JP4544017B2 - Air diffuser - Google Patents

Description

  The present invention relates to an aeration treatment apparatus used for water treatment and purification of industrial wastewater, water and sewage, lakes, rivers, groundwater, etc., removal and recovery of foreign substances in gas, and bioreactors (bioreactors). Specifically, it is an operation of mixing gas and liquid, stirring them and bringing them into gas-liquid contact. Aeration of air in water to dissolve oxygen in the air, ammonia dissolved in water, trichloroethane, chloride Emission of volatile substances such as methylene, chlorine, trihalomethane, and other substances such as hydrogen chloride, sulfur dioxide, and powder in the reaction are absorbed, removed by collection, recovered, and used for enzyme reactions and microbial reactions. The present invention relates to an air diffuser.

Conventional air diffusion treatment devices are roughly classified into an air diffusion type (bubble type) and a mechanical stirring type (surface stirring). In particular, as shown in FIG. 16, the aeration type aeration processing apparatus 110 has a large number of aeration plates 112, diffusion cylinders, and the like arranged at the bottom of the aeration tank 111, and these are connected via a blower 113 and an air supply line 114. Then, aeration processing is performed by supplying pressurized air. In addition, when a nitrogen compound such as ammonia dissolved in a liquid is diffused to be purified and recovered, a packed tower or a plate tower is often used as shown in FIG. In the case of the dispersal treatment apparatus 115 using a packed tower system, a liquid is supplied from the upper part of the packed tower 116 and a gas is supplied from the lower part of the tower. While the packing 117 arranged in the tower is in gas-liquid contact in countercurrent, volatile substances such as ammonia (NH ₄ ⁺ ) and organic solvent in the liquid are diffused to the gas side to purify and recover the liquid. Processing is in progress.

  Moreover, a cylindrical exhaust gas dispersion pipe having a large number of gas ejection holes is used as a gas-liquid contact reaction device of a processing device for exhaust gas containing powder and sulfurous acid gas. An exhaust gas treatment method using this exhaust gas dispersion pipe is disclosed in Japanese Patent Application Laid-Open No. 7-308536 and Japanese Patent Application Laid-Open No. 9-865, but the gas-liquid contact efficiency between the liquid and the bubbles blown out from many gas injection holes is low. . Moreover, there is a problem of clogging due to adhesion growth of gypsum which is a reaction product.

Further, the conventional diffuser processing apparatus using a static mixer (see Japanese Patent Laid-Open Nos. 59-206096, 2001-269692, 2001-62269, and Non-Patent Documents 1 and 2) has a structure. Oxygen absorption (dissolution) efficiency is low due to the above problems, and it is difficult to manufacture a diffuser with a large diameter (500 mm or more in diameter), and even if it can be manufactured, the gas-liquid contact efficiency is low. Furthermore, the manufacturing cost is also expensive.
Furthermore, the diameter of the air outlet hole of the air supply pipe arranged below the conventional static mixer is in the range of 10 to 40 mm. One or a plurality of blowout holes are provided on the upper surface of the air pipe.
Since the bubble diameter supplied from the air outlet is the same as the air outlet, the gas-liquid contact efficiency is low, the oxygen absorption efficiency is low, and the gas-liquid contact time in the mixer, that is, the residence time is lengthened. There is a need.
As a result, the total length of the static mixer, that is, the diffuser is high, and the equipment cost is high.
In addition, the increase in ventilation resistance increases the power cost of an air supply device such as a blower.
Furthermore, plastics, rubbers, and the like are often used as constituent materials of conventional diffuser treatment apparatuses including diffuser plates, diffuser cylinders, static mixers, and the like. For this reason, the life of the diffuser is short due to material deterioration, aging, and the like. In addition, when a new one is exchanged, a large amount of waste is generated, and the waste disposal cost becomes expensive. Furthermore, it is necessary to stop the operation during replacement work. For this reason, a spare tank is required, and the equipment cost becomes expensive.

    Japanese Patent Laid-Open No. 2-198694     JP-A-44-8290     JP-A-53-36182     JP-A-5-168882     Japanese Patent Laid-Open No. 7-284642     JP-A-7-308536     JP-A-9-865     Japanese Patent Laid-Open No. 10-80627     Japanese Patent Laid-Open No. 10-85721     JP 2001-62269 A     JP 59-206096 A     JP 2001-26969 A     S. J. et al. Chen, et al. "Static Mixing Handbook", Research Institute for Chemical Research, June 1973, P62-82, P199-217     Teruichiro Matsumura, Yasushi Morishima, et al. "Static mixer-Basics and applications-" Nikkan Kogyo Shimbun, published September 30, 1981, P1-18, P81-95

  The conventional air diffuser has a low oxygen dissolution and absorption efficiency and requires a large area because the amount of air supplied per air diffuser is small. In addition, for the purpose of mixing and stirring in the aeration tank, air exceeding the required oxygen amount is pressurized and supplied to a diffuser plate or the like. Furthermore, the air resistance passing through the diffuser plate is large. For this reason, a large amount of power is consumed. In addition, conventional diffusion treatment apparatuses such as packed towers and tray towers cause clogging due to the growth of calcium compounds and microorganisms in the liquid on the packings and trays and require regular maintenance management. . Furthermore, the conventional air diffuser using a static mixer has a low oxygen absorption efficiency and is difficult to increase in size. Therefore, the object of the present invention is to improve the efficiency of gas-liquid contact and aeration, release and reaction treatment, effectively purify wastewater etc. with energy saving, space saving, low cost, maintenance-free, An object of the present invention is to provide an air diffusion treatment device used for absorption removal or emission removal and emission recovery. It is another object of the present invention to provide a bioreactor that can be used for highly efficient enzyme reactions and microbial reactions.

