Gas-liquid jet bubbling reactor

Abstract

The present application relates to gas-liquid mixing reaction technical field, specifically to a kind of gas-liquid jet bubbling reactor, including reactor, distribution unit one, distribution unit two and adjusting unit.The size ratio between branch pipe one and reactor diameter is set in the present application, and the uniformity of gas bubble after pumping out is improved by increasing the number of branch pipe two and the uniform distribution of gas outlet hole, the gas holdup in unit area is improved, the problems of bubble coalescence effect and low shearing bubble efficiency are reduced, so as to improve the mass transfer efficiency between final gas and liquid;By setting the angle of gas outlet hole to 45 degrees, an inverted V-shaped pumping area is formed in the front-to-back direction, which improves the gas coverage range, i.e., the gas holdup in unit area, and the angle of gas outlet hole can be adjusted to adapt to different reaction volume requirements, and the gas outlet holes are distributed staggered, reducing the probability of coalescence reaction between bubbles generated by adjacent gas outlet holes, improving the uniformity of bubble distribution and the final mass transfer efficiency.

Description

Technical Field

[0001] This invention relates to the field of gas-liquid mixing reaction technology, specifically a gas-liquid jet bubbling reactor. Background Technology

[0002] The gas-liquid jet bubbling reactor is an enhanced reaction device that combines high-speed jet technology and bubbling mixing principle. It replaces the traditional stirring action with high-speed liquid jet and breaks up bubbles through the shearing action of the jet, thereby enhancing mixing and mass transfer. It is mainly used for chemical reaction processes controlled by gas-liquid mass transfer.

[0003] The current gas-liquid jet bubbling reactor consists of main components such as a sealed reactor body, liquid nozzles, and a gas distributor. Both the liquid nozzles and the gas distributor are located in the lower part of the reactor, with the liquid nozzles positioned below the gas distributor. During operation, the liquid nozzles spray liquid upwards, covering the gas distributor. The gas distributor then pumps gas below the liquid surface, causing the gas to move downwards and then rise in the form of bubbles. During this process, the high pressure of the liquid ejection shears, breaks, and disperses the bubble group, increasing the gas-liquid contact area. During the gas-liquid contact process, the gas and liquid react with each other, producing numerous reactants, which are then collected.

[0004] The following problems exist with current gas-liquid jet bubbling reactors: 1. Existing gas distributors typically consist of a main pipe coaxial with the reactor and multiple secondary pipes located below the main pipe. During gas distribution, gas is ejected downwards into the liquid through the secondary pipes. In this process, the gas ejection angle is fixed. Furthermore, the secondary pipes below are mainly concentrated in the middle area of ​​the lower part of the reactor. Therefore, during jet operation, the bubble distribution direction is concentrated, which easily leads to excessive bubble occupancy per unit area, resulting in bubble coalescence effect and low shear bubble efficiency, thus affecting the final mass transfer efficiency between gas and liquid.

[0005] 2. In the existing liquid ejection process, the liquid ejection direction is fixed upward, so the probability of gas-liquid contact is limited. Therefore, the actual effect of the shearing action is affected, which in turn affects the final mass transfer efficiency between gas and liquid. Summary of the Invention

[0006] Therefore, it is necessary to provide a gas-liquid jet bubbling reactor to solve the problems of the prior art.

[0007] This application provides a gas-liquid jet bubbling reactor, comprising: a reactor, the reactor being a sealed structure, wherein a distribution unit one for ejecting the gas phase and a distribution unit two for ejecting the liquid phase are disposed inside the reactor, the distribution unit two being located below the distribution unit one.

[0008] The distribution unit 1 includes a main pipe, a vertically oriented main pipe is fixedly sleeved on the upper side of the reactor, a branch pipe 1 extending horizontally is fixedly installed below the main pipe, and multiple branch pipes 2 arranged equidistantly from left to right and extending horizontally on both the front and rear sides of the branch pipe 1 are provided. Both the branch pipe 1 and the branch pipe 2 are provided with air outlet holes facing the distribution unit 2.

[0009] The second distribution unit includes a rotating cylinder. A vertically oriented rotating cylinder is rotatably mounted below the reactor. A horizontally oriented branch pipe is fixedly mounted at the upper end of the rotating cylinder, and multiple liquid outlets are provided on the branch pipe.

