Tower type multi-stage series gas-liquid bubbling reactor

Abstract

The invention discloses a tower-type multi-stage series gas-liquid bubbling reactor, which relates to the technical field of gas-liquid multi-phase reaction systems, and comprises: an inner cavity provided with a liquid inlet / outlet, a gas inlet / outlet and an emptying port; the tower plates divide the inner cavity into multiple stages of tower bodies, each stage of tower body is provided with an exhaust structure and a liquid discharge structure, and a liquid outlet and a gas inlet are formed in the tower body at the lowest end; in each stage of tower body, the exhaust structure is arranged on the lower tower plate in a penetrating manner, the liquid discharge structure is arranged on the upper tower plate in a penetrating manner, and a liquid outlet of the liquid discharge structure is positioned on the lower tower plate; the gas uniform distribution bubble breaker is arranged between the exhaust structure and a tower plate above the tower body; in the tower body positioned at the top of the tower, the liquid discharge structure is connected with the liquid inlet; in the tower body at the bottom of the tower, the exhaust structure is connected with the gas inlet; an observation opening and a sampling opening are formed in the side wall of each stage of tower body; the reactor can further reduce liquid phase backmixing and further strengthen gas-liquid mass transfer.

Description

Technical Field

[0001] The invention belongs to the technical field of gas-liquid multiphase reaction system, and more specifically, relates to a tower-type multi-stage series gas-liquid bubbling reactor. Background Art

[0002] Gas-liquid reaction systems are common in many fields such as chemical industry, light industry, environment, energy and biochemistry, and bubbling reactors are widely used in industrial production because of their good gas-liquid mass transfer effect. The gas is dispersed into small bubbles through the gas distributor at the bottom of the reactor. These small bubbles pass upward through the liquid layer under the action of buoyancy. During the rising process, the reactants in the gas phase dissolve into the liquid phase, and the gas and liquid phases transfer substances on the bubble surface and the surrounding liquid film. At the same time, the stirring effect of the bubbles makes the liquid phase fully mixed, increasing the gas-liquid contact area and contact time, and promoting the mass transfer process. In industry, bubbling reactors are generally single-stage reactors, which are basically in a fully mixed kettle flow state, and there is a large problem of gas-liquid backmixing. In a continuous flow reactor, for a reaction process with a reaction order greater than zero, the greater the liquid phase backmixing, the larger the reactor volume required to achieve a certain conversion rate, the longer the reaction residence time, and the lower the efficiency. Patent application number 202220595800.2 provides a corrugated sieve plate multi-stage bubbling tower reactor, which can prevent the gas volume entering the upper reaction zone through the sieve plate from changing in a pulsed manner and prevent the liquid entering the upper reaction zone through the sieve plate from axially mixing, thereby achieving continuous gas-liquid mass transfer and reaction, making the gas-liquid mass transfer and reaction more sufficient and achieving a high conversion rate of the reaction. However, the method of simply setting a sieve plate in the tower cannot solve the problem of upper and lower liquid phase mixing in the tower. Summary of the invention

[0003] The purpose of the present invention is to provide a tower-type multi-stage series gas-liquid bubbling reactor to address the deficiencies of the prior art. The reactor can further reduce liquid phase backmixing and further enhance gas-liquid mass transfer.

[0004] In order to achieve the above object, the present invention provides a tower-type multi-stage series gas-liquid bubbling reactor, comprising: The inner cavity has a liquid inlet and a gas outlet at the top, a drain port at the bottom, and a liquid outlet and a gas inlet below the side wall of the inner cavity; A plurality of tower plates, wherein the tower plates divide the inner cavity into multiple tower bodies from top to bottom, each tower body is provided with an exhaust structure and a liquid discharge structure, and the liquid outlet and the gas inlet are both provided in the tower body at the lowest end; In each stage of the tower body, the exhaust structure is disposed through the tower plate located at the bottom, the drainage structure is disposed through the tower plate located at the top, and the liquid outlet of the drainage structure is located on the tower plate located at the bottom; A gas uniform distribution bubble breaker is arranged between the exhaust structure and the tower plate above the tower body; In the tower body located at the top of the tower, the liquid drainage structure is connected to the liquid inlet; In the tower body located at the bottom of the tower, the exhaust structure is connected to the gas inlet; An observation port and a sampling port are arranged on the side wall of each level of the tower body.

[0005] Optionally, the exhaust structure includes a plurality of air inlet pipes and a gas distributor, the lower ends of the air inlet pipes penetrate the tower plate disposed below the tower body, and the upper ends of the air inlet pipes are connected to the gas distributor.

[0006] Optionally, the liquid drainage structure includes a liquid receiving pit and an overflow downpipe, the liquid receiving pit is arranged on the lower side of the tower plate below the tower body, the bottom of the liquid receiving pit is closed, the lower end of the overflow downpipe is inserted into the liquid receiving pit, and the upper end of the overflow downpipe extends to the adjacent tower body above.

[0007] Optionally, the air inlet pipe is connected to the gas distributor by a U-shaped pipe, and the top of the U-shaped pipe is higher than the top of the overflow downcomer of the tower body below.

[0008] Optionally, the exhaust structure includes a plurality of sieve holes, which are evenly arranged on the tower plate, and a heat exchange tube connected to the gas uniform bubble breaker is arranged in each level of the tower body, and fillers are arranged inside and on the top of the gas uniform bubble breaker.

[0009] Optionally, the gas uniform distribution bubble breaker is arranged in the horizontal direction, and the gas uniform distribution bubble breaker includes at least two single-layer components arranged in the vertical direction, and the setting directions of two adjacent single-layer components are perpendicular to each other. The single-layer components include at least five strip-shaped arch structures, each of the strip-shaped arch structures is composed of two arch-shaped baffles arranged in a chiral cross, the angle between the inclined surfaces of the two arch-shaped baffles is 45°~75°, the distance between the bottom edges of the two arch-shaped baffles is 5cm~15cm, the height of the arch-shaped baffle is 5cm~10cm, the upper and lower sides of the arch-shaped baffle are serrated, the coverage rate of the single-layer component relative to the tower plate is 70%~95%, and the opening rate of the single-layer component is 60%~90%.

[0010] Optionally, the sampling port includes a gas sampling port and a liquid sampling port, the gas sampling port is located at 70% to 90% of the height of the tower body side wall, and the liquid sampling port is located at 10% to 30% of the height of the tower body side wall.

[0011] Optionally, a plurality of observation ports are provided, and a side-view mirror is provided in each observation port, and the height of the side-view mirror is the same as the height of the gas distributor.

[0012] Optionally, in each level of the tower body, a liquid feed pipe or a gas feed pipe is provided in the observation port.

[0013] Optionally, the diameter of each level of the tower body is 200 mm to 2000 mm, and the height of each level of the tower body is 500 mm to 2500 mm.

[0014] The present invention provides a tower-type multi-stage series gas-liquid bubbling reactor, which has the following beneficial effects: 1. The reactor is provided with a gas distributor and an overflow downcomer, which can clearly separate the gas and liquid transfer paths in each level of the tower body, thereby realizing the series connection of multiple gas-liquid bubbling reactors in the reactor, minimizing the back mixing between the tower bodies at each level, and improving the efficiency of the unit volume reactor; 2. Each stage of the reactor is equipped with a gas uniform distribution bubble breaker, which can effectively reduce the size of bubbles and cut and break the large bubbles formed by aggregation, increase the area of ​​gas-liquid contact, and improve the mass transfer and reaction effects; 3. The reactor introduces liquid and gas from the top and bottom respectively, and realizes graded feeding through the liquid feed pipe and gas feed pipe arranged in each stage of the tower body. In this way, the operation of the multi-stage gas-liquid bubbling reactor is more flexible, and the reactor can be suitable for a more complex reaction system.

