A microchannel oscillation separation device and method based on radial flow

Abstract

The present invention discloses a microchannel oscillation separation device and method based on radial flow, which relate to the technical field of sewage treatment. The separation device includes a cylinder, a water inlet pipe, an inlet and outlet water pipes, a backwash gas and liquid inlet pipe, a backwash liquid outlet pipe, a backwash gas outlet, a feed port, a discharge port, a water cap, a three-phase separator and a radial medium particle bed; the radial medium particle bed is filled in an annular space surrounded by a coaxial inner distribution cylinder and an outer distribution cylinder, and the fluid flows in axially, passes through the medium particle bed radially, and finally flows out; and different fluid distribution improvement measures are provided according to different radial flow forms, and a microchannel oscillation separation method based on radial flow is also provided; the present invention adopts the form of radial flow to increase the filtration area of ​​the medium particle bed, improve the processing capacity of the microchannel oscillation separation device, reduce the pressure drop of the medium particle bed, and at the same time improve the distribution uniformity of the fluid in the medium particle bed.

Description

Technical Field

[0001] The present invention relates to the technical field of sewage treatment, and in particular to a microchannel oscillation separation device and method based on radial flow. Background Art

[0002] Microchannel oscillation separators are widely used in wastewater treatment, petroleum refining, coal chemical industry, and other fields due to their stability, high efficiency, low cost, and environmental friendliness. They utilize microchannels formed by gaps between or within dielectric materials to remove fine suspended particles from the liquid phase, making them a key technology for achieving liquid-solid separation. The separation efficiency of a microchannel oscillation separator is closely related to the filtration area and bed height of the media particle bed. However, existing axial-flow microchannel oscillation separators have significant drawbacks. Their media particle bed has a small filtration area, and due to the high pressure drop across the bed, they result in low wastewater treatment capacity and short operating cycles.

[0003] When the flow rate of wastewater to be treated is high, the only options are to increase the diameter and height of the media particle bed or to connect multiple microchannel oscillating separators in parallel to improve the processing capacity of the microchannel oscillating separator. However, increasing the diameter results in a larger footprint, adversely affecting the overall layout of the factory and making the manufacturing and transportation processes quite inconvenient. Increasing the height results in a greater pressure drop across the media particle bed, making it difficult for the backwash gas and liquid to fluidize and boil the media particles. This requires larger backwash gas and backwash water flows, making control difficult and placing higher demands on the site's backwash system. Connecting multiple microchannel oscillating separators in parallel complicates the piping and is less conducive to operation. Radial particle beds, on the other hand, offer a range of recognized advantages, including a large filtration area, a small footprint, and low bed pressure drop. These can be combined with existing microchannel oscillating separators to improve the processing capacity of the microchannel oscillating separator. However, radial particle beds also present problems such as uneven fluid distribution along the axial direction and susceptibility to clogging on both sides of the bed.

[0004] Chinese invention patent publications CN 107382654A, CN 108114510 A, CN 107433055 A, CN 113045376A, and CN 107720872A all relate to a gas-liquid-solid three-phase separator and an ebullated bed reactor or ebullated bed separator containing the same. Ebullated bed separators purify and deeply treat purified water, quench water, and wash water from methanol-to-olefins (MTO), effectively addressing wastewater recycling in the MTO process. However, when used for separation systems with low pollutant concentrations and high throughput, the results are less than ideal, often necessitating the use of multiple or more separators connected in parallel. This complex operation, high investment, and significant floor space requirements limit the industrial application of ebullated bed separators.

[0005] Utility model patent CN 216497936 U provides a radial filter. This device incorporates a flow guide between the water pipe and the granular bed, directing water flow horizontally through the granular bed to achieve radial filtration. A water distribution trough is also located above the granular bed, directing water flow from top to bottom through the bed to achieve vertical filtration, effectively increasing the filtration area and improving filtration effectiveness and efficiency. However, the backwash flow rate is only a fraction of the filtration flow rate, making it difficult to thoroughly clean the filter media and achieve good regeneration. Furthermore, the fluid exhibits multi-dimensional flow directions within the granular bed, preventing a stable flow field and making it difficult to achieve good filtration results.

[0006] Chinese invention patent publication CN 107413122 A relates to a vertical radial flow adsorber. The adsorber places a central flow channel distributor in a pipe where the inner central gas flows. The flow channel distributor is composed of hollow cylinders of equal diameter, porous hollow cylinders, and solid cones. This structural design can effectively reduce the influence of the particle bed height on the uneven distribution of the flow field, thereby increasing the maximum design height of the vertical radial flow adsorber. Therefore, under the condition of the same processing capacity, the design of the adsorber of this invention has the characteristics of small footprint and high flow field uniformity. However, its fluid flows from bottom to top, which is more suitable as an equipment component in the field of large-scale air separation technology. Its adsorption device does not involve the recycling of the particle bed, so it is not suitable for the field of sewage treatment and reuse.