[0010] The first branch pipe is equipped with an adjustment unit for adjusting the orientation of the air outlet on the second branch pipe.

[0011] The reactor is equipped with a spiral guide plate located above the distribution unit.

[0012] Branch pipe 1 and branch pipe 2 form a porous, uniformly downward-facing gas phase ejection area on the lower side of the reactor, while branch pipe 3 forms a synchronously rotating, porous, upward-facing liquid phase ejection area. The actual reaction area of ​​the gas phase ejection area is adjusted by the adjustment unit, and the gas and liquid phases are guided by the guide plate to form bubbles that slowly rise along the lower spiral surface, ultimately forming a multi-point angle adjustable bubbling reaction operation on the lower side in conjunction with the slow guidance of the spiral.

[0013] According to an advantageous embodiment, two branch pipes two located directly below the main pipe are fixedly installed on the branch pipe one. The two branch pipes two have two rows of air outlets, both of which are vertically downward, and the corresponding air outlets in each row are equidistantly distributed from front to back.

[0014] The remaining branch pipe 2 is rotatably mounted on the branch pipe 1; in the initial state, the remaining branch pipe 2 has two rows of air outlets, one on the left and one on the right, and each row is at a 45-degree angle to the vertical lateral section of the corresponding branch pipe 2. The corresponding air outlets in each row are equidistant from front to back.

[0015] According to an advantageous embodiment, two adjacent air outlets on the same branch pipe are staggered left and right, and the air outlet on the middle branch pipe is staggered front and back from the air outlet on the adjacent branch pipe.

[0016] According to an advantageous embodiment, the length of all said branch pipes two gradually increases from both ends of branch pipe one towards the middle of branch pipe one.

[0017] According to an advantageous embodiment, the adjustment unit includes a connecting wheel. The connecting wheel is fixedly installed between two branch pipes located on both sides of the middle branch pipe and facing each other front and back, and the axis of the connecting wheel is collinear with the axis of the corresponding two branch pipes.

[0018] A spiral spring for resetting is fixedly installed between the connecting wheel and the first branch pipe.

[0019] Each of the connecting pulleys is wound with a pull rope, and all the pull ropes converge into the main pipe to form the main rope.

[0020] According to an advantageous embodiment, the third branch pipe is provided with a plurality of branch pipes arranged equidistantly from left to right with vertical axes. The liquid outlet is opened on the branch pipe. The branch pipe is located on the upper side of the third branch pipe. The number of branch pipes is greater than the number of branch pipes in each row of second branch pipes. There is a branch pipe below each pair of opposite second branch pipes.

[0021] According to an advantageous embodiment, the reactor has a diameter of 2000 mm and the left and right lengths of the branch pipe are 1600 mm.

[0022] According to an advantageous embodiment, the distance between the lower side of the guide plate and the branch pipe is 300mm-600mm, and two operating rods are distributed front and back and slide through the upper end of the reactor. The guide plate is fixedly set at the lower end of the operating rods.

[0023] The rotation direction of the third branch pipe is the same as the direction of the spiral ascent of the guide plate.

[0024] In summary, the present invention has at least one of the following beneficial effects: First, by setting the size ratio between the branch pipe one and the reactor diameter, and by increasing the number of branch pipe two and the uniform distribution of the gas outlet holes, the uniformity of the gas after pumping out is improved, the gas content per unit area is increased, and the problems of bubble coalescence effect and low shearing efficiency are reduced, thereby improving the final gas-liquid mass transfer efficiency.

[0025] Second, by setting the outlet angle to 45 degrees, an inverted V-shaped pumping area is formed in the direction from front to back, which improves the gas phase coverage, that is, improves the gas content per unit area. Secondly, the outlet angle is adjustable, which is convenient to adapt to different reaction volume requirements. Moreover, the outlets are staggered to reduce the probability of bubbles from adjacent outlets merging and reacting, improve the uniformity of bubble distribution, and improve the final mass transfer efficiency.

[0026] Third, in this invention, the irregular rising trajectory of the bubble is changed to a spiral rising trajectory along the guide plate by rotating the third branch pipe and the spiral feature of the guide plate, thereby comprehensively delaying the contact time and reaction time between the bubble and the liquid phase, and indirectly improving the final mass transfer efficiency. Attached Figure Description

[0027] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0028] Figure 1 A three-dimensional structural cross-sectional view of a gas-liquid jet bubbling reactor provided according to an embodiment of the present invention is shown.