[0015] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] The above and other objects, features and advantages of the present invention will become more apparent through a more detailed description of exemplary embodiments of the present invention in conjunction with the accompanying drawings, wherein like reference numerals generally represent like components throughout the exemplary embodiments of the present invention.

[0017] Figure 1 A schematic structural diagram of a tower-type multi-stage series gas-liquid bubbling reactor according to an embodiment of the present invention is shown.

[0018] Figure 2 A schematic structural diagram of a sieve plate tower multi-stage series gas-liquid bubbling reactor according to an embodiment of the present invention is shown.

[0019] Figure 3 A schematic diagram of the lateral partial structure of a gas uniform distribution bubble breaker according to an embodiment of the present invention is shown.

[0020] Figure 4 A top view of a gas uniform distribution bubble breaker according to an embodiment of the present invention is shown.

[0021] Description of reference numerals: 1. Top layer of tower; 2. Bottom layer of tower; 3. Liquid inlet; 4. Gas outlet; 5. Drain port; 6. Gas inlet; 7. Liquid outlet; 8. Sieve hole tower plate; 9. Heat exchange tube; 10. Filler; 11. Downward sight mirror tower body; 12. First tower plate; 13. First air inlet pipe; 14. First gas distributor; 15. First overflow down pipe; 16. First liquid receiving pit; 17. Downward sight mirror; 18. First gas uniform distribution bubble breaker; 19. First gas sampling port; 20. First liquid sampling port; 21. Upward sight mirror tower body; 22. Second tower plate; 23. Second air inlet pipe; 24. Second gas distributor; 25. Second overflow down pipe; 26. Second liquid receiving pit; 27. Upward sight mirror; 28. Second gas uniform distribution bubble breaker; 29. ​​Second gas sampling port; 30. Second liquid sampling port; 31. Strip-shaped arch structure; 32. Arch baffle. DETAILED DESCRIPTION

[0022] The preferred embodiments of the present invention will be described in more detail below. Although the preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited by the embodiments set forth herein. On the contrary, these embodiments are provided to make the present invention more thorough and complete, and to fully convey the scope of the present invention to those skilled in the art.

[0023] The present invention provides a tower-type multi-stage series gas-liquid bubbling reactor, comprising: The inner cavity has a liquid inlet and a gas outlet at the top, a drain port at the bottom, and a liquid outlet and a gas inlet below the side wall of the inner cavity; Multiple tower plates, the tower plates divide the inner cavity into multiple tower bodies from top to bottom, each tower body is provided with an exhaust structure and a liquid discharge structure, and the liquid outlet and the gas inlet are both arranged in the tower body at the bottom; In each stage of the tower body, the exhaust structure is disposed through the tower plate located at the bottom, the drainage structure is disposed through the tower plate located at the top, and the liquid outlet of the drainage structure is located on the tower plate located at the bottom; A gas uniform distribution bubble breaker is arranged between the exhaust structure and the tower plate above the tower body; In the tower body located at the top of the tower, the liquid discharge structure is connected to the liquid inlet; In the tower body located at the bottom of the tower, the exhaust structure is connected to the gas inlet; Observation ports and sampling ports are arranged on the side walls of each level of the tower.

[0024] Specifically, the reactor is provided with a liquid inlet and a gas inlet and outlet. The liquid flows from the top to the bottom of the inner cavity, and the gas moves from the bottom to the top of the inner cavity. A drain port is provided at the very bottom of the reactor, so that the liquid that cannot be discharged from the liquid outlet and the impurities precipitated in the liquid can be discharged, thereby realizing regular cleaning of the reactor; a plurality of mutually parallel tower plates are provided in the cavity, and the tower plates are arranged in a horizontal direction to evenly divide the inner cavity into a multi-stage tower body, and each tower body is provided with an exhaust structure and a liquid discharge structure, but the top of the liquid discharge structure of the tower body located at the top layer of the tower is connected to the liquid inlet, so that the liquid can be injected into the reactor, and the exhaust structure in the tower body located at the bottom layer of the tower is connected to the gas inlet, so that the gas can be injected into the reactor, so that Liquid and gas can be transferred step by step through the internal exhaust structure and drainage structure; a gas uniform bubble breaker is also provided in each level of the tower body. The exhaust structure introduces the gas into the tower body, and the gas moves upward from the bottom of the tower body. When passing through the gas uniform bubble breaker, the gas can be evenly distributed, and the bubbles in the liquid in the same level of the tower body are also cut and broken by the gas uniform bubble breaker, which can increase the gas-liquid contact area and improve the mass transfer and reaction effects; observation ports and sampling ports are also provided in each level of the tower body. Through the set holes, when sampling is needed, the sampling port can be opened for sampling to monitor the mixing state of liquid and gas in the tower body at each level, and the state of gas-liquid mixing in the cavity can also be understood through the observation port.

[0025] Optionally, the exhaust structure includes a plurality of air inlet pipes and a gas distributor, the lower ends of the air inlet pipes penetrate through a tower plate disposed below the tower body, and the upper ends of the air inlet pipes are connected to the gas distributor.

[0026] Specifically, exhaust structures are provided at each level of the tower body. The gas enters the air inlet pipe of the lowest tower body through the gas inlet, and is introduced into the gas distributor through multiple air inlet pipes, so that the gas can be evenly discharged into the lowest tower body, and the gas moves to the top of the tower body. When the gas passes through the gas uniform distribution bubble breaker, the gas is evenly distributed again, and the gas can achieve full and efficient contact with the liquid. In each level of the tower body, there is an air inlet pipe that is introduced from the tower body below to the tower body of this level, and then evenly discharged by the gas distributor. The flow direction of the gas will not change, and the gas back mixing will be avoided.

[0027] Optionally, the air inlet pipe and the gas distributor are connected by a U-shaped pipe, and the top of the U-shaped pipe is higher than the top of the overflow downcomer of the tower body below.

[0028] Specifically, the air inlet pipe and the gas distributor are connected by an inverted U-shaped tube. In the same level of the tower body, in addition to the exhaust structure of the tower body of this level, there is also a top extension part of the overflow downcomer of the first level tower body located below. The top of the inverted U-shaped tube needs to be set higher than the top of the overflow downcomer of the tower body below.

[0029] Optionally, the exhaust structure includes a plurality of sieve holes, which are evenly arranged on the tower plate, and a heat exchange tube connected to the gas uniform bubble breaker is arranged in each stage of the tower body, and fillers are arranged inside and on the top of the gas uniform bubble breaker.

[0030] Specifically, the exhaust structure in each stage of the tower body can also be a sieve hole, and a plurality of sieve holes are evenly arranged on the tower plate of each stage of the tower body, so that the tower body gas located below is evenly discharged into the tower body of this stage through the sieve holes, and the gas can be evenly distributed during the flow process; in addition, in a multi-stage series gas-liquid bubbling reactor provided with a sieve plate, a heat exchange tube is also arranged in each stage of the tower body, and the heat exchange tube transfers heat to the liquid and gas in the reactor to improve the reaction efficiency.

