Filler system and method for fluidizing solid particles within a vessel

Abstract

The present disclosure relates to a packing system and a method for fluidizing solid particles within a vessel. The packing system includes at least one packing element defining a longitudinal axis and configured to promote contact between a fluid and a solid in a fluidized bed; the at least one packing element includes a common horizontal bar defined parallel to the longitudinal axis and a plurality of primary lamellas extending angularly from the common horizontal bar, wherein a primary element plane is defined by a lamella axis of at least one primary lamella and the longitudinal axis; the at least one packing element includes at least one additional lamella extending in a secondary plane, wherein the secondary plane is non-parallel to the primary element plane. The packing system promotes mixing of steam and catalyst.

Description

[0001] This divisional application is based on Chinese invention patent application No. 201980046673.1 (international application No. PCT / US2019 / 034006), entitled "Stripper and Packing Device", filed on May 24, 2019.

[0002] Cross-references to related applications

[0003] This application claims priority to U.S. Provisional Patent Application Group No. 62 / 675,975, filed May 24, 2018, which is incorporated herein by reference in its entirety. Technical Field

[0004] This invention relates to fluidized beds in which solids and fluids flow in a counter-current or co-current relationship. More specifically, embodiments disclosed herein relate to fluidized catalytic cracking (FCC) stripper units and internal components, and even more specifically to structured packing elements for promoting contact between solids and fluids in a fluidized bed. Background Technology

[0005] Fluid catalytic cracking (FCC) is a common chemical process in refineries aimed at converting high-molecular-weight heavy hydrocarbons into lighter, lower-molecular-weight hydrocarbon fractions. In this type of process, the hydrocarbon feedstock is evaporated at high temperatures while simultaneously contacting particles of cracking catalyst suspended in and entrained by the feedstock vapor. After the cracking reaction produces the desired molecular weight range and the boiling point decreases accordingly, the resulting product vapor is separated from the catalyst particles. The particles are then stripped to recover any entrained hydrocarbons, regenerated by burning the coke formed on the particles, and recycled by re-contaminating the feedstock for cracking.

[0006] In this process, the desired reduction in the boiling point of hydrocarbons is achieved through controlled catalytic and thermal reactions. These reactions occur almost immediately when the fine mist feedstock comes into contact with the catalyst particles. Within the short time of contact between the catalyst particles and the feedstock, the particles are essentially deactivated due to hydrocarbon adsorption and the deposition of coke and other contaminants on the active sites of the catalyst. It is necessary to continuously strip (e.g., with steam stripping) the deactivated catalyst to recover the adsorbed and entrained volatile hydrocarbons in the pores before regenerating the catalyst (by controlling the combustion of coke in a single or multi-stage regeneration section before returning the catalyst particles to the reaction zone, thereby continuously regenerating the catalyst without altering its properties).

[0007] Stripping is one of the decisive steps in the FCC process. In fact, insufficient stripping results in reactor effluent remaining on and between catalyst particles, leading to an additional combustion load on the regenerator during the regeneration step, generating excessive heat beyond what is needed to drive the catalytic reaction. Consequently, the combustion of hydrocarbon-entrained vapors entering the regenerator represents a loss in the final yield of the conversion products.

[0008] In FCC processes, catalyst stripping typically takes place in deep fluidized beds to promote vigorous mixing and close contact between the fluid flow and catalyst particles within the vessel, and to provide sufficient residence time for stripping. Baffles (e.g., flakes) and packing materials are used to achieve the desired contact. Fluidized beds are generally created by forcing a fluid flow (typically a vapor flow) upward through a bed of solid particles at a velocity sufficient to suspend the particles and induce gas-solid mixing within the bed.

[0009] Typically, after separating the reactor effluent from the catalyst particles, the particles are guided to a stripping chamber where stripping is performed in a descending, dense fluidized phase. A gaseous fluid injected at the bottom of the chamber fluidizes the coking catalyst particles and displaces hydrocarbons trapped in the interstitial spaces between the particles. For this gaseous fluid, a polar material (e.g., steam) is preferred because it is more strongly adsorbed by the catalyst particles, making hydrocarbon displacement easier. Finally, the stripped catalyst particles are transferred to a regeneration zone.

[0010] In FCC stripper vessels, controlling catalyst particle movement is often difficult, and localized defluidization associated with cross-flow (large bubbles flowing directly through a deep fluidized bed or catalyst preferentially flowing downwards towards one side of the vessel) and backmixing (downward flow of poorly fluidized particles or even the recirculation of such particles, especially in the stripping chamber wall region) is hard to avoid. Therefore, controlling the average stripping time of deactivated catalyst particles and the quality of contact between catalyst particles and the gaseous fluid is challenging. Furthermore, any uneven distribution or preferential flow patterns of gas vapor and catalyst particles limit the catalyst's recirculation capacity through the stripper vessel. Typically, excess steam is required in such scenarios to achieve sufficient stripping efficiency. Excess steam increases the gas and liquid loads on equipment connected to the stripper. For example, excess steam increases the amount of acidic water produced per pound of hydrocarbon processed and increases the operating costs for producing and processing the excess steam.

[0011] To overcome these problems, it is necessary to utilize devices within the stripper chamber (such as structured packing elements) to promote effective mixing and improve particle dispersion and homogenization through the stripping fluid. Specifically, as particles pass through the stripping unit, they are redistributed in space, ensuring an organized and agitated state with the fluid and promoting improved contact between the fluid and particle phases. This guides the fluid and particles from a single flow to multiple directions. Furthermore, the device reduces backmixing and cross-contamination of particles, as well as the formation of solid or gas vortices within the stripping chamber.

[0012] Using structured packing elements as internal stripping devices allows for a reduction in the size of the contact area between solid particles and the fluid. In fact, because this contact is significantly improved, a smaller stripping chamber can be used compared to existing technologies, without sacrificing stripping performance even at high catalyst flow rates through the stripping chamber. Therefore, the primary objectives of the packing elements are: to provide uniform counter-current flow contact between catalyst particles and steam (or other gaseous media); to prevent gas bypassing or channeling through the catalyst bed; and to reduce the size of bubbles formed in the fluidized bed.

[0013] Different structured packing elements have been proposed to improve stripping. For example, U.S. Patent No. 6,224,833 to Rall et al. discloses a gas-solid fluidized bed formed within a contact element having paired planar portions or sheets arranged in intersecting planes. Rall et al. Figure 7 The form of structured packing applied to solid flows is shown. Structured packing systems can provide excellent performance; however, they tend to generate cross-flow between the two phases. Once cross-flow begins, it continues through the bed and, if the bed is deep enough, will lead to almost complete phase separation. Once started, cross-flow is difficult to stop and may almost completely bypass both phases. Once a “net flow” of either phase is formed, existing packings are not very effective in redistributing said phases; examination of actual packings shows that a single phase can travel considerable distances within and between layers. Once they reach the next layer, the possibility of redistribution becomes very limited, and the single phase will continue and may expand.

