RU2776393C2 - Device for fluidization system with gas and solid particles for improvement of desorption - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: device is proposed for thorough mixing of solid particles and a gaseous medium in a fluidized layer with gas and solid particles, containing a set of corrugated and/or ribbed flat racks located in alternating intersecting planes, which provide a set of open spaces between alternating intersecting flat racks or next to them. An element has a configuration of a three-dimensional grid, and corrugated and/or ribbed flat racks are made of metal with vertices and recesses or ribs, so that vertices and recesses or ribs are located at an angle of less than 90 degrees from a slope line of the flat rack, when assembled to the element. Angular vertices and recesses or ribs form channels, which increase transverse movement of catalyst particles to spaces between racks, providing improved mixing of vapor and solid particles and their contact.

EFFECT: creation of structured filling elements, which require smaller number of elements for increasing desorption efficiency, as well as require less amount of vapor for achieving optimal desorption efficiency.

26 cl, 8 dwg

Description

Link to related application

[0001] The present application claims the benefit of the priority of U.S. Patent Application No. 15/649,729, filed July 14, 2017, titled "Apparatus for Fluidization System with Gas and Solids to Improve Desorption", the content of which is in its entirety and for all purposes incorporated by reference into this application.

Technical field

[0002] The present invention relates to fluidized beds in which solids and fluids flow in countercurrent. More specifically, the embodiments disclosed herein are directed to internal elements and, more specifically, filling elements to promote contact between solids and fluids in a fluidized bed.

State of the art

[0003] Fluidized Catalytic Cracking (FCC) is a chemical process commonly used in refineries to convert heavy, high molecular weight hydrocarbon materials to lighter, low molecular weight hydrocarbon fractions. In this type of process, the hydrocarbon feed is evaporated at high temperatures while being placed in contact with the cracking catalyst particles which are suspended in the feed vapor and thereby entrained. After the cracking reactions have given the desired range of molecular weights with a corresponding drop in boiling points, the resulting products are separated from the catalyst particles. The particles are then stripped to recover the trapped hydrocarbons, recovered by burning the coke formed thereon, and recycled by placing them again in contact with the feedstock to be cracked.

[0004] In this process, the required reduction in the boiling point of hydrocarbons is achieved through controlled catalytic and thermal reactions. These reactions occur almost instantaneously upon contact of the finely divided feedstock with catalyst particles. However, within a short time of contact of the catalyst particles with the feedstock, rapid deactivation of the particles occurs, mainly due to the adsorption of hydrocarbons and the deposition of coke and other pollutants on the active sites of the catalyst. Thus, it is necessary to continuously desorb the deactivated catalyst, for example by means of steam, to recover the hydrocarbons adsorbed and trapped in the voids, and to regenerate the catalyst, continuously and without changing its properties, by controlled combustion of coke in a single or multi-stage reduction section before recycling the catalyst particles to reaction zone.

[0005] Desorption is one of the critical steps in the fluid catalyzed cracking process. In fact, insufficient desorption causes the effluent from the reactor to remain on and between the catalyst particles, so that during the reduction step, an additional combustion load is imposed on the regenerator with excessive heat generation in excess of the heat required to start the catalytic reaction. As a result, the combustion of the trapped hydrocarbon vapors in the regenerator results in the loss of the final yield of the converted product.

[0006] In a fluid catalytic cracking process, desorption and reduction of the catalyst particles typically occur in a fluidized bed to promote vigorous mixing and intimate contact of the fluid streams and catalyst particles within the vessel. Fluidized beds are typically formed by passing a fluid stream, typically a vapor stream, in an upward direction through a layer of small solids at a flow rate sufficient to suspend the particles and turbulently mix the solids.

[0007] Typically, after separation of the reactor effluent from the catalyst particles, the particles are sent to a desorption chamber where desorption occurs in a descending dense fluidized phase. The gaseous fluid introduced into the bottom of the chamber is used to fluidize the coke-coated catalyst particles and displace entrained hydrocarbons located in the interstitial spaces between the particles. For this gaseous fluid, it is preferable to use a polar material such as steam because it is more strongly adsorbed by the catalyst particles and thus hydrocarbons are more easily displaced. Finally, the desorbed catalyst particles are transferred to a reduction zone.