  In order to solve the above problems, a first air diffusion treatment device of the present invention comprises a cylindrical passage tube through which a fluid flows, which is provided with a static mixer disposed substantially perpendicular to the longitudinal direction. A cylindrical gas ejection portion that supplies gas to the lower end side of the passage pipe through the air feeding line is disposed in the passage pipe, and a gas ejection nozzle is disposed in the gas ejection section. Gas is supplied to the gas ejection part, and liquid is introduced into the passage pipe from the liquid introduction part of the passage pipe without power by the air lift effect of the gas, and both the gas and the liquid flow in the passage pipe in parallel. The gas diffuser is in contact with the gas and liquid inside the passage pipe in the previous period, and is discharged into the liquid from the upper end side of the passage pipe. These aeration processing devices are arranged by disposing a static mixer that performs mixing and stirring of the fluid using flow energy of fluid that does not require mixing and stirring power, and by disposing a gas ejection section below the mixer. The liquid is introduced from below the gas ejection portion by the air lift effect of the gas. The liquid and the gas flow in a parallel flow from the lower end side to the upper end side of the passage tube and are gas-liquid contact mixed to perform aeration, dissipation, and reaction processing. The fluid is composed of a two-component system composed of a gas and a liquid, or a three-component system containing a solid.

  In addition, a second air diffusion treatment device of the present invention for solving the above-described problems is a cylindrical shape through which a fluid flows, which is provided with a static mixer arranged with its longitudinal direction substantially vertical. A gas ejection part for supplying gas into the passage pipe is disposed on the lower end side of the passage pipe and the passage pipe, a static mixer is disposed in the gas ejection part, gas is supplied to the gas ejection part, and the gas is ejected. The liquid is introduced into the passage pipe from the liquid introduction portion of the passage pipe by the air lift effect by the gas. Both the gas and the liquid rise in a parallel flow in the passage tube, both of which are in gas-liquid contact and mixing inside the passage tube, and are discharged into the liquid from the upper end side of the passage tube.

  Further, the static mixer disposed in the passage tube and in the gas jetting portion includes at least two or more spirally wound right-handed or left-handed to form a plurality of fluid passages. The fluid passages communicate with each other through an opening in the longitudinal direction of the blade body, and the blade body is formed of a perforated plate. The static mixer is formed by arranging at least one type of right-handed or left-handed blades.

  According to the diffuser of the present invention, power consumption can be greatly reduced by improving oxygen absorption efficiency by increasing gas-liquid contact efficiency with low pressure loss. Moreover, aeration, dissipation, and reaction processing time are shortened by improving the gas-liquid contact efficiency. Furthermore, the diffuser processing apparatus is improved in the gas supply speed per unit area, the installation area in the horizontal direction is reduced, the space is saved, and the civil engineering and equipment costs are reduced. In addition, construction costs such as air supply piping are reduced. Furthermore, since there is no outage due to clogging, maintenance management costs and production management costs are also reduced. Further, since there is no fluid stagnation part (dead region), it is easy to increase the size. Furthermore, the constituent material of the diffuser according to the present invention can be used semi-permanently by using, for example, a metal such as iron, stainless steel, titanium, hastelloy, etc., and the processing cost can be greatly reduced, and the waste Processing costs can be reduced.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.
FIG. 1 is a schematic view showing a first embodiment according to the present invention. FIG. 2 is a schematic view showing a second embodiment according to the present invention. FIG. 3 is a schematic view showing a third embodiment according to the present invention. FIG. 4 shows an example of the static mixers 2, 9, 13 and 17 used in the first to third embodiments of the present invention. (A) The figure has a right-handed spiral blade. The schematic perspective view of a passage pipe. (B) The figure is a schematic perspective view of a passage tube having a left twisted spiral blade. FIG. 5 is a diagram showing an example of the static mixers 2, 9, 13, and 17 used in the first to third embodiments of the present invention. FIG. 6 is a schematic view of the air diffusion processing apparatus according to the first embodiment (see FIG. 1) of the present invention. FIG. 7 is a perspective view showing an example of a gas ejection nozzle used in the first embodiment (see FIG. 1) of the present invention. FIG. 8 is a schematic view of an air diffuser according to a second embodiment (see FIG. 2) of the present invention. FIG. 9 is a partial schematic bottom view of the air diffuser according to the second embodiment (see FIG. 2) of the present invention. FIG. 10 is a partial schematic perspective view of a gas ejection portion according to a second embodiment (see FIG. 2) of the present invention. FIG. 11 is a schematic cross-sectional view of an aeration treatment apparatus according to a third embodiment (see FIG. 3) of the present invention. FIG. 12 is a view showing an example in the case where the aeration treatment apparatus according to the present invention is applied to the aeration process of the activated sludge method. FIG. 13 is a diagram showing an example in the case where the aeration treatment apparatus according to the present invention is applied to drainage diffusion treatment. FIG. 14 is a view showing an example in the case where the aeration treatment apparatus according to the present invention is applied to an exhaust gas treatment apparatus. FIG. 15 is a view showing an example in which the aeration treatment apparatus according to the present invention is applied to a biological reaction apparatus using an enzyme or a microorganism. FIG. 16 is a schematic view showing an aeration processing apparatus using a conventional diffuser plate method. FIG. 17 is a schematic view showing a conventional diffusion treatment apparatus using a packing method.