[0014] In FCC strippers, the mass flow rate difference between steam and catalyst is very high, and due to the fluidized nature of solids, local crossflow tends to occur around the sheet elements. Computational fluid dynamics (CFD) studies show that a dense catalyst layer forms along the top side of the sheet, while a gas flow (steam) forms on the bottom side. This effectively stops the mixing required for the stripping process.

[0015] Another limitation of the existing design is the bidirectional arrangement of the fins, which provides approximately 95% of the open cross-sectional area and restricts radial mixing. The fin arrangement results in a uniform downward distribution of the catalyst within localized regions. Overall, if the catalyst flow entering the top element is deflected, a very large packing height is required before the catalyst flow is uniformly redistributed across the entire bed. Consequently, the upward-flowing steam is also not uniformly distributed within the element, and as it exits the top of the packing, it further reduces the steam's usability for stripping hydrocarbons.

[0016] In a particular FCC stripper design as described in U.S. Patent Application No. US2009 / 0269252 (the entire contents of which are incorporated herein by reference), Figure 1 (Published in the United States 2009 / 0269252) Figure 1 The diagram illustrates a common configuration for an FCC stripper. The catalyst exits the stripper through an SCSP located on one side of the stripper vessel. This causes the catalyst to flow more predominantly towards the region near the SCSP inlet. This skewed catalyst flow, caused by the asymmetrical SCSP inlet, results in a stagnant region opposite the SCSP inlet. Because the catalyst flows only through a reduced stripper cross-sectional area, the active catalyst flow zone near the SCSP inlet leads to a higher catalyst velocity. This higher catalyst velocity or flow zone entrains a significant amount of stripping steam into the SCSP, resulting in reduced stripping due to the lower upward steam velocity entering the stripper.

[0017] Existing packing designs are very dense in terms of the number of fins and must support a considerable weight. Because the fins support a portion of the catalyst mass, dense packing also exhibits low pressure buildup. Existing structures used in FCC strippers, such as those shown in US Patent Application No. US2009 / 0269252, offer many benefits to the FCC process compared to conventional disc and annular baffle systems. However, it typically does not produce the expected performance improvements: crude stripping efficiency (reflected in H2 in coke and regenerator temperature), pressure buildup, and steam consumption. This can be attributed to phase separation around the packing elements and cross-flow / non-uniform fluidization within the packing zone. Steam / catalyst phase separation and cross-flow reduce the likelihood of mixing required to facilitate the mass transfer needed for stripping.

[0018] In existing designs using long, flat flakes, interphase mixing within a given packing layer is typically not promoted. CFD studies have shown that discrete catalyst and gas phases are formed at the surface of the flakes. This reduces the contact time and mixing required for stripping.

[0019] Current structured packed elements have various limitations. For example, because a portion of the gas flow tends to flow upwards along the underside of the planar portion or sheet, while a portion of the catalyst flow tends to flow downwards from the top side of the sheet, there is little interaction between the gas and the catalyst, thus reducing the mixing of stripping gas and catalyst. This limits gas-catalyst mixing within the element. The sheet-like construction of conventional packed elements only allows bidirectional phase flow within the element, which limits radial mixing within the packed element. Although the flow directions of each element or element layer are oriented 90° to each other, the continuous sheet surface cannot provide good catalyst and gas redistribution across the entire depth of the fluidized bed.

[0020] Such conventional methods and systems are generally considered satisfactory for their intended purposes. However, there remains a need in the art for improved packing elements and systems. Other objectives of embodiments of the invention will become apparent from the following overview and detailed discussion. Summary of the Invention

[0021] The packing system includes: a first packing element layer comprising a plurality of sheets; and a second packing element layer comprising a plurality of sheets. The packing system includes at least one of intra-layer variation or inter-layer variation. Intra-layer variation includes at least one of: (i) a change in the spacing between sheets within at least one of the first or second packing element layers; (ii) a change in the size of the sheets within at least one of the first or second packing element layers; or (iii) a change in the tilt angle of the sheets within at least one of the first or second packing element layers. Inter-layer variation includes: the sheets of the first packing layer having a first spacing, a first size, and a first tilt angle; and the sheets of the second packing layer having a second spacing, a second size, and a second tilt angle. At least one of the second spacing, the second size, or the second tilt angle differs from at least one of the first spacing, the first size, or the first tilt angle.

[0022] In some embodiments, the sheets of the first filler element layer include a first set of sheets having a first width and a second set of sheets having a second width, wherein the second width is narrower than the first width. The first set of sheets may include two sets of sheets. The first set of sheets may be arranged at a first tilt angle, and the second set of sheets may be arranged at a second tilt angle. The second set of sheets may include two sets of sheets. The first set of sheets may be arranged at a third tilt angle, and the second set of sheets may be arranged at a fourth tilt angle. The first tilt angle may be different from the third tilt angle. The first tilt angle and the second tilt angle may be opposite angles to each other. The first set of sheets may be parallel to each other. The second set of sheets may be parallel to each other.

[0023] In some embodiments, the second set of sheets comprises two sets of sheets. The first set of the two sets of the second set of sheets can be arranged at a first tilt angle, and the second set of the two sets of the second set of sheets can be arranged at a second tilt angle. The first tilt angle and the second tilt angle can be opposite angles. The first set of the second set of sheets can be parallel to each other. The second set of the second set of sheets can be parallel to each other.

[0024] The sheet of the first filler element layer can be spaced apart from the adjacent sheet of the first filler element layer by a first distance, wherein the sheet of the second filler element layer can be spaced apart from the adjacent sheet of the second filler element layer by a second distance, the second distance being smaller than the first distance.

[0025] The system may include at least one additional filler element layer. The at least one additional filler element layer may be disposed vertically below the second filler element layer, opposite to the first filler element layer. The at least one additional filler element layer may include multiple sheets. The sheets of the additional filler element layer may have the same angle, spacing, and dimensions as the sheets of the first filler element layer. The tilt angle of the sheets of the additional filler element layer may be the same as and opposite to that of the sheets of the first filler element layer.

[0026] According to another aspect, the packing system includes at least one hollow cone to facilitate contact between solids and fluids in the fluidized bed.