[0008] In addition, the desorption operation is a complex task. In particular, it is difficult to control the movement of catalyst particles and avoid partial loss of fluidization associated with channeling (direct passage of large bubbles through the fluidized bed) and countercurrent mixing (with a downward flow of poorly fluidized particles or even with recirculation of such particles, especially in the area of the walls of the desorption chamber ). Thus, the time range and average desorption time of the deactivated catalyst particles and the quality of contact between grains and gaseous fluid are difficult to control, especially in large volume fluidized beds. In addition, when the catalyst flow rate per unit time is reduced to a level much lower than the calculated flow rate per unit time, large steam to catalyst ratios are required to maintain fluidization of the catalyst in the desorber and ensure sufficient desorption efficiency. Excess steam increases the load of gas and liquid on the equipment connected to the desorber. For example, excess steam can increase the amount of sour water produced per pound (453.6 g) of hydrocarbon processed, as well as increase the operating costs for generating and processing excess steam.

[0009] To overcome these difficulties, it is necessary to use devices located inside the desorber chamber to promote efficient mixing and improve dispersion and homogenization of particles by the stripping fluid. In particular, after passing through the desorption device, the particles are redistributed in space, which provides a state of organized mixing with the fluid and promotes random contacts. Fluid and particles are directed in multiple directions from a single stream. In addition, the device prevents countercurrent mixing and channeling of particles and the formation of solid or gaseous pockets within the desorption chamber.

[0010] The use of structured filler elements as an internal desorber makes it possible to reduce the size of the contact zone between the solid particles and the fluid. In fact, due to the marked improvement in this contact, smaller desorption chambers can be used compared to prior art chambers without loss of desorption performance even at very high catalyst flows through the desorption chamber.

[0011] Filling elements of various structures have been proposed to improve desorption. For example, U.S. Pat. No. 6,224,833 to Rall et al. describes a fluidized bed of gas and solid particles formed within a contact member comprising pairs of flat portions arranged in intersecting planes, each flat portion being formed by one or more shelves and one or more open slots next to each shelf. The shelves and slots are arranged so that the shelf in one of the flat parts intersects the slot in the paired flat part. The fluidized bed may be catalyst particles fluidized by a gas stream, for example, in a catalyst stripper and/or a regenerator in a fluidized catalyst cracking system. The commercial exploitation of US Pat. No. 6,224,833 has shown disadvantages such as a reduced level of stripping efficiency, uneven distribution of gas and steam, and a higher than expected use of stripping steam to achieve the desired stripping efficiency.

[0012] Another example is the corrugated filler described in US Pat. No. 5,716,585 to Senegas et al., consisting of corrugated sheets welded together to form a plurality of internal corrugated channels to allow catalyst and vapor to contact each other. This type of filler has been shown in US Pat. No. 6,242,433 to be less effective in stripping hydrocarbons from the catalyst.

[0013] US Pat. No. 6,251,999 to Lehman et al. discloses a corrugated strip for transversely corrugated filler, the strip having at its bottom edge at least one downwardly protruding pattern having some contour. This corrugated filler is suitable for air distillation towers aboard floating oil platforms or barges.

[0014] There is a need for improved structured filler elements that overcome the difficulties and limitations of US Pat. No. 6,224,833. In addition, there is a need for structured fill elements that require fewer elements to achieve similar levels of desorption, or elements that can increase desorption efficiency with the same number of elements, as described in US Pat. No. 6,224,833. In addition, there is a need for filling elements that require less steam to achieve optimal desorption efficiency.

[0015] Embodiments disclosed herein improve on US Pat. No. 6,224,833 and any type of flat structured filler or such filler as described in US Pat. and solid particles. The embodiments presented herein use, for example, the basic structure of US Pat. No. 6,224,833 and solve the problems associated therewith by providing a new design and manufacturing process for the filler element.

