A gas distribution device for a desulfurization liquid regenerator

Abstract

The application discloses a gas distribution device for a desulfurization liquid regenerator, which comprises an inlet pipe, a communication pipe, a plurality of annular pipes, branch pipes and air injection ports. After entering the inlet pipe, the gas is distributed to the innermost annular pipe through the communication pipe, and then is transferred to each annular pipe outward through the branch pipes. The up-down circulation flow in the vertical direction provides macro overturning power for the liquid phase, so that the gas-liquid two-phase is fully contacted in the vertical direction. The reverse rotating shear flow in the tangential direction continuously shears and updates the gas-liquid interface in the horizontal direction. The local micro-vortex generated by the mixing unit strengthens the bubble breaking and interface mass transfer in the micro scale, and a three-dimensional and multi-level gas-liquid mixing flow field is constructed. The defects of the prior art, such as single flow direction, lack of cooperation between adjacent gas flows and existence of mixing dead zones, are overcome. The gas distribution device can significantly shorten the oxidation reaction time, reduce the suspended sulfur content of the lean liquid, improve the catalyst regeneration rate, reduce the gas supply demand of the oxidation fan and reduce the system operation energy consumption.

Description

Technical Field

[0001] This application relates to the field of desulfurization liquid regeneration tower technology, and in particular to a gas distribution device for a desulfurization liquid regeneration tower. Background Technology

[0002] In wet oxidation desulfurization processes, the desulfurization liquid regeneration tower is the core equipment for achieving catalyst oxidation regeneration. The rich desulfurization liquid, having absorbed hydrogen sulfide, comes into contact with air inside the regeneration tower. The reduced catalyst in the rich liquid is oxidized to its oxidized state under the action of dissolved oxygen, restoring its desulfurization activity. Simultaneously, sulfide ions are oxidized to elemental sulfur and released, thus achieving the recycling and regeneration of the desulfurization liquid.

[0003] Currently, commonly used gas distribution devices in industry mainly include spear-type distributors and pipe network distributors. Spear-type distributors consist of several nozzles with a single outlet direction. The gas mainly rises vertically, resulting in weak horizontal mixing. Dead zones easily form between adjacent nozzles, leading to incomplete local oxidation. Pipe network distributors consist of main pipes, branch pipes, and outlets in the pipe walls, increasing the gas distribution area. However, the outlets are usually only opened in a single direction, limiting the degree of liquid phase turbulence. Furthermore, the outlets all point in the same direction, resulting in a lack of interaction between airflows in adjacent pipes and a low gas-liquid interface renewal rate.

[0004] Existing gas distribution devices suffer from a single gas-liquid mixing flow direction, lacking active mixing mechanisms in the horizontal and tangential directions, resulting in numerous mixing dead zones within the tower. Furthermore, the airflow between adjacent outlet structures lacks synergistic shearing and turbulence effects, leading to insufficient gas-liquid interface renewal. Weak gas supply between pipelines further limits the overall gas-liquid contact area. These deficiencies result in high suspended sulfur content in the lean liquor and insufficient catalyst regeneration, necessitating increased gas supply to compensate for inadequate mixing and thus increasing system energy consumption. Summary of the Invention

[0005] In view of the deficiencies in the prior art, this application provides a gas distribution device for a desulfurization liquid regeneration tower to solve the problem of poor mixing effect in the prior art gas distribution devices.

[0006] The above-mentioned objectives of this application are mainly achieved through the following technical solutions: A gas distribution device for a desulfurization liquid regeneration tower, the gas distribution device comprising an inlet pipe, a connecting pipe, several annular pipes, branch pipes and a jet nozzle; The inlet end of the inlet pipe is used to connect to the gas supply pipeline, and the outlet end of the inlet pipe is connected to the innermost annular pipe through the connecting pipe; a plurality of annular pipes are coaxial and arranged radially from the inside to the outside, and adjacent annular pipes are connected to each other through a plurality of branch pipes. The connecting pipe and the branch pipe are provided with the jet nozzles, and the air outlets of the jet nozzles are respectively oriented upward and downward in the vertical direction; The annular tube is provided with the jet nozzle, the air outlet direction of the jet nozzle forms a preset angle with the tube wall of the annular tube, and the air outlet directions of two adjacent annular tubes are opposite in the tangential direction. The jet nozzles on the annular tube are arranged in groups in the form of mixing units, each mixing unit including at least four jet nozzles, and the jet nozzles in the same mixing unit are evenly arranged along the circumference of the annular tube.

[0007] In an optional implementation, the preset included angle is 15°~20°.

[0008] In an optional embodiment, the jet nozzle on the annular tube includes a horizontal jet nozzle and a vertical jet nozzle; the horizontal jet nozzles on the inner and outer sides of two adjacent annular tubes adopt clockwise and counterclockwise tangential air outlet directions, respectively; the vertical jet nozzles on the inner and outer sides of two adjacent annular tubes adopt clockwise and counterclockwise tangential air outlet directions, respectively.

[0009] In an optional embodiment, auxiliary air outlets are also provided on the pipe wall between two adjacent mixing units on the annular pipe. The auxiliary air outlets are equally spaced along the circumference of the annular pipe, and the auxiliary air outlets are staggered with the mixing units.

[0010] In an optional embodiment, the diameter of the inlet pipe is D, the diameters of the connecting pipe and the annular pipe are both D, the diameter of the branch pipe is 0.7D~0.8D, the diameter of the jet nozzle is 0.2D~0.3D, and the diameter of the auxiliary air outlet is 0.05D~0.1D.

[0011] In an optional embodiment, the number of branch pipes is a multiple of 4, and the branch pipes are evenly distributed along the circumference of the annular pipe.

[0012] In an optional embodiment, the gas distribution device further includes an inlet flange and a connecting flange structure, wherein the inlet flange is disposed at the gas inlet end of the inlet pipe, and the connecting flange structure is disposed between the inlet pipe and the connecting pipe.