[0027] At least one hollow cone may include multiple hollow cones. At least one of the multiple hollow cones may be adjacent to at least one adjacent hollow cone. At least one hollow cone may include a slot disposed around its perimeter. At least one hollow cone may include a longitudinally extending connecting band disposed between the respective slots. At least one connecting band may include a hole. Each longitudinally extending connecting band may extend between the top edge and the bottom edge of the hollow cone. At least one hollow cone is a truncated conical hollow body.

[0028] The system may include a gas passage. At least one hollow cone may taper from an upstream portion toward a downstream portion of the gas passage. The at least one hollow cone may include a first hollow cone and a second hollow cone. Each of the first and second hollow cones may include a respective longitudinally extending connecting band and a respective bottom edge. A portion of the bottom edges of the first and second hollow cones may be adjacent to each other. Each longitudinally extending connecting band may define a respective connecting band axis, wherein, when projected onto a plane perpendicular to the longitudinal main axis of the first hollow cone, the connecting band axis of the first hollow cone and the connecting band axis of the second hollow cone may be coaxial. At least one hollow cone may include at least a partially closed top surface.

[0029] At least one hollow cone may include multiple hollow cones. Each hollow cone may define a longitudinal main axis. Multiple hollow cones may be arranged in a first layer and a second layer, the first layer having a first group of multiple hollow cones, and the second layer may have a second group of multiple hollow cones disposed above the first layer. The corresponding bottom edges of the second group of multiple hollow cones may abut the corresponding top edges of the first group of multiple hollow cones. The first layer may be offset from the second layer such that the longitudinal main axis of the hollow cones in the first layer may be coaxial with the longitudinal main axis of the hollow cones in the second layer.

[0030] According to another aspect, at least one packing element defines a longitudinal axis and is configured to facilitate contact between solids and fluid in a fluidized bed. The at least one packing element includes a common crossbar defined parallel to the longitudinal axis and a plurality of main lamellae extending at an angle from said common crossbar. The plane of the main element is defined by the lamellae axis of at least one main lamellae and the longitudinal axis. The at least one packing element includes at least one additional lamellae extending in a secondary plane. The secondary plane is not parallel to the element plane.

[0031] At least one packing element may include two packing elements. At least one additional sheet of the first packing element may intersect the element plane of the second packing element of the two packing elements. The main sheets may be spaced apart from each other along a longitudinal axis. At least one additional sheet may include multiple additional sheets. The main sheets and additional sheets may extend from both sides of the crossbar. At least one additional sheet may include multiple additional sheets. The main sheets and additional sheets may alternate with each other along a longitudinal axis. The two packing elements may form a mixing chamber. The mixing chamber may be defined between a main sheet and an additional sheet of the first packing element of the two packing elements and a main sheet and an additional sheet of the second packing element of the two packing elements. When projected onto a plane perpendicular to the longitudinal axis of the first packing element, the shape of the mixing chamber may be a parallelogram.

[0032] At least one packing element may be formed from a sheet of a single material. At least one packing element may comprise multiple packing elements forming a layer of the packing system. A second set of packing elements may form a second layer of the packing system. The second layer may be positioned vertically above the first layer. The first and second layers may define an axis oriented vertically parallel to the overall steam flow direction. The element plane of each packing element in the first and second layers may be inclined relative to the vertically oriented axis.

[0033] According to another aspect, a method for fluidizing solid particles within a container having a shell and at least one packing system includes: providing a quantity of said particles within the packing system; and using the packing system to generate fluidization of the solid particles by flowing at least one gas stream through the packing system. The at least one packing system includes at least one of the packing systems described above.

[0034] This method may include guiding solid particles through a packing system in a direction opposite to the flow direction of the gas flow. The method may include providing an additional amount of solid particles within the packing system while at least some of the fluidized solid particles are removed from the packing system as the gas flow passes through it. The method may include maintaining a certain amount of solid particles in the packing system as the gas flow passes through it. The solid particles may be catalyst particles associated with volatile hydrocarbons, and wherein at least some volatile hydrocarbons can be stripped from the catalyst particles by the gas flow during the fluidization process as the gas flow passes through the packing system. The gas flow may include water vapor. The solid particles may be catalyst particles containing coke deposits. The method may include burning the coke deposits to induce regeneration of the catalyst particles as the gas flow passes through the contact device.

[0035] These and other features of the system and method of the present invention will become more apparent to those skilled in the art from the following detailed description of preferred embodiments in conjunction with the accompanying drawings. Attached Figure Description

[0036] To enable those skilled in the art to readily understand how to manufacture and use the apparatus and method of the present invention without excessive experimentation, preferred embodiments will now be described in detail with reference to certain accompanying drawings, wherein: Figure 1 A schematic side view of an FCC stripper vessel having a packing system constructed according to an embodiment of the present invention, showing multiple layers of packing elements; Figure 2 A schematic side view of an FCC stripper vessel having a packing system constructed according to another embodiment of the present invention, showing multiple layers of packing elements; Figure 3 A schematic side view of an FCC stripper vessel having a packing system constructed according to another embodiment of the present invention, showing multiple layers of packing elements; Figure 4A A schematic side view of an FCC stripper vessel having a packing system constructed according to another embodiment of the present invention, showing multiple layers of packing elements; Figure 4B for Figure 4B A schematic side view of a portion of an FCC stripper container, showing multiple thin sheets with slots; Figure 5A The schematic top view of a packing system constructed according to another embodiment of the present invention shows the sheet orientation and sheet width / flow distribution of two vertically stacked layers, wherein the first layer includes two regions with variable sheet widths, and the second layer (below the first layer) includes sheets with the same sheet width. Figure 5B Show Figure 5A A graph showing the decomposition of the sheet orientation and sheet width / flow distribution of the additional layers in the system; Figure 6A for Figure 5A A schematic perspective view of a layer, showing that the sheet in the layer has a non-uniform (varying) sheet width in each region within the layer; Figure 6B for Figure 6A A schematic top view of the layer, showing that the flasks of the layer have uneven (varying) flask widths in a region of the layer; Figure 7 A schematic top view of a portion of a packing system constructed according to another embodiment of the invention, showing a truncated conical packing element; Figure 8 for Figure 7 A schematic side view of the packing system, showing a truncated conical packing element; Figure 9 A schematic top view of a portion of a packing system constructed according to another embodiment of the present invention shows a truncated conical packing element having bent tabs; Figure 10A A schematic side view of a portion of a packing system constructed according to another embodiment of the present invention shows a truncated conical packing element having a connecting strip with holes in the connecting strip; Figure 10B for Figure 10A A schematic top view of a packing system, showing a truncated conical packing element with a connecting band and holes in the connecting band; Figure 11A for Figure 7 A schematic side view of the packing system, showing the top layer of a truncated conical packing element with a closed top surface; Figure 11B This is a schematic top view of a packing system constructed according to another embodiment of the present invention, showing a truncated conical packing element with a closed top surface; Figure 12 A schematic perspective view of a portion of a packing system constructed according to another embodiment of the present invention, showing a plurality of packing elements; Figure 13 for Figure 12 A schematic perspective view of a portion of a packing system, showing a sheet of one of the packing elements; Figure 14 for Figure 12 A schematic perspective view of a portion of a packing system, showing a sheet of one of the packing elements; Figure 15 According to Figure 12 A schematic perspective view of the constructed packing system, showing two layers of packing elements; Figure 16A for Figure 15 A schematic side view of a portion of a packing system, showing multiple packing elements; Figure 16B for Figure 15 A schematic side view of a portion of a packing system, showing adjacent packing elements with overlapping sheets; Figure 16C for Figure 15 A schematic front view of a portion of a packing system, showing a sheet of one of the packing element layers, accompanied by cut lines after the perimeter of the packing system has been formed into a circle; Figure 17 for Figure 15 A schematic top view of a portion of the packing system, showing the top side of the packing element layer; Figure 18A for Figure 15 A schematic perspective view of a portion of a packing system, showing a packing element after bending; Figure 18B for Figure 15 A schematic side view of a portion of a packing system, showing a single “sheet” of a packing element after bending; Figure 19 for Figure 15 A schematic perspective view of a portion of a packing system, showing a part of a packing element before bending; and Figure 20 According to Figure 12 A schematic three-dimensional view of the constructed packing system, showing a layer of packing elements. Detailed Implementation

