Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
  • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
  • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
  • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
  • B01J8/0492—Feeding reactive fluids
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00327—Controlling the temperature by direct heat exchange
  • B01J2208/00336—Controlling the temperature by direct heat exchange adding a temperature modifying medium to the reactants
  • B01J2208/00353—Non-cryogenic fluids
  • B01J2208/00362—Liquid

Definitions

• the present invention applies in the field of exothermic reactions and more particularly to hydrotreatment, hydrodesulphurization, hydrodenitrogenation, hydrocracking, hydrogenation, hydrodeoxygenation or even hydrodearomatization reactions carried out in a reactor. fixed bed.
• the invention more particularly relates to a device for mixing and dispensing fluids in a downflow reactor and its use for carrying out exothermic reactions.
• the exothermic reactions carried out for example in refining and / or in petrochemistry need to be cooled by an additional fluid, called a quenching fluid, in order to prevent a thermal runaway of the catalytic reactor in which they are carried out.
• the catalytic reactors used for these reactions generally comprise at least one solid catalyst bed.
• the exothermic nature of the reactions requires keeping a homogeneous temperature gradient within the reactor in order to avoid the existence of hot spots in the catalyst bed included in the reactor. Areas that are too hot can prematurely decrease the activity of the catalyst and / or lead to non-selective reactions and / or lead to thermal runaway. It is therefore important to have at least one mixing chamber in a reactor, located between two catalyst beds, which allows a uniform temperature distribution of the fluids on a reactor section and a cooling of the reaction fluids to a desired temperature.
• the document FR 2 824 495 A1 describes a quenching device for ensuring an effective exchange between the quench fluid (s) and the fluid (s) of the process.
• This device is integrated in an enclosure and comprises a quenching fluid injection pipe, a fluid collection baffle, the quench box itself, operating the mixing between the quenching fluid and the downflow, and a system dispensing system consisting of a perforated bowl and a dispensing tray.
• the quenching box comprises a deflector ensuring the swirling motion of the fluids in a substantially non-radial direction and not parallel to the axis of said chamber and downstream of the deflector, in the direction of flow of the reaction fluid, at least one exit passage section of the fluid mixture formed in the box.
• This device comprises a horizontal collection means provided with a vertical collection line for receiving the fluids, an injection means placed in the collection line, and an annular mixing chamber of circular section located downstream of the collection means in the flow direction of the fluids.
• the mixing chamber includes an inlet end connected to the collection conduit and an outlet end for fluid passage, and a horizontal pre-distribution tray including at least one chimney.
• the Applicant has developed a device for mixing and dispensing fluids combined, to significantly reduce the space dedicated to the mixing and distribution of fluids in particular in a downflow reactor.
• a first subject of the invention relates to a device for mixing and dispensing fluids for a downflow catalytic reactor, said device comprising:
• At least one collection zone (A) comprising at least one collection means
• At least one substantially vertical collection line adapted to receive a reaction fluid collected by said collection means and at least one injection means opening into said collection line for injecting a quenching fluid
• At least one mixing zone (B) located downstream of the collection means in the direction of circulation of the fluids, said mixing zone (B) comprising at least one chamber blending apparatus connected to said collection line and an outlet end for discharging the fluids;
• said mixing zone (B) is located at the same level as the distribution zone (C), said mixing (B) and dispensing (C) zones being delimited by at least one annular wall comprising at least one lateral passage section capable of passing fluids from said mixing zone (B) to said distribution zone (C).
• said mixing zone (B) is comprised in an annular enclosure comprising said annular wall.
• said annular wall internally delimits said distribution zone (C).
• said annular wall is positioned at a distance d2 from the enclosure of the reactor, the distance d2 ranging from 2% to 20% of the reactor diameter.
• said mixing chamber is positioned at a distance d1 from the reactor enclosure, the distance d1 being between 5 and 300 mm.
• the height of said annular enclosure is between 200 and 800 mm.
• the annular wall comprises a plurality of lateral passage sections distributed over at least two levels.
• said annular wall is substantially cylindrical.