[0031] Optionally, the liquid drainage structure includes a liquid receiving pit and an overflow downpipe. The liquid receiving pit is arranged on the lower side of the tower plate below the tower body. The bottom of the liquid receiving pit is closed. The lower end of the overflow downpipe is inserted into the liquid receiving pit, and the upper end of the overflow downpipe extends to the adjacent tower body above.

[0032] Specifically, the drainage structure provided in each level of the tower body includes a liquid receiving pit and an overflow downcomer. In the tower body located at the top layer, the overflow downcomer is connected to the liquid inlet. The liquid enters the cavity in this way. The liquid first fills the liquid receiving pit, and then as the liquid enters the tower body for a longer time, the liquid level of the tower body becomes higher and higher. When the liquid level is higher than the lower tower body and extends to the overflow downcomer of the tower body of this layer, the liquid enters the lower tower body through the overflow downcomer. In the lower tower body, it first accumulates in the liquid receiving pit, and then the liquid level slowly rises. When the liquid level is higher than the overflow downcomer of the lower tower body, it continues to flow to the next tower body, and finally realizes the flow of the liquid in the tower body step by step. In each level of the tower body, as the liquid level slowly rises, the liquid will come into contact with the gas uniformly distributed bubble breaker, which can separate and cut the bubbles in the liquid to increase the area of ​​gas-liquid contact.

[0033] Optionally, the gas uniformly distributed bubble breaker is arranged in the horizontal direction, and the gas uniformly distributed bubble breaker includes at least two single-layer components arranged in the vertical direction, and the arrangement directions of two adjacent single-layer components are perpendicular to each other. The single-layer components include at least five strip-shaped arch structures, and each strip-shaped arch structure is composed of two arch-shaped baffles arranged in a chiral cross, and the angle between the inclined surfaces of the two arch-shaped baffles is 45°~75°, the distance between the bottom edges of the two arch-shaped baffles is 5cm~15cm, the height of the arch-shaped baffles is 5cm~10cm, the upper and lower sides of the arch-shaped baffles are serrated, the coverage rate of the single-layer component relative to the tower plate is 70%~95%, and the opening rate of the single-layer component is 60%~90%.

[0034] Specifically, the gas uniformly distributed bubble breaker is formed by multiple single-layer components, each layer of components is arranged in the horizontal direction, and each layer of components is arranged in the horizontal direction. Multiple strip-shaped arch structures are arranged in one direction, and the arrangement directions of the strip-shaped arch structures in two adjacent single-layer components are perpendicular to each other; the single-layer component is composed of multiple strip-shaped arch structures, and each strip-shaped arch structure is formed by crossing two arch baffles.

[0035] Optionally, the sampling port includes a gas sampling port and a liquid sampling port, the gas sampling port is located at 70% to 90% of the height of the side wall of the tower body, and the liquid sampling port is located at 10% to 30% of the height of the side wall of the tower body.

[0036] Optionally, a plurality of observation ports are provided, and side view mirrors are provided in the observation ports, and the height of the side view mirrors is the same as the height of the gas distributor.

[0037] Optionally, in each stage of the tower body, a liquid feed pipe or a gas feed pipe is provided in the observation port.

[0038] Specifically, in each level of the tower body, in addition to providing a side-view mirror in the observation port for observing the mixing situation in the inner cavity, a liquid feed pipe and a gas feed pipe may also be provided in the observation port. In each level of the tower body located in the middle, gas or liquid is introduced as needed, thereby realizing flexible operation of the multi-stage series gas-liquid bubbling reactor.

[0039] Optionally, the diameter of each tower body is 200 mm to 2000 mm, and the height of each tower body is 500 mm to 2500 mm.

[0040] like Figure 1As shown, the present invention provides a tower-type multi-stage series gas-liquid bubbling reactor, wherein a liquid inlet 3 and a gas outlet 4 are arranged at the top of the reactor, a drain port 5 is arranged at the bottom, and a liquid outlet 7 and a gas inlet 6 are arranged below the side wall; three tower plates, the tower plates divide the inner cavity from top to bottom into a tower top layer 1, a lower mirror tower body 11, an upper mirror tower body 21 and a tower bottom layer 2, a lower mirror gas-liquid bubbling reactor is arranged in the lower mirror tower body 11, wherein the lower mirror tower body 11 and the upper mirror tower body 21 are separated by a first tower plate 12, the first tower plate 12 is located at the bottom of the lower mirror tower body 11, and an exhaust structure is formed by a plurality of first air inlet pipes 13 and a first gas distributor 14, and the first air inlet pipes 13 and a first gas distributor 14 form an exhaust structure. 13 is welded on the first tower plate 12 and communicated with the upper mirror tower body 21, the top of the first air inlet pipe 13 is connected with the first gas distributor 14, and a drainage structure is formed by the first overflow downcomer 15 and the first liquid receiving pit 16, the first liquid receiving pit 16 is welded on the first tower plate 12, the bottom of the first liquid receiving pit 16 is sealed, and the bottom of the first overflow downcomer 15 passes through the first tower plate 12 and is inserted into the first liquid receiving pit 16; at least two lower mirrors 17 are welded at the lower position of the outer wall of the lower mirror tower body 11, and a first gas sampling port 19 and a first liquid sampling port 20 are respectively arranged on the upper and lower parts of the outer wall, and a first gas uniform distribution bubble breaker 18 is arranged above the first gas distributor 14. An upper mirror gas-liquid bubbling reactor is arranged in the upper mirror tower body 21, wherein the upper mirror tower body 21 and the tower bottom layer 2 are separated by a second tower plate 22, the second tower plate 22 is located at the bottom of the upper mirror tower body 21, and an exhaust structure is formed by a plurality of second air inlet pipes 23 and a second gas distributor 24. The second air inlet pipe 23 is welded on the second tower plate 22 and communicated with the tower bottom layer 2, the top of the second air inlet pipe 23 is communicated with the second gas distributor 24, and a liquid discharge structure is formed by a second overflow downcomer 25 and a second liquid receiving pit 26. The second liquid receiving pit 26 is welded on the second tower plate 22, the bottom of the second liquid receiving pit 26 is sealed, the bottom of the second overflow downcomer 25 passes through the second tower plate 22 and is inserted into the second liquid receiving pit 26, at least two upper mirrors 27 are welded at the lower position of the outer wall of the upper mirror tower body 21, and a second gas sampling port 29 and a second liquid sampling port 30 are respectively arranged at the upper and lower parts of the outer wall, and a second gas uniform distribution bubble breaker 28 is arranged above the second gas distributor 24.

[0041] In this embodiment, the diameter of the tower-type multi-stage series gas-liquid bubbling reactor is 200 mm to 2000 mm, and the height of each stage of the tower body is 500 mm to 2500 mm.

[0042] In this embodiment, the structures of the first gas distributor 14 and the second gas distributor 24 are similar. The gas distributor can be in the shape of a field or a well. Uniformly distributed gas outlet holes with the same diameter are provided at the bottom of the gas distributor. The pore size is 1.0mm~5.0mm, and the opening rate is 0.1%~1.0%; the distance between the first gas distributor 14 and the first tower plate 12 is 3cm~30cm, and the gas velocity of the gas outlet is controlled at 15m / s~80m / s; the distance between the second gas distributor 24 and the second tower plate 22 is 5cm~40cm, and the gas velocity of the gas outlet is controlled at 20m / s~90m / s.