[0037] Embodiments of the invention will be described more fully below with reference to the accompanying drawings, in which exemplary embodiments of the invention are illustrated. However, the invention may be embodied in many different forms and should not be construed as limited to the exemplary embodiments set forth herein. Rather, these embodiments are provided so that the invention is complete and exhaustive, and to fully convey the scope of the embodiments to those skilled in the art. The same numerals always denote the same, but not necessarily identical or completely identical, elements. For purposes of illustration and description and not limitation, Figure 1 The figure shows a schematic diagram of an exemplary embodiment of a packing system constructed according to an embodiment of the present invention, the packing system being configured to facilitate contact between solids and fluids in a fluidized bed, generally indicated by reference numeral 100. Figures 2 to 19 Other embodiments or aspects thereof of the packing system according to the invention are provided and will be described.

[0038] Figures 1 to 6B A packing system 100 is shown, which includes optimization of FCC stripper performance using a multi-zone approach, the multi-zone approach employing multi-size structured packing and / or more than one type of internal components. (See also...) Figures 5A to 6B As shown, in an FCC vessel with an asymmetric riser, stripping packing with multiple slabs of varying widths and spacings within or across packing element layers allows for a more uniform distribution of the gaseous catalyst flow within the catalyst bed (sometimes referred to as the "bed" throughout). The catalyst bed is a dense but fluidized collection of catalyst particles into which a stripping medium (typically steam) is injected to transfer volatile hydrocarbons. The steam maintains the fluidization of the particles, while the internal components of the stripper bed maintain close contact between the stripping medium (e.g., packing system 100) and the particles.

[0039] As in Figures 1 to 4A As shown, the packing system 100 includes multiple packing element layers 102a-102h. Figures 1 to 4A A side view of the container 103, shown in cross-section, illustrates the packing element layers 102a-102h. Each packing element layer 102a-102h comprises multiple sheets 104a-104h. Each sheet 104a-104h has a... Figure 6A The thin sheets shown have a similar rectangular shape, and the thin sheets 104a-104h can also be arranged in parallel (with...). Figure 6ASimilar to the sheet material, a layer is formed. This layer can be cylindrical or annular, or various other suitable shapes. The packing system 100 includes intra-layer variations and / or inter-layer variations. Intra-layer variations are variations or inconsistencies within a given layer of packing element layers 102a-102h. Intra-layer variations include: variations in the spacing between sheets 104a-104h in the respective packing element layers 102a-102h, variations in the size of sheets 104a-104h in the respective packing element layers 102a-102h, and / or variations in the tilt angle of sheets 104a-104h in the respective packing element layers 102a-102h. Interlayer variations include: a sheet 104a-104h of a given layer of filler layers 102a-102h having a first spacing, a first tilt angle, and a first size; and a sheet of a different layer of filler layers 102a-102h having a second spacing, a second tilt angle, or a second size. The second spacing, second tilt angle, and / or second size differs from the first spacing, first tilt angle, and / or first size.

[0040] As in Figure 1 As shown, system 100 includes a first filler element layer 102a, which has sheets 104a that are closer together than the sheets 104c of the third filler element layer 102c. The sheets 104a of the first filler element layer 102 are also shorter in length than the sheets 104c of the third filler element layer 102c (e.g., their dimensions are different). Figures 2 to 4A Different embodiments are shown regarding the interlayer variations in the dimensions of sheets 104a-104h, the spacing between sheets 104a-104h, and the tilt angle of sheets 104a-104h. The spacing between sheets is defined as the vertical distance between the panels of sheets 104a-104h.

[0041] Figures 1 to 4A Structured packing utilizes a multi-size modular design to optimize FCC stripper performance through a multi-zone approach, employing multi-size structured packing and / or more than one type of internal component. For Figures 1 to 4A The "region" includes at least one filler element layer 102a-102h. For example, for Figure 1 The implementation scheme includes a first region comprising layers 102a and 102b, wherein each layer 102a and 102b is structurally similar to the other. Figure 1 The second region of the implementation scheme includes layers 102c-102f, wherein layers 102c-102f have similar structures to each other.

[0042] Several implementation schemes for different packing arrangements are proposed to achieve the purposes described herein. Figure 1 The packing elements are shown to be more compact in the top and bottom layers (e.g., layers 102a-102b and 102g-102h), while the middle region is filled with more open layers, such as the third, fourth, fifth, and sixth layers 102c-102f, respectively. The top two layers 102a-102b promote good downward distribution of the catalyst (as shown in...). Figures 1 to 4A The steam (directed from the center) is directed into the bed, and the bottom two layers of 102g-102h help to direct the upward-moving steam (such as in...) Figures 1 to 4A The particles are evenly distributed in the bed (in a directional manner). Figure 1 The more compactly packed flakes 104a-104b in the packing layers 102a and 102b provide regions for optimal catalyst distribution, while the more open regions formed by layers 102c-102f are optimized for better fluidization. Figure 1 The third zone is formed by the bottom two layers 102g-102h and includes more compactly packed flakes 104g-104h, providing optimal steam distribution. Using multi-size structured packing or multiple types of internal components optimizes the configuration, resulting in improved stripping efficiency and improved fluidization. Improved stripping performance allows for reduced stripping steam, fewer internal components, improved product recovery, and reduced coke load on the regeneration system. For improved schemes, the multi-zone approach also provides additional flexibility to achieve the desired outcome. The multi-zone approach provides improved stripping efficiency by optimizing catalyst / steam contact and improving the fluidization of the catalyst bed in the FCC stripper.