FIG. 1 is a schematic view showing a first embodiment according to the present invention. A stationary mixer 2 formed of right-handed or left-handed blades is provided in a passage pipe 1 through which a cylindrical fluid arranged with the longitudinal direction substantially vertical flows, and below that A gas injection part 5 in which a gas injection nozzle to which a gas is supplied via an air feed line 4 is disposed in the space part 3 of the gas, and a liquid introduction for supplying liquid (FL) to the lower end side of the passage pipe 1 is further provided. Part 6 is arranged. In the diffuser 7 thus configured, gas (FG) is jetted and supplied upward from the gas jetting part 5 to the lower end part of the static mixer 2 in the passage pipe 1 via the space part 3. Is done. Due to the air lift effect generated by the buoyancy of the gas (FG), the liquid (FL) is introduced into the space 3 in the passage tube 1 without power from the liquid introduction portion 6 on the lower end side of the passage tube 1. The gas (FG) and the accompanying liquid (FL) flow through the static mixer 2 while rising in parallel flow, and are discharged into the liquid in a gas-liquid contact while being refined. As a result, the liquid and the gas are sufficiently in gas-liquid contact, and aeration, emission, or chemical reaction proceeds. The supply pressure of the gas (FG) may be a pressure obtained by adding about 100 mmH ₂ O to the water depth.
In addition, it is preferable to arrange | position the position of the gas ejection part 5 in the range of 0.2 times-3 times the diameter of the static mixer 2 from the lower end of the static mixer 2. Further, the liquid introducing portion 6 may be used by providing an opening in the tube wall below the passage tube 1 and allowing the liquid to flow therethrough. Thereby, the opening area of the liquid introducing | transducing part 6 increases, and the circulation amount of a liquid improves. Further, the liquid introduction section 6 may be used with the longitudinal cross-sectional shape widened (for example, a fan shape). By increasing the opening area of the liquid introduction part 6, the amount of liquid (FL) introduced is improved.

  In the present embodiment, the gas (FG) that rises by jetting and supplying gas (FG) upward from the gas jet nozzle of the gas jet part 5 through the air feed line 4 from below the stationary mixer 2 ( The gas (FG) and the liquid (FL) that rise while entraining the liquid (FL) supplied from the liquid introduction part 6 of the passage tube 1 by the air lift effect generated by the buoyancy of the FG) and the liquid (FL) are cocurrently flown in the static mixer 2. The inside is flowing. As a result, the gas (FG) and the liquid (FL) are continuously in gas-liquid contact by a mixing and stirring function and subjected to aeration, release, chemical reaction processing, or the like. This gas-liquid mixing and stirring operation is performed with no power and high efficiency, thus saving energy.

  FIG. 2 is a schematic view showing a second embodiment of the present invention. A first static mixer 9 is provided in a cylindrical passage tube 8 through which a fluid arranged with the longitudinal direction substantially vertical flows, and an air feed line 11 is provided in a space 10 below the first static mixer 9. The gas ejection part 12 which supplies gas (FG) via is arrange | positioned. A second static mixer 13 is provided in the gas ejection part 12. Further, a liquid introduction part 14 for supplying liquid (FL) is disposed on the lower end side of the passage pipe 8. In the air diffusion processing device 15 configured as described above, the gas (FG) is disposed in the gas ejection portion 12 through the space portion 10 at the lower end portion of the first static mixer 9 in the passage tube 8. The second static mixer 13 is sprayed and supplied after being refined. The liquid (FL) is introduced into the space 10 from the liquid introduction part 14 on the lower end side of the passage pipe 8 without power by the air lift effect generated by the buoyancy of the jetted gas (FG). The atomized gas (FG) and the accompanying liquid (FL) flow in the first static mixer 9 while rising in parallel flow, and are discharged into the liquid while continuously contacting with gas and liquid. As a result, the liquid and the gas are sufficiently in gas-liquid contact, and aeration, dissipation, chemical reaction processing, and the like proceed. The first static mixer 9 and the second static mixer 13 are not limited to this embodiment, and various stationary mixers can be selected and used as appropriate for the rotation angle, the number of blades, the aperture ratio, etc. Is done. The supply pressure of the gas (FG) supplied to the gas ejection part 12 may be a pressure obtained by adding about 300 to 11000 Pa to the water depth. Furthermore, the piping position of the air feed line 11 may pass through the side wall of the passage pipe 8 and be disposed in the space portion 10 to supply gas (FG). Furthermore, the longitudinal cross-sectional shape of the liquid introducing portion 14 may be widened (for example, a fan shape). By increasing the opening area of the liquid introducing portion 14, the amount of liquid (FL) introduced is improved and the processing time is shortened.

FIG. 3 is a schematic view showing a third embodiment according to the present invention. A static mixer 17 is provided in a cylindrical passage pipe 16 through which a fluid flows, and a gas ejection part 20 for supplying gas (FG) through an air feed line 19 in a space 18 below the static mixer 17. Are arranged. The air feed line 19 is piped from above to below through a longitudinal opening in the center of the static mixer 17. The air feeding line 19 may be piped from the lower end side of the passage pipe 16.
In the air diffusion treatment device 21 configured as described above, the gas (FG) is ejected upward from the gas ejection unit 20 via the air feeding line 19 from below the stationary mixer 17, thereby supplying the gas Similarly, the liquid (FL) introduced from the liquid introduction part 22 on the lower end side of the passage pipe 16 flows in the static mixer 17 together with the rising gas (FG) and continuously contacts the gas-liquid. proceed.
Note that the gas-liquid contact efficiency is further improved by disposing and using the static mixer 17 in the gas ejection portion 20 as in the second embodiment of the present invention. The number of gas ejection portions 20 can be appropriately adjusted according to the purpose.