[0013] In an optional embodiment, the gas distribution device further includes a support assembly, which includes a support base, a support beam, a support frame, a pad, and U-bolts and nuts. The support beam is fixed to the inner wall of the regeneration tower by the support base, and the annular pipe and the branch pipe are fixed to the support beam by the U-bolts and nuts and the pad.

[0014] In an optional embodiment, the number of annular tubes is at least two, and the diameter of each annular tube increases sequentially from the inside to the outside.

[0015] In an optional embodiment, two adjacent annular pipes and two branch pipes connecting the two adjacent annular pipes form a mixing region, and a plurality of mixing regions are arranged radially in sequence.

[0016] Compared with the prior art, the advantages of this application are: The gas distribution device for a desulfurization liquid regeneration tower in this application includes an inlet pipe, a connecting pipe, several annular pipes, branch pipes, and jet nozzles. The inlet end of the inlet pipe is connected to a gas supply pipeline, and the outlet end of the inlet pipe is connected to the innermost annular pipe through the connecting pipe. The several annular pipes are coaxial and arranged radially from the inside to the outside, and adjacent annular pipes are connected by several branch pipes. The connecting pipe and the branch pipes are provided with jet nozzles, and the outlet directions of the jet nozzles are respectively facing upward and downward in the vertical direction. The annular pipes are provided with jet nozzles, and the outlet direction of the jet nozzles forms a preset angle with the pipe wall of the annular pipe, and the outlet directions of the jet nozzles on two adjacent annular pipes are opposite in the tangential direction. The jet nozzles on the annular pipes are arranged in groups in the form of mixing units, each mixing unit including at least four jet nozzles, and the jet nozzles in the same mixing unit are evenly arranged along the circumference of the annular pipe.

[0017] This gas distribution device employs an inlet pipe, connecting pipes, several coaxial annular pipes, and branch pipes to form a multi-stage gas distribution network from the inside out. Gas enters through the inlet pipe and is distributed to the innermost annular pipe via the connecting pipes, then distributed outwards through the branch pipes to each annular pipe. This radial distribution path ensures uniform distribution of gas to all areas within the tower, overcoming the uneven radial gas distribution problem caused by asymmetrical pipe layouts or insufficient gas supply at the ends in existing pipe network distributors. This guarantees a sufficient gas supply to all radial locations within the tower from the source.

[0018] In the vertical direction, the jet nozzles on the connecting pipe and branch pipes exit air upwards and downwards respectively, forming an opposing airflow structure. The upward-sprayed gas drives the desulfurization-rich liquid to generate an upward flow, while the downward-sprayed gas drives the liquid phase to generate a downward flow, creating a counter-current circulation flow in the vertical direction. Unlike the simple push flow formed by gas rising only in a single vertical direction in existing distributors, the opposing airflows construct a closed circulation loop in the vertical direction, allowing the liquid phase to continuously tumble and mix in the vertical direction. This effectively eliminates stratification and short-circuiting phenomena in the vertical direction within the tower, increasing the contact time and frequency of the gas and liquid phases in the vertical direction.

[0019] In the horizontal tangential direction, the gas outlets on the annular tubes exit at a predetermined angle to the tube wall, causing the gas to enter the liquid phase obliquely rather than being ejected directly radially or vertically. The gas velocity can be decomposed into radial and tangential components, with the tangential component driving the liquid phase to rotate circumferentially along the annular tube. More importantly, the gas outlets on adjacent annular tubes exit in opposite tangential directions; that is, while the inner annular tube drives the liquid phase to rotate clockwise, the adjacent outer annular tube drives it to rotate counterclockwise. These two counter-rotating liquid flows meet in the annular region between adjacent annular tubes, forming a shear layer with opposite velocities, generating a strong shear flow effect. This shear flow causes the gas-liquid interface to be continuously stretched, torn, and renewed under shearing action, significantly increasing the gas-liquid contact area and enhancing the mass transfer rate of oxygen from the gas phase to the liquid phase.

[0020] The jet nozzles on the annular tube are arranged in groups as mixing units, with at least four nozzles uniformly distributed along the circumference of the annular tube within each mixing unit. When multiple nozzles in the same mixing unit emit gas simultaneously, the gas flow from each nozzle merges into the liquid phase from different directions on the cross-section of the annular tube, forming a multi-directional converging local flow structure. The multiple gas flows collide and interfere with each other in the convergence region, generating local micro-vortices. This causes intense three-dimensional turbulence in the liquid phase within the mixing unit region, further breaking down large bubbles into smaller bubbles, increasing the gas-liquid specific surface area, accelerating the renewal of the liquid boundary layer, and reducing mass transfer resistance.

[0021] During overall operation, the vertical up-and-down circulating flow provides macroscopic overturning force for the liquid phase, enabling full contact between the gas and liquid phases in the vertical direction; the tangential reverse rotational shear flow continuously shears and renews the gas-liquid interface in the horizontal direction; and the local micro-vortices generated by the mixing unit enhance bubble breakage and interfacial mass transfer at the microscale, constructing a three-dimensional, multi-layered gas-liquid mixing flow field. This overcomes the shortcomings of existing distributors, such as single flow direction, lack of coordination between adjacent airflows, and the existence of mixing dead zones. It can significantly shorten the oxidation reaction time, reduce the suspended sulfur content in lean liquid, improve catalyst regeneration rate, reduce the gas supply demand of the oxidation blower, and reduce the system's operating energy consumption. Attached Figure Description

[0022] To more clearly illustrate the technical solutions in the embodiments of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0023] Figure 1 A front view of the gas distribution device provided in an embodiment of this application; Figure 2A top view of the gas distribution device provided in the embodiments of this application; Figure 3 A perspective view of the gas distribution device provided in the embodiments of this application; Figure 4 Appendix provided for the embodiments of this application Figure 2 Partial sectional view at point AA; Figure 5 Appendix provided for the embodiments of this application Figure 2 Partial sectional view at point BB; Figure 6 A partial cross-sectional view of the auxiliary air outlet provided in an embodiment of this application; In the diagram: 1. Inlet flange; 2. Inlet pipe; 3. Connecting pipe; 4. Ring pipe; 5. Branch pipe; 6. Air nozzle; 7. Support base; 8. Support beam; 9. Support frame; 10. Gasket; 11. U-bolt and nut; 12. Connecting flange structure; 13. Auxiliary air outlet. Detailed Implementation

[0024] The present invention will be further described below with reference to the accompanying drawings and specific embodiments. It should be noted that the description of these embodiments is intended to aid in understanding the invention, but does not constitute a limitation thereof. The specific structural and functional details disclosed herein are merely for describing exemplary embodiments of the invention. However, the invention can be embodied in many alternative forms and should not be construed as being limited to the embodiments described herein.

