamber 2 is in a separation space between the adjacent radial positions of two (e.g. first) injectors.

[0062] According to one or more embodiments, obstacles 9 are arranged downstream of the at least one first injector 5 of hydrocarbon feedstock 6 and / or of the at least one second injector 7 of diluent 8. According to one or more embodiments, obstacles 9 are arranged downstream of the at least one first or second injector at an axial distance of between 0*L and 0.3*L, and preferably between 0.01*L and 0.1*L.

[0063] According to one or more embodiments, obstacles 9 are arranged in the downflow reactor 3 at an axial distance Hi (eg Hi , H2, etc.) from the mixing chamber 2 of between OL and 0.9*L, preferably between 0.01*L and 0.6*L, for example between 0.01*L and 0.4*L.

[0064] According to one or more embodiments, the rows of obstacles 11 are spaced apart by a distance of between 0.05*L and 0.4*L. With reference to Figure 2, according to one or more embodiments, the device according to the invention comprises at least one row of obstacles 9, relative to the central / vertical axis Z, arranged at a predetermined height from the inner wall of the mixing chamber 2 and / or the downflow reactor 3. According to one or more embodiments, the obstacles 9 of the row of obstacles 11, thus arranged in a “string”, are positioned substantially equidistant from each other. Advantageously, a row of obstacles 11 comprises (all) the obstacles 9 of a horizontal plane, perpendicular to the central / vertical axis Z.

[0065] According to one or more embodiments, the perimeter of the internal wall of the mixing chamber 2 and / or of the downflow reactor 3, occupied by the row of obstacles 11, is between 15% and 80% and preferably between 30% and 70%, such as 40% to 60%.

[0066] According to one or more embodiments, the row of obstacles 11 reduces the passage section of the internal wall of the mixing chamber 2 and / or of the downflow reactor 3 by 1% to 35% and preferably by 5% to 20%, such as by 10% to 20%.

[0067] According to one or more embodiments, a row of obstacles 11 comprises at least 2 obstacles 9, for example between 2 and 24 obstacles 9, preferably between 4 and 12 obstacles 9. According to one or more embodiments, a row of obstacles 11 in the mixing chamber 2 comprises at least 2 obstacles 9, for example between 2 and 24 obstacles 9, preferably between 4 and 12 obstacles 9, such as 4 obstacles 9.

[0068] According to one or more embodiments, the number of obstacles 9 of a row of obstacles 11 in the mixing chamber 2 is an integer multiple of the number of first injectors 5. According to one or more embodiments, a row of obstacles 11 in the mixing chamber 2 comprises as many obstacles as first injectors 5.

[0069] According to one or more embodiments, a row of obstacles 11 in the downflow reactor 3 comprises at least 2 obstacles 9, for example between 2 and 24 obstacles 9, preferably between 3 and 12 obstacles 9, very preferably between 4 and 8 obstacles 9, such as 8 obstacles 9.

[0070] According to one or more embodiments, the number of obstacles in a row of obstacles 11 in the downflow reactor 3 is an integer multiple of the number of first injectors 5. According to one or more embodiments, a row of obstacles 11 in the downflow reactor 3 comprises as many obstacles as there are first injectors 5.

[0071] According to one or more embodiments, the mixing chamber 2 comprises between 0 and 4 rows of obstacles 11, such as 1 row of obstacles 11 preferably arranged above the (eg first) injectors.

[0072] According to one or more embodiments, the downflow reactor 3 comprises at least

[0073] 1 row of obstacles 11 , for example between 1 and 10 rows of obstacles 11 , preferably between

[0074] 2 and 8 rows of obstacles 11 , very preferably between 3 and 6 rows of obstacles 11 , such as 3 rows of obstacles 11 .

[0075] According to one or more embodiments, the downflow reactor 3 comprises: a first row of obstacles 11 arranged at an axial distance Hi from the mixing chamber 2 of between 0*L and 0.9*L; preferably a second row of obstacles 11 arranged at an axial distance from the first row of obstacles 11 of between 0.05*L and 0.4*L; and preferably a third row of obstacles 11 arranged at an axial distance from the previous row of obstacles 11 of between 0.05*L and 0.4*L.