[0007] Utility model patent CN 210021628 U provides a regenerative radial flow adsorber, comprising a cylindrical adsorber body, a head, and a radial flow adsorbent bed within the cylindrical body. The manhole and discharge port of this adsorber are both located at the top of the device, making loading and unloading of the adsorbent convenient. Furthermore, the device also incorporates a through-hole in the outer cylinder sealing section and a removable pipe installed in the through-hole, effectively addressing the issues of flange seal failure and water leakage caused by accumulated water during steam regeneration. However, the device, in which the adsorption fluid flows from bottom to top and the regeneration medium flows from top to bottom, is not suitable for sewage treatment and does not consider the regeneration effect of the filler or the flow field uniformity of the adsorbent bed.

[0008] Chinese invention patents CN 115180744 A and CN 115215460 A disclose a cross-flow nanofiltration microchannel separator. This device utilizes a structure combining a liquid-solid cyclone separator and a cross-flow particle bed, effectively removing fine particulate matter and coke powder from the purified water of a hydrocracking unit. However, the cyclone at the top of the cross-flow nanofiltration microchannel separator performs less effectively on the packing than a three-phase separator. The Johnson screens on both sides of the cross-flow particle bed are prone to clogging, preventing effective backwashing. Furthermore, the cross-flow filtration mechanism fails to account for the uniform distribution of fluid pressure drop across the bed. Summary of the Invention

[0009] The purpose of the present invention is to solve the shortcomings of the prior art and propose a microchannel oscillation separation device and method based on radial flow, so as to achieve the purpose of effectively improving the processing capacity of the microchannel oscillation separator and improving the flow field uniformity of the radial flow particle bed.

[0010] In order to achieve the above object, the present invention adopts the following technical solutions:

[0011] A microchannel oscillating separation device based on radial flow, comprising a cylinder, a lower head, an upper head, a water inlet pipe, a feed port, a discharge port, a water inlet and outlet pipes, a backwash gas and liquid inlet pipe, a backwash liquid outlet pipe, a backwash gas outlet, a three-phase separator, an inner distribution cylinder, an outer distribution cylinder, a radial flow medium particle bed, and a water cap, wherein:

[0012] The cylinder is overlapped and connected with the upper head and the lower head, the water inlet pipe is located at the central axis position of the top of the upper head, the water inlet and outlet pipes are located on both sides of the middle of the cylinder, the backwash gas and liquid inlet pipe is located at the bottom of the cylinder, the backwash liquid outlet pipe is located on both sides of the upper part of the cylinder, the backwash gas outlet is located on one side of the upper head, and the three-phase separator is arranged in the upper area of ​​the cylinder;

[0013] The outer distribution tube, the inner distribution tube, and the medium particle bed are all located in the lower middle area of ​​the cylinder and below the three-phase separator. A support plate is provided at the bottom of the outer distribution tube, and the medium particle bed is filled in the annular space surrounded by the support plate and the coaxially arranged outer distribution tube and inner distribution tube. The feed port is arranged on both sides of the cylinder and located on the upper part of the medium particle bed, and the discharge port is connected to the bottom of the outer distribution tube; the outer distribution tube and the inner distribution tube are both provided with water caps, the pores of the water caps are 0.05mm-0.5mm, and an annular sealing plate is provided between the top of the outer distribution tube and the cylinder. The cavity area surrounded by the annular sealing plate, the outer distribution tube and the cylinder is the outer flow channel, and the cavity area in the inner distribution tube is the inner flow channel

[0014] Furthermore, the fluid flows axially into the inner flow channel, radially passes through the medium particle bed, and finally flows out from the outer flow channel; when the inlet and outlet water pipes are arranged on both sides of the bottom of the particle bed, the axial flow modes of the inner and outer flow channels are the same, which is Z-type radial flow; when the inlet and outlet water pipes are arranged on both sides of the top of the particle bed, the axial flow modes of the inner and outer flow channels are opposite, which is π-type radial flow.

[0015] Furthermore, when the radial flow mode is Z-type flow: a guide cone is provided in the inner flow channel, the structure of the guide cone is a complete cone or an incomplete cone distributor, and the overall height of the guide cone is 0.6-1 times the height of the inner distribution tube.

[0016] Furthermore, when the radial flow mode is Z-type flow: the water caps in the inner distribution tube and the outer distribution tube are arranged in a non-uniform distribution, the number of water caps decreases as the height decreases, and the ratio of the number of water caps in the upper, middle and lower parts is approximately 4:3:2.

[0017] Furthermore, when the radial flow mode is π-type flow: the ratio of the radius of the inner flow channel to the height of the medium particle bed is between 1:8 and 1:12, and the ratio of the cross-sectional area of ​​the inner flow channel to that of the outer flow channel is between 1:2 and 1:4.

