CN117282180B - Pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation - Google Patents
Pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation Download PDFInfo
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- CN117282180B CN117282180B CN202311162795.1A CN202311162795A CN117282180B CN 117282180 B CN117282180 B CN 117282180B CN 202311162795 A CN202311162795 A CN 202311162795A CN 117282180 B CN117282180 B CN 117282180B
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- 239000000428 dust Substances 0.000 title claims abstract description 75
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- 239000002245 particle Substances 0.000 claims abstract description 55
- 238000012216 screening Methods 0.000 claims abstract description 32
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- 238000001914 filtration Methods 0.000 claims description 6
- 238000007789 sealing Methods 0.000 claims description 6
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- 230000001360 synchronised effect Effects 0.000 claims description 2
- 238000013461 design Methods 0.000 abstract description 13
- 238000005299 abrasion Methods 0.000 abstract description 9
- 238000007664 blowing Methods 0.000 abstract description 7
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- 239000004744 fabric Substances 0.000 description 48
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- 230000001965 increasing effect Effects 0.000 description 8
- 239000000835 fiber Substances 0.000 description 7
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- 238000004062 sedimentation Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000004088 simulation Methods 0.000 description 5
- 230000009471 action Effects 0.000 description 4
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- 238000004458 analytical method Methods 0.000 description 3
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- 230000009286 beneficial effect Effects 0.000 description 2
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- 239000008187 granular material Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
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- 238000004364 calculation method Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000012938 design process Methods 0.000 description 1
- 238000010410 dusting Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/0039—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with flow guiding by feed or discharge devices
- B01D46/0041—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with flow guiding by feed or discharge devices for feeding
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/42—Auxiliary equipment or operation thereof
- B01D46/48—Removing dust other than cleaning filters, e.g. by using collecting trays
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
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Abstract
The invention provides an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation, and relates to the technical field of dust collectors. The design method breaks through the traditional design thought of uniform airflow distribution, adopts the air inlet kinetic energy dissipation thought to carry out the structural design of the dissipation box, has the advantages of simplicity, reasonability, low production cost and convenient installation and use, and essentially reduces the invalid gas flow in the bag-type dust collector, improves the ash dropping efficiency, reduces the blowing times, and weakens the impact and abrasion of the airflow on the bag, thereby prolonging the service life of the bag. Furthermore, the design of the movable guide plate is innovatively adopted in the air inlet channel, and the position of the guide plate is adjusted according to different air inlet working conditions, so that the flow field optimization of the dust remover is realized. In addition, the primary screening device is designed at the end part of the dissipation box, the characteristic that particles in the high-speed vortex of the dissipation box are inconsistent with the motion trail of the air flow is fully utilized, the collection function of a small part of larger particles is realized, and micro-turbulence is formed to further consume the energy of air intake. Finally, the performance of the bag-type dust collector is improved.
Description
Technical Field
The invention relates to the technical field of dust collectors, in particular to an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation.
Background
At present, most cloth bag dust collectors are designed mainly to realize flow field optimization through air inlet uniform distribution, and the influence of the kinetic energy of dust-containing gas in a box on the flow speed and concentration of the dust-containing gas is not considered from the energy perspective. Dust-containing gas with too high flow speed can cause severe impact on the cloth bag in a local area, so that the service life of the cloth bag is shortened, the reasonable gas movement speed can prolong the service life of the cloth bag, and the frequency of replacing the cloth bag is reduced. The particle sedimentation difficulty that high gas kinetic energy can lead to not only more easily causes the jam of sack, and the large granule and the hard granule in the high concentration dust-laden gas can produce mechanical abrasion to the sack in the long-term in-process of contacting with the sack moreover for the filtration efficiency of sack cleaner reduces, and sack life shortens greatly.
Disclosure of Invention
In view of the above, the present invention provides an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation to solve the above problems.