[0025] In wet oxidative desulfurization processes, the desulfurization liquid regeneration tower is the core equipment for achieving the oxidative regeneration of the desulfurization catalyst. Its basic principle is as follows: the rich desulfurization liquid, having absorbed hydrogen sulfide, comes into full contact with air within the regeneration tower. The reduced catalyst in the rich liquid (such as tannin, complexed iron, PDS, etc.) is oxidized to its oxidized state under the action of dissolved oxygen, restoring its desulfurization activity. Simultaneously, the sulfide ions in the rich liquid are oxidized to elemental sulfur and released, thus achieving the recycling and reuse of the desulfurization liquid. The quality of the regeneration directly determines the suspended sulfur content of the lean liquid, the catalyst regeneration rate, and the operational stability and economy of the entire desulfurization system.

[0026] The gas-liquid mixing process within the desulfurization liquid regeneration tower is a crucial factor determining regeneration efficiency. Air enters the rich desulfurization liquid through a gas distribution device installed inside the tower. The structure and arrangement of the gas distribution device determine the dispersion state of bubbles in the liquid phase, the gas-liquid contact area, and the flow pattern of the liquid phase, thereby affecting the oxygen mass transfer rate and the oxidation regeneration efficiency of the catalyst.

[0027] Currently, commonly used gas distribution devices in industry mainly include two types: spear-type distributors and pipe network distributors. Spear-type distributors typically consist of several vertically or inclined nozzles, with air ejected from the openings at the ends of the nozzles into the liquid phase. This type of distributor has a simple structure, but it has the following drawbacks: the nozzles emit gas in a single direction, the gas mainly rises vertically in the liquid phase, the liquid flow pattern is dominated by a simple upward flow, the horizontal mixing capacity is weak, and there are many areas of insufficient gas-liquid mixing on the cross-section of the tower, especially the area between adjacent nozzles, which easily forms flow dead zones, leading to incomplete local oxidation and a high suspended sulfur content in the lean liquid.

[0028] Pipeline distributors typically consist of a main pipe, branch pipes, and outlets on the pipe walls. Gas is distributed from the main pipe to the branch pipes and then discharged through the outlets. Compared to spear-type distributors, pipeline distributors have a larger gas distribution area, but their outlets are usually only opened in a single direction (vertically upward or horizontally). The gas flow direction in the liquid phase remains relatively unidirectional, making it difficult to form multidirectional gas-liquid mixing flow within the column. Furthermore, in existing pipeline distributors, the outlet directions of each outlet are usually consistent, resulting in a lack of interaction between airflows in adjacent pipes. This limits the degree of turbulence in the liquid phase, leads to a low gas-liquid interface renewal rate, and makes it difficult to further improve mass transfer efficiency.

[0029] In summary, existing gas distribution devices generally suffer from the following common defects: First, the gas-liquid mixing flow direction is singular, mainly relying on vertical upward flow for mixing, lacking active mixing mechanisms in the horizontal and tangential directions, resulting in numerous mixing dead zones within the tower; second, the airflow between adjacent outlet structures lacks synergy, failing to form effective shear and turbulence effects, and the gas-liquid interface renewal is insufficient; third, the uniformity of gas distribution is insufficient, the gas supply between pipelines is weak, and the overall gas-liquid contact area is limited. These defects lead to incomplete oxidation regeneration of the desulfurization rich liquor, manifested as high suspended sulfur content in the lean liquor and insufficient catalyst regeneration rate, thus requiring an increase in the gas supply of the oxidation blower to compensate for insufficient mixing, increasing system energy consumption and operating costs.

[0030] like Figure 1 , Figure 2 as well as Figure 3 As shown, Figure 1 A front view of the gas distribution device provided in an embodiment of this application; Figure 2 A top view of the gas distribution device provided in the embodiments of this application; Figure 3 A perspective view of a gas distribution device provided in an embodiment of this application; a gas distribution device for a desulfurization liquid regeneration tower, the gas distribution device including an inlet pipe 2, a connecting pipe 3, several annular pipes 4, branch pipes 5, and a jet nozzle 6, wherein: like Figure 1 , Figure 2 as well as Figure 3 As shown, the air inlet end of the inlet pipe 2 is used to connect to the air supply pipeline, and the air outlet end of the inlet pipe 2 is connected to the innermost annular pipe 4 through the connecting pipe 3; a plurality of annular pipes 4 are coaxial and arranged radially from the inside to the outside, and adjacent annular pipes 4 are connected by a plurality of branch pipes 5. The inlet end of inlet pipe 2 is used to connect to an external air supply line, which can be the outlet line of the oxidation blower or a compressed air line. The outlet end of inlet pipe 2 is connected to the innermost annular pipe 4 via connecting pipe 3. Connecting pipe 3 serves as a transitional connection between inlet pipe 2 and annular pipe 4, its function being to smoothly introduce the concentrated airflow delivered by inlet pipe 2 into the annular pipe 4 network, avoiding drastic changes in airflow direction and local pressure loss at the connection point. Inlet pipe 2 and connecting pipe 3 can be connected by welding to ensure sealing, or by flange connection for ease of installation and maintenance. Connecting pipe 3 can be arranged horizontally, or extended radially or tangentially depending on the internal space layout of the tower, as long as reliable communication between inlet pipe 2 and the innermost annular pipe 4 is achieved.