[0018] Furthermore, when the radial flow mode is π-type flow: the water caps in the inner distribution tube and the outer distribution tube are arranged in a uniform distribution mode.

[0019] Furthermore, the water caps of the inner and outer distribution tubes are arranged at a height of 0.6-0.8 times the overall height of the medium particle bed, and the top area is sealed.

[0020] Furthermore, the separation medium particle size of the medium particle bed is 0.1-2 mm, the material is an organic or inorganic material with adsorptive properties, and the stacking height of the separation medium is 500-5000 mm.

[0021] A microchannel oscillation separation method based on radial flow, using the microchannel oscillation separation device based on radial flow, the method includes an adsorption process and a desorption process, wherein:

[0022] The adsorption process includes: the wastewater to be treated first enters the inner flow channel from the water inlet pipe, then enters the radial flow medium particle bed from the surrounding water caps arranged on the inner distribution cylinder. Pollutants with a particle size greater than 0.5mm in the wastewater are intercepted by the water caps, and the remaining fine pollutants are separated through collision and interception in the microchannels formed by the random stacking of medium particles. The wastewater then flows out laterally from the water caps arranged on the outer distribution cylinder. The treated clear liquid is finally discharged from the outer inlet and outlet pipes of the cylinder through the outer flow channel.

[0023] The desorption process includes: the radial flow microchannel oscillation separation device is operated periodically. After a certain period of continuous adsorption or when the pressure loss reaches a certain value, a certain proportion of gas-liquid mixture is alternately introduced into the inlet and outlet pipes on both sides of the medium particle bed and the backwash gas-liquid inlet pipe at the bottom, so that the medium particles are fluidized and boiled, and then the fine pollutants on the medium particles are separated through the cyclone field in the three-phase separator. Finally, the regenerated medium particles flow out from the bottom of the three-phase separator and return to the medium particle bed. The backwash liquid and desorbed fine particles are discharged from the backwash liquid outlet pipes on both sides of the three-phase separator, and the backwash gas is discharged from the backwash gas outlet at the top.

[0024] Furthermore, during backwashing, the gas-liquid mixture is introduced into the inlet and outlet water pipes or the backwash gas-liquid inlet pipe, and the two are used alternately.

[0025] Compared with the prior art, the present invention has the following beneficial effects:

[0026] (1) The present invention adopts the flow form of fluid radially passing through the medium particle bed. Under the same particle bed height and diameter, the filtration area is increased, the bed pressure drop is reduced, and the sewage treatment capacity and the operation cycle of the device are improved;

[0027] (2) The present invention adopts a method of regulating the ratio of the inner flow channel radius to the separation medium bed height and the ratio of the cross-sectional area of ​​the inner flow channel to the outer flow channel for the π-type radial flow microchannel oscillating separator; and adopts a method of non-uniform arrangement of the water cap along the axial height and adding a guide cone in the inner flow channel for the Z-type radial flow microchannel oscillating separator; thereby effectively improving the distribution of the fluid in the radial particle bed and solving the problem of uneven fluid distribution in the core of the radial separator;

[0028] (3) The present invention strengthens the regeneration effect of the filler through the three-phase separator at the top of the microchannel oscillation separator, and the medium particle bed is changed to a radial structure. Compared with the original microchannel separator, the pressure drop during the regeneration process is smaller, the intensity is greater, and the regeneration effect on the filler is more thorough. At the same time, the two backwash gas and liquid inlets are used alternately to effectively solve the problem of water cap blockage on both sides of the medium particle bed. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 This is a schematic diagram of a microchannel oscillating separation device based on Z-type radial flow, a preferred embodiment of the present invention;

[0030] Figure 2 This is a schematic diagram of the arrangement of the inner distribution tube water cap of a microchannel oscillating separation device based on Z-type radial flow, in a preferred embodiment of the present invention;

[0031] Figure 3 This is a preferred embodiment of the present invention, a schematic diagram of the arrangement of the outer distribution tube water cap of the microchannel oscillation separation device based on Z-type radial flow;

[0032] Figure 4 This is a schematic diagram of a microchannel oscillating separation device based on π-type radial flow, a preferred embodiment of the present invention;

[0033] Figure 5 This is a schematic diagram of the arrangement of the inner distribution tube water cap of a microchannel oscillating separation device based on π-type radial flow, in a preferred embodiment of the present invention;

[0034] Figure 6 This is a preferred embodiment of the present invention, a schematic diagram of the arrangement of the outer distribution tube water cap of the microchannel oscillation separation device based on π-type radial flow;

[0035] Figure 7The Z-type radial microchannel oscillation separator in Example 1 of the present invention is 250m 3 Comparison of suspended solids content in inlet and outlet during long-term operation at a treatment flow rate of 1.5 / h;

[0036] Figure 8 The π-type radial microchannel oscillation separator in Example 2 of the present invention is 120m 3 Comparison of suspended solids content at the inlet and outlet during long-term operation at a treatment flow rate of 1.533 W / h.