[0029] Figure 2 A cross-sectional front view of a gas-liquid jet bubbling reactor provided according to an embodiment of the present invention is shown.

[0030] Figure 3 A partial cross-sectional perspective view of the three-dimensional structure between the main pipe, branch pipe one, and branch pipe two provided according to an embodiment of the present invention is shown.

[0031] Figure 4 A partial cross-sectional front view of the area between branch pipe one, branch pipe two, and the main rope provided according to an embodiment of the present invention is shown.

[0032] Figure 5 A bottom view of branch pipe one and branch pipe two provided according to an embodiment of the present invention is shown.

[0033] Figure 6 A frontal view of the initial air outlet orientation angle of the second branch pipe according to an embodiment of the present invention is shown.

[0034] Figure 7 A front view schematic diagram of the branch pipe 2 changing the orientation angle of the air outlet provided according to an embodiment of the present invention is shown.

[0035] Figure 8 A partial cross-sectional view of the main tube and guide plate provided according to an embodiment of the present invention is shown.

[0036] The above-mentioned attached drawings include the following reference numerals: 1. Reactor; 2. Distribution unit one; 20. Main pipe; 21. Branch pipe one; 22. Branch pipe two; 23. Air outlet; 3. Distribution unit two; 30. Rotating cylinder; 31. Branch pipe three; 32. Sub-pipe; 4. Adjustment unit; 40. Connecting wheel; 41. Scroll spring; 42. Pull rope; 43. Main rope; 5. Guide plate. Detailed Implementation

[0037] To make the above-mentioned objects, features, and advantages of the present invention more apparent and understandable, specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. Many specific details are set forth in the following description to provide a thorough understanding of the present invention. However, the present invention can be practiced in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of the present invention. Therefore, the present invention is not limited to the specific embodiments disclosed below.

[0038] like Figure 1 and Figure 2As shown, a gas-liquid jet bubbling reactor includes a reactor 1, which is a sealed structure. The reactor 1 is provided with a distribution unit 2 for ejecting the gas phase and a distribution unit 3 for ejecting the liquid phase. The distribution unit 3 is located below the distribution unit 2.

[0039] like Figure 1 , Figure 2 , Figure 5 and Figure 6 As shown, the distribution unit 2 includes a main pipe 20. The main pipe 20 with a vertical axis is fixedly sleeved on the upper side of the reactor 1. The main pipe 20 is connected to an external air pump (not shown in the figure). A branch pipe 21 with a left-right axis is fixedly installed below the main pipe 20. Multiple branch pipes 22 with an axis extending left-right are provided on both the front and rear sides of the branch pipe 21. Both the branch pipe 21 and the branch pipe 22 have air outlet holes 23 facing the distribution unit 3.

[0040] like Figure 1 and Figure 2 As shown, the distribution unit 2 3 includes a rotating cylinder 30. The rotating cylinder 30 with a vertical axis is rotatably arranged below the reactor 1. The upper end of the rotating cylinder 30 is fixedly arranged with a horizontal branch pipe 31. The rotating cylinder 30 is connected to an external pipe through a liquid rotary joint. An external water pump (not shown in the figure) pumps the liquid phase into the rotating cylinder 30 through the pipe. The branch pipe 31 is provided with multiple liquid outlets.

[0041] A regulating unit 4 is provided inside the branch pipe 21 to adjust the orientation of the air outlet 23 on the branch pipe 22; a spiral guide plate 5 is provided inside the reactor 1 above the distribution unit 2.