[0043] Figure 2 Another embodiment of system 100 is shown, wherein the top four layers 102a-102d have more compactly packed sheets 104a-104d to maximize the interaction of the steam catalyst and the stripping efficiency. Figure 2 The bottom four layers, 102e-102h, are essentially for the purpose of fluidizing the bed uniformly. Figure 2 A first region with four top layers 102a-102d is shown, wherein the four top layers 102a-102d are structurally similar to each other. Figure 2 The more compactly packed sheets 104a-104d in the packing layers 102a-102d provide areas for optimizing the distribution of steam and catalyst. Figure 2 The second region comprises four bottom layers 102e-102h, which have similar structures to each other. Figure 2 The more open regions formed by layers 102e-102h are optimized for better fluidization (e.g., more uniformity).

[0044] Figure 3 Another embodiment of system 100 is provided, wherein the top four layers 102a-102d have more spaced thin sheets 104a-104d so that the open area is sufficient for the self-stripping of hydrocarbons from the spent catalyst; and more compact elements are used at the bottom to maximize the interaction of the steam catalyst and the stripping efficiency. Figure 3 A first region with top layers 102a-102d is shown, wherein top layers 102a-102d are structurally similar to each other. Figure 3 The more open regions formed by the top layers 102a-102d (e.g., with less densely filled flakes 104a-104d) are optimized for better fluidization (e.g., more uniformity). Figure 3 The second region comprises four bottom layers 102e-102h, which have similar structures to each other. Figure 3 The more compactly packed sheets 104e-104h in the bottom four packing layers 102e-102h provide areas for optimizing the distribution of steam and catalyst.

[0045] Stripping efficiency is also related to residence time. Figures 4A to 4B The diagram shows a third, fourth, fifth, and sixth layer 102c-102f (e.g., more open layers) having sheets 104c-104f, the sheets 104c-104f having a 45° tilt angle (a shallower sheet angle compared to the commonly used 60° sheets) and a hole 106. Figure 4A The shallower inclined sheets 104c-104f increase the effective residence time and the contact area between the steam catalyst and the vapor catalyst. The pores 106 in the sheets 104c-104f promote the interaction between the steam catalyst and the vapor catalyst and prevent premature overflow of the stripper. Figure 4A A first region is shown, comprising a first layer 102a and a second layer 102b, wherein each layer 102a and 102b is structurally similar to each other in terms of sheet size and spacing, but the sheets 104a and 104b are at opposite angles. Figure 4A Thin sheets 104a and 104b with Figure 4A Compared to sheets 104c-104f, sheets 104a and 104b have steeper tilt angles; for example, sheets 104a and 104b can have tilt angles of approximately 60°, meaning they form an angle of approximately 30° downwards relative to the vertical axis V. Even Figure 4A The thin sheets 104a and 104b are at opposite angles to each other, but their tilt angles relative to the vertical axis V are the same. Figure 4AThe second region includes the third, fourth, fifth and sixth layers 102c-102f, wherein layers 102c-102f have similar structures to each other in terms of sheet size and spacing, but sheets 104c and 104d are at opposite angles, and sheets 104e and 104f are at opposite angles. Figure 4A The more compactly packed flakes 104a-104b in the packing layers 102a and 102b provide regions for optimizing catalyst distribution. The increased spacing between flakes 104c-104f, the varying flake angles, and the pores 106 (in the flakes 104c-104f) further enhance the catalyst distribution. Figure 4B (As shown in the diagram) can be optimized for better fluidization and increased efficiency. Figure 4A The dwell time in all layers 102c-102f. Figure 4A The third region is formed independently of the seventh and eighth layers 102g-102h and includes more compactly filled sheets 104g-104h, providing optimized vapor distribution.

[0046] Figures 1 to 4B The multi-zone design allows for optimized layout, resulting in improved stripping efficiency and improved fluidization. The embodiment of the packing system 100 disclosed herein improves the efficiency of the FCC stripper by optimizing the construction of its internal components. This is achieved by dividing the internal components of the stripper bed into two or more distinct zones, each zone containing packing elements (sheets) or devices of a specific size. Those skilled in the art will readily understand that, although... Figures 1 to 4B It is described as rectangular flat sheets arranged in a ring within a stripping container, but different shapes suitable for the sheets can also be used for various layers.

[0047] Typically, the majority of stripping occurs in the top section of the bed, where interparticle steam movement is relatively easy, and some steam within the particles is also removed. This region is relatively fluidized due to the high steam load. As the catalyst flows downwards through the bed, the stripping efficiency per unit bed height decreases exponentially. Hydrocarbons trapped in catalyst particles at lower positions in the bed must be removed, requiring more efficient contact between the stripping steam and the catalyst. Embodiments of the system 100 disclosed herein utilize multiple regions with different packing sizes (or internal component types) to optimize catalyst / steam contact. Typically, more compact packing elements (e.g., ...) Figure 1 Layers 102a-102b and 102g-102h are used for intense mixing and stripping. More open and porous packing elements (e.g., in...) are used. Figure 1 (The layers 102c-102f) are used for fluidization.

[0048] As in Figures 5A to 6BAs shown, the packing system 200 utilizes multiple slab widths (e.g., variations within the layer) in a given layer to provide a more uniform gaseous catalyst flow distribution on the catalyst bed. This variation in width is particularly useful for FCC stripper systems with an asymmetric spent catalyst riser (SCSP) arrangement. Many FCC units use a generally cylindrical stripper vessel 203 in which the catalyst is extracted from the side of the vessel 203 at outlet 205, creating an asymmetric catalyst flow pattern within the vessel 203 and the packing layer, which is amplified by the construction of elements / slabs within the packing sections. The vessel 203 can be... Figure 4A Similar to container 103. Conventional packed systems maintain open passages in only one lateral direction at each layer, then rotate the layers relative to each other in an attempt to achieve some lateral uniformity. In system 200, the open nature of the device at each layer ensures that laterally open passages are maintained in all directions, which minimizes any tendency for crossflow. Multi-width slabs 204a and 204b, described in more detail below, are arranged in the packing element layer 202 to ensure that no uneven flow distribution or preferential crossflow occurs in the bed. Improved gas catalyst flow distribution results in reduced steam entrainment and improved stripping efficiency due to better steam utilization.