• the section of said mixing chamber is of parallelogram section and has a ratio between the height "h" of the section and the width "I" of said section is between 0.2 and 5.0.
• said mixing zone (B) comprises two diametrically opposite mixing chambers in said mixing zone (B).
• the chimneys located at the periphery of said distribution zone (C) are extended below the distribution plate and are bent, the bending angle ⁇ , taken between the longitudinal axis of the extension of the chimneys below said plateau.
• distribution (12) and the plane perpendicular to the longitudinal axis of the enclosure being between 0 and 90 degrees.
• the device according to the invention further comprises a dispersive system disposed below said distribution plate, said dispersive system comprising at least one dispersing device.
• said dispersing device is a grid comprising at least one guide system capable of collecting and transporting at least a portion of the flow of liquid from said distribution zone (C).
• said mixing (B) and dispensing (C) zones are delimited by two annular walls each comprising at least one lateral passage section capable of passing fluids from said mixing zone (B) to said distribution zone ( VS).
• Another subject of the invention relates to a downflow catalytic reactor comprising an enclosure containing at least two fixed catalyst beds separated by an intermediate zone comprising a device for mixing and dispensing fluids according to the invention.
• FIG. 1 represents an axial section of a downflow catalytic reactor comprising at least two solid catalyst beds, and comprising a compact device for mixing and dispensing fluids according to the prior art.
• the arrow in bold represents the flow direction of the fluids in the reactor.
• FIG. 2 represents an axial section of a downflow catalytic reactor comprising at least two solid catalyst beds, and comprising a compact device for mixing and dispensing fluids according to an alternative embodiment according to the invention.
• the arrow in bold represents the flow direction of the fluids in the reactor.
• the mixing chamber has not been shown.
• FIG. 3 represents a section of the compact device for mixing and dispensing fluids according to the section represented by the line X-X 'in dotted line in FIG. 2.
• FIG. 4 represents an axial section of the mixing and dispensing device according to FIG. 2.
• FIG. 5 is a perspective view of part of the mixing and dispensing device according to FIG. 2.
• FIGS. 6a, 6b and 6c show alternative embodiments of the mixing and dispensing device according to FIG. 2.
• FIG. 7 is a schematic representation of an alternative embodiment of the mixing and dispensing device according to the invention. Detailed description of the invention
• the compact mixing and dispensing device is used in a reactor in which exothermic reactions such as hydrotreatment, hydrodesulphurization, hydrodenitrogenation, hydrocracking, hydrogenation, hydrogenation, hydrotreatment, hydrotreatment, hydrotreatment, hydrotreatment, hydrothermalization, hydrogenation, hydrotreatment hydrodeoxygenation or even hydrodearomatization.
• the reactor has an elongate shape along a substantially vertical axis. From the top to the bottom of said reactor is circulated at least one reaction fluid (also called "process fluid" according to the English terminology) through at least one fixed bed of catalyst.
• the reaction fluid is collected and is then mixed with a quench fluid (also called “quench fluid” according to English terminology) in said device before being distributed to the catalyst bed located downstream of a distribution tray.
• a quench fluid also called "quench fluid” according to English terminology
• the downstream and the upstream are defined with respect to the flow direction of the reaction fluid.
• the reaction fluid may be a gas or a liquid or a mixture containing liquid and gas; this depends on the type of reaction carried out in the reactor.
• FIG. 1 relates to a mixing and dispensing device according to the prior art
• FIGS. 2 to 7 relates to a mixing and dispensing device according to the invention.
• Figures 2 to 7 show some elements of Figure 1; the references of Figures 2 to 7 identical to those of Figure 1 designate the same elements.
• the device according to the invention can, without departing from the scope of the invention, be used in any reactor or device and in any field where it is desirable to obtain a good mixture, material and / or heat and good fluid distribution.
• FIG. 1 illustrates a mixing and dispensing device according to the prior art arranged in an elongate reactor 1 along a substantially vertical axis in which at least one reaction fluid is passed from top to bottom through two catalyst beds 2 and 14.