  Further, by providing a plurality of gas ejection portions 20, it is possible to use the passage pipe 16 having a large diameter (diameter of 500 mm or more), and the gas supply capacity per unit is greatly improved, and the processing time and reaction time are increased. Shortened. In addition, the piping quantity of the pneumatic line is reduced, and the piping work cost and the maintenance management cost are also reduced. Furthermore, the size of the facility can be easily increased.

FIG. 4 shows an example of the static mixers 2, 9, 13 and 17 used in the first to third embodiments of the present invention. FIG. 4 (a) shows a right-handed (clockwise) spiral. FIG. 4B is a schematic perspective view of a passage tube having a left-hand twisted (counterclockwise) blade body. (A) In the figure, three right-handed blade bodies 25 are provided in a static mixer 24 arranged in a cylindrical passage tube 23. The blade body 25 is formed of a perforated plate having a large number of perforated holes 26. Further, the fluid passage 27 has three fluid passages 27, and the fluid passages 27 communicate with each other over the entire length of the blade body 25 through the opening 28.
(B) In the figure, similarly, three left twist blade bodies 31 are provided in a static mixer 30 disposed in a cylindrical passage tube 29. The blade body 31 is formed of a perforated plate having a large number of perforated holes 32. Three fluid passages 33 are provided, and the fluid passages 33 communicate with each other over the entire length of the blade body 31 through the opening 34. In the passage pipes 23 and 29 having the stationary mixers 24 and 30 arranged as shown in (a) or (b), the gas (FG) rising in parallel flow from below the passage pipes 23 and 29. And liquid (FL), while flowing through right or left-handed spiral blades, rotate and split in the right or left direction, merging, reversing and shearing stress action continuously, The liquid is contacted and discharged into the liquid.

The sum total of the surface area (m ² ) of the blade body 31 installed in the passage tube 29 that influences the mixing and stirring performance of the static mixer installed in the air diffusion treatment device of the present invention is as follows. A range of 10 to 150 m ² / m ³ is preferable per unit volume (m ³ ). More preferably, it is the range of 25-80 m < ² > / m < ³ >. The diameter of the holes (26, 32) drilled in the blade bodies 25, 31 is preferably in the range of 5 to 30 mm, and the aperture ratio of the holes (26, 32) is preferably in the range of 5 to 80%. Furthermore, the rising speed of the gas in the passage pipe (23, 29) is preferably in the range of 0.1 to 10 m / s, more preferably in the range of 0.5 to 5 m / s. Furthermore, the twisting angles (rotation angles) of the blade bodies 25 and 31 are preferably 90 °, 180 °, and 270 °, but can also be used at 15 °, 30 °, 45 °, 60 °, and the like. When manufacturing a passage tube having a large diameter (diameter 500 mm or more), a blade body (25, 31) having a small twist angle such as 15 ° or 30 ° is manufactured, and for example, three blade bodies are connected to each other. You may arrange | position and use so that (degree) +30 degree + 30 degree = 90 degree. By doing so, the manufacturing process becomes easy, and the manufacturing process cost is also reduced. A combination of blades having different twist angles can be appropriately selected and used depending on the application.

FIG. 5 is a diagram showing another example of the static mixers 2, 9, 13 and 17 used in the first to third embodiments of the present invention.
In FIG. 5, spiral right-handed and left-handed blades 36 and 37 having a plurality of fluid passages are provided in a cylindrical passage pipe 35 in multiple stages through a cylindrical space 38. ing. A cylindrical space 39 is formed below the left twisted blade body 37. The arrangement of the right and left twisted blade bodies 36 and 37 in the passage pipe 35 is not limited to this FIG. 5, and the combination of arranging the blade bodies 36 and 37 in multiple stages depends on the application. For example, various uses such as right + left + right and right + left + right + left are possible. In the cylindrical passage pipe 35 configured as described above, the gas (FG) and the liquid (FL) rising in parallel from the lower side of the passage pipe 35 through the space portion 39 are the left twisted blade body 37. , While flowing through the space 38 and the right twisted blade body 36, they are in gas-liquid contact while continuously repeating the rotation and division in the left direction and the right direction, merging, reversing, and shear stress action, Discharged inside.

  FIG. 6 is a schematic view of the air diffusion processing apparatus according to the first embodiment (see FIG. 1) of the present invention. The air diffuser 40 has a stationary mixer 41 provided therein, and a cylindrical passage pipe 43 having a space 42 and a gas supply section 45 having a gas ejection section 44 are connected to the lower part of the static mixer 41. It is comprised by the two support plates 46 to be made. The air feed tube 45 has a gas ejection part 44 provided with a gas ejection nozzle 48 for ejecting gas in the vertical direction, and the opposite side of the gas inlet side is closed. The diffuser 40 thus configured is disposed in the liquid, and the gas (FG) is sent from the gas jetting part 44 through the air feed pipe 45 by a blower or a compressor, and the pressurized gas (FG) is passed through the passage pipe. 43 is supplied into the space 42. The liquid (FG) is entrained from the liquid introduction part 47 at the lower end of the passage tube 43 by the air lift effect due to the buoyancy of the supplied gas (FG), and is allowed to flow through the stationary mixer 41 in parallel while being entrained. Liquid contact is performed and discharged into the liquid, and aeration, release, and reaction process proceed. By using the gas ejection nozzle 48 in the gas ejection part 44, the gas (FG) is efficiently dispersed in the liquid (FG), and the gas-liquid contact efficiency is improved. The gas ejection nozzle 48 is preferably, for example, a gas ejection nozzle 48 having the shape shown in FIG. The supply pressure of the pressurized gas (FG) to the gas ejection part 44 may be a pressure obtained by adding the pressure loss of the air pipe 45 to the water depth. For example, if the water depth is 5 m, the supply pressure may be about 50000 Pa.