[0031] Several annular pipes 4 are coaxially arranged and radially arranged from the inside out. The center of each annular pipe 4 coincides with the axis of the regeneration tower, and the diameter of each annular pipe 4 increases sequentially from the inside out. Adjacent annular pipes 4 are connected by several branch pipes 5, which extend radially and are welded or flanged to the adjacent inner and outer annular pipes 4 at their respective ends. Gas enters from the innermost annular pipe 4 and is distributed to each annular pipe 4 through the branch pipes 5, forming a radial gas distribution path from the inside out. The number of branch pipes 5 can be determined based on the circumference of the annular pipes 4 and the requirements for gas supply uniformity, ensuring symmetry in gas supply in all directions. In addition to gas distribution, the branch pipes 5 also have jet nozzles 6 on their walls, allowing the area covered by the branch pipe 5 to participate in gas-liquid mixing and preventing the area covered by the branch pipe 5 from becoming a weak point in gas supply.

[0032] like Figure 1 , Figure 2 as well as Figure 3 As shown, the connecting pipe 3 and the branch pipe 5 are provided with the jet nozzle 6, and the air outlet direction of the jet nozzle 6 is facing upward and downward in the vertical direction, respectively. like Figure 4 as well as Figure 5As shown, the connecting pipe 3 and the branch pipe 5 are respectively provided with upward-facing jet nozzles 6 and downward-facing jet nozzles 6. The gas ejected from the upward-facing jet nozzle 6 drives the surrounding desulfurization-rich liquid to rise under the combined action of buoyancy and jet force, while the gas ejected from the downward-facing jet nozzle 6 drives the liquid phase to fall against the direction of buoyancy. The jet nozzles 6 in the two directions can be arranged alternately on the same pipe section or concentrated in different sections of the pipe section. When the upper and lower jet nozzles 6 work simultaneously, a symmetrical circulating flow structure is formed around the connecting pipe 3 and the branch pipe 5: the rising flow and the falling flow form a closed loop in the vertical direction, and the liquid phase continuously tumbles in this loop, so that the gas and liquid phases repeatedly contact and mix in the vertical direction. This vertical circulating flow effectively overcomes the liquid phase stratification and short-circuit problems caused by the gas only rising in one direction in the existing distributor, and increases the contact time and mixing degree of the gas and liquid phases in the vertical direction.

[0033] like Figure 1 , Figure 2 as well as Figure 3 As shown, the annular pipe 4 is provided with the jet nozzle 6. The air outlet direction of the jet nozzle 6 forms a preset angle with the pipe wall of the annular pipe 4, and the air outlet directions of two adjacent annular pipes 4 on the jet nozzle 6 are opposite in the tangential direction. An annular pipe 4 is equipped with a jet nozzle 6. The outlet direction of the jet nozzle 6 forms a preset angle with the pipe wall of the annular pipe 4. Since the jet nozzle 6 is not opened along the radial or vertical direction of the annular pipe 4, but rather obliquely on the pipe wall, the velocity vector of the gas ejected from the jet nozzle 6 can be decomposed into a radial component, a vertical component, and a tangential component along the annular pipe 4. The tangential component drives the liquid phase to rotate and flow around the circumference of the annular pipe 4, the radial component drives the liquid phase to flow radially between adjacent annular pipes 4, and the vertical component participates in vertical mixing. By reasonably setting the preset angle, the proportions of each directional component can be adjusted, thereby optimizing the intensity and directional distribution of the gas-liquid mixture.

[0034] like Figure 1 , Figure 2 as well as Figure 3As shown, the jet nozzles 6 on two adjacent annular pipes 4 have opposite tangential directions of gas output. When the jet nozzle 6 on the inner annular pipe 4 outputs gas with a clockwise tangential component, the jet nozzle 6 on the adjacent outer annular pipe 4 outputs gas with a counterclockwise tangential component. The two annular pipes 4 drive the liquid phase to generate rotating flows in opposite directions. The two counter-rotating liquid flows meet in the annular region between adjacent annular pipes 4 and generate strong velocity shear. In this shear layer, the velocity gradient of the liquid phase increases significantly, and the gas-liquid interface is continuously stretched, deformed, and broken under shear stress. Large bubbles are torn into smaller bubbles, and the gas-liquid specific surface area increases significantly. At the same time, the shearing effect accelerates the renewal of the liquid phase boundary layer, reduces the liquid film mass transfer resistance, and significantly improves the mass transfer rate of oxygen from the gas phase to the liquid phase. This shear flow effect cannot be generated in existing distributors where all gas outlets are oriented in the same direction and the airflow in adjacent pipes flows in the same direction.

[0035] The jet nozzles 6 on the annular pipe 4 are arranged in groups in the form of mixing units, each mixing unit including at least four jet nozzles 6, and the jet nozzles 6 in the same mixing unit are evenly arranged along the circumference of the annular pipe 4.

[0036] The same mixing unit includes four jet nozzles 6, which are arranged at 90-degree intervals along the cross-section of the annular tube 4, corresponding to the upper, lower, left, and right directions of the annular tube 4 cross-section, respectively. When the four jet nozzles 6 in the same mixing unit simultaneously emit gas, the four gas streams converge into the liquid phase around the annular tube 4 from different directions, forming a multi-directional converging flow structure in the region where the mixing unit is located. The multiple gas streams collide and interfere with each other in the convergence area, generating local micro-vortices, causing strong three-dimensional turbulence in the liquid phase in this region. The shearing effect of the micro-vortices further breaks up the bubbles, increases the gas-liquid contact area, and accelerates the renewal and mixing of the local liquid phase. Adjacent mixing units are arranged at intervals along the circumference of the annular tube 4, and the micro-vortices generated by each mixing unit are distributed sequentially in the circumferential direction, so that the liquid phase around the annular tube 4 is uniformly excited by turbulence in the circumferential direction, avoiding insufficient local mixing.