• the reaction fluid can be a gas (or a mixture of gases) or a liquid (or a mixture of liquid) or a mixture containing liquid and gas.
• the mixing and dispensing device is placed under the catalyst bed 2, with respect to the flow of the reaction fluid in the chamber 1.
• a support grid 3 makes it possible to carry the catalyst bed 2 so as to clear a space collection (A) under this one (also called here collection area (A)).
• the height H1 of the collection space (A) is typically between 10 and 300 mm.
• This collection space or collection zone (A) makes it possible to collect the flow coming from the catalyst bed 2 at the level of the collection means 5.
• the collection means 5, also called a baffle, is a solid plate only opened at a location 6 to drain the flow of fluid to the annular mixing chamber 9.
• the reaction fluid from the bed 2 is thus constrained in the collection zone (A) to pass through the vertical collection pipe 7 which communicates with the opening 6
• a quenching fluid is injected into the collection line 7 via an injection line 8.
• the quenching fluid may be liquid or gaseous or a mixture containing liquid or gas.
• Said chamber 9 is connected at its inlet end to the collection pipe 7. The quenching fluid and the reaction fluid from the upper bed 2 are thus forced to pass through said chamber 9 in which they mix by undergoing a rotary flow.
• the mixture of fluids flows on the pre-distribution plate 11 located downstream of the chamber mixing 9, in the direction of the flow of fluids.
• the height H2 (see FIG. 1) taken between the collecting means 5 and the pre-distribution plate 11 is between 300 and 600 mm.
• the mixing chamber 9 is positioned at the periphery of the reactor.
• the gas and liquid phases of the mixture separate on the perforated plate 11, which is provided with one or more central chimneys 4 configured to allow the passage of the gas.
• the liquid passes through the perforations of the plate to form a shower head or rain type shower.
• the role of the perforated plate 11 is to distribute the flow coming out of the mixing chamber 9 to feed the distribution plate 12 in a relatively balanced manner, said distribution plate 12 being positioned downstream of the distribution plate, in the direction of the circulation of fluids.
• the height H3 (see FIG. 1) measured between the pre-distribution plate 11 and the distribution plate 12 is between 100 and 700 mm.
• the distribution plate 12 comprises chimneys 13, whose function is to redistribute the gas and liquid phases at the inlet of the catalyst bed 14 located downstream of this distribution plate.
• the mixing and dispensing device therefore comprises a mixing zone and a dispensing zone positioned one above the other in a stepped manner.
• the fluid mixture is made on a height H2 and the fluid distribution is performed on a height H3. Therefore, the total space H in the chamber 1 of a mixing and distribution device according to the prior art is equal to H1 + H2 + H3 (see Figure 1).
• the applicant has developed a new device for mixing and dispensing fluids, more compact than that described above, and having a good mixture of phases and a good distribution on the catalyst bed located below such devices.
• FIG. 2 represents a mixing and dispensing device according to the invention arranged in a reactor 1 of elongate shape along a substantially vertical axis in which at least one reaction fluid is circulated from above downwards through at least one a catalyst bed 2.
• the device according to the invention is disposed under the catalyst bed 2, with respect to the flow of the reaction fluid in the chamber 1.
• a support grid 3 makes it possible to support the catalyst bed 2 of to clear a collection zone (A) disposed under the catalyst bed 2.
• the collection zone (A) is necessary to allow the drainage of the reaction fluid to a collection line 7 (which will be described below) .
• the flowing reaction fluid is for example composed of a gas phase and a liquid phase.
• the reaction fluid passing through the catalyst bed 2 upstream is collected by a collecting means 5 (also called here collecting cabinet) substantially horizontal leading to a substantially vertical collection line 7 disposed either below the zone collection (A) at a zone called mixing zone (B) (as shown in Figure 2), or at the collection zone (A) (not shown in the figures).
• substantially vertical (e) and substantially horizontal (e) is meant in the sense of the present invention a variation of a plane with the vertical, respectively the horizon, an angle ⁇ between ⁇ 5 degrees.