FIG. 8 is a schematic view of an air diffusion treatment device according to a second embodiment (see FIG. 2) of the present invention.
As in the first embodiment shown in FIG. 6, the air diffuser 49 is provided with a first static mixer 51, and a cylindrical passage tube having a space 52 and a liquid introduction portion 53 below the first static mixer 51. 50, a cylindrical air feed pipe 55 having a first static mixer 51 and a gas ejection portion 54, and two support plates 56 that support the passage pipe 50 and the air feed pipe 55. . The gas ejection portion 54 is provided with a second stationary mixer 57 formed of a plurality of right-handed or left-handed spiral blades. The gas-liquid contact action between the gas (FG) and the liquid (FL) is the same as in FIG. 6 and will not be described. However, the second static mixer 57 is disposed in the gas ejection portion 54 of the air feeding tube 55. Thus, the jetted gas (FG) is refined by the generation of turbulence by the mixing / stirring function of the second static mixer 57 and rises in the space 52 in parallel with the liquid (FL). The gas (FG) and the liquid (FL) are further refined while flowing through the first static mixer 51, and the gas-liquid contact is performed with high efficiency, discharged into the liquid, aerated, and diffused. And the reaction process proceeds. The first static mixer 51 and the second static mixer 57 are not limited to the present embodiment, and various types of static mixers can be appropriately selected as described above.

FIG. 9 is a partial schematic bottom view of the air diffusion treatment device according to the second embodiment (see FIG. 2) of the present invention.
The bottom surface of the air diffuser 58 is composed of three right-handed blade bodies 60 and a cylindrical air feed pipe 61 forming a static mixer 9 installed in a cylindrical passage pipe 59. Yes. The blade body 60 is formed of a perforated plate having a large number of holes 62 perforated in the thickness direction, and has an opening 63 over the entire length of the blade body 60 in the longitudinal direction.

FIG. 10 is a partial schematic perspective view of a gas ejection portion including the static mixer 13 according to the second embodiment (see FIG. 2) of the present invention. The air feed pipe 64 is configured in an inverted T shape, and the cylindrical gas ejection portion 65 forms three fluid passages 67 in which three right-handed spiral blade bodies 66 are provided. The fluid passage 67 communicates with the entire length in the longitudinal direction of the blade body 66 through the opening 68. The blade body 66 is formed of a perforated plate having a large number of holes 69 perforated in the thickness direction. In the air feed pipe 64 in which the second stationary mixer 13 is installed, the flow of the gas (FG) to be ejected is a straight flow straight through the opening 68 and three spiral blades. Turbulent flow is generated in the liquid (FL) by the interaction of the spiral flow flowing along the body 66 and the split flow passing through the hole 69 of the blade body 66, and the gas (FG) is refined. By using the gas (FG) refined in the liquid (FL), the gas-liquid contact efficiency is further improved with the gas (FG) having a low supply pressure. In addition, as for the arrangement position of the gas ejection part 65, the separation distance from the lower end side of the static mixer installed in the passage pipe 59 is preferably in the range of 0.2 to 5 times the diameter of the passage pipe. Furthermore, the supply rate of the amount of gas supplied into the gas ejection part 65 is preferably in the range of 2000 to 14000 Nm ³ / (m ² · hour) depending on the physical properties of the gas and the liquid and the purpose of use. It should be noted that the gas ejection portion 65 may be internally provided with three left-handed spiral blades. As a result, the gas (FG) ejected while rotating in the left direction by the gas ejection part 65 is caused to flow between the gas (FL) and the liquid (by the right twisted blade body 66 disposed on the upper part of the gas ejection part 65. The upward flow with FG) is further refined by generating a large shear stress by the reversal action from the left direction to the right direction, and the absorption efficiency of the gas (FG) is further improved. Further, the combination of the twist angle (rotation angle) and twist direction of the blade body 66, the hole diameter, the opening ratio of the holes, and the like can be appropriately selected according to the application.

    FIG. 11 is a schematic cross-sectional view of a diffuser according to a third embodiment (see FIG. 3) of the present invention. In the air diffuser 70, two or more 90 ° right twist blade bodies 72 are provided in a passage pipe 71 through which a cylindrical fluid flows to form a first stationary mixer 73, and the first stationary mixer 73 is formed. A cylindrical air supply pipe 75 that supplies gas through an opening 74 in the mold mixer 73 is disposed, two gas ejection portions 76 are disposed, and the inside of the gas ejection portion 76 is a second stationary type. A mixer 77 is provided inside. The blade body 72 is formed of a perforated plate having a number of perforated holes 78. In the air diffuser 70 configured as described above, the gas (FG) is gas (FG) pressurized by a gas supply means such as a blower, a compressor, a gas cylinder (not shown), etc. From the lower part of the first static mixer 73, the liquid is jetted and supplied through the part 76 and the space part 79. The liquid (FL) is introduced into the space 79 in the passage pipe 71 from the liquid introduction section 80 at the lower end of the passage pipe 71 by an air lift effect generated by the buoyancy of the gas (FG). The gas (FG) and the accompanying liquid (FL) are continuously refined by flowing through the first static mixer 73 while rising in a parallel flow in the passage pipe 71 and mixing and stirring. The gas-liquid contacts and is discharged into the liquid. As a result, the liquid and the gas are in gas-liquid contact with high efficiency, and aeration, diffusion, chemical reaction, or the like proceeds continuously. Similarly to the above, the twist direction, twist angle (rotation angle), number of sheets, hole diameter, aperture ratio, diameter, height, etc. of the spiral blade used in this embodiment are appropriately determined according to the application. Selectable can be used. In the diffuser 70 according to the present embodiment, the gas supply speed per unit is improved by increasing the diameter of the passage pipe 71 (diameter 500 mm or more), energy saving by shortening the reaction processing time, and the aeration tank, diffusion Space saving can be achieved by reducing the volume of the tank and the like, and further, maintenance-free operation can be achieved with a structure in which no fluid stagnation (dead area) occurs in the diffuser 70.