[0042] During operation, an external water pump pumps the liquid phase into branch pipe 31 through rotating cylinder 30 and sprays it upward through the outlet. An external motor drives rotating cylinder 30 and branch pipe 31 to rotate synchronously, continuously spraying the liquid phase upward while revolving, filling reactor 1 with the liquid phase. Then, an external gas pump pumps the gas phase into branch pipe 21 and branch pipe 22 through main pipe 20 and sprays it downward through each gas outlet 23. The multi-point uniform spraying method improves the gas content per unit area. In the above process, the gas phase is sprayed downward through multiple evenly distributed points and forms bubbles in the liquid phase, gradually rising upward. The liquid phase is sprayed from bottom to top. During this process, the kinetic energy of the high-speed jet causes the liquid phase to form a rotating flow field and continuously impact the rising bubbles, accelerating the mixing between the gas and liquid phase in the bubbles. In addition, the adjustment unit 4 adjusts the orientation of the gas outlet 23 on some branch pipe 22, increasing the area covered by gas bubbles during the pumping process. This ensures that the gas phase can fully contact the liquid phase at different reaction rates, improving the uniformity of gas phase distribution per unit area.

[0043] The formed bubbles rise gradually and the guide plate 5 changes the direction of the bubbles' ascent, causing the bubbles to rise in a spiral, which delays the contact time and movement path between the bubbles and the liquid phase, thus indirectly increasing the reaction time and enhancing the gas-liquid mixing effect.

[0044] like Figure 5 and Figure 6 As shown, two branch pipes 22 located directly below the main pipe 20 are fixedly installed on branch pipe 21. The air outlets 23 on the two branch pipes 22 are arranged in two rows, left and right, and are vertically downward. The corresponding air outlets 23 are distributed equidistantly from front to back in each row. The remaining branch pipe 22 is rotatably installed on branch pipe 21. In the initial state, the air outlets 23 on the remaining branch pipe 22 are arranged in two rows, left and right, and are at a 45-degree angle to the vertical lateral section of the corresponding branch pipe 22. The corresponding air outlets 23 are distributed equidistantly from front to back in each row.

[0045] The two adjacent air outlets 23 on the same branch pipe 22 are staggered left and right, and the air outlet 23 on the middle branch pipe 22 is staggered front and back from the air outlet 23 on the adjacent branch pipe 22; the length of all branch pipes 22 gradually increases from both ends of branch pipe 1 21 towards the middle of branch pipe 1 21.

[0046] like Figure 1 , Figure 3 and Figure 4 As shown, the adjustment unit 4 includes a connecting wheel 40. The connecting wheel 40 is fixedly installed between two branch pipes 22 located on both sides of the middle branch pipe 22 and opposite to each other through a connecting frame. The axis of the connecting wheel 40 is collinear with the axis of the corresponding two branch pipes 22. A spiral spring 41 for resetting is fixedly installed between the connecting wheel 40 and the branch pipe 21. Each connecting wheel 40 is wound with a pull rope 42. All pull ropes 42 converge into the main pipe 20 to form a main rope 43. The upper end of the main rope 43 is connected to the operating rod 1. The operating rod 1 passes through the main pipe 20 and is operated from the outside. The area where the operating rod 1 passes through the main pipe 20 is sealed.

[0047] Firstly, regarding the materials of the spiral spring 41, connecting wheel 40, connecting frame, pull rope 42, main rope 43, and operating lever 1, it should be noted that the materials of the above components are all rust-proof and corrosion-resistant, which can maintain a certain service life during the angle adjustment process within the main pipe 20. Secondly, the materials of the above components are specifically designed for the type of gas phase. For example, for a certain acidic gas phase, the component material should have corresponding corrosion resistance.

[0048] During operation, an external water pump continuously pumps the liquid phase into reactor 1, while an external air pump pumps the gas phase through the main pipe 20 into branch pipe 21. The gas phase then flows from branch pipe 21 into each branch pipe 22, and is finally pumped out through the air outlet 23 on branch pipe 21 and branch pipe 22. In addition, multiple branch pipes 22 of different lengths and the branch pipe 22 in the central area work together to pump gas in, forming a spray area with an approximately circular horizontal cross-section at the bottom of reactor 1. This utilizes the circular cross-sectional feature of reactor 1. At this point, the gas phase enters the liquid phase and forms bubbles. The bubbles are first ejected from top to bottom and then begin to rise from the bottom. During the movement of the bubbles, the gas phase inside the bubbles slowly mixes and reacts with the liquid phase to produce the reaction product (usually a gas).

[0049] Meanwhile, compared to the existing pumping method that uses a small number of outlets, the operation process of pumping gas downwards at multiple points ensures a uniform gas phase distribution, increases the gas content per unit area, facilitates full contact and reaction between the gas and liquid phases, and enhances the mixing effect.