• the collecting means 5 consists of a solid plate disposed in the plane perpendicular to the longitudinal axis of the chamber under the support grid 3 of the catalyst bed 2. The plate of the collecting means 5 extends radially on the the entire surface of the reactor 1.
• the collection means 5 collects the flow of the reaction fluid from the catalytic bed 2 upstream and direct it to said collection line 7.
• the collection means 5 is remote from the support grid 3 of the catalyst bed 2 with a height ⁇ (FIG. 4).
• the height ⁇ is chosen so as to limit the pressure drop during the collection of the fluid flowing from the catalyst bed 2 and to limit the guard height, ie the height formed by the liquid accumulated in the collection means 5.
• the guard height does not modify the drainage of the reaction fluid to the collection pipe 7, nor its flow in this pipe, nor its flow through the upper catalytic bed 2.
• the height ⁇ is between 10 and 200 mm, preferably between 30 and 150 mm, even more preferably between 40 and 100 mm.
• the reaction fluid from the bed 2 is forced in the collection zone (A) to pass through the vertical collection pipe 7.
• the height ⁇ is between 10 and 400 mm, preferably between 30 and 300 mm, and even more preferably between 50 and 250 mm.
• the mixing zone (B) comprises a mixing chamber 9 (see FIGS. 3 and 5) located downstream of the collecting means 5 in the direction of circulation of the fluids.
• the mixing chamber 9 comprises an inlet end directly connected to the collection pipe 7 and an outlet end 10 for discharging the fluids (see FIGS. 3 and 5).
• the technical considerations of the collection line 7 and the injection means 8 are identical to those of the mixing and dispensing device according to the prior art.
• the distribution zone (C) as for it comprises a distribution plate 12 supporting a plurality of chimneys 13.
• a characteristic of the present invention resides in the establishment of the mixing zone (B) at the same level as the zone of distribution (C), said mixing (B) and distribution (C) zones being delimited by at least one annular wall (16) comprising at least one lateral passage section capable of passing fluids from said mixing zone (B) to said distribution area (C).
• the mixing zone (B) is positioned in an annular enclosure 15 comprising said annular wall 16, at the periphery of the reactor enclosure, arranged concentrically with the reactor enclosure. and internally delimiting the distribution zone (C) by said annular wall 16, preferably substantially cylindrical, which annular wall comprises at least one lateral passage section 17a or 17b suitable for the passage of fluids from the mixing zone (B) to the distribution area (C).
• the annular wall 16 comprises at least two lateral passage sections 17a and 17b.
• the outlet end 10 of the mixing chamber 9 opens into the annular enclosure 15 (see Figures 3 or 5).
• the configuration of the mixing chamber 9 in the mixing zone (B) allows a tangential flow of the mixture of fluids both in the mixing chamber itself and in the annular enclosure 15, this tangential flow making it possible to optimize the effectiveness of the mixture.
• the mixture between the reaction fluid and the quenching fluid continues to be effected at the level of the annular enclosure 15.
• the dimensions of the annular enclosure 15 are chosen in such a way that they allow the fluid mixture to be rotated. in said annular enclosure 15 before entering the distribution zone (C).
• the height H'2 of the annular enclosure 15 is between 200 and 800 mm, preferably between 300 and 700 mm, and even more preferably between 300 and 600 mm.
• the annular enclosure 15 may be sectioned, ie said enclosure comprises two ends.
• the length of the annular enclosure 15, defined by the angle formed by the planes passing through both ends of said enclosure may be between 270 and 360 degrees, preferably between 315 and 360 degrees.
• the annular enclosure 15 internally surrounds the distribution zone (C) by a height H'3 comprising a distribution plate 12 (also called here distributor plate or distribution plate) and a plurality of chimneys 13. More precisely, the chimneys 13 are open at their upper end by an upper opening and have along their lateral wall a series of lateral orifices (not shown in the figures) intended for the passage separated from the liquid phase (through the orifices) and the gas phase ( through the upper opening) inside the chimneys, so as to achieve their intimate mixing inside said chimneys.