Application example 1

FIG. 12 is a diagram showing an example in which the aeration treatment apparatus according to the present invention is applied to an aeration process such as an activated sludge method.
The air diffuser 81 is disposed at the bottom of the aeration tank 82 that stores the raw water. The blower 83 and the air supply line 84 that supply air to the lower part of the air diffuser 81 and the raw water supply line 85 that supplies the raw water. A treated water discharge line 86 for discharging treated water is also provided. Moreover, it is preferable to install the liquid introduction part of the air diffusion treatment device 81 at a position separated from the bottom surface of the aeration tank 82 by 50 to 200 mm. In the air diffusion treatment device 81 configured as described above, the raw water is diffused by the air lift effect due to the buoyancy of the air supplied from the lower end side of the air diffusion treatment device 81 via the blower 83 and the air feed line 84. The raw water and air are mixed and stirred while passing through the inside in parallel flow, oxygen in the air is dissolved in the raw water, and the raw water is purified by batch or continuously by the action of aerobic microorganisms. The treated water is discharged from the discharge line 86.
Note that the supply rate of the amount of air flowing from the lower side to the upper side in the air diffuser 81 is within a range of 2 to 6 meters in the aeration tank 82 when the processing efficiency is 90% or more, and COD (chemical oxygen demand), depending on physical properties such as BOD (biochemical demand), but is preferably in the range of 1800~21000Nm ³ / ^{(m 2} · h), more preferably 3600~12000Nm ³ / ^{(m 2} · h ). In addition, when the diffuser 81 having a diameter of 150 millimeters is used, the aeration and stirring area per unit is in the range of about 3 to 8 m ² . Further, the discharge pressure of the blower 83 may be a pressure obtained by adding the pressure of the water depth of the aeration tank 82 and the pressure loss of the air feed line 84. Aeration processing is possible with a low air supply pressure and a low pressure loss, which saves energy. Here, N means normal (indicator state) and means a volume (m ³ ) at 0 ° C. and 1 atm.
Comparing the ventilation resistance (pressure loss) of the conventional diffuser plate method and the method of the present invention, the method of the present invention is 1/5 to 3/5 of the conventional method. Further, Table 1 shows the result of comparing the performances of the conventional methods A, B, C using the static mixer in the conventional cylinder and the method of the present invention. As shown in Table 1, according to the method of the present invention, the air supply speed per one scattering cylinder is 100 Nm ³ / (m ² · min), whereas the conventional method is 80,12,17 Nm ³ / (m ²・ Min). Similarly, the oxygen absorption efficiency at a water depth of 5 m is 8.3, 10.5, and 13.0% with respect to 15%. Furthermore, it influences the gas-liquid contact efficiency unit volume ^{(m 3)} surface area per ^{(m 2)} for ^55m 2 / ^{m 3,} a 2,16,8m ² / ^{m 3.}
Nm ³ / m ² · min means the air supply speed in the standard state per unit cross-sectional area (m ² ) of the air diffusion treatment device of the present invention and the conventional air diffusion cylinder.

Application example 2

FIG. 13 is a diagram showing an example in the case where the air diffusion treatment device according to the present invention is applied to a diffusion treatment of volatile substances in waste water.
The air diffusion treatment device 87 according to the present invention is the same as that of the embodiment of FIG. 12, but is arranged at the bottom of the tubular diffusion tank 88 and supplies air to the lower part of the air diffusion treatment device 87. 89, an air feed line 90, a waste water supply line 91 for supplying waste water, and a treated water discharge line 92 for discharging purified treated water. The exhaust line 93 is provided with a cooling device or adsorption device for recovering volatile substances. In the diffuser processing device 87 configured in this way, volatile substances such as trichloromethane, trihalomethane, ammonia, chlorine, krypton, etc. in the wastewater are diffused by mass transfer to the supplied air side by gas-liquid contact. The drainage is purified. As for the supplied air, volatile substances are collected and purified by a cooling device or an adsorption device through an exhaust line 93. The purified air is released into the atmosphere.
Note that the type of gas supplied is not limited to air, and an inert gas such as nitrogen, helium, argon, or carbon monoxide gas can be used as appropriate. For example, it is possible to dissipate (deoxidize) the dissolved oxygen in the liquid by using nitrogen gas. The supply rate per unit cross-sectional area (m ² ) of the gas supplied into the diffuser processing device 87 depends on the physical properties such as the boiling point, solubility, vapor pressure, etc. of the volatile substances in the wastewater, the concentration of concentration, the efficiency of the emission treatment, etc. Accordingly, the range of 3600-18000 Nm ³ / (m ² · hour) is preferable in the case of a water depth of 1 to 5 meters in the stripping tank 88, but more preferably 7200 to 15000 Nm ³ / (m ² · hour). It is a range.