Disclosure of the essence of the invention

[0016] An embodiment disclosed herein relates to a gas-solids fluidized bed comprising a vessel having a shell and an open inner region within the shell, and comprising at least one corrugated filling element disposed in the open inner region. The corrugated filler element comprises a plurality of corrugated or ribbed flat posts arranged in alternating intersecting planes that provide a plurality of windows or open spaces between or adjacent to the alternating intersecting flat posts forming a three-dimensional lattice configuration. The flat posts of the corrugated filler element may include openings located at critical points to facilitate the flow of gas and/or catalyst between the flat posts. Fluidized bed with gas and solid particles also contains solid particles in the area of the fluidized bed and at least one gas stream flowing against the flow of solid particles, which causes fluidization of the solid particles in the corrugated filling elements and in the fluidized bed.

[0017] According to another embodiment, the corrugated flat struts comprise peaks and valleys, with the peaks and valleys inclined at less than 90 degrees to the line of inclination of the corrugated flat strut, when assembled to form a corrugated filler element. The dimensions of the peaks and valleys may vary as needed for any particular process or device, however, the height of the peaks is usually from about 1/16 inch (1.5875 mm) to about 2 inches (50.8 mm), but is usually about 1 /4 inches (6.350 mm) high. The depth of the depressions typically ranges from about 1/16 inch (1.5875 mm) to about 2 inches (50.8 mm), but is usually about 1/4 inch (6.350 mm) deep. The width of the peaks and valleys is not limited and typically ranges from about 1/4 inch (6.350 mm) to about 24 inches (609.6 mm), but is usually about 3/4 inch (19.050 mm) and forms channels that effectively guide hard particles into open areas inside the corrugated filling element.

[0018] According to another embodiment, the ribbed flat posts include ribs on the top surface and/or bottom surface and/or side surface of the flat posts. The ribs form channels inclined at an angle of less than 90 degrees to the line of inclination of the ribbed flat post when assembled to form a corrugated filling element. The dimensions of the fins can vary as needed for any particular process or device and typically range in height from about 1/16" (1.5875 mm) to about 2" (50.8 mm), but are typically about 1/4" ( 6.350 mm) in height. In addition, the ribs are not limited in shape, which may include, for example, square, rectangular, circular, or curved surfaces that form channels between the ribs on the surface of the posts. The spacing of the fins can be varied as needed and are typically spaced from 1/4" (6.350mm) to 24" (609.6mm) apart. Typically, the fins are spaced 3/4 inch (19.050 mm) apart, or at distances that efficiently and effectively form channels that direct solids into open areas within the corrugated core.

[0019] In accordance with another embodiment, holes in the corrugated and/or ribbed flat racks are drilled at critical locations to facilitate cross-mixing of solids and stripping fluid. The holes have a diameter of at least about 1/4 inch (6.350 mm) or more, and may be round, oblong, or other shape.

[0020] In accordance with another implementation, the height of the corrugated filler element may be from about 1 inch (25.400 mm) to about 36 inches (914.4 mm) or more, and preferably from about 6 inches (152.40 mm) to about 24 inches (609.6 mm).

[0021] According to another embodiment, the flat posts are inclined at an angle of less than 90 degrees.

[0022] According to another embodiment, the channels formed by the corrugated and/or ribbed flat posts do not slope in the same direction on the posts.

[0023] In another embodiment, the channels formed by the grooved and/or ribbed flat posts on adjacent posts do not point in the same direction.

Brief description of the drawings

[0024] FIG. 1 is a schematic view of a column showing a fluidized bed containing an embodiment of the corrugated filler element disclosed herein.

[0025] FIG. 2 is a schematic view of an embodiment of the corrugated filler element disclosed herein.

[0026] FIG. 3 is a schematic top and side view of an embodiment of the dimensions and arrangement of the corrugated filler element of a single corrugated flat stud.

[0027] FIG. 4 is a schematic view of the corrugated filling element from various angles.

[0028] FIG. 5A is a schematic view of an embodiment of a corrugated filler channel pattern on corrugated or ribbed flat posts.

[0029] FIG. 5B is a schematic view of an embodiment of a corrugated filler channel pattern on corrugated or ribbed flat studs.

[0030] FIG. 5C is a schematic view of an embodiment of a corrugated filler channel pattern on corrugated or ribbed flat studs.

[0031] FIG. 5D is a schematic view of an embodiment of a corrugated filler channel pattern on corrugated or ribbed flat posts.