• a distribution plate 12 also called here distributor plate or distribution plate
• the chimneys 13 are open at their upper end by an upper opening and have along their lateral wall a series of lateral orifices (not shown in the figures) intended for the passage separated from the liquid phase (through the orifices) and the gas phase ( through the upper opening) inside the chimneys, so as to achieve their intimate mixing inside said chimneys.
• the shape of the lateral orifices can be very variable, generally circular or rectangular, these orifices being preferentially distributed on each of the chimneys according to several substantially identical levels from one chimney to the other, generally at least one level, and preferably from 2 to 10 levels, so as to allow the establishment of an interface as regular as possible between the gas phase and the liquid phase.
• the mixing and dispensing device according to the invention does not comprise a pre-distribution plate 11 provided with chimneys.
• the mixing chamber 9 is positioned at the periphery of the reactor 1, in the mixing zone (B) included in an annular enclosure 15, located at the same level as the zone of distribution (C).
• the mixing and distribution of fluids are no longer performed on two distinct levels.
• the mixing and dispensing device according to the invention is therefore significantly more compact compared to those known from the prior art.
• the annular enclosure 15 is separated from the distribution zone (C) by an annular wall 16, concentric to the reactor chamber and preferably substantially cylindrical, comprising a plurality of lateral passage sections 17a and 17b allowing the passage of liquid and gas from the chamber of mixture 9 and circulating in the annular chamber 15 of the mixing zone (B) to the distribution zone (C).
• Said lateral passage sections 17a / 17b may be indifferently in the form of an orifice or a slot.
• the annular wall 16 separating the mixing zone (B) from the distribution zone (C) is located at a distance d2 from the chamber of the reactor 1, the distance d2 being between 2% and 20% of the diameter of the reactor, preferably between 3% and 15% of the reactor diameter, more preferably between 6% and 12% of the reactor diameter.
• annular enclosure 15 is delimited on the external side by the enclosure of the reactor 1 and on the inner side by said annular wall 16, said annular wall 16 being located in the space between the enclosure of the reactor 1 and the chimneys 13 located the outermost, ie the chimneys 13 is distributed substantially along the circle of larger diameter.
• the annular wall 16 comprises a plurality of lateral passage sections 17a and 17b distributed over at least one level, preferably at least two levels.
• the lateral passage sections 17a make it possible in particular for the liquid to pass from the mixing zone (B) to the distribution zone (C) and the lateral passage sections 17b in particular allow the passage of the mixing zone (B) to the distribution zone (C).
• the gas and / or liquid phases of the mixture enter said distribution zone (C) by means of the lateral passage sections 17a and 17b situated on the annular wall 16.
• the distribution plate 12 extends radially over the entire distribution zone (C) of the device and is disposed in the plane perpendicular to the longitudinal axis of the chamber 1 of the reactor. Said distribution plate 12 optimizes the distribution of the cooled reaction fluid on the catalyst bed 14 located downstream of said distribution plate.
• the mixing chamber 9 has a substantially annular shape and may be of parallelogram or circular section.
• parallelogram section is meant any four-sided section whose opposite sides of said section are parallel in pairs, for example the parallelogram section may be a rectangular section (see Figure 3), a square section, or a section in rhombus.
• Circular section means a section in the form of a circle or an oval.
• the height or the diameter of said chamber will be chosen so as to minimize the pressure drop and so as to limit the space requirement in the reactor.
• the length of the mixing chamber 9 is defined by the angle formed by the planes passing through the two ends of said chamber (represented by the angle ⁇ in FIG. 3).
• the length of said chamber is between 0 and 270 degrees.
• the length of said chamber is between 30 and 200 degrees, more preferably between 90 and 180 degrees.
• the mixing chamber 9 is situated at a distance d1 from the chamber of the reactor 1, said distance d1 being between 5 and 300 mm, preferably between 5 and 150 mm (see FIG.
• the dimensions of the height section "h” and width “I” are such that the ratio between the height “h” and the width “I” is included between 0.2 and 5.0, preferably between 0.5 and 2.0 (see FIG.