Application example 3

FIG. 14 is a view showing an example in which the air diffusion treatment device according to the present invention is applied to exhaust gas treatment such as wet flue gas desulfurization device.
A plurality of diffuser treatment devices 94 are arranged at predetermined positions in a cylindrical reaction tank 95, and an air supply line 97 for supplying exhaust gas and a water or absorption liquid are supplied below the diffuser treatment device 94 via a blower 96. There are provided a new liquid supply line 98, a discharge line 100 for discharging the absorbent 99 to the outside of the reaction tank 95, and an exhaust line 101 for exhausting the cleaned exhaust gas from the upper part of the reaction tank 95. In the air diffusion treatment device 94 configured in this way, the exhaust gas containing HCl, SO _x , NO _x , NH ₃ , H ₂ S, dust and the like is diffused through the blower 96 and the air feed line 97. An absorbing liquid and gas comprising an alkaline aqueous solution such as NaOH, C _a CO ₃ , Ca (OH) ₂ , Mg (OH) ₂ or an acidic aqueous solution such as H ₂ SO ₄ , HCl supplied from the lower side of the apparatus 94 to the upper side. The chemical reaction process proceeds by contact with the liquid, and the exhaust gas that has been dissolved or collected in the absorbing liquid and purified and discharged is discharged into the atmosphere via the exhaust line 101.
When such an air diffuser 94 is applied to the removal and collection of foreign substances in the exhaust gas, for example, it is supplied into the air diffuser 94 when applied to a flue gas desulfurizer by the lime / gypsum method. The exhaust gas supply rate per unit cross-sectional area (m ² ) is 7200 to 15000 Nm ³ / (m ² · hour in the case where the water depth in the reaction tank 95 is in the range of 0.5 to 3 meters and the absorption efficiency is 90% or more. ) Is preferred. Compared with the conventional gas-liquid contact method using a diffuser plate, a dispersion tube, etc., the exhaust gas and the liquid are mixed and stirred with high efficiency under a low pressure loss, thereby enabling a short-time treatment. In addition, the processing speed can be improved to save space and the equipment cost can be reduced. Furthermore, by arranging the diffuser 94 having a large diameter (diameter of 500 mm or more), the processing capacity is improved and the space is further saved. Furthermore, since it is difficult for the stagnation part (dead area) of the fluid to occur in the diffuser 94, it prevents adhesion and growth of calcium compounds when applied to a flue gas desulfurization apparatus using the lime / gypsum method. This enables continuous operation and reduces maintenance costs.

Application example 4

FIG. 15 is a view showing an example in which the aeration treatment apparatus according to the present invention is applied to a biological reaction apparatus using enzymes or microorganisms.
The diffuser processing apparatus 102 is disposed at a predetermined position in a cylindrical bioreactor (biological reaction apparatus) 103, an air feed line 104 for supplying gas to the lower side of the diffuser processing apparatus 102, and a stock solution supply line for supplying a stock solution. 105, a reaction product discharge line 106 for discharging the reaction product, an exhaust line 107 for discharging at least one kind of gas from the top of the bioreactor 103, and a circulating liquid line for circulating the stock solution from the liquid level to the bottom of the bioreactor 103 108 is provided. In the bioreactor 103, a catalyst carrier 109 or a biocatalyst carrying an enzyme or a microorganism is dispersed in a liquid. In the air diffusion processing apparatus 102 configured as described above, gas is supplied from the lower side to the upper side of the air diffusion processing apparatus 102 via the air supply line 104 by gas supply means such as a blower, a compressor, and a gas cylinder (not shown). The The stock solution is supplied through the stock solution supply line 105 by a supply means such as a pump or pressurization.
The reaction product and gas are discharged to the outside from the reaction product discharge line 106 and the exhaust line 107. In addition, the stock solution forms a circulating flow from the liquid surface of the bioreactor 103 to the lower part through the circulating liquid line 108. The gas and the undiluted solution flow in the diffuser treatment apparatus 102 in a parallel flow and are stirred, and the biological reaction proceeds by the biocatalytic function of the enzyme or the microorganism in the undiluted solution. When the aeration treatment apparatus 102 of the present invention is applied as a bioreactor, the gas flow rate in the bioreactor can be operated in a high gas flow rate range of 0.1 to 5 m / s as compared with the conventional bubble column system. For example, a high oxygen transfer rate is achieved. Further, the flow rate distribution in the bioreactor is made uniform, the oxygen transfer rate is made uniform, and the reaction product is homogenized. Furthermore, since it has a mixing and stirring function, there is no generation of a dead area (dead space) in the bioreactor (103), and the enlargement is facilitated. Furthermore, the occurrence of gas channeling is prevented to promote a homogeneous reaction, and the gas dispersion in the high viscosity liquid is made uniform. Furthermore, by improving the reaction rate, space saving and energy saving are achieved, and production costs are reduced. In addition, it can utilize also as a gas-liquid reaction apparatus which does not use a biocatalyst. In addition, the superficial velocity of the gas in the conventional bubble column type bioreactor is in the range of 0.01 to 0.1 m / s.