[0049] Now for reference Figures 5A to 6B The packing element layer 202 in the packing system 200 includes a sheet-like structure that directionally promotes a greater flow of catalyst from the SCSP-side stripper wall (e.g., the wall near inlet 205) to the center, and simultaneously promotes a greater flow of catalyst from the wall opposite the SCSP towards the center. System 200 may also include, as in... Figures 1 to 4B The system 100 shown comprises one or more layers 102a-102h. In a standard sheet configuration, the width of the sheets pointing downwards in either direction (east-west or north-south) is the same, thus ensuring an equal distribution of catalyst flow on each side of the sheet within the layer (e.g., 50% catalyst in one direction and 50% catalyst in the other). This can be achieved through... Figure 5A The diagram shows the southern part of unit 201 on the second floor. North, south, east, and west are... Figure 5A and Figure 6A The symbols N, S, E, and W are used to represent them. Figures 5A to 6B In one embodiment, for at least one layer in the filler system 200, the widths of the sheets 204a and 204b are different from those of the adjacent layers in each direction.

[0050] As in Figures 5A to 5B As shown, each layer, such as layer 201 or 202, can have an overall annular shape, and different numbers of layers can exist. Figure 5BIn the proposed implementation, there are a total of eight layers, some similar to the first layer 202, and some similar to the second layer 201. The eight layers are arranged in an alternating vertical configuration such that the first and third layers are identical (with sheets of different widths within each layer, as in layer 202), and the second and fourth layers are identical (with sheets of constant width within each layer, as in layer 201). This is achieved by… Figure 5B The table and the ratio of the provided sheet widths (70 / 30 for variable widths and 50 / 50 for constant width sheets) are shown.

[0051] As in Figures 6A to 6B As shown, the sheets 204 of the first filler element layer 202 include a first set of sheets 204a having a first width W1 and a second set of sheets 204b having a second width W2, wherein the second width W2 is narrower than the first width W1. The first set of sheets 204a includes two sets of sheets (those in regions A and B). The first set of sheets (e.g., the sheets 204a in region A) is arranged at a first angle, and the second set of sheets (e.g., the sheets 204b in region B) is arranged at a second angle. The first angle and the second angle are arranged at opposite angles to each other. In other words, the inclination angles relative to the vertical axis of the container 203 are the same, but some sheets 204a are inclined downwards from west to east, while other sheets 204a are inclined downwards from east to west. The second set of sheets 204b includes two sets of sheets.

[0052] Continue to refer to Figures 6A to 6B The first group of two sets of the second set of sheets 204b (e.g., sheet 204b in region A) is arranged at a third angle, and the second group of two sets of the second set of sheets 204b (e.g., sheet 204b in region B) is arranged at a fourth angle. The third and fourth angles are opposite angles. The first angle is opposite to the third angle. For example, if the typical sheet width is 5 inches, then as in Figure 6A As shown, region A (northwest and southwest quadrants) may have a 7-inch sheet 204a pointing downwards from east (illustratively shown by directional arrows on the plate 204a) and a 3-inch sheet pointing downwards from east to west. On the other hand, region B (northeast and southeast quadrants) has a 3-inch sheet 204b pointing downwards from west to east and a 7-inch sheet 204a pointing downwards from east to west (illustratively shown by directional arrows on the sheet 204a). The wider sheet 204a will allow for an increased percentage of catalyst flow along that direction (illustratively shown by directional arrows on the upward-facing surface of the sheet 204a). This will facilitate the transfer of more catalyst flow from the SCSP stripper side (e.g., the west side) towards the center, and simultaneously promote more catalyst flow from the wall side opposite the SCSP (e.g., the east side) towards the center.

[0053] Those skilled in the art will readily understand that the sheet width is not limited to three inches or seven inches; these dimensions are provided merely for illustrative purposes. Furthermore, the sheet spacing in regions A and B can be varied as needed, for example, if the filler in region B is loose (with...). Figure 1 Similar to the thin sheets of 104c, it allows for freer flow, while the packing in region A is more compact (similar to...). Figure 1 (Similar to the thin sheet 102a) to achieve more intense mixing and stripping. A wider spacing will have less flow resistance and reduce cross-flow of gas vortices beneath the sheet.

[0054] Compared to conventional packing systems, Figures 5A to 6B The proposed implementation provides improved flow distribution and reduces crosstalk, which tends to improve stripper performance and steam utilization, and reduce steam consumption. System 200 offers lower cost due to increased spacing, thus requiring less packing per unit volume, more uniform head in the stripper, increased head in the riser, and better stripping, which lowers regeneration temperature, increases catalyst circulation, and improves product yield.

[0055] As in Figures 7 to 8 As shown, the packing system 300 relates to a conical element design for improving the operation of an FCC stripper. The packing system 300 can be used in conjunction with... Figures 1 to 4B In containers such as 103 and similar containers. The hollow conical packing element / hollow conical packing body 302 is shown as a truncated cone 302. As described below, the hollow conical packing element / hollow conical packing body 302 utilizes a multidirectional arrangement with a significantly fewer number of "lamps" to improve stripping efficiency, improve head accumulation, and reduce steam consumption, and also utilizes a stripper packing design that makes it easy to change the height, width, and angle of the packing lamps. The packing system 300 includes a plurality of hollow truncated cones 302, wherein each truncated cone 302 is adjacent to at least one adjacent truncated cone 302 to promote contact between solids and fluid in the fluidized bed. The truncated cones are welded together to form Figure 8 and Figure 11A The structure shown is an open truncated cone 302 that provides the tortuosity and bubble formation points required to ensure adequate steam / catalyst mixing. The relatively short and narrow surface of the forming element minimizes the possibility of phase separation occurring within the element itself. The packing system 300 uses a multidirectional arrangement with a significantly fewer number of "plates" to improve stripping efficiency, improve head accumulation, and reduce steam consumption. The truncated cone (e.g., element 302) achieves this by uniformly distributing the catalyst flowing downwards through the stripper bed. The upward-flowing stripping steam has a relatively high number of bubbles and also remains uniformly distributed. This maximizes the surface area for mass transfer, thus providing excellent stripping performance.