[0076] According to one or more embodiments, the mixing chamber 2 comprises 1 row of obstacles 11 preferably arranged above the (eg first) injectors, and the downflow reactor 3 comprises at least 1 row of obstacles 11, for example between 1 and 10 rows of obstacles 11, preferably between 2 and 8 rows of obstacles 11, very preferably between 3 and 6 rows of obstacles 11, such as 3 rows of obstacles 11, the distance between two rows preferably being between 0.05*L and 0.4*L.

[0077] According to one or more embodiments, the radial position of the obstacles 9 of a row of obstacles 11 is in a separation space between the radial position of two adjacent obstacles 9 of an adjacent row of obstacles 11, ie, each row of obstacles 11 has a rotation (along the vertical axis Z) relative to an adjacent row of obstacles 11. According to one or more embodiments, the radial position of the obstacles 9 of a row of obstacles 11 has a rotation by an angle of between 10° and 35°, preferably between 15° and 30°, relative to the radial position of the obstacles 9 of an adjacent row of obstacles 11, and preferably at an angle of 1807N, with N the number of obstacles in a row.According to one or more embodiments, the rows of obstacles 11 are arranged relative to each other to together cover the entire perimeter of the internal wall of the mixing chamber 2 and / or the downflow reactor 3, according to a view along the vertical axis Z.

[0078] Furthermore, compared to crown-type internals which can significantly reduce the flow area and increase the gas velocity in the central zone of the downflow reactor 3, which can produce a parabolic profile of the flow and far from the plug flow flow, the row(s) of obstacles 11 according to the invention makes it possible to homogenize the flow of the catalyst without significantly reducing the flow area of ​​the downflow reactor 3.

[0079] With reference to Figure 3, according to one or more embodiments, at least a portion of the mixing chamber 2 comprises a central bulk part 12 (“plug” according to English terminology) arranged substantially along the central / vertical axis Z and defining an annular orifice 13 of the mixing chamber 2, through which the catalyst particles pour and / or flow into the mixing chamber 2.

[0080] The catalyst

[0081] The catalyst is a solid catalyst (e.g. particles of density, size and grain shape chosen for use in a fluidized bed). The densities, sizes and shapes of fluidized bed catalysts are known to those skilled in the art and will not be described further. The catalyst may be any type of catalytic cracking catalyst.

[0082] According to one or more embodiments, the catalyst is an FCC type catalyst, containing for example what is commonly called a matrix made of clay, silica or silica alumina, optionally binder, and / or zeolite, for example from 15% to 70% by weight of zeolite relative to the weight of the catalyst, preferably a Y zeolite and / or a ZSM-5 zeolite. According to one or more embodiments, the catalyst comprises a ZSM-5 zeolite. According to one or more embodiments, the grain density of the catalyst is between 1000 kg / m 3 and 2000 kg / m 3 . According to one or more embodiments, the grain density of the catalyst is between 1250 kg / m 3 and 1750 kg / m 3 .

[0083] According to one or more embodiments, the catalyst comprises at least one binder (eg from 30% to 85% by weight) chosen from alumina, silica, silica-alumina, magnesia, titanium oxide, zirconia, clays and boron oxide, alone or as a mixture and preferably from silica, silica-alumina and clays, alone or as a mixture.

[0084] According to one or more embodiments, the catalyst comprises at least one doping element (eg from 0 to 10% by weight) chosen from phosphorus, magnesium, sodium, potassium, calcium, iron, boron, manganese, lanthanum, cerium, titanium, tungsten, molybdenum, copper, zirconium and gallium, alone or as a mixture.

[0085] According to one or more embodiments, the catalyst comprises and / or consists of zeolite, such as ZSM-5, optionally doped.

[0086] The charge

[0087] According to one or more embodiments, the hydrocarbon feedstock 6 is a heavy feedstock, characterized by a boiling start temperature close to 340°C, often greater than 380°C, such as a heavy cut, for example from a vacuum distillation unit, such as vacuum gas oil or VGO or a vacuum residue, an atmospheric residue, a vacuum gas oil from a conversion unit, such as a coker gas oil or HCGO or a heavy cut from an ebullated bed or entrained bed hydroconversion unit (such as the H-Oil, LC-Fining, EST, VCC or Uniflex processes), a recycle from a hydrocracking step, alone or in a mixture.