An intake device of a pulse bag-type dust collector based on intake kinetic energy dissipation, comprising: dissipation case, preliminary screening device and intake duct; the dissipation box is of a cube structure and is provided with a gas inlet, so that the flow direction plane of gas flowing into the dissipation box from the gas inlet is vertical to the flow direction plane of gas flowing out of the dissipation box, and the gas makes high-speed vortex motion in the dissipation box to realize energy dissipation; one end of the dissipation box is connected with a primary screening device, the other end of the dissipation box is connected with an air inlet channel with a wedge-shaped structure, a V-shaped baffle plate group is arranged at the connection area of the dissipation box and the primary screening device, and the primary screening device realizes particle air separation through an impeller and an impeller bin; the dissipation box is communicated with the air inlet, a fixed guide plate and a plurality of movable assemblies are respectively connected in the air inlet, the movable guide plate is installed on the movable assemblies, and the movable assemblies are used for controlling the movable guide plate to move up and down to obtain an optimized flow field of the air inlet.
Compared with the prior art, the invention has the beneficial effects that: the design is reasonable and simple in structure, low in production cost, convenient to install and use, and capable of effectively reducing air intake energy of an air inlet channel, essentially reducing ineffective air flow in the bag-type dust remover, effectively weakening impact and abrasion of air flow to a bag, prolonging service life of the bag, and improving ash dropping efficiency. The dust-containing gas firstly enters the dissipation box through the gas inlet and then enters the air inlet channel until entering the bag-type dust remover. The flow direction of the gas flowing into the dissipation box through the air inlet pipeline is perpendicular to the flow direction of the gas flowing into the air inlet channel through the dissipation box, so that the gas flow is caused to realize high-speed vortex flow in the dissipation box, the air inlet energy consumption is realized, the impact of the gas flow on the cloth bag is reduced, and dust hopper flying of the cloth bag dust collector is avoided. The V-shaped baffle plate group is arranged at the joint of the dissipation box and the primary screening device, part of large particles are not completely changed along with the air flow under the action of centrifugal force, and fall into the primary screening device, so that the dust concentration is reduced, and the primary screening device is a closed space and cannot cause additional influence on a flow field. The rest dust-containing gas flows into the air inlet channel and is gradually and uniformly distributed by the guide plate group. The invention has the advantages of reasonable and simple structure, low production cost and convenient installation and use, reduces the air inlet energy of the air inlet channel, reduces the ineffective air flow in the bag-type dust collector, improves the air inlet uniformity from the air inlet channel to the bag-type dust collector, and can effectively weaken the impact and abrasion of air flow to the bag, thereby prolonging the service life of the bag and improving the ash dropping efficiency. And moreover, the design of the movable guide plates is adopted in the air inlet channel, the optimal positions of the guide plates under the working conditions of different air inlet speeds are calculated through fluid simulation, the movable guide plate group can adjust the height positions according to the requirements of the working conditions of different air inlet speeds, the optimized airflow direction change and distribution are realized in the air inlet channel, the high-speed airflow is prevented from converging, and the air inlet energy consumption is further realized. In addition, the primary screening device is designed at the end part of the dissipation box, the characteristic that particles in the high-speed vortex of the dissipation box are inconsistent with the motion trail of the airflow is fully utilized, the collection function of a small part of larger particles is realized, meanwhile, micro turbulence is formed near the baffle group, the air inlet energy is further consumed, and the utilization of the high-speed vortex-shaped airflow is realized with a simple structure with low cost as much as possible.
Further, the length and the width of the dissipation box are respectively matched with the sizes of the box body and the air inlet channel in the bag-type dust collector, the installation and the operation are convenient, the thickness of the dissipation box accounts for 1/15-1/10 of the total length of the box body, and the thickness of the dissipation box is reasonably designed according to the filtering speed interval of the bag-type dust collector.
Further, the gas inlet of the dissipation box is arranged on the end face of the rear side of the dissipation box and is connected with the gas inlet pipeline at a position which is highly centered; the connection position of the dissipation box and the primary screening device is arranged at the front end of the dissipation box and is opposite to the direction of the gas inlet; the connection position of the dissipation box and the air inlet channel is arranged on the side face of the dissipation box, and the width and the height of the opening are consistent with those of the air inlet channel.