Implementation of the invention

[0032] Embodiments of the present invention are described more fully below with reference to the accompanying drawings, which show exemplary embodiments of the invention. The present invention may, however, be embodied in many different forms and should not be construed as limited to the exemplary embodiments provided herein; rather, these embodiments are provided so that this description is detailed and complete and fully conveys the scope of the embodiments to those skilled in the art. Like reference designators refer to like, but not necessarily the same or identical elements throughout the description.

[0033] FIG. 1 proposes an embodiment of a corrugated filling element in a fluidized bed (5) with gas and solid particles, disclosed in this document. The corrugated filling element (1) is shown located inside the cylindrical vessel (2). The cylindrical vessel (2) may also be, for example, square or rectangular and made of materials suitable for use in a fluid catalytic cracker. The cylindrical vessel (2) can be used for various types of fluidized bed treatment of gases and solids, such as processes involving heat transfer, mass transfer and/or chemical reactions. For example, the cylindrical vessel (2) can be used to strip hydrocarbons from spent catalyst or to recover spent catalyst by burning coke from spent catalyst in fluid catalytic cracking processes. In addition, the cylindrical vessel (2) can be used to realize heat exchange between gases and hot catalyst in fluid catalytic cracking, or as a flow straightener for the catalyst stream or catalyst homogenizer for conditioning the catalyst entering the fluid catalytic cracking riser, or as devices to prevent entrainment in the fluidized bed, as in other processes.

[0034] As shown in FIG. 1, the corrugated filling element (1) comprises a plurality of corrugated and/or ribbed flat posts (3) (ribbed flat posts not shown) extending at an acute angle of less than 90 degrees over the entire cross section of the cylindrical vessel (2) (or part of it). A plurality of corrugated flat posts (3) extend in alternating intersecting planes and are connected together by conventional means either at one end or at an intermediate portion along their lengths. The width and thickness of the corrugated (and/or ribbed) flat posts (3) are not limited and are determined from mechanical considerations with typical values, for example, 3 inches (76.2 mm) and 5/32 inches (3.96875 mm), respectively. Windows size (4), i.e. open spaces or slots that are formed between the flat posts (3) depends on the height of the filling element. Windows (4) allow gas and solids to pass through. In addition, the corrugated flat posts (3) themselves can be perforated to allow fluid and gas to pass through. As such, the corrugated flat posts (3) arranged in alternating intersecting planes provide a three-dimensional lattice configuration having substantially square or diamond-shaped open spaces, i.e. windows (4) between each of the corrugated flat posts (3). Thus, the angle formed by the alternating intersecting corrugated flat posts (3) is usually 60 or 90 degrees, but may be different if necessary.

[0035] FIG. 2 shows an embodiment of a corrugated filler element (1) as well as details of corrugated flat posts (3), which are made of non-flat or corrugated metal and look similar to the corrugated metal processing trays sold under the trademark RIPPLE TRAY, as described in the US patent No. 2767 967. FIG. 3 shows corrugations, i.e. waves or ridges and grooves, which form channels and consist of peaks (8) and troughs (9) that create waves in corrugated flat struts (3). These peaks and valleys form channels that are at an angle of less than 90 degrees, and typically approximately 45 degrees, to the line of inclination of the corrugated flat stud (3), when assembled into a corrugated filler element (1). This arrangement is different from the corrugated sheets described in US Pat. No. 5,716,585. Although the distance between each valley and the depth and height of each valley (9) and peak (8) are not limited, the actual angles and depths of the peaks and valleys forming the channels are optimized to improve the desorption efficiency. In one embodiment, and as shown in FIG. 3, the angle of the tops (8) and troughs (9) that form the channels is approximately 45 degrees from the line of inclination of the corrugated flat strut (3), and the distance through each trough (9) is typically approximately 3/4 inch (19.05 mm) but may vary from approximately 1/4" (6.350 mm) to approximately 24" (609.6 mm) and the tops and valleys are usually approximately 1/4" (6.350 mm) in height/depth but may undergo a change of approximately 1/16 inch (1.5875 mm) and approximately 2 inches (50.8 mm), respectively.