[0037] In an optional embodiment, the gas distribution device for the desulfurization liquid regeneration tower of this application includes an inlet pipe 2, a connecting pipe 3, several annular pipes 4, branch pipes 5, and a jet nozzle 6. The inlet end of the inlet pipe 2 is connected to the gas supply pipeline, and the outlet end of the inlet pipe 2 is connected to the innermost annular pipe 4 through the connecting pipe 3. The several annular pipes 4 are coaxial and arranged radially from the inside to the outside, and adjacent annular pipes 4 are connected by the several branch pipes 5. The jet nozzle 6 is provided on the connecting pipe 3 and the branch pipes 5. Furthermore, the air outlets 6 are oriented vertically upwards and downwards respectively; the annular pipe 4 is provided with air outlets 6, the air outlets 6 are at a preset angle to the pipe wall of the annular pipe 4, and the air outlets 6 on two adjacent annular pipes 4 are opposite in tangential direction; the air outlets 6 on the annular pipe 4 are arranged in groups in the form of mixing units, each mixing unit includes at least four air outlets 6, and the air outlets 6 in the same mixing unit are evenly arranged along the circumference of the annular pipe 4.

[0038] like Figure 1 , Figure 2 as well as Figure 3 As shown, this gas distribution device employs an inlet pipe 2, connecting pipes 3, several coaxial annular pipes 4, and branch pipes 5 to form a multi-stage gas distribution network from the inside out. Gas enters through the inlet pipe 2 and is distributed to the innermost annular pipe 4 via the connecting pipes 3, then progressively distributed outwards to each ring of annular pipes 4 via the branch pipes 5. This radial distribution path from the inside out ensures that the gas is evenly distributed radially to all areas within the tower, overcoming the problem of uneven radial gas distribution caused by asymmetrical pipe layout or insufficient gas supply at the end in existing pipe network distributors. This ensures that all radial positions within the tower receive sufficient gas supply from the source.

[0039] In the vertical direction, the jet nozzles 6 on the connecting pipe 3 and the branch pipe 5 emit gas upwards and downwards respectively, forming an opposing airflow structure. The upward-sprayed gas drives the desulfurization-rich liquid to generate an upward flow, while the downward-sprayed gas drives the liquid phase to generate a downward flow. The two form a circulating flow in opposite directions in the vertical direction. Unlike the simple push flow formed by gas rising only in a single vertical direction in existing distributors, the opposing airflows construct a closed circulation loop in the vertical direction, allowing the liquid phase to continuously tumble and mix in the vertical direction. This effectively eliminates stratification and short-circuiting phenomena in the vertical direction within the tower, and increases the contact time and frequency of the gas and liquid phases in the vertical direction.

[0040] In the horizontal tangential direction, the gas outlet 6 on the annular pipe 4 forms a predetermined angle with the pipe wall, causing the gas to enter the liquid phase obliquely rather than being ejected directly in the radial or vertical direction. The gas velocity can be decomposed into radial and tangential components, with the tangential component driving the liquid phase to rotate along the circumference of the annular pipe 4. More importantly, the gas outlets 6 on adjacent annular pipes 4 have opposite tangential directions; that is, while the inner annular pipe 4 drives the liquid phase to rotate clockwise, the adjacent outer annular pipe 4 drives the liquid phase to rotate counterclockwise. The two counter-rotating liquid flows meet in the annular region between adjacent annular pipes 4, forming a shear layer with opposite velocities, generating a strong shear flow effect. This shear flow causes the gas-liquid interface to be continuously stretched, torn, and renewed under shear action, significantly increasing the gas-liquid contact area and enhancing the mass transfer rate of oxygen from the gas phase to the liquid phase.

[0041] The jet nozzles 6 on the annular pipe 4 are arranged in groups in the form of mixing units, with at least four jet nozzles 6 uniformly distributed around the circumference of the annular pipe 4 within each mixing unit. When multiple jet nozzles 6 in the same mixing unit emit gas simultaneously, the gas flow from each jet nozzle 6 merges into the liquid phase from different directions on the cross-section of the annular pipe 4, forming a multi-directional converging local flow structure. The multiple gas flows collide and interfere with each other in the converging region, generating local micro-vortices, causing strong three-dimensional turbulence in the liquid phase in the region where the mixing unit is located. This further breaks down large bubbles into smaller bubbles, increases the gas-liquid specific surface area, accelerates the renewal of the liquid phase boundary layer, and reduces mass transfer resistance.

[0042] During overall operation, the vertical up-and-down circulating flow provides macroscopic overturning force for the liquid phase, enabling full contact between the gas and liquid phases in the vertical direction; the tangential reverse rotational shear flow continuously shears and renews the gas-liquid interface in the horizontal direction; and the local micro-vortices generated by the mixing unit enhance bubble breakage and interfacial mass transfer at the microscale, constructing a three-dimensional, multi-layered gas-liquid mixing flow field. This overcomes the shortcomings of existing distributors, such as single flow direction, lack of coordination between adjacent airflows, and the existence of mixing dead zones. It can significantly shorten the oxidation reaction time, reduce the suspended sulfur content in lean liquid, improve catalyst regeneration rate, reduce the gas supply demand of the oxidation blower, and reduce the system's operating energy consumption.

[0043] like Figure 1 , Figure 2 as well as Figure 3As shown, in an optional embodiment, the preset angle is 15°~20°. When the preset angle is too small, the tangential component of the gas velocity from the jet nozzle 6 is too small, resulting in insufficient ability to drive the liquid phase rotational flow, weakened shear flow effect between adjacent annular pipes 4, and insufficient shear renewal at the gas-liquid interface. When the preset angle is too large, the tangential component is too large, while the radial and vertical components are correspondingly reduced, resulting in insufficient penetration depth of the gas in the radial and vertical directions. This makes it difficult to effectively drive liquid phase mixing in the region between adjacent annular pipes 4 and in the vertical direction. Furthermore, an excessively large tangential velocity may cause the liquid phase to rotate as a whole rather than undergo local shear, thus reducing mixing efficiency. Within the range of 15°~20°, the tangential, radial, and vertical components of the gas velocity from the jet nozzle 6 achieve a better proportional relationship, which can generate sufficient tangential shear to drive the reverse rotational shear flow between adjacent annular pipes 4, and also ensure sufficient flow driving force in the radial and vertical directions, so that the mixing mechanism in all three directions can function effectively.