Further, the air inlet is provided with equidistant stiffening beams, the movable guide plates are vertically arranged and are of arc-shaped plate structures, the intrados of the arc-shaped plate structures faces one end, connected with the dissipation box, of the air inlet, and the height of each movable guide plate accounts for 15% -25% of the longitudinal height of the air inlet; each movable guide plate is sequentially distributed at equal intervals from one end, close to the dissipation box, in the air inlet channel to the other end, two ends of the movable guide plate are connected with movable assemblies, and the movable assemblies are fixedly connected with the air inlet channel reinforcing beam.
Further, the fixed guide plate both ends and intake duct fixed connection, fixed guide plate contain flat guide plate and oblique guide plate, and flat guide plate is located intake duct entrance bottom, oblique guide plate and flat guide plate and intake duct both sides fixed connection, oblique guide plate inclination 45, and flat guide plate and oblique guide plate length are close with adjacent movable guide plate length.
Further, the moving assembly comprises a screw, a sleeve, a bearing, a base, a sealing ring, a limit switch and a motor; the two ends of the movable guide plate are respectively connected with a sleeve, a screw rod is penetrated in the sleeve, the screw rod is in threaded connection with the sleeve, and the two ends of the sleeve are respectively provided with a sealing ring; the two ends of the screw rod are respectively and rotatably connected with a base through bearings, the base is connected with a reinforcing beam, and a limit switch is arranged on one side, close to the sleeve, of the base; the motor is connected with the end parts of the screw rods through the coupler, and the motors connected with the two screw rods of the same moving assembly are connected in parallel, so that synchronous movement is realized.
Further, the primary screening device comprises a particle channel and a V-shaped baffle, one end of the particle channel is communicated with the end part of the dissipation box, and the other end of the particle channel is communicated with a particle collecting device at the bottom of the ash bucket of the bag-type dust collector; the V-shaped baffle plate group is arranged in the connection area of the dissipation box and the primary screening device.
Further, the V-shaped baffle group comprises an upper V-shaped baffle group and a lower V-shaped baffle group, the upper V-shaped baffle group is arranged above the lower V-shaped baffle group, and the V-shaped baffles in the upper V-shaped baffle group and the V-shaped baffles in the lower V-shaped baffle group are distributed at equal intervals from top to bottom; the V-shaped baffles in the upper V-shaped baffle group are inclined downward toward one end of the gas inlet, and the V-shaped baffles in the lower V-shaped baffle group are inclined upward toward one end of the gas inlet.
Further, the primary screening device further comprises an impeller bin, an impeller and a driving motor, wherein the impeller bin is arranged on the particle channel, the impeller is fixed in the center of the impeller bin through an impeller shaft, the impeller is driven by the driving motor to intermittently rotate, the impeller bin wraps the impeller, at least 2 impeller blades are ensured to be in contact with the impeller bin, and the independent gas pressure of the upper space and the lower space of the impeller bin is realized; the impeller bin is communicated with the dissipation box and the collecting port at the bottom of the ash bucket through the particle channel, so that particles pass through and gas does not pass through.
Drawings
FIG. 1 is a schematic diagram of an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation provided by an embodiment of the invention;
fig. 2 is a schematic diagram of a combination of a primary screening device and a dissipation tank of an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation according to an embodiment of the invention;
FIG. 3 is a schematic diagram of a movable deflector and a movable assembly of an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation according to an embodiment of the present invention;
FIG. 4 is a schematic view of a V-shaped baffle group of an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation, which is provided by the embodiment of the invention;
FIG. 5 is a schematic diagram of a baffle group and a fixed baffle distribution of an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation according to an embodiment of the present invention;
FIG. 6 is a schematic installation diagram of an air inlet device of a pulse bag-type dust collector based on air inlet kinetic energy dissipation according to an embodiment of the invention;
FIG. 7 is a velocity cloud image of a section of a base model A;
FIG. 8 is a velocity cloud of the C section of the base model;
FIG. 9 is a velocity cloud of a large baffle model A cross-section;
FIG. 10 is a velocity cloud of a large baffle model C section;
FIG. 11 is a velocity cloud of dissipating case model A section;
FIG. 12 is a velocity cloud of dissipating case model C section;
FIG. 13 is a graph showing the comparison of sedimentation ratios of particles of different particle diameters under the conditions of a base model, a large deflector model and a dissipation tank model.