[0088] According to one or more embodiments, the hydrocarbon feedstock 6 is a light feedstock, characterized by a lower boiling point of 450°C, often lower than 400°C, such as a gasoline cut or a diesel cut, for example from an atmospheric distillation unit, or from a conversion unit, such as a gasoline or a diesel from a hydrocracking unit, or a gasoline or a diesel from a coking unit or a gasoline or a diesel from an ebullated bed or entrained bed hydroconversion unit (such as the H-Oil, LC-Fining, EST, VCC or Uniflex processes), or a gasoline or a diesel from an FCC unit, or a recycle from the FCC unit in question, alone or as a mixture. According to one or more embodiments, it is also possible to process a mixture of light and heavy cuts, or even a complete crude.Upon contact with the downflow 4 of hot catalyst particles, the pulverized hydrocarbon feedstock 6 vaporizes and endothermic cracking reactions occur along the downflow reactor 3, thus reducing the temperature and producing: recoverable products (e.g. C1-C4 gas comprising olefins; a gasoline cut comprising aromatics); optionally a light diesel cut (“Light Cycle Oil” or LCO according to English terminology); optionally a heavy diesel cut (“Heavy Cycle Oil” or HCO according to English terminology);

[0089] - optionally an oil in the form of slurry; and optionally a solid residue (coke) adsorbed on the catalyst.

[0090] The method according to the invention

[0091] The process according to the present invention comprises a catalytic cracking step for the production of light olefins (and in particular ethylene and propylene), aromatics (and in particular benzene, toluene and xylenes), and gasoline (and optionally LCO, HCO and slurry), by catalytic cracking of the hydrocarbon feedstock 6 (fed by the first injector 5) by contacting with the descending flow 4 of hot catalyst particles (fed by the line 1), and optionally the diluent 8 (fed by the second injector 7) in the mixing chamber 2 then in the descending flow reactor 3.

[0092] According to one or more embodiments, the downward flow 4 of the catalyst particles in the pipe 1 upstream of the mixing chamber 2 is in a dense fluidized regime and preferably with a mass flow greater than 200 kg / m 2 s, for example to preferably allow a regime with descending bubbles.

[0093] In this application, the term "dense fluidized bed" means a gas-solid fluidized bed operating in a homogeneous regime, in a bubbling regime or in a turbulent regime.

[0094] In the present application, the term "homogeneous fluidized bed" means a gas-solid fluidized bed whose gas velocity is between the minimum fluidization velocity and the minimum bubbling velocity. These velocities depend on the properties of the solid catalyst (density, size, grain shape, etc.). The solid volume fraction is between a value close to 0.45 and the maximum solid volume fraction corresponding to a fixed, non-fluidized bed, generally close to 0.6. In the present application, the term "bubbling fluidized bed" means a gas-solid fluidized bed whose gas velocity is between the minimum bubbling velocity and the transition velocity to the turbulent regime. These velocities depend on the properties of the solid catalyst (density, size, grain shape, etc.). The solid volume fraction is between a value close to 0.35 and a value close to 0.45.

[0095] In this application, the term "turbulent fluidized bed" means a gas-solid fluidized bed whose gas velocity is between the transition velocity to the turbulent regime and the transport velocity. The volume fraction of solid is between a value close to 0.25 and a value close to 0.35.

[0096] In this application, the term "transported fluidized bed" means a gas-solid fluidized bed whose gas velocity is greater than the transport velocity. The solid volume fraction is less than a value close to 0.25. In this application, the term "transport velocity" corresponds to the velocity with which essentially all of the solid is entrained by the gas.

[0097] According to one or more embodiments, the injectors 5 are adapted to atomize the hydrocarbon feedstock 6 (liquid) and penetrate the catalyst flow.