[0050] Furthermore, it is necessary to add explanation regarding the angle and distribution of the air outlets 23 on the two side branch pipes 22. By staggering the distribution, interference between pumped bubbles in adjacent air outlets 23 is avoided, which would cause excessive bubble occupation in a unit area and affect the gas-liquid reaction process (i.e., all bubbles in a unit area share a small amount of liquid phase in the same piece). This reduces the problem of reduced total bubble area due to bubble aggregation effect, which affects the mass transfer efficiency between the gas and liquid phases. Secondly, by setting the angle of the air outlets 23 to 45 degrees, the bubbles on the two side branch pipes 22 are ejected at an oblique angle, thereby forming an inverted V-shaped pumping area in the direction from front to back of the corresponding branch pipes 22, increasing the gas phase coverage, i.e., increasing the gas content per unit area.

[0051] Regarding the operation process of adjustment unit 4, it should be noted that, please refer to... Figure 6 and Figure 7 Initially, the vent 23 is tilted at an angle of 45 degrees. When the reaction demand increases, i.e., the amount of bubbles pumped per unit area increases, the operator pulls the control lever upwards, causing the control lever to move the main rope 43 upwards. The main rope 43 simultaneously pulls each auxiliary rope, causing the connecting wheel 40 to rotate synchronously with the two corresponding branch pipes 22. All branch pipes 22 on the left side of the main pipe 20 rotate counterclockwise, and all branch pipes 22 on the right side of the main pipe 20 rotate clockwise, causing the aforementioned V-shaped pumping area to rotate in the set direction. Therefore, the area covered by the pumping increases, meeting the operational requirements, and the reaction operation efficiency can be improved through the above method.

[0052] like Figure 3As shown, branch pipe 31 is provided with multiple branch pipes 32 arranged equidistantly from left to right with vertical axes. The liquid outlet is opened on the branch pipe 32. The branch pipe 32 is located on the upper side of branch pipe 31. The number of branch pipes 32 is greater than the number of branch pipes 22 in each row of branch pipe 22. There is a branch pipe 32 below each pair of branch pipes 22 that are opposite each other.

[0053] By adjusting the distribution of the branch pipes 32, during the rotation of the branch pipe 31 to pump the liquid, each branch pipe 32 forms a spiral liquid pumping trajectory during rotation, ensuring that the liquid phase pumping trajectory and the pumping bubble path of each gas outlet 23 will contact and interfere, thereby increasing the contact probability between the liquid phase and the gas phase, and ultimately improving the uniform mixing effect of the gas and liquid phases.

[0054] like Figure 1 and Figure 2 As shown, the diameter of reactor 1 is 2000mm, the left and right lengths of branch pipe 21 are 1600mm, and the diameter of the approximately circular distribution surface formed by all branch pipes 22 and branch pipe 21 is the same as that of branch pipe 21.

[0055] Compared to existing common perforation and pumping methods, the current method typically sets the perforation area at the center of the cross-section, causing the gas phase to be pumped downwards from the center. This is not conducive to the uniformity of the initial gas phase distribution. Therefore, by setting the above proportion, combined with the uniform perforation in branch pipe 1 21 and branch pipe 2 22, the uniformity of the gas phase pumping is improved, ultimately improving the mixing effect of the gas and liquid phases. In addition, the length of the above branch pipe 1 21 can be adjusted to match the diameter of reactor 1 to ensure uniform perforation and uniform pumping in the horizontal cross-section. Furthermore, the diameter length, the 45-degree inclination angle of the above-mentioned gas outlet 23, and the subsequent adjustment angle range have all been obtained by external technical personnel through multiple rounds of actual testing. Under the conditions described above, the required uniform mixing effect can be ensured, which will not be elaborated further.

[0056] like Figure 1 and Figure 2 As shown, the distance between the lower side of the guide plate 5 and the branch pipe 21 is 300mm-600mm. Two operating rods 2 are distributed front and back and slide through the upper end of the reactor 1. The guide plate 5 is fixedly set at the lower end of the operating rods 2. The part of the operating rods 2 that passes through the reactor 1 is sealed. The operating rods 2 are driven to move up and down by an external electric push rod (not shown in the figure).