FIG. 16 is a schematic view showing an aeration processing apparatus using a conventional diffuser plate method.
In the conventional aeration processing apparatus 110, a large number of diffuser plates 112 are arranged on the bottom surface in the aeration tank 111, and air is supplied to the diffuser plates 112 via the blower 113 and the air supply line 114. The diffuser plate 112 is formed of a fine porous body and generates fine bubbles. The amount of air blown from the general diffuser plate 112 is 50 to 400 NL / min. The ventilation resistance is 1000 to 3000 Pa (Pascal). The constituent material of the conventional diffuser plate is rubber, plastic or the like.

FIG. 17 is a schematic diagram showing a conventional diffusion treatment apparatus using a packing method. In the conventional radiation treatment apparatus 115, a cylindrical radiation tower 116 is filled with a regular or irregular packing. Gas and raw water flow countercurrently through the filling 117 and come into gas-liquid contact to be diffused. In the case of a general packing method, the gas supply rate is in the range of 10 to 100 Nm ³ / (m ² · hour).

  In addition, the constituent material of the diffuser according to the present invention can be appropriately selected and used from one kind of metal, ceramics, plastic, glass, FRP, or a composite material of these materials. By using a metal material such as stainless steel or titanium, it can be used semi-permanently. The generation of industrial waste is suppressed. Conventional constituent materials such as diffuser plates and diffuser cylinders are often made of plastic, rubber or the like. There are problems with clogging and durability.

  It is a schematic diagram which shows 1st Example based on this invention.   It is a schematic diagram which shows 2nd Example based on this invention.   It is a schematic diagram which shows 3rd Example based on this invention.   FIGS. 1A and 1B show examples of static mixers 2, 9, 13 and 17 used in the first to third embodiments of the present invention. FIG. 4A shows a passage tube having a right-handed spiral blade. FIG. (B) The figure is a schematic perspective view of a passage tube having a left twisted spiral blade.   It is a figure which shows one example of the static mixers 2, 9, 13, and 17 used by 1st Example to 3rd Example of this invention.   BRIEF DESCRIPTION OF THE DRAWINGS It is the schematic of the aeration process apparatus which concerns on 1st Example (refer FIG. 1) of this invention.   It is a perspective view which shows one example of the gas ejection nozzle used in the 1st Example (refer FIG. 1) of this invention.   It is the schematic of the aeration process apparatus which concerns on 2nd Example (refer FIG. 2) of this invention.   It is a partial schematic bottom view of the diffuser processing apparatus which concerns on 2nd Example (refer FIG. 2) of this invention.   It is a partial schematic perspective view of the gas ejection part which concerns on 2nd Example (refer FIG. 2) of this invention.   It is a schematic sectional drawing of the aeration processing apparatus which concerns on the 3rd Example (refer FIG. 3) of this invention.   It is a figure which shows the example at the time of applying the aeration process apparatus which concerns on this invention to the aeration process of an activated sludge method.   It is a figure which shows the example at the time of applying the aeration process apparatus which concerns on this invention to the discharge process of waste_water | drain.   It is a figure which shows the example at the time of applying the aeration processing apparatus which concerns on this invention to an exhaust gas processing apparatus.   It is a figure which shows the example at the time of applying the aeration process apparatus which concerns on this invention to the biological reaction apparatus using an enzyme or microorganisms.   It is a schematic diagram which shows the aeration processing apparatus by the conventional diffuser board system.   It is a schematic diagram which shows the diffusion processing apparatus by the conventional filler system.

Explanation of symbols

1, 8, 16, 23, 29, 35, 43, 50, 59, 71: Passage tube 2, 9, 13, 17, 24, 30, 41,
51, 57, 73, 77: Static mixer 3, 10, 18, 38, 39, 42, 52, 79: Space part 5, 12, 20, 44, 54, 65, 76: Gas ejection part 6, 14 , 22, 47, 53, 80: Liquid introduction part 7, 15, 21, 40, 49, 58, 70,
81, 87, 94, 102: Air diffuser 4, 11, 19, 84, 90, 97, 104: Air feed line 45, 55, 61, 64, 75: Air feed tube

Claims (2)

A plurality of right-handed (clockwise) or left-handed (counterclockwise) spiral blades are provided inside a cylindrical passage tube through which fluid flows, and a plurality of fluids are contained in the passage tube. A passage is formed, the fluid passages communicate with each other through an opening in the longitudinal direction of the blade body, and the blade body includes one stationary mixer made of a porous body, and the longitudinal direction is substantially vertical. a cylindrical passage pipe disposed in the a liquid introducing portion provided at a lower end of said passage tube, an upper side of the liquid introduction portion, is disposed below the first static mixer, said A right twist (clockwise) or a left twist (counterclockwise) inside a cylindrical passage pipe through which gas flows and supplies gas into the passage pipe through an air feed line connected from the upper end side of the passage pipe. Direction) and a plurality of blades in a spiral shape, and a plurality of pipes inside the tubular passage tube through which gas flows. The body passage is formed, the fluid passage between the communicating through the longitudinal opening of the sail body, said sail body has a plurality of gas ejection portion of another static mixer consisting of a perforated plate is internally provided The gas introduction means supplies the gas to the gas ejection part so that the rising speed in the cylindrical passage tube through which the fluid flows is 0.1 to 10 m / s, and introduces the liquid The liquid is introduced into the passage pipe from the section, and the gas and the liquid rise in a parallel flow in the passage pipe, are in contact with gas-liquid in the static mixer 1 and are discharged from the upper end side of the passage pipe. An aeration process apparatus characterized by being made. 2. The dispersion according to claim 1, wherein a total surface area (m ² ) of the blades per unit volume (m ³ ) of the passage pipe is in a range of 10 to 150 m ² / m ^3. Qi treatment device.

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