[0098] According to one or more embodiments, the operating conditions of the pipe 1 and the downflow reactor 3 are chosen from the following conditions: temperature (at the reactor outlet) between 520°C and 750°C and preferably less than 650°C; absolute total pressure between 0.1 MPa and 0.5 MPa; mass ratio of the catalyst 4 to the hydrocarbon feedstock 6 C / O between 5 (kg / h) / (kg / h) and 35 (kg / h) / (kg / h) and preferably between 15 (kg / h) / (kg / h) and 30 (kg / h) / (kg / h); contact time t c between the hydrocarbon feedstock 6 and the catalyst less than 10 seconds, preferably between 0.5 seconds and 4 seconds; mass flow of catalyst particles between 50 and 850 kg / (m 2 s), preferably between 400 and 750 kg / (m 2 s); and gas surface velocity between 2 m / s and 26 m / s, preferably between 6 m / s and 16 m / s.

[0099] In this description, the contact time tc is defined as the product of the solid volume fraction £ s by bed height H s (eg reactor height L), divided by the superficial gas velocity vsg, this integrated throughout the bed height, as defined below in the mathematical formula Math 1. Math 1

[0100] According to one or more embodiments, a quantity of diluent 8 (e.g. nitrogen and / or water vapor) is added to the feedstock to reduce the partial pressure of hydrocarbons in the feedstock and the diluent is introduced in an amount representing 0% or 0.1% to 40% by weight, preferably 1% to 35% by weight and preferably between 1% and 30% by weight relative to the mass of the hydrocarbon feedstock 6.

[0101] According to one or more embodiments, at the end of the catalytic cracking step in the downflow reactor 3, the gaseous products and the catalyst, and optionally the unconverted vaporized feedstock, are separated in the gas / solid separator (not shown) containing a dense fluidized bed where the cracking reactions can continue.

[0102] According to one or more embodiments, the operating conditions of the separator are chosen from the following conditions: temperature (at the reactor outlet) between 500°C and 750°C, preferably between 550°C and 700°C, even more preferably between 580°C and 685°C; absolute total pressure between 0.1 MPa and 0.5 MPa and preferably between 0.1 MPa and 0.4 MPa and preferably between 0.1 MPa and 0.3 MPa; mass ratio of the catalyst to the feed (unconverted vaporized feed and gaseous products) C / O between 5 (kg / h) / (kg / h) and 40 (kg / h) / (kg / h); contact time tc between the feedstock and the catalyst of between 500 milliseconds (ms) and 10 seconds; and partial pressure of hydrocarbons in the feedstock (PPHfeedstock) of between 0.01 MPa and 0.3 MPa, preferably between 0.02 MPa and 0.2 MPa and more preferably between 0.05 MPa and 0.15 MPa.

[0103] According to one or more embodiments, at the outlet of the separator the coked catalyst is sent to an optional stripper (not shown) to strip the hydrocarbons remaining adsorbed on the surface of the catalyst using a second diluent.

[0104] According to one or more embodiments, the operating conditions of the stripper are chosen from the following conditions: residence time of the catalyst in the stripper: between 10 seconds and 180 seconds, preferably between 30 seconds and 120 seconds; superficial gas velocity between the minimum fluidization velocity and the transition velocity to the turbulent regime, for example between 0.01 m / s and 0.5 m / s, preferably between 0.15 m / s and 0.4 m / s; solid flux between 25 kg / m 2 s and 200 kg / m 2 s, preferably between 50 kg / m 2 s and 150 kg / m 2 s and preferably between 50 kg / m 2 s and 100 kg / m 2s; temperature between 500°C and 750°C, preferably between 550°C and 650°C; absolute total pressure between 0.1 MPa and 0.5 MPa and preferably between 0.1 MPa and 0.4 MPa and preferably between 0.1 MPa and 0.3 MPa; solid volume fraction between 0.25 and 0.6, preferably between 0.4 and 0.6.

[0105] According to one or more embodiments, at the outlet of the separator or stripper, the coked solid is transported into a regenerator (not shown) in which an air supply burns the coke from the catalyst to produce a hot regenerated catalyst and combustion gases, the hot regenerated catalyst being able to supply the downflow 4 with hot catalyst particles.

[0106] According to one or more embodiments, the operating conditions of the regenerator are chosen from the following conditions: superficial gas velocity between 0.1 m / s and 2 m / s, preferably 0.2 m / s and 1.5 m / s; catalyst residence time between 30 seconds and 20 minutes, preferably between 1 minute and 10 minutes; temperature between 500°C and 840°C, preferably between 650°C and 750°C.