• the height "h" of the mixing chamber is chosen so as to minimize the pressure drop and so as to limit the space requirement in the reactor. Indeed, the pressure drop of the mixing device according to the invention depends on the section of the mixing chamber.
• the diameter "d" of said mixing chamber is between 0.05 and 0.8 m, more preferably between 0.1 and 0.5 m more preferably between 0.15 and 0.5 m, and even more preferably between 0.15 and 0.4 m.
• the pressure drop of the device according to the invention depends on the diameter in the mixing chamber.
• ⁇ is the pressure drop
• p m the average density of the gas + liquid mixture in the mixing chamber
• V m the mean speed of the gas + liquid mixture
• ⁇ is the coefficient loss of charge associated with the mixing device.
• the outlet 10 of the mixing chamber 9 has a height "h” and / or a width " ⁇ " lower at the height "h” and / or the width "I” of the section of the mixing chamber 9 (out of the outlet) in order to further improve the homogeneity of the mixture.
• the ratio h '/ h and / or l / l is between 0.5 and 1, preferably between 0.7 and 1.
• the outlet 10 of the mixing chamber 9 has a diameter "d" less than the diameter "d" of the section of the mixing chamber 9 (out of outlet) in order to further improve the homogeneity of the mixed.
• the ratio of / d is between 0.5 and 1, preferably between 0.7 and 1.
• the mixing chamber 9 may comprise at least one deflection means (not shown in the figures) on at least one of the internal walls of said mixing chamber.
• the presence of at least one means of deflection of the mixture of fluids passing through said chamber makes it possible to increase the exchange surface between the two phases and therefore the efficiency of the transfers of heat and material between the liquid phase and the gaseous phase. passing through said chamber.
• Said deflection means may be in several geometric forms to improve the efficiency of the mixing chamber, it being understood that said forms allow at least a partial deviation of the path of the fluid mixture passing through said chamber.
• the deflection means may be in the form of a baffle, triangular section, square, rectangular, ovoid or any other form of section.
• the deflection means may also be in the form of one or more fin (s) or one or more fixed blades (s).
• two mixing chambers 9 can be positioned in the mixing zone (B) in order to reduce the height "h” or the diameter "d" of said mixing chambers, while ensuring a good mixing of the fluids and a good homogeneity in temperature.
• the two mixing chambers are diametrically opposed in the reactor chamber.
• a collection line 7 and an injection means 8 are associated.
• a dispersion system may be positioned to distribute the fluids evenly over the catalyst bed 14 downstream of said system.
• the dispersion system comprises one or more dispersion devices 19 (see FIG. 6b) that can be associated with each chimney 13, be in common with several chimneys 13, or be in common with all the chimneys 13 of the distribution plate. 12.
• Each dispersing device 19 has a substantially flat and horizontal geometry, but may have a perimeter of any shape. Moreover, each dispersion device 19 can be located at different height.
• said dispersing device is in the form of grids, and may optionally comprise deflectors.
• the distance separating the dispersion system from the bed of granular solids situated immediately below is chosen so as to keep the mixing state of the gaseous and liquid phases as far as possible as it is at the outlet of the chimneys 13.
• the distribution plate 12 and catalyst bed 14 located below said distribution plate is between 50 and 400 mm, preferably between 100 and 300 mm.
• the distance between the distribution plate 12 and said dispersing device 19 is between 0 and 400 mm, preferably between 0 and 300 mm.
• the distribution plate 12 is placed on the dispersion device 19.
• the distribution zone (C) comprising the distribution plate 12 and the chimneys 13 does not extend radially over the entire section of the reactor chamber because the mixing zone (B) comprising the mixing chamber 9 internally surrounds said distribution zone (C). Therefore, to overcome the absence of the distribution plate 12 and chimneys 13 at the periphery of the reactor, ie the zone located below the annular enclosure 15, several fluid deflection means can be envisaged for distributing the fluids in such a way that homogeneous above the catalyst bed 14 located downstream of the mixing and dispensing device, in the direction of fluid flow, and more particularly in the area below the mixing zone (B).