[0037] In the figure: 1. Cylinder; 2. Lower head; 3. Upper head; 4. Water inlet pipe; 5. Water inlet and outlet pipes; 6. Backwash gas and liquid inlet pipe; 7. Backwash liquid outlet pipe; 8. Backwash gas outlet; 9. Feed inlet; 10. Discharge port; 11. Manhole; 12. Water cap; 13. Skirt; 14. Three-phase separator; 15. Inner distribution tube; 16. Outer distribution tube; 17. Medium particle bed; 18. Guide cone. DETAILED DESCRIPTION

[0038] The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all the embodiments.

[0039] It should also be noted that the endpoints of the ranges and any values ​​disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be considered to be specifically disclosed herein.

[0040] Existing axial-flow microchannel oscillating separators have significant drawbacks. Their upper granular bed has a small filtration area, and due to its high bed pressure drop, it leads to low wastewater treatment capacity and short operating cycles. Radial granular beds, on the other hand, offer advantages such as a large filtration area, a small footprint, and low bed pressure drop, effectively addressing these drawbacks. However, they also present issues such as uneven axial fluid distribution and susceptibility to clogging on both sides of the bed.

[0041] Based on this, in this application, a microchannel oscillation separation device and method based on radial flow was invented, which organically combined the radial particle bed with the existing microchannel oscillation separator, and effectively improved the core problem of uneven fluid distribution in the radial separator and the problem of blockage on both sides of the bed.

[0042] Specifically, the core problem of uneven fluid distribution and blockage on both sides of the bed in the radial separator is improved as follows: the π-type radial flow microchannel oscillation separator improves the axial uniform distribution problem of the fluid by regulating the ratio of the inner flow channel radius to the separation medium bed height and the ratio of the cross-sectional area of ​​the inner flow channel to the outer flow channel; the Z-type radial flow microchannel oscillation separator improves the axial uniform distribution problem of the fluid by the uneven arrangement of the water cap along the axial height and the addition of a guide cone in the inner flow channel.

[0043] like Figure 1 As shown, a microchannel oscillation separation device based on radial flow, specifically, a microchannel oscillation separation device with Z-type radial flow in the radial flow mode, includes a cylinder 1, a lower head 2, an upper head 3, a water inlet pipe 4, an inlet and outlet water pipes 5, a backwash gas and liquid inlet pipe 6, a backwash liquid outlet pipe 7, a backwash gas outlet 8, a feed port 9, a discharge port 10, a manhole 11, a water cap 12, a skirt 13, a three-phase separator 14, an inner distribution tube 15, an outer distribution tube 16 and a radial flow medium particle bed 17, wherein: the inlet and outlet water pipes 5 can be used as a conventional water outlet pipe in addition to being used as a backwash gas and liquid inlet pipe; the feed port 9 can also be used as a manhole.

[0044] Specifically, the top and bottom of the cylinder 1 overlap and connect with the upper head 3 and the lower head 2 respectively, and the water inlet pipe 4 is located at the center axis position of the top of the upper head 3; the inlet and outlet water pipes 5 are located on both sides of the lower middle part of the cylinder 1, more specifically, the inlet and outlet water pipes 5 are located on both sides of the bottom of the medium particle bed 17; the backwash gas and liquid inlet pipe 6 is located at the center position of the bottom of the cylinder 1, the backwash liquid outlet pipe 7 is located on both sides of the upper part of the cylinder 1, the backwash gas outlet 8 is located on one side of the upper head 3, the manhole 11 is installed at the bottom of the lower head 2, and the skirt 13 is connected to the bottom of the barrel body with the same center axis.

[0045] The three-phase separator 14 is arranged in the upper region of the cylinder 1. Specifically, the three-phase separator 14 includes an outer shell and an inner shell, wherein: the outer shell has a cylindrical upper portion and a conical lower portion; the inner shell has a conical upper portion and a cylindrical lower portion; guide vanes are provided between the inner and outer shells, and the guide vanes are installed at an angle to the vertical direction (not shown in the figure); the inner shell is connected to the liquid phase outlet (i.e., the backwash liquid outlet pipe 7) on both sides and the gas phase outlet (i.e., the backwash gas outlet 8) at the top; and the bottom of the outer shell is connected to the solid phase outlet (i.e., connected to the inlet of the inner distribution tube 15). The arrangement of the three-phase separator 14 can enhance the regeneration effect of the packing, and combined with the change of the medium particle bed layer to a radial structure, the pressure drop during the regeneration process is smaller, the intensity is greater, and the regeneration effect on the packing is more thorough.