[0036] Thus, the corrugated metal of the corrugated flat struts (3) and the ribs of the ribbed flat struts (not shown) promote radial mixing, which increases the contact of the solids with the fluidizing gaseous medium. In contrast, flat surfaced racks, i.e. racks that are not corrugated or ribbed as described herein, assist in the separation of catalyst particles from the gas and move the particles down the top flat surface of the rack away from the open space windows (4) where the catalyst will be mixed with the fluidizing gas (7). In particular, since the waves, that is, the tops and valleys that form the channels of the corrugated flat posts (3), and the ribs that form the channels on the flat posts, are angled to enhance the lateral movement of the catalyst particles into the windows (4) of the open space, it is better mixing and contact of solid particles and vapors occurs. Thus, the multidirectional movement of the catalyst particles on the corrugated and/or ribbed flat racks leads to better contact between the catalyst and the fluidized gas (7) inside the corrugated filling element (1), in contrast to the delamination of the catalyst on the filling element of the prior art. Thus, the corrugated filler element (1) provides improved desorption efficiency for a given amount of desorption steam and desorption stages.

[0037] The corrugated filler element (1) provides an increased number of desorption stages per element due to internal backflow within the corrugated filler element (1). Thus, the corrugated filler element (1) provides fewer filler elements needed to achieve similar levels of desorption compared to prior art filler elements, or the corrugated filler element (1) provides increased desorption efficiency for the same number of elements, or, in alternatively, the wavy filling element (1) provides the reduced amount of steam required to achieve optimum desorption efficiency.

[0038] The corrugated filler element (1) can be made using materials and technologies that are already well established, such as materials used to make RIPPLE TRAY and KFBE trademarked structured filler elements and/or other stripper filler elements.

[0039] FIG. 5A, 5B, 5C, and 5D show, in a non-limiting manner, some of the plurality of patterns formed by oblique ribs and flat strut waves, respectively.

[0040] A plurality of corrugated and/or ribbed flat posts (3) are connected to each other in an oriented, interconnected and intersecting manner, forming a wavy filler element (1). FIG. 4 shows views of the corrugated filling element (1) from different angles. A plurality of corrugated filling elements (1) can be placed one after the other in spaced or contacting positions inside the cylindrical vessel (2). Adjacent corrugated filling elements (1) may be aligned or they may be rotated through an angle such as 45 degrees, 90 degrees or other desired angle relative to each other. The angle formed by the plane of each corrugated flat rack (3) and the longitudinal axis of the cylindrical container (2) undergoes a change depending on the angle of intersection chosen for the corrugated flat racks. For example, when using an intersection angle of 90 degrees, the corrugated flat posts (3) extend at 45 and 135 degrees to the axis of the vessel. When choosing an intersection angle of 60 degrees, flat corrugated posts (3) run at an angle of 60 and 120 degrees to the axis of the column.

[0041] Each corrugated filler element (1) may be sized to completely fill the cross section of the cylindrical vessel (2), or several smaller corrugated filler elements (1) may be positioned next to or on top of each other to fill the cross section of the vessel, or parts of the cross section of the vessel, for example, wavy filling elements (1) can be spaced apart along the perimeter of the cross section of the vessel, leaving the center of the cross section open. When positioned next to each other, the corrugated filler elements (1) may be oriented in the same or different directions and may be located within a plurality of rows offset from each other.

[0042] In accordance with one embodiment, a fluidized bed (5) with gas and solids is formed in a part of a cylindrical vessel (2) in which a corrugated filling element (1) or a plurality of corrugated filling elements (1) is placed. FIG. 1, the fluidized bed (5) with gas and solid particles is formed by solid particles in the form of particles, shown by arrows (6), and an upward flowing gaseous fluid, shown by arrows (7). Solid particles (6) have a given shape, size and composition, and gas (7) has a given composition and velocity. In a preferred embodiment, solids (6) are added from the top and removed from the bottom of the fluidized bed (5) with gas and solids in a continuous manner to move the solids (6) and gas (7) through the fluidized bed in opposite directions. Alternatively, the solids (6) are left in the fluidized bed (5) until the treatment is complete and then drained from the fluidized bed.