[0044] like Figure 1 , Figure 2 as well as Figure 3 As shown, in an optional embodiment, the jet nozzle 6 on the annular pipe 4 includes a horizontal jet nozzle 6 and a vertical jet nozzle 6; the horizontal jet nozzles 6 on the inner and outer sides of two adjacent annular pipes 4 adopt clockwise and counterclockwise tangential air outlet directions, respectively; the vertical jet nozzles 6 on the inner and outer sides of two adjacent annular pipes 4 adopt clockwise and counterclockwise tangential air outlet directions, respectively.

[0045] The jet nozzles 6 on the annular pipe 4 are further subdivided into two types: horizontal jet nozzles 6 and vertical jet nozzles 6. These two types act on different dimensions of liquid phase motion in space. The horizontal jet nozzles 6 primarily drive the liquid phase to generate rotational and radial flow in the horizontal plane, with their tangential components constructing a counter-rotating shear layer in the horizontal plane. The vertical jet nozzles 6, while driving the liquid phase to generate vertical up-and-down flow, introduce a rotational component in the vertical plane with their tangential components. This makes the upward and downward flow of the liquid phase not a simple linear motion, but a helical motion with rotational characteristics. Both types of jet nozzles 6 use opposite tangential outlet directions on adjacent annular pipes 4, ensuring that the shear flow in the horizontal plane and the rotational flow in the vertical plane maintain a consistent shear logic in direction; that is, the inner and outer rings always form opposite movements. This makes the trajectory of the liquid phase in three-dimensional space more complex, and the update of the gas-liquid interface is no longer limited to a single plane, but occurs simultaneously on multiple planes through shearing and fragmentation, further improving mass transfer efficiency.

[0046] like Figure 6As shown, in an optional embodiment, an auxiliary air outlet 13 is also provided on the pipe wall between two adjacent mixing units on the annular pipe 4. The auxiliary air outlet 13 is arranged at equal intervals along the circumference of the annular pipe 4, and the auxiliary air outlet 13 is staggered with the mixing unit.

[0047] When multiple jet nozzles 6 simultaneously emit gas within a mixing unit, a strong multidirectional converging flow is formed in the region where the mixing unit is located, resulting in high liquid-phase turbulence intensity and thorough gas-liquid mixing. Between two adjacent mixing units lies a pipe wall section. The direct driving effect of the jet nozzle 6 on the liquid phase in this section rapidly decreases with increasing distance. The turbulent kinetic energy of the liquid phase decreases from the center of the mixing unit towards both sides, reaching its lowest point at the midpoint between the two mixing units.

[0048] Auxiliary air outlets 13 are evenly spaced along the circumference of the annular pipe 4 to ensure continuous and uniform gas replenishment across the entire arc segment between mixing units. The staggered arrangement of the auxiliary air outlets 13 and mixing units means that the positions of the auxiliary air outlets 13 on the circumference of the annular pipe 4 are spatially offset from the positions of the jet nozzles 6 within the mixing units; they do not overlap or align. The jet nozzles 6 within the mixing units, with their larger aperture and higher exhaust velocity, serve as the primary mixing drive, creating multi-directional converging flow and micro-vortex turbulence. The auxiliary air outlets 13, with their smaller aperture and lower exhaust velocity, serve as the supplementary dispersion function, maintaining the basic gas holdup and minor disturbances in the region between mixing units. The two form a primary-auxiliary cooperative relationship in terms of exhaust intensity. In terms of flow field structure, if the auxiliary air outlets 13 and the jet nozzles 6 within the mixing units were aligned circumferentially, the weak airflow from the auxiliary air outlets 13 would directly superimpose on the strong jet from the jet nozzles 6, and its disturbance effect would be completely masked by the main jet, failing to independently improve the weak areas between mixing units. The staggered arrangement allows the airflow from the auxiliary exhaust port 13 to act on the area outside the jet coverage of the jet port 6, truly generating independent disturbance excitation in the low mixing zone and playing its role in supplementing mixing.

[0049] The auxiliary vent 13 replenishes the surrounding liquid phase with trace amounts of gas in a diffuse manner. On the one hand, this increases the gas holdup in this region; on the other hand, the rising motion of the microbubbles creates a slight disturbance to the surrounding liquid phase, disrupting the laminar flow state in the low-mixing region. The microbubbles generated by the auxiliary vent 13 are complementary in size to the main bubbles generated by the jet nozzle 6. The microbubbles have a larger specific surface area and a longer residence time, which is beneficial for the complete dissolution and mass transfer of oxygen.

[0050] like Figure 1 , Figure 2 as well as Figure 3As shown, in an optional embodiment, the diameter of the inlet pipe 2 is D, the diameters of the connecting pipe 3 and the annular pipe 4 are both D, the diameter of the branch pipe 5 is 0.7D~0.8D, the diameter of the jet nozzle 6 is 0.2D~0.3D, and the diameter of the auxiliary air outlet 13 is 0.05D~0.1D.