[0043] In this embodiment, the first overflow downcomer 15 and the second overflow downcomer 25 can be one or more, and the liquid descending speed therein is controlled at 0.1m / s~1.0m / s; the bottoms of the two overflow downcomers are respectively inserted into the liquid receiving pit of the next tower section, and the bottom ends thereof are 3cm~5cm below the tower plate of the next section; the top of the first overflow downcomer 15 is located at a height position of 50%~70% of the lower mirror tower body 11, and the top of the second overflow downcomer 25 is located at a height position of 60%~80% of the upper mirror tower body 21.

[0044] In this embodiment, the first air inlet pipe 13 and the second air inlet pipe 23 can be one or more, and the gas distributor and the tower plate can be directly connected, and the gas velocity in the air inlet pipe is controlled at 10m / s~20m / s; the air inlet pipe and the gas distributor can also be connected by an inverted U-shaped pipe, and the top of the U-shaped pipe is 10cm~30cm higher than the top of the overflow downcomer located in the tower body below, and the gas velocity in the air inlet pipe is controlled at 5m / s~15m / s.

[0045] In this embodiment, if Figure 3 and Figure 4 As shown, the gas uniform distribution bubble breaker in each stage of the tower body is located 10 cm to 50 cm above the gas distributor, and the gas uniform distribution bubble breaker is placed horizontally in the reactor. Structurally, the gas uniform distribution bubble breaker consists of 2 to 30 single-layer components, and the upper and lower adjacent single-layer components are horizontally staggered at 90°. The single-layer component is composed of 5 to 50 strip-shaped arch structures 31, each strip-shaped arch structure 31 is composed of two arch baffles 32 that are chirally crossed, the angle between the inclined surfaces of the two arch baffles 32 is 45° to 75°, the distance between the bottom edges of the two baffles is 5 cm to 15 cm, and the height of the arch baffle 32 is 5 cm to 10 cm; the upper and lower sides of the arch baffle 32 are serrated, the width between the two serrations is 5 mm to 10 mm, and the depth of the serrations is 8 mm to 15 mm; the coverage rate of the single-layer component on the cross section of the reactor is 70% to 95%, and the opening rate of the single-layer component (the ratio of the area of ​​the gas-liquid flow channel to the cross section of the reactor) is 60% to 90%.

[0046] In this embodiment, the lower mirror 17 is on the side wall of the tower body, and the lower mirror 17 is at the same height as the gas distributor; the upper mirror 27 is located on the side wall of the upper mirror tower body 21 10 cm to 20 cm higher than the top of the second overflow downcomer 25 .

[0047] In this embodiment, the pipe of the lower sight glass 17 can be changed into a liquid feed pipe to achieve the graded entry of liquid materials into the reactor; the pipe of the upper sight glass 27 can be changed into a gas feed pipe to achieve the graded entry of gas materials into the reactor.

[0048] In this embodiment, the first gas sampling port 19 and the second gas sampling port 29 are respectively arranged at 70%~90% height positions of the side walls of the lower mirror tower body 11 and the upper mirror tower body 21, and the first liquid sampling port 20 and the second liquid sampling port 30 are respectively located at 10%~30% height positions of the side walls of the lower mirror tower body 11 and the upper mirror tower body 21.

[0049] like Figure 2 As shown, the present invention also provides a sieve plate type tower multi-stage series gas-liquid bubbling reactor, most of the structure is the same as the structure of the tower multi-stage series gas-liquid bubbling reactor, except that the gas distributor between adjacent tower bodies is changed to a sieve hole tower plate 8, the diameter of the sieve hole is 1.0mm~5.0mm, and the opening rate is 0.1%~1.0%; as needed, heat exchange tubes 9 can be added in the reactor, and the heat exchange tubes 9 are respectively connected and fixed to the gas uniform distribution bubble breaker; fillers 10 can be added to the gas uniform distribution bubble breaker 18 and the gas uniform distribution bubble breaker, and can also be bulk fillers or structured fillers.

[0050] The specific implementation of the multi-stage series gas-liquid bubbling reactor: Example 1

[0051] A tower-type multi-stage series gas-liquid bubbling reactor has 6 stages of gas-liquid bubbling reactors, with a diameter of 800 mm and a height of 1200 mm for each stage, wherein the first stage is the top stage of the tower, the sixth stage is the lower stage of the tower, the second and fourth stages are lower-view mirror gas-liquid bubbling reactors, and the third and fifth stages are upper-view mirror gas-liquid bubbling reactors.

[0052] For the 2nd, 4th and 6th stage gas-liquid bubbling reactors, the first gas distributor is in a well shape, with a bottom aperture of Φ3mm, an open porosity of 0.25%, and is evenly distributed. The distance between the first gas distributor and the first tower plate is 5cm. The first overflow downcomer is set to 1, with a diameter of Φ57×3mm; the first overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 4cm below the next tower plate; the top of the first overflow downcomer is located at 70% of the height of the lower mirror tower body. Two first air inlet pipes with a diameter of Φ45×3mm are also provided to connect the first gas distributor with the first tower plate. The first gas uniformly distributed bubble breaker is located 40cm above the first gas distributor and is placed horizontally. The first gas uniformly distributed bubble breaker consists of 3 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles that are chirally crossed. The angle between the two arch-shaped baffles is 55°, the distance between the bottom edges of the two baffles is 6 cm, and the height of the arch-shaped baffle is 8 cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 6 mm, and the depth of the serrations is 8 mm. The coverage rate of the single-layer component on the cross section of the reactor is 75%, and the opening rate of the single-layer component is 80%. Two down-view mirrors are set on the side wall of the down-view mirror tower body, and the down-view mirror is at the same height as the first gas distributor. The first gas sampling port is located at 80% of the height of the side wall of the down-view mirror tower body, and the first liquid sampling port is located at 20% of the height of the side wall of the down-view mirror tower body.

[0053] For the 1st, 3rd and 5th stage gas-liquid bubbling reactors, the second gas distributor is in a well shape, with a bottom aperture of Φ3.2mm, an open porosity of 0.3%, and is evenly distributed. The distance between the second gas distributor and the second tower plate is 6cm. The second overflow downcomer is set to 1, with a diameter of Φ57×3mm; the second overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 5cm below the next tower plate; the top of the second overflow downcomer is located at 80% of the height of the upper mirror tower body. There are also 2 second air inlet pipes with a diameter of Φ45×3mm, which are connected to the second tower plate at the second gas distributor. The second gas uniformly distributed bubble breaker is located 35cm above the second gas distributor and is placed horizontally. The second gas uniformly distributed bubble breaker consists of 3 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles that are chirally crossed. The angle between the two arch-shaped baffles is 60°, the distance between the bottom edges of the two baffles is 6.5 cm, and the height of the arch-shaped baffle is 9 cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 6.5 mm, and the depth of the serrations is 8 mm. The coverage rate of the single-layer component on the cross section of the reactor is 73%, and the opening rate of the single-layer component is 86%. Two upper mirrors are arranged on the side wall of the upper mirror tower, and the upper mirror is 15 cm higher than the top of the second overflow downcomer. The second gas sampling port is located at 75% of the height of the side wall of the upper mirror tower, and the second liquid sampling port is located at 22% of the height of the side wall of the upper mirror tower.