[0043] After passing upward through the fluidized bed (5), the gas (7) enters the dilute phase above the fluidized bed (5) and may pass through a separator such as a cyclone (not shown) to remove any entrained solids before they are delivered to the final or intermediate destination. Solid particles (6) after removal from the fluidized bed (5) can also be delivered to the final or intermediate destination.

[0044] The corrugated filling element (1) can be positioned in the required vertical position in the fluidized bed (5). In some applications, it may be desirable to position the corrugated filler element (1) or a plurality of corrugated filler elements (1) near the upper and lower boundaries of the fluidized bed (5), while in other applications it may be desirable to position the elements (1) at a preselected distance from borders. In other applications, the elements (1) may pass above or even below the fluidized bed (5).

[0045] The type of treatment that occurs in the fluidized bed (5) may include heat transfer, mass transfer, combustion, and/or chemical reaction. For example, the fluidized bed (5) can be used to strip hydrocarbons from spent catalyst or burn coke deposits on spent catalyst in fluid catalytic cracking systems. For example, there is a fluid catalytic cracking system (not shown) using a wavy filler element (1) that removes volatile hydrocarbons from spent catalyst solids in a desorption chamber before passing the catalyst particles to a regenerator that burns coke deposits to recovery of catalyst particles. The reactor section chamber includes a feed riser that supplies the catalyst particles and the reactor effluent to an open area of the reaction chamber where the catalyst particles are separated from the reactor effluent. The catalyst particles then flow by gravity downwards and through the corrugated filler element (1). Steam or other stripping gas is fed through the flow line into the desorber chamber at a location below the wavy filler element (1) and is directed upward to fluidize the catalyst particles inside the wavy filler element (1) and, as a result, desorb the volatile hydrocarbons associated with the catalyst particles. Because the catalyst particles are well fluidized by the gas stream, a higher degree of processing efficiency can be achieved compared to known desorption processes.

[0046] The separated gas stream containing stripped volatile hydrocarbons may be directed from the stripper to a fluid catalytic cracking reactor (not shown) or to another desired location via the flow line. The desorbed catalyst particles are carried in another flow path from the desorber to a regenerator which burns coke on and within the catalyst to effectively restore the activity of the catalyst particles. The catalyst particles can then be returned to the fluid catalytic cracking reactor (not shown). The gas from the upper chimney of the regenerator is sent to a scrubber (not shown) or otherwise treated. Cyclone separators (not shown) are used in both the regenerator and the fluidized catalyst cracking reactor to remove entrained catalyst particles from the separated gas streams.

[0047] The results described above reflect the advantages of the desorption device according to the embodiments described herein. In particular, the improved contact between the gaseous fluid and the catalyst particles in the corrugated filler element (1) results in reduced hydrocarbon entrainment into the regenerator and a reduction in the required regenerator combustion load and the amount of volatile hydrocarbon components that, when transferred to the regenerator, preferentially burn in the rarefied space, resulting in high temperatures that can adversely affect the mechanical integrity of the regenerator components.

[0048] It should be understood that the embodiments disclosed herein as defined by the appended claims should not be limited to the specific details set forth in the foregoing description, as many obvious variations are possible.

Claims (37)