[0051] Inlet pipe 2, connecting pipe 3, and annular pipe 4 all use the same diameter D, ensuring a relatively constant gas velocity along the main path and avoiding local pressure loss and uneven airflow distribution caused by sudden changes in pipe diameter. Branch pipe 5 has a diameter of 0.7D~0.8D, slightly smaller than the main pipe diameter, allowing for a moderate increase in gas velocity when entering branch pipe 5 from annular pipe 4. This helps the gas overcome friction resistance and reach the ends of each branch pipe 5 evenly, while preventing excessive pressure drop in branch pipe 5 due to an excessively small diameter, which could lead to insufficient gas supply to distant branch pipes. The jet nozzle 6 has a diameter of 0.2D~0.3D, ensuring sufficient jet velocity to drive the surrounding liquid phase when ejected from nozzle 6. Simultaneously, the ratio of nozzle 6 area to pipe cross-sectional area is within a reasonable range, ensuring smooth gas discharge from nozzle 6 without generating excessive back pressure within the pipe. The diameter of the auxiliary air outlet 13 is 0.05D~0.1D, which is much smaller than the diameter of the jet nozzle 6. This ensures that the auxiliary air outlet 13 disperses the gas in a low flow and low momentum manner, without interfering with the flow structure constructed by the main jet nozzle 6. It only serves to supplement the gas and cause minor disturbances.

[0052] like Figure 1 , Figure 2 as well as Figure 3 As shown, in an optional embodiment, the number of branch pipes 5 is a multiple of 4, and the branch pipes 5 are evenly distributed along the circumference of the annular pipe 4.

[0053] The number of branch pipes 5 is a multiple of 4, ensuring a symmetrical circumferential distribution of gas from the inner annular pipe 4 to the outer annular pipe 4. This avoids significant differences in gas flow rate across different segments of the outer annular pipe 4 due to asymmetrical branch pipe layout. It also ensures that the gas flow reaction forces experienced by the gas distribution device during operation are balanced circumferentially, reducing vibration and stress concentration caused by uneven stress. The uniform circumferential distribution of branch pipes 5 further guarantees equal angular intervals between adjacent branch pipes 5, resulting in consistent fan-shaped areas covered by each branch pipe 5. This ensures that the gas supply to each segment of the outer annular pipe 4 is essentially the same, thus creating a uniform gas distribution across the tower's cross-section.

[0054] like Figure 1 , Figure 2 as well as Figure 3As shown, in an optional embodiment, the gas distribution device further includes an inlet flange 1 and a connecting flange structure 12. The inlet flange 1 is disposed at the gas inlet end of the inlet pipe 2, and the connecting flange structure 12 is disposed between the inlet pipe 2 and the connecting pipe 3.

[0055] The inlet flange 1 is used to achieve a detachable connection between the gas distribution device and the external gas supply pipeline. During device installation, the inlet flange 1 is bolted to the gas supply pipeline flange. For maintenance or replacement, it can be directly disassembled without cutting the pipeline. The connecting flange structure 12 is located between the inlet pipe 2 and the connecting pipe 3, structurally dividing the gas distribution device into two independently detachable modules: the inlet section and the distribution section. This split design allows for the installation of the connecting pipe 3, the annular pipe 4, and the branch pipe 5 into the tower first, even in situations with limited space, and then connecting them to the inlet section via the connecting flange, reducing installation difficulty. Furthermore, when a component needs maintenance or replacement, only the connecting flange needs to be removed to extract the entire distribution section without damaging the connection between the inlet pipe 2 and the external gas supply pipeline, improving maintenance efficiency.

[0056] like Figure 1 , Figure 2 as well as Figure 3 As shown, in an optional embodiment, the gas distribution device further includes a support assembly, which includes a support base 7, a support beam 8, a support frame 9, a pad 10, and U-bolts and nuts 11. The support beam 8 is fixed to the inner wall of the regeneration tower by the support base 7, and the annular pipe 4 and the branch pipe 5 are fixed to the support beam 8 by the U-bolts and nuts 11 and the pad 10.

[0057] During operation, the gas distribution device is continuously subjected to the reaction force generated by the gas jet and the impact force generated by the liquid flow. Without reliable fixed support, the pipeline system may experience vibration, displacement, or even fatigue fracture. The support base 7 is welded or bolted to the inner wall of the regeneration tower, providing a stable foundation for the entire support system. The support beam 8, as the main load-bearing component, extends horizontally and bears the weight and operating load of the annular pipe 4 and branch pipe 5. U-bolts and nuts 11 tighten the annular pipe 4 and branch pipe 5 onto the support beam 8; their U-shaped structure can adapt to pipelines of different diameters and is easy to install and disassemble. A pad 10 is placed between the pipeline and the support beam 8, serving two purposes: firstly, to buffer and dampen vibrations, absorbing minor vibrations during pipeline operation; and secondly, to prevent wear and stress concentration caused by rigid contact between the pipeline and the support beam 8. This support assembly design ensures the structural stability of the gas distribution device during long-term operation, extending the device's service life.

[0058] like Figure 1 , Figure 2 as well as Figure 3As shown, in an optional embodiment, the number of the annular tubes 4 is at least two, and the diameter of each annular tube 4 increases sequentially from the inside to the outside.

[0059] The number of annular tubes 4 can be determined based on the diameter of the regeneration tower and the required gas coverage area. When the regeneration tower diameter is large, three, four, or even more annular tubes 4 can be installed to increase the radial coverage of the gas distribution. The diameter of each annular tube 4 increases sequentially from the inside out. The radial spacing between adjacent annular tubes 4 can be determined according to the mixing effect requirements. If the spacing is too large, the shear flow region between adjacent annular tubes 4 will be too wide, and the shear strength will be weakened; if the spacing is too small, the liquid phase flow cross-section between the annular tubes 4 will be insufficient, which may cause local blockage. The arrangement of multiple annular tubes 4 causes the counter-rotating shear flow to form multiple alternating shear layers in the radial direction. The liquid phase repeatedly undergoes shearing and mixing when passing through each shear layer. The number of gas-liquid interface renewals increases with the increase of the number of annular tubes 4, and the overall mass transfer effect is improved accordingly.

[0060] like Figure 1 , Figure 2 as well as Figure 3 As shown, in an optional embodiment, two adjacent annular pipes 4 and two branch pipes 5 connecting the two adjacent annular pipes 4 form a mixing region, and a plurality of mixing regions are arranged radially in sequence.