Marked in the figure as: 1. a gas inlet; 2. a dissipation case; 3. an upper V-shaped baffle group; 4. a lower V-shaped baffle group; 5. fixing a guide plate; 6. a movable deflector; 7. a primary screening device; 8. an impeller bin; 9. an air inlet channel; 10. a particle channel; 11. a bag-type dust collector; 12. an impeller; 13. a driving motor; 14. a bearing; 15. a base; 16. a screw; 17. a seal ring; 18. a sleeve; 19. a motor; 20. a limit switch; 21. a stiffening beam; 22. ash bucket collecting bin.
Detailed Description
The present invention will be further described in detail with reference to specific embodiments in order to make the objects, technical solutions and advantages of the present invention more apparent.
As shown in fig. 1 to 6, the air inlet device of the pulse bag-type dust collector based on air inlet kinetic energy dissipation is applicable to the structure of a general vertical bag-type dust collector 11, and consists of a dissipation box 2, a primary screening device 7, an air inlet channel 9 and the like. The dissipation tank 2 is provided with a gas inlet 1, the gas inlet 1 being arranged to introduce a dust-laden gas into the dissipation tank 2. The bottom of the other end of the dissipation box 2 is connected with a primary screening device 7, and the primary screening device 7 is used for collecting large particles which are preliminarily filtered out. The dissipation case 2 is a case body with a cube structure, the height of the high air inlet channel 9 of the dissipation case 2 is consistent, and the width is consistent with the width of the middle case body.
The connection part of the dissipation box 2 and the primary screening device 7 is provided with a V-shaped baffle group, and the V-shaped baffle group is arranged on one side, far away from an air inlet pipeline, of the dissipation box 2. The V-arrangement baffle group comprises an upper V-arrangement baffle group 3 and a lower V-arrangement baffle group 4, the upper V-arrangement baffle group 3 and the lower V-arrangement baffle group 4 are composed of a plurality of baffles, the V-arrangement baffles are rectangular plate structures, and the V-arrangement baffles are connected to the inner wall of the dissipation box 2. In the present embodiment, the upper V-shaped barrier group 3 and the lower V-shaped barrier group 4 are each composed of a plurality of barriers. The upper V-shaped baffle group 3 is arranged above the lower V-shaped baffle group 4, and the V-shaped baffles in the upper V-shaped baffle group 3 and the V-shaped baffles in the lower V-shaped baffle group 4 are all distributed at equal intervals from top to bottom. The V-shaped baffles in the upper V-shaped baffle group 3 are inclined downward toward one end of the air intake duct, and the V-shaped baffles in the lower V-shaped baffle group 4 are inclined upward toward one end of the air intake duct.
The particle channel 10 of the primary screening device 7 is internally provided with an impeller bin 8 with a circular section, the impeller bin 8 is internally provided with an impeller 12, the impeller 12 is driven by a driving motor 13, and in the rotating process, at least 2 blades of the impeller 12 are contacted with the impeller bin 8, so that the space of the particle channel 10 in front of and behind the impeller bin 8 is isolated, and the influence of the pressure field of a dissipation box on the area of the particle collecting device is avoided. The particle channel 10 is communicated with an ash bucket collecting bin 22 at the bottom of the ash bucket, and particles collected by the primary screening device 7 are collected in the collecting bin.
The air inlet channel 9 is connected to the side wall of the dissipation box 2, and the dissipation box 2 is communicated with the air inlet channel 9. The air inlet channel 9 is of a wedge-shaped structure, air is introduced from the side face of the air inlet channel 9, and an opening structure at the bottom face of the air inlet channel 9 is communicated with an ash bucket of the bag-type dust collector 11. The plane of flow of the gas flowing into the dissipation tank 2 from the gas inlet 1 is perpendicular to the plane of flow of the gas flowing into the intake duct 9 from the dissipation tank 2. The air inlet 9 is respectively connected with a movable guide plate 6 and a fixed guide plate 5, and the fixed guide plate 5 is positioned between the movable guide plate 6 and the dissipation box 2. The two ends of the fixed guide plate 5 are respectively connected to the two inner side walls of the air inlet 9, and the fixed guide plate 5 is of an obtuse angle structure. The flat baffle of the fixed baffle 5 is arranged on the bottom surface of the air inlet channel 9, the opening of the fixed baffle 5 faces one end of the dissipation box 2, namely, faces the air inflow direction, and the inclined plate of the fixed baffle 5 is inclined at an angle of 45 degrees.