[0056] The packing system 300 with packing element 302 is designed to reduce cross-flow mechanisms and the tendency for localized phase separation around the element surface by reducing the number of flakes and combining random flake orientation. The hollow conical packing element / hollow conical packing body 302 also distributes the catalyst more uniformly radially within the packing element below. The truncated conical packing element 302 reduces weight, thus requiring less support. Furthermore, the amount of metal required per unit volume is reduced, and the truncated conical shape is generally more structurally robust, thus requiring less thickness in the material forming the truncated conical packing element. The more open design improves pressure buildup, while the 360° lateral openness results in more uniform distribution and reduces the tendency for cross-flow.

[0057] Continue to refer to Figures 7 to 8 Each truncated cone 302 includes a slot 306 disposed around the perimeter of the body 302. Each truncated cone includes a plurality of longitudinally extending connecting bands 304 disposed between the respective slots 306. Each longitudinally extending connecting band 304 extends between the top edge (e.g., top ring 308) and the bottom edge (e.g., bottom ring 310) of the truncated cone 302. Each body 302 may include a plurality of connecting bands covering approximately 30-50% of the conical perimeter, such as 4 to 6 connecting bands, or other suitable number. The top ring 308 and the bottom ring 310 are each open to allow flow through them.

[0058] As in Figure 7As shown, each connecting band 304 of a given truncated cone 302 defines a connecting band axis L within the perimeter of the truncated cone 302. When the connecting band axis L is projected onto a plane perpendicular to the longitudinal axis A of their respective truncated cone 302, the connecting band axis L of one truncated cone 302 is not parallel to the axis L of an adjacent truncated cone 302 in the same row 303. In other words, the connecting bands 304 of adjacent truncated cones 302 in the same row are not aligned. The cones in a given row are rotated relative to each other such that, for example, a first cone 302a has connecting bands arranged at 0°, 90°, 180°, and 270° (relative to the axis perpendicular to axis A), while a second cone 302b adjacent to the first cone has connecting bands arranged at 45°, 135°, 225°, and 315°. The angle of the truncated cone is designed to allow the catalyst to flow freely through it. For example, the axis L of each connecting band forms an angle of approximately 30° to 45° relative to its respective longitudinal axis A. The width of the connecting bands is minimized, and different numbers of connecting bands 204 (3, 4, 5, 6, etc.) can be used depending on the application. The open nature of the truncated cone element / truncated cone 302 allows the gas and catalyst to move freely, but at the same time prevents vertical crossflow by forcing the phase into a vertical tortuous path, for example, when the catalyst flows downward through a connecting band 304 of a truncated cone 302, the vertical flow is interrupted by the top ring 308 or bottom ring 310 of the truncated cone below. Any large aggregates of any phase will be rapidly forced apart and moved vertically.

[0059] As in Figure 9 As shown, another embodiment of the cone 402 is illustrated. The cone 402 similarly has a truncated cone shape and includes a slot 406 and a connecting band 404 similar to those of the truncated cone 302, except that the material cut to form the slot 406 is not completely removed, and at least some of the material cut for a given slot 406 is bent inward to form a tab 411, thereby enhancing the mixing effect of the catalyst and the steam.

[0060] As in Figures 10A to 10B As shown, another embodiment of the hollow cone 502 is illustrated. The body 502 is similar to 302 in that it has a truncated cone shape and includes a slot 506 and a connecting band 504, but differs in that at least one of the connecting bands 504 includes a hole 511 to further reduce weight and improve bubble formation.

[0061] As in Figures 7 to 8 and 11A to Figure 11BAs shown, one or more of the truncated cones 302 / 402 / 502 are arranged in layers 301, which have bodies 302 arranged in rows 303. These bodies are stacked one on top of the other and welded together to form a structurally repeating packing system 300. To improve the initial distribution of the catalyst into the packed section, the top layer 301 of the element has a closed top. These cones / truncated cones are indicated by the numeral 602. The truncated cone 602 is similar to the truncated cone 302 in that it has an opening 606, a connecting band 604, and a bottom ring 610, but differs in that the truncated cone 602 has a closed top 608 instead of an open top ring 308. The closed top 608 can be in the form of a disc. This additional resistance to catalyst flow will promote better distribution. Additionally, at a selected horizontal height within the packing system 300, some individual elements 302 / 402 / 502 may have a closed top similar to, or a partially closed top, that of the closed top 608. These intermediate constraints will serve as additional redistribution devices.

[0062] As described above, compared to conventional packing designs, conical elements improve fluidization uniformity, providing better distribution at the inlet and within the bed, and increasing bubble formation / breakdown within the bed. The tortuosity of the flow path increases, but not at the expense of increased flow resistance (i.e., pressure drop). Other advantages of the embodiments described herein include: improved distribution within the packing (uniform flux of solids in the effective stripping region) promotes radial distribution; improved contact with the medium; potentially reduced stripping medium requirements; significantly fewer flakes leading to a more open design; significantly reduced likelihood of steam / catalyst crosstalk; improved head accumulation as steam flows upwards in the stripper; reduced flakes supporting catalyst mass; inherent strength of the truncated cone shape resulting in reduced material requirements, weight, and cost; increased product recovery; and reduced coke production.

[0063] As in Figures 12 to 20 As shown, the packing system 700 includes a plurality of packing elements 702 formed by a series of sheet bodies 705. (Reference) Figures 12 to 14 Each packing element 702 defines a longitudinal axis Y and is configured to facilitate contact between solids and fluid in a fluidized bed. Each packing element 702 defines an element plane B. Each packing element 702 includes a plurality of main sheets 706 extending from a common crossbar 708 defined parallel to the longitudinal axis Y, and a plurality of additional sheets 710. Some additional sheets 710a extend in a first sub-plane C, while additional sheets 710b, opposite to the additional sheets 710a on the crossbar 708, extend in a second sub-plane D. The first sub-plane C and the second sub-plane D are parallel to each other and offset. The main sheets 706 are defined within and parallel to the element plane B. The sub-planes C and D are not parallel to the element plane B. Figures 12 to 13In this implementation, the sub-planes C and D are inclined relative to the component plane B. For example, in... Figure 14 As shown, the sheet body 705 is considered to include two main sheets 706 extending from opposite sides of the crossbar 708 and two additional sheets 710a and 710b extending from opposite sides of the crossbar 708. The four sheets together form an “X” shaped sheet body with an offset between the two legs of the “X” (e.g., sheets 710a and 710b).