[0061] The mixing region, a closed or semi-closed space defined by two adjacent annular pipes 4 and the branch pipes 5 connecting them, is the main area where gas-liquid mixing occurs. Within this mixing region, the jet nozzles 6 on the inner and outer annular pipes 4 emit gas in opposite tangential directions, driving the liquid phase to form a counter-rotating shear flow within the mixing region. The upper and lower jet nozzles 6 on the branch pipes 5 create a vertical circulating flow within the mixing region. The mixing units on the annular pipes 4 generate local micro-vortices within the mixing region. This makes the mixing region the most active area for gas-liquid mass transfer. Multiple mixing regions are arranged radially in sequence, ensuring that all radial positions from the center to the edge of the tower are covered by the mixing region. This eliminates the defect of insufficient mixing between pipes in traditional distributors, achieving complete gas-liquid mixing coverage across the cross-section of the tower.

[0062] It should be understood that the terms "first," "second," etc., are used only for distinguishing descriptions and should not be construed as indicating or implying relative importance. Although the terms "first," "second," etc., may be used herein to describe various units, these units should not be limited by these terms. These terms are only used to distinguish one unit from another. For example, a first unit may be referred to as a second unit, and similarly, a second unit may be referred to as a first unit, without departing from the scope of the exemplary embodiments of the invention.

[0063] It should be understood that the term "and / or" in this article is merely a description of the relationship between related objects, indicating that three relationships can exist. For example, A and / or B can mean: A exists alone, B exists alone, and A and B exist simultaneously. The term " / and" in this article describes another relationship between related objects, indicating that two relationships can exist. For example, A / and B can mean: A exists alone, and A and B exist alone. In addition, the character " / " in this article generally indicates that the related objects before and after it are in an "or" relationship.

[0064] It should be understood that in the description of this invention, the terms "upper," "vertical," "inner," "outer," etc., indicate the orientation or positional relationship as commonly placed when the disclosed product is used, or the orientation or positional relationship commonly understood by those skilled in the art. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0065] In the description of this invention, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," and "connect" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0066] The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the exemplary embodiments of the invention. As used herein, the singular forms “a,” “an,” and “the” are intended to include the plural forms unless the context clearly indicates otherwise. It should also be understood that the terms “comprising,” “including,” “containing,” and / or “including” as used herein specify the presence of the stated features, integers, steps, operations, units, and / or components, and do not exclude the presence or addition of one or more other features, quantities, steps, operations, units, components, and / or combinations thereof.

[0067] Specific details are provided in the following description to provide a complete understanding of the exemplary embodiments. However, those skilled in the art will understand that the exemplary embodiments can be implemented without these specific details. In other embodiments, well-known processes, structures, and techniques may be omitted in the depiction of non-essential details to avoid obscuring the exemplary embodiments.

[0068] The above are merely specific embodiments of this application, enabling those skilled in the art to understand or implement this application. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of this application. Therefore, this application is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features claimed herein.

[0069] It should be noted that the information disclosed in the background section above is only used to enhance the understanding of the background of this disclosure, and therefore may include information that does not constitute prior art known to those skilled in the art.

Claims

1. A gas distribution device for a desulfurization liquid regeneration tower, characterized in that, The gas distribution device includes an inlet pipe, a connecting pipe, several annular pipes, branch pipes, and a jet nozzle; The inlet end of the inlet pipe is used to connect to the gas supply pipeline, and the outlet end of the inlet pipe is connected to the innermost annular pipe through the connecting pipe; a plurality of annular pipes are coaxial and arranged radially from the inside to the outside, and adjacent annular pipes are connected to each other through a plurality of branch pipes. The connecting pipe and the branch pipe are provided with the jet nozzles, and the air outlets of the jet nozzles are respectively oriented upward and downward in the vertical direction; The annular tube is provided with the jet nozzle, the air outlet direction of the jet nozzle forms a preset angle with the tube wall of the annular tube, and the air outlet directions of two adjacent annular tubes are opposite in the tangential direction. The jet nozzles on the annular tube are arranged in groups in the form of mixing units, each mixing unit including at least four jet nozzles, and the jet nozzles in the same mixing unit are evenly arranged along the circumference of the annular tube.

2. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: The preset included angle is 15°~20°.

3. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: The jet nozzles on the annular tube include horizontal jet nozzles and vertical jet nozzles; the horizontal jet nozzles on the inner and outer sides of two adjacent annular tubes adopt clockwise and counterclockwise tangential air outlet directions, respectively; the vertical jet nozzles on the inner and outer sides of two adjacent annular tubes adopt clockwise and counterclockwise tangential air outlet directions, respectively.

4. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: An auxiliary air outlet is provided on the pipe wall between two adjacent mixing units on the annular pipe. The auxiliary air outlets are arranged at equal intervals along the circumference of the annular pipe, and the auxiliary air outlets are staggered with the mixing units.

5. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 4, characterized in that: The diameter of the inlet pipe is D, the diameter of the connecting pipe and the annular pipe is D, the diameter of the branch pipe is 0.7D~0.8D, the diameter of the jet nozzle is 0.2D~0.3D, and the diameter of the auxiliary air outlet is 0.05D~0.1D.

6. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: The number of branch pipes is a multiple of 4, and the branch pipes are evenly distributed along the circumference of the annular pipe.

7. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: The gas distribution device further includes an inlet flange and a connecting flange structure. The inlet flange is disposed at the gas inlet end of the inlet pipe, and the connecting flange structure is disposed between the inlet pipe and the connecting pipe.

8. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: The gas distribution device further includes a support assembly, which includes a support base, a support beam, a support frame, a pad, and U-bolts and nuts. The support beam is fixed to the inner wall of the regeneration tower by the support base, and the annular pipe and the branch pipe are fixed to the support beam by the U-bolts and nuts and the pad.

9. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: The number of annular tubes is at least two, and the diameter of each annular tube increases sequentially from the inside to the outside.

10. The gas distribution device for a desulfurization liquid regeneration tower as described in claim 1, characterized in that: Two adjacent annular pipes and two branch pipes connecting the two adjacent annular pipes form a mixing region, and multiple mixing regions are arranged radially in sequence.

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