[0054] The above-mentioned 6-stage gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 1000ppm enters the tower through the liquid inlet at the top of the tower top layer, flows through the 1-6-stage gas-liquid bubbling reactor from top to bottom, and maintains the liquid level of each stage through the first overflow downcomer and the second overflow downcomer, and finally flows out of the reactor through the liquid outlet on the upper side wall of the tower bottom layer. The liquid inlet flow rate is controlled at 2.5m 3 / h, the liquid residence time is 72.3min, and the liquid descending speed in the first overflow downcomer and the second overflow downcomer is controlled at 0.34m / s.

[0055] The gas with an ozone concentration of 48.8 mg / l from the air source ozone generator enters the tower from the gas inlet on the side wall of the bottom layer of the tower, and passes through the 6-1 gas-liquid bubbling reactor from bottom to top. In each gas-liquid bubbling reactor, it is evenly distributed in the reactor for the first time through the first gas distributor or the second gas distributor, and then redistributed through the first gas uniform bubble breaker or the second gas uniform bubble breaker, and fully and efficiently contacts the liquid, and finally discharges the reactor through the gas outlet at the top of the top layer of the tower. The gas flow rate is 150m 3 / h, the empty tower gas velocity is 0.083m / s, the gas velocity in each layer of the air inlet pipe is 15.8m / s, the gas outlet velocity at the bottom of the first gas distributor is 33.2m / s, and the gas outlet velocity at the bottom of the second gas distributor is 27.6m / s.

[0056] The wastewater discharged from the liquid outlet on the upper side wall of the bottom layer of the tower contains 48 ppm of phenol, and the phenol degradation rate can reach 95.2%. Example 2

[0057] A tower-type multi-stage series gas-liquid bubbling reactor has 8 stages of gas-liquid bubbling reactors, with a diameter of 600 mm and a height of 1000 mm for each stage, wherein the first stage is the top layer of the tower, the eighth stage is the lower layer of the tower, the second, fourth and sixth stages are lower-view mirror gas-liquid bubbling reactors, and the third, fifth and seventh stages are upper-view mirror gas-liquid bubbling reactors.

[0058] For the 2, 4, 6, and 8-stage gas-liquid bubbling reactors, the first gas distributor is cross-shaped, with a bottom aperture of Φ2mm, an open porosity of 0.2%, and is evenly distributed. The distance between the first gas distributor and the first tower plate is 15cm. The first overflow downcomer is set to 1, with a diameter of Φ45×3mm; the first overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 4cm below the next tower plate; the top of the first overflow downcomer is located at 75% of the height of the lower mirror tower body. Two first air inlet pipes with a diameter of Φ45×3mm are set to connect the first gas distributor with the first tower plate. The first gas uniformly distributed bubble breaker is located 30cm above the first gas distributor and is placed horizontally. The first gas uniformly distributed bubble breaker consists of 5 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 6 strip-shaped arch structures, each of which is composed of two arch-shaped baffles with chiral crosses, the angle between the two arch-shaped baffles is 70°, the distance between the bottom edges of the two baffles is 7cm, and the height of the arch-shaped baffle is 7cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 8mm, and the depth of the serrations is 8mm. The coverage rate of the single-layer component on the cross section of the reactor is 73%, and the opening rate of the single-layer component is 82%. Two down-view mirrors are set on the side wall of the down-view mirror tower body, and the down-view mirror is at the same height as the first gas distributor. The first gas sampling port is located at 90% of the height of the side wall of the down-view mirror tower body, and the first liquid sampling port is located at 15% of the height of the side wall of the down-view mirror tower body.

[0059] For the 1st, 3rd, 5th and 7th stage gas-liquid bubbling reactors, the second gas distributor is cross-shaped, with a bottom aperture of Φ2mm, an open porosity of 0.25%, and is evenly distributed. The distance between the second gas distributor and the second tower plate is 6cm. The second overflow downcomer is set to 1, with a diameter of Φ57×3mm; the second overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 5cm below the next tower plate; the top of the second overflow downcomer is located at 75% of the height of the upper mirror tower body. Two second air inlet pipes with a diameter of Φ45×3mm are set, which are connected to the second tower plate at the second gas distributor. The second gas uniformly distributed bubble breaker is located 35cm above the second gas distributor and is placed horizontally. The second gas uniformly distributed bubble breaker consists of 5 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles with chirality crossing, the angle between the two arch-shaped baffles is 65°, the distance between the bottom edges of the two baffles is 7cm, and the height of the arch-shaped baffle is 8cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 7mm, and the depth of the serrations is 9mm. The coverage rate of the single-layer component on the cross section of the reactor is 75%, and the opening rate of the single-layer component is 81%. Two upper mirrors are set on the side wall of the upper mirror tower, and the upper mirror is 15cm higher than the top of the overflow downcomer. The second gas sampling port is located at 80% of the height of the side wall of the upper mirror tower, and the second liquid sampling port is located at 20% of the height of the side wall of the upper mirror tower.

[0060] The above 8-stage gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 2000ppm enters the tower through the liquid inlet at the top of the tower top layer, flows through the 1-8-stage gas-liquid bubbling reactor from top to bottom, and the liquid level of each stage is maintained by two overflow downcomers, and finally flows out of the reactor through the liquid outlet on the upper side wall of the tower bottom layer. The liquid inlet flow rate is controlled at 2m 3 / h, the liquid residence time is 50.9min, and the liquid descending speed in the first overflow downcomer and the second overflow downcomer is controlled at 0.27m / s.

[0061] The gas with an ozone concentration of 113 mg / l from the oxygen source ozone generator enters the tower from the gas inlet on the side wall of the bottom layer of the tower, and passes through the 8-1 gas-liquid bubbling reactor from bottom to top. In each gas-liquid bubbling reactor, it is evenly distributed in the reactor for the first time through the first gas distributor or the second gas distributor, and then redistributed through the first gas uniform bubble breaker or the second gas uniform bubble breaker, and fully and efficiently contacts the liquid, and finally discharges the reactor through the gas outlet at the top of the top layer of the tower. The gas flow rate is 100m 3 / h, the empty tower gas velocity is 0.098m / s, the gas velocity in each layer of the air inlet pipe is 10.5m / s, the gas outlet velocity at the bottom of the first gas distributor is 49.2m / s, and the gas outlet velocity at the bottom of the second gas distributor is 39.3m / s.

[0062] The wastewater discharged from the liquid outlet on the upper side wall of the bottom layer of the tower contains 37 ppm of phenol, and the phenol degradation rate can reach 98.2%. Example 3

[0063] A tower-type multi-stage series gas-liquid bubbling reactor has 6 stages of gas-liquid bubbling reactors, with a diameter of 700 mm and a height of 1200 mm for each stage, wherein the first stage is the top stage of the tower, the sixth stage is the lower stage of the tower, the second and fourth stages are lower-view mirror gas-liquid bubbling reactors, and the third and fifth stages are upper-view mirror gas-liquid bubbling reactors.