The movable assembly is provided with a plurality of movable assemblies, and the movable assembly is composed of a bearing 14, a base 15, a screw 16, a sealing ring 17, a sleeve 18, a motor 19, a limit switch 20 and the like, in the embodiment, 5 movable guide plates 6 are arranged in total, the movable guide plates 6 are fixedly connected with the sleeve 18, the sleeve 18 is connected with the screw 16 through threads, and the movable guide plates 6 are limited to have the freedom degree in the axial direction of the screw 16 due to the fact that the movable mechanism is arranged in pairs, and when the screw 16 rotates, the sleeve 18 moves up and down to realize position adjustment. Sealing rings 17 are arranged at two ends of the sleeve 18, bases 15 are arranged at two ends of the screw 16, the screw 16 is connected with the bases 15 through cylindrical inclined bearings 14, and limit switches 20 are arranged in the direction of the bases 15, which is close to the sleeve 18, so that the maximum movable range of the sleeve 18 is limited. The base 15 is fixed to the reinforcing beam 21 and is connected thereto by bolts.
The movable guide plates 6 are arc-shaped plate structures, and the inner cambered surfaces of the arc-shaped plate structures face towards one end of the air inlet channel 9, which is connected with the dissipation box 2, namely, face the air inflow direction. The movable guide plates 6 are vertically arranged, and arc endpoints of the movable guide plates 6 are on the same vertical line.
The dimensions of the movable deflectors 6 are different, the height of the movable deflectors 6 is related to the height of the air inlet 9 in the vertical direction, and in this embodiment, the height of the movable deflectors 6 is 20% of the height of the corresponding positions of the air inlet 9.
When in use, the air inlet device is connected to the bag-type dust collector 11, and the opening at the bottom of the air inlet channel 9 is arranged opposite to the ash bucket of the bag-type dust collector 11. The dust-containing gas is input into the dissipation box 2 through the gas inlet 1, the dust-containing gas in the dissipation box 2 is flushed onto each V-shaped baffle, part of large particles do not completely change the moving direction along with the flow direction of the gas flow under the action of centrifugal force, and the large particles fall into the primary screening device 7, and the primary screening device 7 is in a non-gas flow structure due to the blocking action of the impeller 12, so that the particles can fall into the ash bucket collecting bin 22 along the particle channel 10, and the rest of dust-containing gas flows into the gas inlet channel 9. The fixed guide plate 5 is arranged in the air inlet 9, air flow is guided to flow to the movable guide plate 6, the height position of the movable guide plate 6 can be designed through fluid mechanics virtual simulation or data of monitoring points in the bag-type dust collector 11 according to different air inflow working conditions, and the screw 16 is driven to rotate through the motor 19, so that the height of the movable guide plate 6 is adjusted. The paired motors 19 are connected in parallel and synchronously move, the height position of the guide plate is judged according to the pitch of the screw 16 for setting the pulse number of the motors 19, and the position height of the sleeve 18 is calibrated through the limit switch 20, so that the movable guide plate 6 is ensured to be accurate in position and consistent in horizontal height in the air inlet channel 9. The dust-containing gas is distributed evenly by each movable deflector 6 step by step and then flows into the ash bucket.