[0064] Now for reference Figure 15 and Figures 16A to 16C The system 700 includes a plurality of packing elements 702 arranged in parallel, wherein one of the additional sheets 710a of the first packing element 702a intersects with the element plane B of the second sheet 702b of the two packing elements. The packing elements 702 are arranged in layer 701a. For clarity, the element plane B of the second packing element 702b is not shown in the image. Figure 16A As shown, but will be defined as parallel to and aligned with the main sheet 706 of the second packing element 702b. The two packing elements 702a and 702b form a mixing chamber 712. The mixing chamber 712 is defined between a main sheet 706, crossbar 708, and additional sheet 710a of the first packing element 702a and a main sheet 706, crossbar 708, and additional sheet 710b of the second packing element 702b. When projected onto a plane perpendicular to the longitudinal axis Y of the first packing element, the shape of the mixing chamber 712 is, for example, as shown in... Figure 16B The diagram shows a parallelogram. (As shown in...) Figure 16B As shown, the catalyst is guided into the mixing chamber 712 as it flows downward along the additional sheet 710a of the packing element 702b (and between the two main sheets in the foreground and background portions) (schematically indicated by downward-angled arrows). Simultaneously, rising water vapor or other steam (from...) Figure 16B (The upward angled arrow is schematically shown) is guided into the mixing chamber 712 by the additional sheet 710b of the first packing element 702a. This facilitates the mixing of steam and catalyst.

[0065] As in Figure 19As shown, each filler element 702 is formed from a sheet 703 of a single material. The sheet of the single material is cut along a line 716 defining the additional sheet 710 on a laser or plasma bed. After or simultaneously with the cutting, each additional sheet is bent along its respective bend line 715. The bend is schematically shown by an arc-shaped arrow around the bend line 715. The bending can be performed using a bending machine. Each filler element 702, and thus the entire filler system 700, is also easier to manufacture because it is made entirely of sheet 703, which can be cut into shape on a laser or plasma bed and bent by a bending machine. There are no complex welding or bending operations required by other conventional filler system designs.

[0066] As in Figures 15 to 17 As shown, once each filler element 702 is bent and welded (or otherwise secured) to other elements, these elements can be formed into layers 701a or 701b having a cylindrical or annular shape. If needed, each filler element 702 can be welded to adjacent elements to form longer elements 702. Each element 702 forms a row within layers 701a and 701b. The ends 707 of the rows of elements 702 can be welded to a fixed perimeter band, etc., to form layers 701a and 701b; or the rows of elements 702 can be welded directly to each other, where their sheets intersect a common plane, for example, a sheet 710a of one element 702 can be welded to a sheet 706 of an adjacent element 702, where the additional sheet 710a intersects the element plane B of the adjacent element 702. These layers 701a or 701b can be stacked vertically, as in... Figure 15 As shown in the diagram, the first and second layers of the packing system define a vertically oriented axis Z parallel to the overall steam flow direction. The element plane B of each packing element 702 in the first layer 701a and the second layer 701b of the packing system is inclined relative to the vertically oriented axis Z. Layers 701a and 701b are rotated relative to each other such that their respective crossbars 708 are angled relative to each other. Now refer to... Figure 20 This shows a single layer 701a. Layer 701a and... Figures 15 to 17 It is similar to layer 701a, except that it includes more rows of filler elements 702.

[0067] Embodiments of the present invention relate to an improved stripper packing design disclosed herein, which allows for easy variation of the height, width, and angle of the packing slabs. The packing minimizes (or completely eliminates) vertical and horizontal surfaces. Vertical surfaces offer no contact benefit, while horizontal surfaces only increase the likelihood of clogging. Embodiments of the present invention are intended to make it easier to vary the height, width, and angle of the slabs, thereby enabling optimization. It is also easier to manufacture with fewer components.

[0068] The results described above reflect the advantages of the stripping system according to the embodiments described herein. In particular, the improved contact between the gaseous fluid and the catalyst particles within the structured packing system results in reduced hydrocarbon entrainment. It should be understood that because many obvious variations are possible, the embodiments disclosed herein, as defined by the appended claims, are not limited to the specific details set forth in the above description.

Claims

1. A packing system, the packing system comprising: At least one packing element, the at least one packing element defining a longitudinal axis and configured to facilitate contact between solids and fluids in a fluidized bed; The at least one packing element includes a common crossbar defined parallel to the longitudinal axis and a plurality of main sheets extending at an angle from the common crossbar, wherein the plane of the main elements is defined by the sheet axis of at least one main sheet and the longitudinal axis; the at least one packing element includes at least one additional sheet extending in a secondary plane, wherein the secondary plane is not parallel to the plane of the main elements.

2. The packing system according to claim 1, wherein, The at least one packing element comprises two packing elements, wherein the at least one additional sheet of the first packing element intersects with the element plane of the second packing element of the two packing elements.

3. The packing system according to claim 1, wherein, The main sheets are spaced apart from each other along the longitudinal axis.

4. The packing system according to claim 1, wherein, The at least one additional sheet includes a plurality of additional sheets, wherein the main sheet and the additional sheets extend from two sides of the common crossbar.

5. The packing system according to claim 1, wherein, The at least one additional sheet includes a plurality of additional sheets, wherein the main sheet and the additional sheets alternate with each other along a longitudinal axis.

6. The packing system according to claim 1, wherein, The at least one packing element includes two packing elements, wherein the two packing elements form a mixing chamber, the mixing chamber being defined between one of a main sheet and an additional sheet of a first packing element of the two packing elements and one of a main sheet and an additional sheet of a second packing element of the two packing elements.

7. The packing system according to claim 6, wherein, When projected onto a plane perpendicular to the longitudinal axis of the first packing element, the mixing chamber has a parallelogram shape.

8. The packing system according to claim 1, wherein, The at least one filler element is formed from a sheet of a single material.

9. The packing system according to claim 1, wherein, The at least one packing element includes a plurality of packing elements forming a layer of the packing system, wherein a second group of packing elements forms a second layer of the packing system, the second layer being disposed vertically above the first layer, the first layer and the second layer defining a vertically oriented axis parallel to the overall steam flow direction, and the main element plane of each packing element in the first layer and the second layer being inclined relative to the vertically oriented axis.

10. A method for fluidizing solid particles within a container, the container having a shell and at least one packing system, the method comprising: A certain amount of the particles are provided within the packing system; as well as Fluidization of solid particles is achieved by using a packing system to allow at least one gas stream to flow through the packing system. The at least one packing system includes: At least one packing element, the at least one packing element defining a longitudinal axis and configured to facilitate contact between solids and fluid in a fluidized bed; The at least one packing element includes a common crossbar defined parallel to the longitudinal axis and a plurality of main sheets extending at an angle from the common crossbar, wherein the plane of the main elements is defined by the sheet axis of at least one main sheet and the longitudinal axis; the at least one packing element includes at least one additional sheet extending in a secondary plane, wherein the secondary plane is not parallel to the plane of the main elements.

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