[0046] The outer distribution tube 16, inner distribution tube 15, and media particle bed 17 are all located in the lower-middle region of the cylinder 1 and below the three-phase separator 14. The solid phase outlet of the three-phase separator 14 is connected to the inlet of the inner distribution tube 15. A support plate (not shown) is provided at the bottom of the outer distribution tube 16. The media particle bed 17 is loaded into the annular space enclosed by the support plate and the coaxially arranged outer distribution tube 16 and inner distribution tube 15. The feed port 9 is arranged on both sides of the cylinder 1 and located above the media particle bed 17. The discharge port 10 is connected to the bottom of the outer distribution tube 16. Water caps 12 are installed on both the outer distribution tube 16 and the inner distribution tube 15. The pores of the water caps 12 range from 0.05 mm to 0.5 mm, allowing the fluid to flow radially through the bed without leaking the media particles. An annular sealing plate is provided between the top of the outer distribution tube 16 and the cylinder body 1. The cavity area enclosed by the annular sealing plate, the outer distribution tube 16 and the cylinder body 1 is the outer flow channel, and the cavity area in the inner distribution tube 15 is the inner flow channel.

[0047] The fluid flows into the inner flow channel axially, passes through the medium particle bed radially, and finally flows out from the outer flow channel; in Z-type radial flow, the axial flow mode of the inner and outer flow channels is the same.

[0048] Further, if Figure 2-3 As shown, the water caps 12 in the inner distribution tube 15 and the outer distribution tube 16 are arranged in a non-uniform distribution, and the number of water caps 12 decreases as the height decreases. The water caps 12 are arranged in a number of groups along the height direction of the inner and outer distribution tubes 16, and each group includes a number of water caps 12 uniformly arranged along the inner radial direction of the tube, such as Figure 2 The left side shows a schematic diagram of the structure of a single group of water caps 12 in the inner distribution tube 15 arranged evenly along the radial direction. Figure 2 The diagram on the right side of the middle is a schematic diagram showing the structure of the multiple water caps 12 in the inner distribution tube 15 arranged non-uniformly along the height direction. Figure 3 The diagram shows the structure of the water caps 12 on the outer distribution tube 16 when it is deployed. Similarly, the water caps 12 are arranged unevenly along the height. Specifically, the number of water caps 12 decreases as the height decreases. In one possible embodiment, the inner and outer distribution tubes 15 and 16 are evenly divided along the height into upper, middle, and lower sections, with the ratio of the number of water caps 12 in these sections being approximately 4:3:2.

[0049] In addition, the water caps 12 of the inner and outer distribution cylinders 16 are arranged at a height of 0.6-0.8 times the overall height of the medium particle bed 17, and the top area is sealed.

[0050] Furthermore, the bottom of the inner flow channel is fixedly connected with a guide cone 18. The structure of the guide cone 18 is a complete cone (see Figure 1) or an incomplete cone distributor, such as a half-cone. The shape curve of the guide cone 18 includes, but is not limited to, an optimal shape curve. The overall height of the guide cone 18 is 0.6-1 times the height of the inner distribution tube 15. By adding the guide cone 18 to the inner flow channel, the flow area at different axial heights is changed, and the static pressure variation trends of the inner and outer flow channels are different, achieving the effect of uniform flow distribution.

[0051] The medium particle bed 17 is one or more granular separation media with a particle size of 0.1-2 mm and is made of an adsorbent organic or inorganic material such as adsorbent resin, graphene, activated clay, etc. The stacking height of the separation media is 500-5000 mm.

[0052] A microchannel oscillation separation device with Z-type radial flow is adopted, and the water cap 12 is arranged unevenly along the axial height and a guide cone 18 is added in the inner flow channel, which effectively improves the distribution of the fluid in the radial particle bed and solves the problem of uneven fluid distribution in the core of the radial separator.

[0053] A microchannel oscillating separation device based on radial flow, specifically, a microchannel oscillating separation device with a π-type radial flow in radial flow mode, such as Figure 4 As shown, the inlet and outlet pipes 5 are located on either side of the lower middle portion of the cylinder 1. More specifically, they are located on either side of the top of the media granular bed 17. Similarly, in addition to serving as conventional outlet pipes, the inlet and outlet pipes 5 can also serve as backwash gas and liquid inlet pipes. Furthermore, the ratio of the radius of the inner flow channel to the height of the media granular bed 17 is between 1:8 and 1:12, and the ratio of the cross-sectional area of ​​the inner flow channel to the outer flow channel is between 1:2 and 1:4.

[0054] The fluid flows into the inner flow channel axially, passes through the medium particle bed radially, and finally flows out of the outer flow channel; in π-type radial flow, the axial flow modes of the inner and outer flow channels are opposite.