The design breaks through the traditional design thought of uniform air flow distribution, adopts the design thought of dissipation of air inlet kinetic energy to carry out the structural design of the dissipation box, maximally realizes reasonable and simple structure, low production cost and convenient installation and use, effectively reduces the air inlet energy of the air inlet channel 9, essentially reduces the ineffective air flow in the bag-type dust collector 11, and can effectively weaken the impact and abrasion of air flow on a bag, thereby prolonging the service life of the bag and improving the ash dropping efficiency. Furthermore, the movable guide plate 6 is adopted in the air inlet channel 9, the position of the guide plate is adjusted according to different air inlet flow working conditions, so that air flow uniform distribution is better realized, and the problem that local high-speed air flow occurs in the ash bucket of the bag-type dust collector 11 to influence the particle sedimentation effect is avoided. Besides, the primary screening device 7 is designed at the end part of the dissipation box, the characteristic that particles in the high-speed vortex of the dissipation box are inconsistent with the motion trail of the airflow is fully utilized, the collection function of a small part of larger particles is realized, meanwhile, micro turbulence is formed near the baffle group, the air inlet energy is further consumed, and the utilization of the high-speed vortex-shaped airflow is realized with a simple structure with low cost as much as possible.
In the aspect of mathematical models
In practical production application, the dust removal effect in the earlier stage can reach the standard, and the dust removal effect is poor after a period of working, which is generally caused by abrasion of a cloth bag or damage of cloth bag fibers, so that most of researches are based on air inlet uniform distribution or improvement of sedimentation efficiency and analysis and improvement of the cloth bag.
Impact of high intake energy on the performance of the impulse type bag-type dust collector 11 equipment. Because the equipment handling capacity is determined, namely, under the condition of determining the gas flow of an inlet and an outlet, the higher air inlet kinetic energy can be reflected as higher local air speed, firstly, the higher air flow speed in the cloth bag area of the middle box body easily causes serious scouring of the cloth bag, so that the abrasion of the cloth bag is aggravated, the cloth bag fibers are damaged, the air leakage phenomenon is easily generated, the filtering performance of the cloth bag is reduced, and the dust collection efficiency is affected; secondly, the high wind speed in the ash bucket area easily causes the difficult ash falling, the ash accumulation in the cloth bag and the generation of secondary dust. When the partial dust deposition of the cloth bag is obvious, the equipment resistance is increased, and the air flow speed of the cloth bag with less dust deposition is high, so that the cloth bag fibers are easily damaged, the filtering performance is affected, and the ineffective blowing times are increased. When the whole volume of the cloth bag is obvious, the blowing frequency is set according to the pressure, so that the equipment blowing times are increased, the more the blowing times are, the faster the cloth bag fibers are damaged, and the dust removal efficiency is reduced; under the condition that the blowing frequency is set according to the time interval, the equipment resistance can be increased, and the larger pressure difference between the inside and the outside of the cloth bag can cause the obvious increase of the energy consumption of the dust removing equipment and damage the cloth bag fibers, so that the service life of the cloth bag is shortened, and the dust removing efficiency is reduced. These conditions all have an impact on the performance index of the dust collector equipment and are directly related to environmental protection, maintenance and energy consumption.
The bag resistance is obviously influenced by the flow rate of filtered gas, and obvious kinetic energy difference exists before and after the gas passes through the bag, namely, although the gas has high gas kinetic energy when reaching the surface of the bag, obvious uneven air flow distribution and characteristics exist, and a large amount of ineffective flow exists, after the gas passes through the bag, the ineffective flow is obviously reduced, and the uniformity of the air flow is obviously improved, so that the gas kinetic energy is greatly consumed when passing through the bag, and the energy consumption process can cause the damage of the bag fiber structure besides heat generation. Similarly, excessive ineffective gas flow at the bottom of the hopper can cause difficulty in settling the particles or secondary dusting of settled particles, also due to unnecessary gas kinetic energy consumption. The outward appearance of these processes is a flow field flow spread, while the inward cause is the higher intake kinetic energy dissipation in unreasonable areas. In the structural design process of the pulse type bag-type dust collector 11, if the intake kinetic energy dissipation can be realized in a reasonable area, the adverse effect caused by the uneven air flow can be fundamentally improved.
The energy dissipation consists mainly of turbulent dissipation and eddy dissipation. In turbulence, turbulent motion results in transfer of energy and viscous dissipation, which means that energy is gradually converted into microscopic frictional heat at various scales of the turbulent structure, due to the irregularities and randomness of the turbulence. Turbulence creates complex vortex structures on different scales that, due to the viscosity of the fluid, gradually reduce the velocity differences inside the vortex, eventually dissipating energy in the form of heat.