[0064] For the 2nd, 4th and 6th stage gas-liquid bubbling reactors, the first gas distributor is in a well shape, with a bottom aperture of Φ2.5mm, an open porosity of 0.3%, and is evenly distributed. The distance between the first gas distributor and the first tower plate is 35cm. The first overflow downcomer is set to 1, with a diameter of Φ57×3mm; the first overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom end is 6cm below the next tower plate; the top of the first overflow downcomer is located at 67% of the height of the lower mirror tower body. There are also two first air inlet pipes with a diameter of Φ57×3mm, which are connected to the first tower plate through an inverted U-shaped pipe in the first gas distributor, and the top of the inverted U-shaped pipe is 150mm higher than the top of the first overflow downcomer. The first gas uniformly distributed bubble breaker is located 40cm above the first gas distributor and is placed horizontally. The first gas uniformly distributed bubble breaker consists of 6 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles that are chirally crossed. The angle between the inclined surfaces of the two arch-shaped baffles is 55°, the distance between the bottom edges of the two baffles is 7cm, and the height of the arch-shaped baffle is 8cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 6mm, and the depth of the serrations is 8mm. The coverage rate of the single-layer component on the cross section of the reactor is 76%, and the opening rate of the single-layer component is 82%. Two down-view mirrors are arranged on the side wall of the down-view mirror tower, and their positions are at the same height as the first gas distributor. The first gas sampling port is located at 70% of the height of the side wall of the down-view mirror tower, and the first liquid sampling port is located at 20% of the height of the side wall of the down-view mirror tower.

[0065] For the 1st, 3rd, and 5th-stage gas-liquid bubbling reactors, the second gas distributor is in a well shape, with a bottom aperture of Φ3.2mm, an open porosity of 0.4%, and is evenly distributed. The distance between the second gas distributor and the second tower plate is 6cm, and the gas velocity of the gas outlet is controlled at 25m / s~35m / s. The second overflow downcomer is set to 1, with a diameter of Φ57×3mm. The second overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 5cm below the next tower plate; the top of the second overflow downcomer is located at 70% of the height of the upper mirror tower body. Set up 2 second air inlet pipes with a diameter of Φ57×3mm, and the second gas distributor is connected to the second tower plate through an inverted U-shaped pipe. The top of the inverted U-shaped pipe is 150mm higher than the top of the second overflow downcomer. The second gas uniformly distributed bubble breaker is located 35cm above the second gas distributor and is placed horizontally. The second gas uniformly distributed bubble breaker consists of 6 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles that are chirally crossed. The angle between the two arch-shaped baffles is 60°, the distance between the bottom edges of the two baffles is 7 cm, and the height of the arch-shaped baffle is 8 cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 6.5 mm, and the depth of the serrations is 8 mm. The coverage rate of the single-layer component on the cross section of the reactor is 76%, and the opening rate of the single-layer component is 82%. Two upper mirrors are arranged on the side wall of the upper mirror tower, and their height is 15 cm higher than the top of the second overflow downcomer. The second gas sampling port is located at 75% of the height of the side wall of the upper mirror tower, and the second liquid sampling port is located at 20% of the height of the side wall of the upper mirror tower.

[0066] The above-mentioned 6-stage gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 1500ppm enters the tower through the liquid inlet at the top of the tower top layer, flows through the 1-6-stage gas-liquid bubbling reactor from top to bottom, and maintains the liquid level of each stage through the first overflow downcomer and the second overflow downcomer, and finally flows out of the reactor through the liquid outlet on the upper side wall of the tower bottom layer. The liquid inlet flow rate is controlled at 1.3m 3 / h, the liquid residence time is 106.5min, and the liquid descending speed in the first overflow downcomer and the second overflow downcomer is controlled at 0.18m / s.

[0067] The gas with an ozone concentration of 43.6 mg / l from the air source ozone generator enters the tower from the gas inlet on the side wall of the bottom layer of the tower, and passes through the 6-1 gas-liquid bubbling reactor from bottom to top. In each gas-liquid bubbling reactor, it is evenly distributed in the reactor for the first time through the first gas distributor or the second gas distributor, and then redistributed through the first gas uniform bubble breaker or the second gas uniform bubble breaker, and fully and efficiently contacts the liquid, and finally discharges the reactor through the gas outlet at the top of the top layer of the tower. The gas flow rate is 120m 3 / h, the empty tower gas velocity is 0.087m / s, the gas velocity in each layer of the air inlet pipe is 9.5m / s, the gas outlet velocity at the bottom of the first gas distributor is 28.9m / s, and the gas outlet velocity at the bottom of the second gas distributor is 21.7m / s.

[0068] The wastewater discharged from the liquid outlet on the upper side wall of the bottom layer of the tower contains 47 ppm of phenol, and the phenol degradation rate can reach 96.9%. Example 4

[0069] A tower-type multi-stage series gas-liquid bubbling reactor has 6 stages of gas-liquid bubbling reactors, with a diameter of 800 mm and a height of 1200 mm for each stage, wherein the first stage is the top stage of the tower, the sixth stage is the lower stage of the tower, the second and fourth stages are lower-view mirror gas-liquid bubbling reactors, and the third and fifth stages are upper-view mirror gas-liquid bubbling reactors.

[0070] For the 2nd, 4th and 6th stage gas-liquid bubbling reactor, the tower plate is a sieve hole tower plate with a sieve hole diameter of 4.0mm and an opening rate of 0.3%. The first overflow downcomer is set to 1 with a diameter of Φ57×3mm; the first overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom end is 4cm below the next tower plate; the top of the first overflow downcomer is located at 70% of the height of the lower mirror tower body. The first gas uniform distribution bubble breaker is located 40cm above the first gas distributor and is placed horizontally. The first gas uniform distribution bubble breaker consists of 3 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component consists of 8 strip-shaped arch structures, each of which consists of two arch baffles with chiral cross-sections, the angle between the two arch baffles is 55°, the distance between the bottom edges of the two baffles is 6cm, and the height of the arch baffle is 8cm. The upper and lower sides of the arch baffle are serrated, the width between the two serrations is 6mm, and the depth of the serrations is 8mm. The coverage rate of the single-layer component on the reactor cross section is 75%, and the opening rate of the single-layer component is 80%. The first gas uniform distribution bubble breaker is a BX300 type structured packing with a packing height of 400mm. Two down-view mirrors are set on the side wall of the down-view mirror tower, 150mm above the sieve plate. The first gas sampling port is located at 80% of the height of the side wall of the down-view mirror tower, and the first liquid sampling port is located at 20% of the height of the side wall of the down-view mirror tower.

[0071] For the 1st, 3rd and 5th stage gas-liquid bubbling reactors, the tower plates are sieve-hole tower plates with a sieve hole diameter of 3.5 mm and an opening rate of 0.3%. The second overflow downcomer is set to 1 with a diameter of Φ57×3 mm; the second overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 5 cm below the next tower plate; the top of the second overflow downcomer is located at 80% of the height of the upper mirror tower body. The second gas uniform bubble breaker is located 35 cm above the second gas distributor and is placed horizontally. The second gas uniform bubble breaker consists of 3 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component consists of 8 strip-shaped arch structures, each of which consists of two arch-shaped baffles with chiral cross-sections, the angle between the inclined surfaces of the two arch-shaped baffles is 60°, the distance between the bottom edges of the two baffles is 6.5 cm, and the height of the arch-shaped baffle is 9 cm. The upper and lower sides of the arched baffle are serrated, the width between the two serrations is 6.5mm, and the depth of the serrations is 8mm. The coverage rate of the single-layer component to the cross section of the reactor is 73%, and the opening rate of the single-layer component is 86%. Above the second gas uniform distribution bubble breaker is the BX300 type structured packing, and the packing height is 400mm. Two upper mirrors are arranged on the side wall of the upper mirror tower, 15cm higher than the top of the second overflow downcomer. The second gas sampling port is located at 80% of the height of the side wall of the upper mirror tower, and the second liquid sampling port is located at 20% of the height of the side wall of the upper mirror tower.