[0055] In addition, if Figure 5-6 As shown, the water caps 12 in the inner distribution tube 15 and the outer distribution tube 16 are arranged in a uniform distribution. Figure 5 The left side shows a schematic diagram of the uniform radial arrangement of the water caps 12 in the inner distribution tube 15. Figure 5 The right side shows a schematic diagram of the uniform arrangement of the water caps 12 in the inner distribution tube 15 along the height direction. Figure 6 What is shown is a schematic diagram of the water caps 12 being evenly arranged on the outer distribution tube 16 when it is unfolded.

[0056] A microchannel oscillation separation device with π-type radial flow is adopted, and the ratio of the inner flow channel radius to the separation medium bed height and the ratio of the cross-sectional area of ​​the inner flow channel to the outer flow channel are adjusted. This effectively improves the distribution of the fluid in the radial particle bed and solves the problem of uneven fluid distribution in the core of the radial separator.

[0057] Utilizing a microchannel oscillation separation device based on radial flow, the present application also provides a microchannel oscillation separation method based on radial flow, which includes an adsorption process and a desorption process, wherein:

[0058] The adsorption process includes: the wastewater to be treated first enters the inner flow channel from the water inlet pipe 4, then enters the radial flow medium particle bed 17 laterally from the surrounding water caps 12 arranged on the inner distribution tube 15. Pollutants with a particle size greater than 0.5 mm in the wastewater are intercepted by the water caps 12, and the remaining fine pollutants are separated by collision, interception, and other effects in the microchannels formed by the random stacking of the medium particles. The wastewater then flows out laterally from the water caps 12 arranged on the outer distribution tube 16. The treated clear liquid is finally discharged from the outer inlet and outlet pipes 5 on the outside of the cylinder 1 (the inlet and outlet pipes 5 are used as outlet pipes in this case) through the outer flow channel;

[0059] In the microchannel oscillating separation device with Z-type radial flow, see Figure 1 The treated clear liquid is finally discharged from the inlet and outlet pipes 5 arranged on both sides of the bottom of the medium particle bed 17 through the external flow channel;

[0060] The radial flow mode is a π-type radial flow microchannel oscillation separation device, see Figure 4 The treated clear liquid is finally discharged from the inlet and outlet pipes 5 arranged on both sides of the top of the medium particle bed 17 through the external flow channel.

[0061] The desorption process includes: the radial flow microchannel oscillation separation device is operated periodically. After continuous adsorption for 3-7 days or when the pressure loss reaches a certain value, such as greater than 0.3 MPa, a gas-liquid mixture with a ratio of 5:1 is alternately introduced into the inlet and outlet pipes 5 on both sides of the medium particle bed 17 (at this time, the inlet and outlet pipes 5 are used as backwash gas and liquid inlet pipes) and the backwash gas and liquid inlet pipe 6 at the bottom, so that the medium particles are fluidized and boiled, and then the fine pollutants on the medium particles are separated by the cyclone field in the three-phase separator 14. Finally, the regenerated medium particles flow out from the bottom of the three-phase separator 14 and return to the medium particle bed 17. The backwash liquid and desorbed fine particles are discharged from the backwash liquid outlet pipes 7 on both sides of the three-phase separator 14, and the backwash gas is discharged from the backwash gas outlet 8 at the top.

[0062] Likewise:

[0063] In the microchannel oscillating separation device with Z-type radial flow, see Figure 1, the gas-liquid mixture is alternately introduced into the water inlet and outlet pipes 5 on both sides of the bottom of the medium particle bed 17;

[0064] The radial flow mode is a π-type radial flow microchannel oscillation separation device, see Figure 4 The gas-liquid mixture is alternately introduced into the water inlet and outlet pipes 5 on both sides of the top of the medium particle bed 17.

[0065] The above adsorption and desorption processes are carried out alternately.

[0066] Furthermore, during backwashing, the gas-liquid mixture is introduced into either the inlet and outlet pipes 5 (i.e., the inlet and outlet pipes serve as the backwash gas and liquid inlet pipes) or the backwash gas and liquid inlet pipe 6, with the two being used alternately. The specific use cycle is determined by the clogging of the water caps on both sides of the radial media granular bed. Alternating the two backwash gas and liquid inlets effectively solves the problem of water cap clogging on both sides of the media granular bed.

[0067] The method effectively solves the problems of small filtration area, low processing capacity and short equipment operation cycle in existing microchannel oscillation separation.

[0068] The present invention will be further described below with reference to specific examples. However, it should be understood that these examples are intended to illustrate the present invention only and are not intended to limit the scope of the invention. The methods described in the following examples, where specific conditions are not specified, are generally based on conventional conditions or the conditions recommended by the manufacturer. Unless otherwise indicated, all percentages and parts are by weight.

[0069] Example 1

[0070] A methanol-to-olefins water purification device with a processing capacity of 200 cubic meters per hour was built in a factory in Yan'an, Shaanxi Province. The Z-type radial flow microchannel oscillation separator of the present invention was used for experiments. The previous device was an axial flow microchannel oscillation separator with a processing capacity of 50 cubic meters per hour, which mainly removed suspended matter and COD in the purified water. The inlet and outlet water samples of the device were collected at different times every day for detection and analysis to examine the purification effect of the radial microchannel separator.