Turbulence energy:
wherein: k is turbulence energy, m 2 /s 2 The method comprises the steps of carrying out a first treatment on the surface of the v is the average velocity, m/s; i is the turbulence intensity, m/s.
Turbulence intensity:
wherein: i is turbulence intensity, m/s; re is the Reynolds number.
The Reynolds number calculation formula:
wherein: ρ is density, kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the v is the average velocity, m/s; l is the turbulence scale, m; mu is dynamic viscosity, pa.s; k is turbulence energy, m 2 /s 2 The method comprises the steps of carrying out a first treatment on the surface of the v is the kinematic viscosity, m 2 S; epsilon is the turbulent dissipation ratio.
Kinematic viscosity:
wherein: v is the kinematic viscosity, m 2 S; mu is dynamic viscosity, pa.s; ρ is density, kg/m 3 。
Turbulent energy dissipation is caused by viscous dissipation terms which reduce the pulsating kinetic energy into heat [14] Substituting formula (1), formula (2) and formula (4) into formula (3) can obtain a turbulent dissipation rate formula, as shown in formula (5):
wherein: epsilon is the turbulent dissipation ratio; mu is dynamic viscosity, pa.s; v is the average velocity, m/sThe method comprises the steps of carrying out a first treatment on the surface of the ρ is density, kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the L is the turbulence scale, m.
Turbulent dissipation rate is an important parameter describing the energy conversion in the movement of a fluid and it represents the rate at which the kinetic energy of a unit volume of fluid is converted into internal energy per unit time. From this, an integral of the turbulent energy dissipation rate ε over time and space can be derived as shown in equation (6):
wherein: e (E) 1 Is turbulent energy consumption, J; epsilon is the turbulent dissipation ratio; mu is dynamic viscosity, pa.s; v is the average velocity, m/s; ρ is density, kg/m 3 The method comprises the steps of carrying out a first treatment on the surface of the L is the turbulence scale, m; v is the volume, m 3 The method comprises the steps of carrying out a first treatment on the surface of the t is time, s.
Vortex energy dissipation E 2 The relation over time is shown in formula (7):
wherein: e (E) 2 J is eddy energy dissipation; mu is dynamic viscosity, pa.s; omega is the vorticity of the water-soluble fiber,wherein (1)>Is hamiltonian, < >>Is the velocity vector, m/s; v is the volume, m 3 The method comprises the steps of carrying out a first treatment on the surface of the t is time, s.
The total energy dissipation E of the bag-type dust collector can be obtained by the formula (6) and the formula (7), as shown in the formula (8):
from the above equation (8), it is clear that the amount of energy dissipation has a positive correlation with the turbulence velocity and the vortex velocity, and that the larger the velocity, the larger the spatial scale, and the longer the holding time, the more energy dissipation.
Therefore, a reasonable flow field for the pulse bag-type dust collector has the following characteristics: the occurrence of ineffective gas movement in the ash bucket area and the cloth bag area (the generation cause is that the gas energy is too high) is avoided; the flow velocity of the ash bucket area is low, especially near the bottom of the ash bucket; the cloth bag area has low flow velocity and uniform distribution. Therefore, when the pulse type bag-type dust collector is designed, the flow velocity distribution of dust-containing gas reaching the box body is uniform, and the influence of high-speed air flow on key areas is required. The gas kinetic energy is consumed in the air inlet passage area in a turbulent flow and vortex mode, and excessive influences are not caused on the bottom of the ash bucket and the bottom of the cloth bag, so that the structure of the dissipation box is designed, the gas energy dissipation in the air inlet passage area is maximized, the gas energy values in the bottom of the ash bucket and the area of the cloth bag are correspondingly reduced, and reasonable energy dissipation planning is further achieved.
In the aspect of flow field simulation, flow field characteristics of a basic air inlet channel 9 model, an air inlet uniform distribution model and a dissipation box model are compared and analyzed, and impact of flow fields generated under different air inlet kinetic energy conditions on the bottom area of a cloth bag and difference of gas movement speeds of ash hoppers are evaluated.