[0072] The above-mentioned 6-stage gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 1000ppm enters the tower through the liquid inlet at the top of the tower top layer, flows through the 1-6-stage gas-liquid bubbling reactor from top to bottom, and the liquid level of each stage is maintained by two overflow downcomers, and finally flows out of the reactor through the liquid outlet on the upper side wall of the tower bottom layer. The liquid inlet flow rate is controlled at 5.8m 3 / h, the liquid residence time is 31.2min, and the liquid descending speed in the two overflow downcomers is controlled at 0.79m / s.

[0073] The gas with an ozone concentration of 122 mg / l from the oxygen source ozone generator enters the tower from the gas inlet on the side wall of the bottom layer of the tower, and passes through the 6-1 gas-liquid bubbling reactor from bottom to top. In each gas-liquid bubbling reactor, the gas is distributed through the sieve plate, and then redistributed through the first gas uniform bubble breaker or the second gas uniform bubble breaker, and then fully and efficiently contacts the liquid through the structured packing, and finally discharges the reactor through the gas outlet at the top of the top layer of the tower. The gas flow rate is 150m 3 / h, the empty tower gas velocity is 0.083m / s, and the tower plate sieve hole gas velocity is 27.7m / s.

[0074] The wastewater discharged from the liquid outlet on the upper side wall of the bottom layer of the tower contains 39 ppm of phenol, and the phenol degradation rate can reach 96.1%. Example 5

[0075] A tower-type multi-stage series gas-liquid bubbling reactor has 6 stages of gas-liquid bubbling reactors, with a diameter of 800 mm and a height of 1200 mm for each stage, wherein the first stage is the top stage of the tower, the sixth stage is the lower stage of the tower, the second and fourth stages are lower-view mirror gas-liquid bubbling reactors, and the third and fifth stages are upper-view mirror gas-liquid bubbling reactors.

[0076] For the 2nd, 4th and 6th stage gas-liquid bubbling reactors, the first gas distributor is cross-shaped, with a bottom aperture of Φ3mm, an open porosity of 0.25%, and is evenly distributed. The distance between the first gas distributor and the first tower plate is 5cm. The first overflow downcomer is set to 1, with a diameter of Φ57×3mm; the first overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 4cm below the next tower plate; the top of the first overflow downcomer is located at 70% of the height of the lower mirror tower body. Two first air inlet pipes with a diameter of Φ45×3mm are set to connect the first gas distributor to the first tower plate. The first gas uniformly distributed bubble breaker is located 40cm above the first gas distributor and is placed horizontally. The first gas uniformly distributed bubble breaker consists of 3 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles with chiral cross-sections. The angle between the two arch-shaped baffles is 55°, the distance between the bottom edges of the two baffles is 6 cm, and the height of the arch-shaped baffle is 8 cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 6 mm, and the depth of the serrations is 8 mm. The coverage rate of the single-layer component on the cross section of the reactor is 75%, and the opening rate of the single-layer component is 80%. Two down-view mirrors are set on the side wall of the down-view mirror tower body, at the same height as the first gas distributor. The first gas sampling port is located at 80% of the height of the side wall of the down-view mirror tower body, and the first liquid sampling port is located at 20% of the height of the side wall of the down-view mirror tower body.

[0077] For the 1st, 3rd and 5th stage gas-liquid bubbling reactors, the second gas distributor is in a well shape, with a bottom aperture of Φ3.2mm, an open porosity of 0.3%, and is evenly distributed. The distance between the second gas distributor and the second tower plate is 6cm. The second overflow downcomer is set to 1, with a diameter of Φ57×3mm; the second overflow downcomer is inserted into the liquid receiving pit of the next tower section, and its bottom is 5cm below the next tower plate; the top of the second overflow downcomer is located at 80% of the height of the upper mirror tower body. Two second air inlet pipes with a diameter of Φ45×3mm are set, which are connected to the second tower plate at the second gas distributor. The second gas uniformly distributed bubble breaker is located 35cm above the second gas distributor and is placed horizontally. The second gas uniformly distributed bubble breaker consists of 3 single-layer components, and the upper and lower adjacent single-layer components are staggered at 90° horizontally. The single-layer component is composed of 8 strip-shaped arch structures, each of which is composed of two arch-shaped baffles that are chirally crossed. The angle between the inclined surfaces of the two arch-shaped baffles is 60°, the distance between the bottom edges of the two baffles is 6.5 cm, and the height of the arch-shaped baffle is 9 cm. The upper and lower sides of the arch-shaped baffle are serrated, the width between the two serrations is 6.5 mm, and the depth of the serrations is 8 mm. The coverage rate of the single-layer component on the cross section of the reactor is 73%, and the opening rate of the single-layer component is 86%. Two upper mirrors are set on the side wall of the upper mirror tower, 15 cm higher than the top of the second overflow downcomer. The second gas sampling port is located at 75% of the height of the side wall of the upper mirror tower, and the second liquid sampling port is located at 22% of the height of the side wall of the upper mirror tower.

[0078] The upper sight glass of the 3rd and 5th stage gas-liquid bubbling reactors is changed to a gas inlet.

[0079] The above-mentioned 6-stage gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 1000ppm enters the tower through the liquid inlet at the top of the tower top layer, flows through the 1-6-stage gas-liquid bubbling reactor from top to bottom, and the liquid level of each stage is maintained by two overflow downcomers, and finally flows out of the reactor through the liquid outlet on the upper side wall of the tower bottom layer. The liquid inlet flow rate is controlled at 5.5m 3 / h, the liquid residence time is 32.9min, and the liquid descending speed in the two overflow downcomers is controlled at 0.75m / s.

[0080] The gas with an ozone concentration of 108 mg / l from the oxygen source ozone generator enters the tower from the gas inlet on the side wall of the bottom layer of the tower, and passes through the 6-1 gas-liquid bubbling reactor from bottom to top. In each gas-liquid bubbling reactor, it is evenly distributed in the reactor for the first time through two gas distributors, and then redistributed through two gas uniform bubble breakers. At the same time, part of the ozone-containing gas enters from the newly modified gas inlet on the side wall of the 3rd and 5th gas-liquid bubbling reactor, merges into the mainstream gas in the tower, and fully and efficiently contacts with the liquid. Finally, all the gas is discharged from the reactor through the gas outlet at the top of the top layer of the tower.

[0081] The gas flow rate entering the tower from the gas inlet on the side wall of the bottom layer of the tower is 100m 3 / h, the gas flow rate into each layer of level 3 and 5 is 20m 3 / h, the gas velocity in the air inlet pipe is 11.8m / s~16.8m / s, the gas outlet velocity at the bottom of the first gas distributor is 27.2m / s~35m / s, and the gas outlet velocity at the bottom of the second gas distributor is 27.6m / s~38.0m / s.