[0071] 1. Material properties and related parameters of methanol to olefins purified water

[0072] The purified water from methanol to olefins is a liquid-solid two-phase mixture containing a large amount of COD and suspended solids. The COD content is between 500-800 mg / L and the suspended solids content is 5-50 mg / L. The main components of the purified water are aromatic hydrocarbons and alkanes.

[0073] 2. Methanol to Olefins Purification Water Treatment Unit

[0074] The equipment structure of the Z-type radial flow microchannel oscillation separator is as follows Figure 1 The structural dimensions are shown in Table 1 below.

[0075] Table 1 Dimensions of Z-type radial flow microchannel oscillating separator

[0076]

[0077] 3. Operating conditions

[0078] In a methanol-to-olefins purified water treatment process, a Z-shaped radial flow microchannel oscillating separator was used for process modification according to the method of the present invention to deeply treat purified water containing suspended solids and COD. The pressure during operation of the device was 0.2-1.5 MPa, the purified water temperature was 60-70°C, and the treatment capacity was 200m 3 / h.

[0079] 4. Implementation Effect

[0080] After the purified water from methanol to olefins was treated by the Z-type radial flow microchannel oscillation separator, the initial separation effect was that the suspended solids content was reduced from 12.46 mg / L to 0.37 mg / L, the turbidity was reduced from 30.7 NTU to 1.15 NTU, and the COD content was reduced from 699 mg / L to 148 mg / L. During the test, the device was operated at a flow rate of 200 m 3 / h continuous operation for two cycles totaling 336 hours, the inlet and outlet suspended solids content is as follows Figure 7 As shown, compared with the previous cycle of 48 hours, the operation cycle was significantly extended, the average suspended solids content at the inlet was 11.35 mg / L, the average suspended solids content at the outlet was 0.48 mg / L, and the suspended solids removal rate reached 95.77%; the average turbidity at the inlet was 29 NTU, the average turbidity at the outlet was 1.42 NTU, and the removal rate was 95.10%; the COD removal rate was also maintained at above 75%, achieving deep treatment of purified water and enabling its reuse.

[0081] Example 2

[0082] This embodiment is a π-type radial flow microchannel oscillation separation device used to treat purified water in a power plant's stripping process. The device has a sewage treatment capacity of 120 cubic meters per hour and is mainly used to remove suspended matter in the purified water.

[0083] 1. Material properties and related parameters of stripping water

[0084] Purified water is a mixture of liquid and solid phases. The main pollutants in the water are suspended solids, with a content of 20-60 mg / L.

[0085] 2. Methanol to Olefins Purification Water Treatment Unit

[0086] The equipment structure of the π-type radial flow microchannel oscillation separator is as follows: Figure 2As shown in Table 1, the main structural dimensions are the same as those in Table 1, but without the guide cone.

[0087] 3. Operating conditions

[0088] In a power plant's stripping process, a π-shaped radial flow microchannel oscillating separation device was used to perform deep treatment of purified water containing suspended solids. The device operated at a pressure of 0.2-1.0 MPa and had a processing capacity of 120 m³ / h.

[0089] 4. Implementation Effect

[0090] After the purified water was treated by the π-type radial flow microchannel oscillation separator, the initial separation effect was that the solid suspended matter content was reduced from 42.7mg / L to 3.7mg / L, and the turbidity was reduced from 20.6NTU to 1.20NTU. During the test, the device was operated continuously for five cycles at a flow rate of 120m3 / h, with backwashing every 72 hours for a total of 360 hours. The suspended matter content at the inlet and outlet was as follows: Figure 8 As shown, the average suspended solids content at the inlet is 35.1 mg / L, the average suspended solids content at the outlet is 2.5 mg / L, and the suspended solids removal rate reaches 92.88%; the average turbidity at the inlet is 19.7 NTU, the average turbidity at the outlet is 0.94 NTU, and the removal rate is 95.22%, achieving deep treatment of purified water and enabling its reuse.

[0091] The above description is only a preferred specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any technician familiar with the technical field, within the technical scope disclosed by the present invention, who makes equivalent replacements or changes based on the technical solution and inventive concept of the present invention, should be covered by the scope of protection of the present invention.