• the grids further comprise a guide system 21 in the form of at least one guide ramp 21 for collecting at least a portion of the flow of liquid from the distribution zone (C) and to conduct it at the periphery of the chamber of the reactor 1 in order to distribute the fluids radially over the entire surface of the reactor chamber above the second catalyst bed 14.
• the guide ramp may have a U-shaped or V-shaped profile in order to directing the liquid stream received at the periphery of the reactor, and may optionally include one or more perforations to allow the flow of said liquid flow below the grids.
• the annular enclosure 15 of the mixing zone (B) comprises at least one opening (perforation) 20, preferably comprising a plurality of openings 20, allowing at least partially to collect the fluids of the mixing chamber 9 opening into the annular chamber 15, thereby partially distributing the fluids at the periphery of the reactor chamber.
• the size and shape of the openings 20 are chosen in such a way that they only allow the collection of a minor portion of the fluids in the annular enclosure 15. Most of the fluids pass through the passage section (s). lateral 17a and / or 17b.
• the distribution zone (C) is positioned at the periphery of the reactor enclosure, and internally delimiting the mixing zone (B) by an annular wall 16, preferably substantially cylindrical, which annular wall 16 comprises at least one lateral passage section 17a or 17b suitable for the passage of fluids from the mixing zone (B) to the distribution zone (C).
• the mixing zone (B) is comprised in an annular enclosure 15 positioned in the distribution zone (C), the position of the annular enclosure 15 being as it forms two distribution zones (C), said mixing zone being delimited by two annular walls 16 each comprising at least one lateral passage section capable of passing fluids from said mixing zone (B) to said distribution zones (VS).
• the distance "d2" must be understood as lying between the reactor enclosure and the wall 16 closest to the reactor enclosure, ie the annular wall of larger diameter (see FIG. .
• the mixing and dispensing device according to the invention has the following advantages: - an increased compactness of the fact integration at the same height of the mixing zone and the fluid distribution zone;
• the device not according to the invention (Device A) is compared with a device according to the invention (Device B).
• the heights H1 and ⁇ of the collection space (A) are identical and are equal to 120 mm.
• the height between the distribution plate 12 and the top of the second catalytic bed 14 is fixed at 400 mm.
• the comparisons between these two devices are based on their compactness in a catalytic reactor.
• the bulk of a conventional mixing device, as disclosed in document FR 2 952 835 A1, between the upper end of the collection pipe 7 and the pre-treatment tray. distribution 11 is about 650 mm.
• the height H '2 of the annular enclosure 15 of the device according to the invention is 600 mm and the distance "d2" distance "d2" between the wall 16 of the annular enclosure 15 and the chamber of the reactor is 350 mm, allowing the fluid to rotate in the mixing zone (B) before entering the distribution zone (C).
• the device according to the invention allows a space saving of 24% compared to the device A.
• the space gained by the compactness of the device according to the invention compared to the device of the prior art can thus be used for catalyst beds.
• the device according to the invention also improves the performance of a reactor by increasing the amount of catalyst in the catalyst beds.

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• Chemical Kinetics & Catalysis (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

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• 2015
  • 2015-04-01 FR FR1552785A patent/FR3034325B1/fr not_active Expired - Fee Related
• 2016
  • 2016-02-16 WO PCT/EP2016/053290 patent/WO2016155938A1/fr active Application Filing
  • 2016-02-16 CA CA2979007A patent/CA2979007A1/fr not_active Abandoned
  • 2016-02-16 US US15/563,116 patent/US20180071703A1/en not_active Abandoned
  • 2016-02-16 JP JP2017550741A patent/JP2018510060A/ja active Pending
  • 2016-02-16 RU RU2017134969A patent/RU2017134969A/ru unknown
  • 2016-02-16 EP EP16707400.4A patent/EP3277417A1/de not_active Withdrawn
  • 2016-02-16 CN CN201680019965.2A patent/CN107405591A/zh active Pending

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