1. A gas-solids fluidized bed vessel having a shell and an open inner area within the shell; at least one corrugated filling element located inside the open inner area and containing a plurality of corrugated and/or ribbed flat posts located in alternating intersecting planes, which provide a plurality of open spaces between or next to the alternating intersecting flat posts, and the corrugated filling element has three-dimensional lattice configuration; solid particles in the corrugated filling element and at least one gas flow flowing towards the solid particles through the corrugated filling element and causing fluidization of the solid particles inside the corrugated filling element to form a fluidized bed with gas and solid particles. 2. The gas and solids fluidized bed vessel of claim 1, wherein the corrugated flat struts comprise longitudinal or transverse vertices and troughs, or combinations thereof. 3. The gas and solids fluidized bed vessel of claim 2, wherein the tops and bottoms are at an angle of less than 90 degrees from the line of inclination of said flat post when assembled into a corrugated filling element. 4. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-3, in which the corrugated filling element contains corrugated flat posts. 5. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-4, in which the corrugated filling element contains ribbed flat posts. 6. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-5, in which the ribs of the ribbed flat posts are located at an angle of less than 90 degrees from the line of inclination of the flat posts when assembled into a wavy filler element. 7. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-6, in which the corrugated and/or ribbed flat posts contain one or more holes. 8. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-7, in which the height of the corrugated filling element is from about 1 inch (25.400 mm) to about 36 inches (914.4 mm). 9. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-8, in which the height of the corrugated filling element is from about 6 inches (152.4 mm) to about 24 (609.6 mm) inches. 10. The gas and solids fluidized bed vessel of claim 2, wherein the tops are from about 1/16 inch (1.5875 mm) to about 2 inches (50.8 mm) high, and the depressions are from about 1/16" (1.5875 mm) to about 2" (50.8 mm) deep, and the width of the peaks and valleys is from about 1/4 inch (6.350 mm) to about 24 inches (609.6 mm). 11. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-10, wherein the fins of the ribbed flat strut are from about 1/16 inch (1.5875 mm) to about 2 inch (50.8 mm) high, and the distance between the ribs is from about 1/4 inch (6.35 mm) to about 24 inches (609.6 mm). 12. The gas and solids fluidized bed vessel of claim 2, wherein the tops and bottoms are at an angle of approximately 45 degrees from the line of inclination of the flat post when assembled into a corrugated filler element. 13. The gas solids fluidized bed vessel of claim 2, wherein the tops and bottoms are angled in the same or different directions on flat posts. 14. The gas solids fluidized bed vessel of claim 2, wherein the tops and bottoms of each flat rack are present in the same or opposite direction with respect to tops and bottoms on adjacent racks. 15. The gas solids fluidized bed vessel of claim 6, wherein the ribs of each flat strut are in the same or opposite direction to the ribs on the adjacent strut(s). 16. Vessel for a fluidized bed with gas and solid particles according to one of paragraphs. 1-15 comprising gas flow conduits communicating with the vessel to direct the gas flow into the open interior and through the corrugated filler element and to remove the gas flow from the vessel after the gas flow has passed through the corrugated filler element. 17. The gas and solids fluidized bed vessel of claim 16, comprising solids flow conduits in communication with the vessel for directing the solids to the corrugated filler and removing the solids from the vessel after flowing through the corrugated filler. 18. The gas and solids fluidized bed vessel of claim 17, wherein said gas flow conduits and solids conduits are arranged to provide countercurrent solids and gas. 19. The gas-solids fluidized bed vessel of claim 17, wherein said solids are catalyst particles. 20. A method for fluidizing solid particles in a vessel having a shell and at least one wavy filling element located in an open internal area inside the shell, moreover, the corrugated filling element contains a plurality of corrugated and/or ribbed flat posts located in alternating intersecting planes, which provide a plurality of open spaces between or near the alternating intersecting corrugated flat posts, and the corrugated filling element has a three-dimensional lattice configuration, and this method includes the following stages: ensuring the amount of solid particles inside the corrugated filler element and performing fluidization of solid particles in the corrugated filling element by flowing at least one gas flow through said element. 21. The method of claim 20, further comprising the step of directing solid particles through the corrugated filler element in a direction opposite to the direction of gas flow. 22. The method of claim 21, further comprising the step of providing additional solids to the corrugated filling element, removing at least some of the fluidized solids from the corrugated filling element as a gas flow passes through the corrugated filling element. 23. The method according to one of paragraphs. 20-22, also comprising the step of retaining said amount of solid particles in the corrugated filler element while flowing a gas flow through the corrugated filler element. 24. The method according to one of paragraphs. 20-23, according to which the solid particles are catalyst particles associated with volatile hydrocarbons, moreover, at the stage of flowing a gas stream through a corrugated filling element, at least some of the volatile hydrocarbons are desorbed from the catalyst particles by means of a gas stream during said fluidization. 25. The method of claim 24, wherein the gas stream contains water vapor. 26. The method according to one of paragraphs. 20-25, according to which the solid particles are catalyst particles containing coke deposits, and also comprising a step of burning coke deposits to regenerate catalyst particles during said step of flowing said gas stream through the contacting device.

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