[0057] It should be noted that, see reference Figure 8 The guide plate 5 not only serves as the main component for guiding the bubbles to rise, but also has a cavity inside. Flexible tubes that penetrate the reactor 1 are fixedly installed on both the upper and lower sides of the guide plate 5. The rotation direction of the branch pipe 31 is the same as the direction of the spiral ascent of the guide plate 5.

[0058] Initially, the distance between the bottom of the guide plate 5 and the branch pipe 21 is set. During the reaction operation, the distance between the guide plate 5 and the branch pipe 21 is adjusted by moving the operating lever 2 up and down through an external electric push rod. After adjusting the distance, a stable buffer zone is created for the bubbles and the airflow field, ensuring that the bubbles are evenly distributed before they rise and contact the guide plate 5. This avoids the problem of uneven gas distribution entering the spiral guide area of ​​the guide plate 5 due to a small height difference, which could lead to problems such as excessively high or low local gas holdup. This ensures that the bubbles can enter the spiral guide area in a uniformly distributed manner. In addition, the pumping process of the branch pipe 31 ensures that the bubbles rise in the spiral direction, reducing the possibility of agglomeration caused by turbulent bubble movement.

[0059] It should be further explained that the existing technology uses a gas distributor and liquid inlet at the bottom, generating a large number of bubbles in the central area at the bottom to react with the liquid. This technical solution adds distribution unit 1 (2), distribution unit 2 (3), adjustment unit 4, and guide plate 5. Distribution unit 1 (2) forms a multi-point uniform downward pumping operation at the bottom of reactor 1, conforming to the horizontal cross-section of reactor 1 while adjacent gas outlets 23 are staggered to maximize the uniform mixing effect. Furthermore, the inclined gas outlets 23 on both sides, in conjunction with adjustment unit 4, form an angle-adjustable pumping operation, increasing the coverage area of ​​the pumped bubbles and ensuring the uniformity of the bubble distribution in the gas phase. Ultimately, this increases the gas content in the liquid phase. Secondly, the continuously rotating pumping operation at the bottom, formed by the distribution unit 2 3, allows the bubbles to rise in the spiral direction, reducing the aggregation effect caused by turbulent bubble movement. Furthermore, the guide plate 5 guides the bubbles to rise spirally, delaying the contact time and reaction time between the bubbles and the liquid phase, thus improving the final reaction effect. Therefore, compared with the prior art, the gas-liquid reaction quality is significantly improved. In addition, the above-mentioned added components are all external conventional components that can be used for a long time after a single installation, so the cost of the added components is negligible. In summary, this technical solution is a specific improvement made entirely based on and to solve the defects of the prior art.

[0060] In the description of this invention, it should be understood that the orientation or positional relationship indicated by directional terms such as "front, back, up, down, left, right", "horizontal, vertical, horizontal" and "top, bottom" is generally based on the orientation or positional relationship shown in the accompanying drawings, and is only for the convenience of describing this invention and simplifying the description. Unless otherwise stated, these directional terms 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, and therefore should not be construed as a limitation on the scope of protection of this invention; the directional terms "inner" and "outer" refer to the inner and outer contours relative to the outline of each component itself.

[0061] Furthermore, the terms "first," "second," "number one," and "number two" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first," "second," "number one," or "number two" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0062] In the description of this invention, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "connected," "installed," and "linked" 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 mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal communication between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0063] The embodiments described herein are preferred embodiments of the present invention and are not intended to limit the scope of protection of the present invention. Therefore, all equivalent changes made in accordance with the structure, shape and principle of the present invention should be covered within the scope of protection of the present invention.