[0107] Examples

[0108] With reference to Figure 3, the flows in a reference device A and a device according to the invention B operating under reaction-free conditions were compared in order to study the hydrodynamics.

[0109] The reference device A and the device according to the invention B comprise: a pipe 1, composed of a cylindrical section, a narrowing cone and a cylindrical section; a frustoconical mixing chamber 2 (S1 / S2 being less than 1) comprising a central bulk part 12 defining an annular orifice 13; a cylindrical downflow reactor 3 having a length of 4.07 m and an internal diameter of 0.42 m; four first injectors 5 of hydrocarbon feedstock 6 positioned in counter-current to the downflow 3 of catalyst particles with an angle of 30° upwards relative to the horizontal direction; and four second injectors 7 of diluent 8 (water vapor) positioned in counter-current to the downflow 3 of catalyst particles with an angle of 30° upwards relative to the horizontal direction.

[0110] Reference device A has no obstacles positioned at the internal walls.

[0111] The device according to the invention has three rows of obstacles 11 positioned at the wall of the downflow reactor 3. Each row of obstacles 11 includes 8 prisms of isosceles triangular section with a base of 0.07 m and a height of 0.096 m. In this example the base of the prism is perpendicular to the vertical axis Z. The perimeter occupied by the obstacles 9 of a row of obstacles 11 is 46% of the total perimeter of the downflow reactor 3. The section occupied by the obstacles 9 of a row of obstacles 11 is 16% of the section of the downflow reactor 3.

[0112] The first row of obstacles 11, the second row of obstacles 11 and the third row of obstacles 11 are positioned at a distance of 0.4 m, 0.6 m and 1.4 m from the first injectors 5 of hydrocarbon feedstock 6, respectively. Each row of obstacles 11 has a rotation of 22.5° relative to the previous row of obstacles 11, in particular to direct the catalyst particles flowing between two obstacles 9 towards more diluted zones.

[0113] The configurations of the reference device A and the device according to the invention B were simulated in CFD with the Barracuda© tool under the following operating conditions: the catalyst flow of 607 kg / m 2 s; the catalyst has a diameter d5o of 73 pm and a grain density of 1418 kg / m 3(ie, group A of the Geldart classification); the air flow rate of 1.85 kg / s has a ratio between the first injectors 5 and the second injectors 7 of 70 / 30; the first injectors 5 are positioned 0.2 m above the second injectors 7; the rotation angle between the first injectors 5 and the second injectors 7 is 45°; the gas velocity at the outlet of the injectors is 90 m / s for the first injectors 5 and 76 m / s for the second injectors 7; the flow is in ambient conditions without reaction; a central spacer 12 is positioned in the center of the mixing chamber 2.

[0114] Figure 4 shows the Volume Fraction of Particles, noted FVP, for the two configurations A and B of the reference device A and the device according to the invention B, respectively, on 13 sections. The first two sections are respectively at the height of the first and second injectors 5 and 7, and the following sections are spaced 0.35 m apart.

[0115] Advantageously, the radial distribution of the solid throughout the downflow reactor 3 is always more homogeneous for the device according to the invention B compared to the reference device A. In addition, it should be noted that there is a significant concentration of the solid near the wall for the reference device A compared to the device according to the invention B.

[0116] Figure 5 shows the radial profiles A and B of the volume fraction of the FVP particles, and of the Mass Flux of the Particles, noted FM P, of the reference device A and the device according to the invention B of figure 3, respectively. The radial profiles A and B are produced in a direction x (perpendicular to the vertical axis Z) at a height of 2.8 m below the first injectors 5. It can be noted that the device according to the invention B produces a more homogeneous radial profile B with a better distribution of the phases. The coefficient of variation of the values ​​of volume fraction of the FVP particles on these radial profiles A and B is 15% for the reference device A and 5% for the device according to the invention B.Equivalently, the coefficient of variation of the FMP particle mass flux values ​​for profiles A and B is 16% for reference device A and 5% for device according to the invention B, which indicates better dispersion of the catalyst over the section for device according to the invention B.