Claims

1. A microchannel oscillation separation device based on radial flow, characterized in that: It includes a cylinder, a lower head, an upper head, a water inlet pipe, a feed port, a discharge port, a water inlet and outlet pipes, a backwash gas and liquid inlet pipe, a backwash liquid outlet pipe, a backwash gas outlet, a three-phase separator, an inner distribution cylinder, an outer distribution cylinder, a radial flow medium particle bed and a water cap, wherein: The cylinder is overlapped and connected with the upper head and the lower head, the water inlet pipe is located at the central axis position of the top of the upper head, the water inlet and outlet pipes are located on both sides of the middle of the cylinder, the backwash gas and liquid inlet pipe is located at the bottom of the cylinder, the backwash liquid outlet pipe is located on both sides of the upper part of the cylinder, the backwash gas outlet is located on one side of the upper head, and the three-phase separator is arranged in the upper area of ​​the cylinder; The outer distribution tube, the inner distribution tube, and the medium particle bed are all located in the lower middle area of ​​the cylinder and below the three-phase separator. A support plate is provided at the bottom of the outer distribution tube. The medium particle bed is loaded in the annular space surrounded by the support plate and the coaxially arranged outer distribution tube and inner distribution tube. The feed port is arranged on both sides of the cylinder and located above the medium particle bed. The discharge port is connected to the bottom of the outer distribution tube. The outer distribution tube and the inner distribution tube are both provided with water caps, the pores of the water caps are 0.05mm-0.5mm, and an annular sealing plate is provided between the top of the outer distribution tube and the cylinder. The cavity area surrounded by the annular sealing plate, the outer distribution tube, and the cylinder is the outer flow channel, and the cavity area in the inner distribution tube is the inner flow channel. The fluid flows axially into the inner flow channel, then radially passes through the medium particle bed, and finally flows out of the outer flow channel. When the inlet and outlet pipes are arranged on both sides of the bottom of the particle bed, the axial flow modes of the inner and outer flow channels are the same, which is a Z-type radial flow. When the inlet and outlet pipes are arranged on both sides of the top of the particle bed, the axial flow modes of the inner and outer flow channels are opposite, which is a π-type radial flow. When the radial flow mode is Z-type flow: a guide cone is provided in the inner flow channel, and the structure of the guide cone is a complete cone or an incomplete cone distributor, and the overall height of the guide cone is 0.6-1 times the height of the inner distribution tube; When the radial flow is a Z-shaped flow, the water caps in the inner and outer distribution tubes are arranged in a non-uniform manner, the number of water caps decreases as the height decreases, and the ratio of the number of water caps in the upper, middle, and lower parts is 4:3:2; When the radial flow mode is π-type flow: the ratio of the radius of the inner flow channel to the height of the medium particle bed is between 1:8 and 1:12, and the ratio of the cross-sectional area of ​​the inner flow channel to that of the outer flow channel is between 1:2 and 1:4; When the radial flow mode is π-type flow: the water caps in the inner distribution tube and the outer distribution tube are arranged in a uniform distribution mode.

2. The microchannel oscillation separation device based on radial flow according to claim 1, characterized in that: The water caps of the inner and outer distribution tubes are arranged at a height of 0.6-0.8 times the overall height of the medium particle bed, and the top area is sealed.

3. The microchannel oscillation separation device based on radial flow according to claim 1, characterized in that: The separation medium particle size of the medium particle bed is 0.1-2 mm, and the material is an organic or inorganic material with adsorption properties. The stacking height of the separation medium is 500-5000 mm.

4. A microchannel oscillation separation method based on radial flow, characterized in that: Utilizing the radial flow-based microchannel oscillation separation device according to any one of claims 1 to 3, the method includes an adsorption process and a desorption process, wherein: The adsorption process includes: the wastewater to be treated first enters the inner flow channel from the water inlet pipe, then enters the radial flow medium particle bed from the surrounding water caps arranged on the inner distribution cylinder. Pollutants with a particle size greater than 0.5mm in the wastewater are intercepted by the water caps, and the remaining fine pollutants are separated through collision and interception in the microchannels formed by the random stacking of medium particles. The wastewater then flows out laterally from the water caps arranged on the outer distribution cylinder. The treated clear liquid is finally discharged from the outer inlet and outlet pipes of the cylinder through the outer flow channel. The desorption process includes: the radial flow microchannel oscillation separation device is operated periodically. After a certain period of continuous adsorption or when the pressure loss reaches a certain value, a certain proportion of gas-liquid mixture is alternately introduced into the inlet and outlet pipes on both sides of the medium particle bed and the backwash gas-liquid inlet pipe at the bottom, so that the medium particles are fluidized and boiled, and then the fine pollutants on the medium particles are separated through the cyclone field in the three-phase separator. Finally, the regenerated medium particles flow out from the bottom of the three-phase separator and return to the medium particle bed. The backwash liquid and desorbed fine particles are discharged from the backwash liquid outlet pipes on both sides of the three-phase separator, and the backwash gas is discharged from the backwash gas outlet at the top.

5. The microchannel oscillation separation method based on radial flow according to claim 4, characterized in that: During backwashing, the gas-liquid mixture is introduced into the inlet and outlet pipes or the backwash gas-liquid inlet pipe, and the two are used alternately.

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