[0082] The wastewater discharged from the liquid outlet on the upper side wall of the bottom layer of the tower contains 28 ppm of phenol, and the phenol degradation rate can reach 97.2%.

[0083] Comparative Example 1 A tower gas-liquid bubbling reactor, the overall size of which is the same as that of Example 1, with a diameter of 800 mm, a total feed liquid height of 6 m, 5 layers of corrugated sieve plates added in the middle, and the tower gas-liquid bubbling reactor is evenly divided into 6 layers, a well-shaped gas distributor is provided at the bottom of the tower, the bottom opening is Φ3 mm, the opening rate is 0.25%, and the porous structure is evenly distributed.

[0084] The above tower gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 1000 ppm enters the tower through the top of the tower, flows through the gas-liquid bubbling reactor from top to bottom, and flows out of the reactor through the liquid outlet at the bottom of the tower. The liquid inlet flow rate is controlled at 2.5m 3 / h, and the liquid residence time is 72.3min.

[0085] The gas with an ozone concentration of 47.8 mg / l from the air source ozone generator enters the tower from the gas distributor at the bottom of the tower, passes through the gas-liquid bubbling reactor from bottom to top, contacts and reacts with the liquid, and finally exits the reactor through the gas outlet at the top of the tower. The gas flow rate is 150m 3 / h, the empty tower gas velocity is 0.083m / s, and the gas outlet velocity at the bottom of the gas distributor is 33.2m / s.

[0086] The phenol content in the wastewater discharged from the liquid outlet on the side wall of the bottom layer of the tower is 349 ppm, and the phenol degradation rate can reach 65.1%.

[0087] Comparative Example 2 A tower gas-liquid bubbling reactor, the overall size of which is the same as that of Example 4, with a diameter of 800 mm and a total feed-liquid height of 6 m. Five layers of corrugated sieve plates are added in the middle to evenly divide the tower gas-liquid bubbling reactor into 6 layers. A well-shaped gas distributor is provided at the bottom of the tower, with a bottom opening of Φ3 mm and an opening rate of 0.3%, which is evenly distributed porous.

[0088] The above tower gas-liquid bubbling reactor is used in the ozone oxidation system of phenol-containing wastewater. Wastewater with a phenol concentration of 1000 ppm enters the tower through the top of the tower, flows through the gas-liquid bubbling reactor from top to bottom, and flows out of the reactor through the liquid outlet at the bottom of the tower. The liquid inlet flow rate is controlled at 5.8m 3 / h, and the liquid residence time is 31.2min.

[0089] The gas with an ozone concentration of 121 mg / l from the oxygen source ozone generator enters the tower from the gas distributor at the bottom of the tower, passes through the gas-liquid bubbling reactor from bottom to top, contacts and reacts with the liquid, and finally exits the reactor through the gas outlet at the top of the tower. The gas flow rate is 150m 3 / h, the empty tower gas velocity is 0.083m / s, and the gas outlet velocity at the bottom of the gas distributor is 27.2m / s.

[0090] The phenol content in the wastewater discharged from the liquid outlet on the side wall of the bottom layer of the tower was 307 ppm, and the phenol degradation rate was 69.3%.

[0091] The embodiments of the present invention have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A tower-type multi-stage series gas-liquid bubbling reactor, characterized in that: include: The inner cavity has a liquid inlet and a gas outlet at the top, a drain port at the bottom, and a liquid outlet and a gas inlet below the side wall of the inner cavity; A plurality of tower plates, wherein the tower plates divide the inner cavity into multiple tower bodies from top to bottom, each tower body is provided with an exhaust structure and a liquid discharge structure, and the liquid outlet and the gas inlet are both provided in the tower body at the lowest end; In each stage of the tower body, the exhaust structure is disposed through the tower plate located at the bottom, the drainage structure is disposed through the tower plate located at the top, and the liquid outlet of the drainage structure is located on the tower plate located at the bottom; A gas uniform distribution bubble breaker is arranged between the exhaust structure and the tower plate above the tower body; In the tower body located at the top of the tower, the liquid drainage structure is connected to the liquid inlet; In the tower body located at the bottom of the tower, the exhaust structure is connected to the gas inlet; An observation port and a sampling port are arranged on the side wall of each level of the tower body.

2. The tower type multi-stage series gas-liquid bubbling reactor according to claim 1, characterized in that: The exhaust structure includes a plurality of air inlet pipes and a gas distributor. The lower ends of the air inlet pipes penetrate the tower plate arranged below the tower body, and the upper ends of the air inlet pipes are connected to the gas distributor.

3. The tower type multi-stage series gas-liquid bubbling reactor according to claim 2, characterized in that: The liquid drainage structure includes a liquid receiving pit and an overflow downpipe. The liquid receiving pit is arranged on the lower side of the tower plate below the tower body. The bottom of the liquid receiving pit is closed. The lower end of the overflow downpipe is inserted into the liquid receiving pit, and the upper end of the overflow downpipe extends to the adjacent tower body above.

4. The tower type multi-stage series gas-liquid bubbling reactor according to claim 3, characterized in that: The air inlet pipe is connected to the gas distributor by a U-shaped pipe, and the top of the U-shaped pipe is higher than the top of the overflow downcomer of the tower body below.

5. The tower type multi-stage series gas-liquid bubbling reactor according to claim 1, characterized in that: The exhaust structure includes a plurality of sieve holes, which are evenly arranged on the tower plate. A heat exchange tube connected to the gas uniformly distributed bubble breaker is arranged in each stage of the tower body, and fillers are arranged inside and on the top of the gas uniformly distributed bubble breaker.

6. The tower type multi-stage series gas-liquid bubbling reactor according to claim 2, characterized in that: The gas uniformly distributed bubble breaker is arranged in the horizontal direction, and the gas uniformly distributed bubble breaker includes at least two single-layer components arranged in the vertical direction, and the arrangement directions of two adjacent single-layer components are perpendicular to each other. The single-layer components include at least five strip-shaped arch structures, and each of the strip-shaped arch structures is composed of two arch-shaped baffles arranged in a chiral cross, and the angle between the inclined surfaces of the two arch-shaped baffles is 45°~75°, the distance between the bottom edges of the two arch-shaped baffles is 5cm~15cm, the height of the arch-shaped baffle is 5cm~10cm, and the upper and lower sides of the arch-shaped baffle are serrated. The coverage rate of the single-layer component relative to the tower plate is 70%~95%, and the opening rate of the single-layer component is 60%~90%.

7. The tower type multi-stage series gas-liquid bubbling reactor according to claim 1, characterized in that: The sampling port includes a gas sampling port and a liquid sampling port. The gas sampling port is located at 70% to 90% of the height of the side wall of the tower body, and the liquid sampling port is located at 10% to 30% of the height of the side wall of the tower body.

8. The tower type multi-stage series gas-liquid bubbling reactor according to claim 2, characterized in that: There are multiple observation ports, each of which is provided with a side-view mirror, and the height of the side-view mirror is the same as the height of the gas distributor.

9. The tower type multi-stage series gas-liquid bubbling reactor according to claim 1, characterized in that: In each level of the tower body, a liquid feed pipe or a gas feed pipe is arranged in the observation port.

10. The tower type multi-stage series gas-liquid bubbling reactor according to claim 1, characterized in that: The diameter of each level of the tower body is 200mm~2000mm, and the height of each level of the tower body is 500mm~2500mm.

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