Claims

Claims 1. Device for catalytic cracking in a fluidized bed with descending gas-solid co-current comprising, from top to bottom: - a pipe (1) adapted to transport a downward flow (4) of catalyst particles; - a mixing chamber (2) connected to the pipe (1) and adapted to be supplied by the pipe (1) with downward flow (4), the mixing chamber (2) comprising an internal wall and at least one first injector (5) of hydrocarbon feedstock (6); and - a descending gas-solid co-current fluidized bed reactor (3) connected to the mixing chamber (2) and adapted to be supplied by the mixing chamber (2) with a mixture comprising catalyst particles and hydrocarbon feedstock, the descending gas-solid co-current fluidized bed reactor (3) comprising an inner wall, wherein the inner wall of the mixing chamber (2) and / or the descending gas-solid co-current fluidized bed reactor (3) comprises one or more discontinuous obstacles (9).

2. Device according to claim 1, wherein the obstacles (9) are adapted to distribute catalyst particles substantially towards the interior of the mixing chamber (2) and / or the descending gas-solid co-current fluidized bed reactor (3).

3. Device according to claim 1 or claim 2, in which the obstacles (9) comprise an upper surface oblique and descending inwards.

4. Device according to any one of the preceding claims, wherein the obstacles (9) are adapted to prevent the accumulation of catalyst particles on the obstacles (9).

5. Device according to any one of the preceding claims, wherein the obstacles (9) are adapted to distribute catalyst particles along the wall of the mixing chamber (2).

6. Device according to any one of the preceding claims, in which the obstacles (9) comprise an oblique and laterally descending upper surface.

7. Device according to any one of the preceding claims, in which the obstacles (9) are in the shape of a prism, cylinder, pyramid, cone, and / or truncated cone. Device according to any one of the preceding claims, wherein obstacles (9) are arranged in the mixing chamber (2) upstream of the at least one first injector (5). Device according to any one of the preceding claims, wherein obstacles (9) are arranged in the downflow reactor (3) at an axial distance Hi from the mixing chamber (2) of between 0*L and 0.9*L, L being the length of the downflow gas-solid co-current fluidized bed reactor (3). Device according to any one of the preceding claims, comprising at least one row of obstacles (11) arranged at a predetermined height from the inner wall of the mixing chamber (2) and / or the downflow reactor (3). Device according to claim 10, wherein the perimeter of the inner wall of the mixing chamber (2) and / or the downflow reactor (3), occupied by the row of obstacles (11), is between 15% and 80%.Device according to claim 10 or claim 11, wherein the row of obstacles (11) reduces the passage section of the inner wall of the mixing chamber (2) and / or the downflow reactor (3) by 1% to 35%. Device according to any one of claims 10 to 12, wherein the row of obstacles (11) in the mixing chamber (2) comprises between 2 and 24 obstacles (9), and / or the row of obstacles (11) in the downflow reactor (3) comprises between 2 and 24 obstacles (9). Device according to any one of claims 10 to 13, wherein the radial position of the obstacles (9) of a row of obstacles (11) is in a separation space between the radial position of two adjacent obstacles (9) of an adjacent row of obstacles (11). Process for descending gas-solid co-current fluidized bed catalytic cracking comprising the following steps:. - transporting a dense downward flow (4) of catalyst particles in a pipe (1); - supplying a mixing chamber (2) via the pipe (1) with the downward flow (4), the mixing chamber (2) comprising an internal wall and at least one first injector (5) of hydrocarbon feedstock (6); - feeding a descending gas-solid co-current fluidized bed reactor (3) through the mixing chamber (2) with a mixture comprising catalyst particles and feedstock hydrocarbon, the descending gas-solid co-current fluidized bed reactor (3) comprising an inner wall; and - at least partially cracking the hydrocarbon feedstock (6) in the presence of the catalyst particles in the descending gas-solid co-current fluidized bed reactor (3), to produce an effluent (10) comprising at least partially coked catalyst and gaseous cracking products, wherein the inner wall of the mixing chamber (2) and / or of the descending gas-solid co-current fluidized bed reactor (3) comprises a plurality of obstacles (9).

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