Claims

1. A gas-liquid jet bubbling reactor, characterized in that, include: The reactor is a sealed structure, and a distribution unit 1 for ejecting the gas phase and a distribution unit 2 for ejecting the liquid phase are provided inside the reactor. The distribution unit 2 is located below the distribution unit 1. The distribution unit 1 includes a main pipe, a vertically oriented main pipe is fixedly sleeved on the upper side of the reactor, a branch pipe 1 extending horizontally is fixedly installed below the main pipe, and multiple branch pipes 2 arranged equidistantly from left to right and extending horizontally on both the front and rear sides of the branch pipe 1 are provided, and both the branch pipe 1 and the branch pipe 2 are provided with air outlet holes facing the distribution unit 2. The second distribution unit includes a rotating cylinder. A vertically oriented rotating cylinder is rotatably arranged below the reactor. A horizontally oriented branch pipe is fixedly arranged at the upper end of the rotating cylinder. Multiple liquid outlets are arranged on the branch pipe. The first branch pipe is equipped with an adjustment unit for adjusting the orientation of the air outlet on part of the second branch pipe. The reactor is equipped with a spiral guide plate located above the distribution unit. The adjustment unit includes a connecting wheel. The connecting wheel is fixedly installed between the two branch pipes located on both sides of the middle branch pipe and facing each other front and back, through a connecting frame. The axis of the connecting wheel is collinear with the axis of the corresponding two branch pipes. A spiral spring for resetting is fixedly installed between the connecting wheel and the first branch pipe. Each of the connecting wheels is wound with a pull rope, and all the pull ropes converge into the main pipe to form the main rope. In the initial state, the corresponding air outlet tilt angle is 45 degrees. When the reaction demand increases, that is, the amount of bubbles pumped out per unit area increases, the operator pulls the operating rod one upward, causing the operating rod one to move the main rope upward. The main rope pulls each auxiliary rope in sync, causing the connecting wheel to drive the two corresponding branch pipes two to rotate in sync. All branch pipes two on the left side of the main pipe rotate counterclockwise, and all branch pipes two on the right side of the main pipe rotate clockwise. The guide plate is slidably mounted inside the reactor. The rotation direction of the branch pipe three is the same as the direction of the spiral ascent of the guide plate. Initially, the distance between the bottom of the guide plate and the branch pipe one is a set value. During subsequent reaction operations, the distance between the guide plate and the branch pipe one is adjusted by moving the operating rod two up and down through an external electric push rod. After adjusting the distance, a stable buffer zone is created for the bubbles and the airflow field, ensuring that the bubbles are evenly distributed before they rise and contact the guide plate. This avoids the gas from entering the spiral guide area of ​​the guide plate before it is evenly distributed due to the small height difference. Branch pipe one and branch pipe two form a porous, uniformly downward-facing gas phase ejection area on the lower side of the reactor, and the actual reaction area of ​​the gas phase ejection area is adjusted by the regulating unit. Meanwhile, branch pipe three forms a synchronously rotating, porous, upward-facing liquid phase ejection area. The gas and liquid phases are guided by the guide plate to form bubbles and slowly rise along the lower spiral surface. Finally, the lower side of the reactor presents a multi-point angle adjustable bubbling state and the reaction is carried out by the slow guidance of the guide plate spiral.

2. The gas-liquid jet bubbling reactor according to claim 1, characterized in that: Two branch pipes 2 located directly below the main pipe are fixedly installed on branch pipe 1. The two branch pipes 2 have two rows of air outlets on the left and right sides, and both are vertically downward. Correspondingly, each row of air outlets is distributed at equal intervals from front to back. The remaining branch pipe 2 is rotatably mounted on the branch pipe 1; in the initial state, the remaining branch pipe 2 has two rows of air outlets, one on the left and one on the right, and each row is at a 45-degree angle to the vertical lateral section of the corresponding branch pipe 2. The corresponding air outlets in each row are equidistant from front to back.

3. The gas-liquid jet bubbling reactor according to claim 2, characterized in that: The two adjacent air outlets on the same branch pipe are staggered left and right, and the air outlet on the middle branch pipe is staggered front and back from the air outlet on the adjacent branch pipe.

4. A gas-liquid jet bubbling reactor according to claim 2, characterized in that: The length of all two branches gradually increases from both ends of the first branch towards the middle of the first branch.

5. A gas-liquid jet bubbling reactor according to claim 1, characterized in that: The third branch pipe is provided with multiple branch pipes arranged equidistantly from left to right with vertical axes. The liquid outlet is opened on the branch pipe. The branch pipe is located on the upper side of the third branch pipe. The number of branch pipes is greater than the number of branch pipes in each row of the second branch pipe. There is a branch pipe below each pair of opposite second branch pipes.

6. A gas-liquid jet bubbling reactor according to claim 1, characterized in that: The reactor has a diameter of 2000 mm, and the left and right lengths of the first branch pipe are 1600 mm.

Images