As shown in fig. 7, a velocity cloud of the longitudinal interface (section a) of the inlet of the basic model is shown. As shown in fig. 8, a velocity cloud of the transverse interface (C-section) of the base model is shown. Fig. 7 shows that a distinct jet forms near the partition on section a. Fig. 8 shows that in section C, the upper left, upper right and bottom of the hopper all find high velocity zones. Wherein, the left upper corner high-speed area exists in the section C-1, and the highest speed reaches 12m/s; the upper right corner high speed region exists at section C-1 (12 m/s), section C-2 (13 m/s), section C-3 (10 m/s), section C-4 (6.5 m/s), section C-5 (7.7 m/s), the remaining sections being less than 5m/s. The high velocity zone at the bottom of the hopper is present at section C-2 (10 m/s), section C-3 (10 m/s), section C-4 (10 m/s), section C-5 (7.7 m/s), section C-6 (6 m/s). Meanwhile, in the section C-1, a large-area high-speed area exists in the central area of the ash bucket, and the speed is 10-14 m/s. Meanwhile, the right side wall speed of the ash bucket with the cross section C-1, the cross section C-2 and the cross section C-3 reaches about 9 m/s.
As shown in fig. 9, the velocity cloud image of the longitudinal interface (a section) of the air inlet and flow equalizing field model of the large flow guide plate is shown, and as shown in fig. 10, the velocity cloud image of the transverse interface (C section) of the air inlet and flow equalizing field characteristic of the large flow guide plate is shown, so that the inlet jet flow is greatly weakened relative to the basic model. In section C, there are high velocity zones in the upper left and right corners of the hopper and the bottom of the hopper. Wherein, the high-speed area at the upper right corner exists in the section C-1, the highest speed reaches 9m/s, the section C-2 (8.6 m/s), the section C-3 (5.8 m/s), and the rest sections are smaller than 5m/s; the upper left corner high velocity region exists in section C-3, with the highest velocity reaching 16.7m/s, section C-1 (9 m/s), section C-2 (12 m/s), section C-4 (8.6 m/s), and the remaining sections less than 5m/s. The high-speed area at the bottom of the ash bucket is stored at 5m/s.
As shown in fig. 11, a velocity cloud of the longitudinal section (section a) of the air inlet of the dissipative tank model is shown. As shown in fig. 12, a velocity cloud of the transverse cross-section (section C) of the velocity cloud of the dissipative tank model. Under the action of the dissipation box air inlet channel 9, the speed of the main air inlet channel 9 is obviously reduced, and under the action of the guide plate, the inlet airflow is divided into 5 small jet flows, the speed is gradually reduced while the airflow is diffused at the left side wall of the ash bucket, and the impact on the side wall and the bottom of the ash bucket is obviously weakened. In section C, the velocity of all areas of the hopper is lower than 5m/s, but there is still a region of relatively high gas flow, still concentrated in the upper right corner region of the hopper, where section C-1 (4.2 m/s), section C-2 (3.3 m/s), section C-3 (3.8 m/s), section C-4 (3.3 m/s) and the remaining sections are less than 3m/s. Meanwhile, the gas velocity is relatively higher in the central area of a part of the cross section ash bucket, wherein the velocity of the rest cross sections is lower, namely 2-3 m/s, and the cross section C-2 (3-4 m/s), the cross section C-2 (4-5 m/s) and the cross section C-3 (3-4 m/s).
According to the analysis of the velocity cloud image, the A section velocity cloud image shows that the different guide plate structures and the air inlet 9 structure mainly realize the regulation and control of the air inlet 9 and the flow field in the hopper by changing the jet flow state of the inlet pipeline, and the gas flow velocity in the ash bucket area is reduced. The hazard of higher gas flow rates in the ash bucket area is mainly manifested in the following two aspects: on the one hand, the high-speed air flow at the top of the ash bucket area can cause the cloth bag to moveThe abrasion between the cloth bag and the supporting piece is increased, so that the service life of the cloth bag is influenced, the maintenance period of equipment is shortened, or the filtering parameters are reduced through the phenomena of air leakage of the cloth bag and the like; on the other hand, the high-speed airflow at the bottom of the ash bucket can influence the blanking efficiency of pulse ash removal, so that ash removal is difficult or cloth bag resistance is increased. Both aspects have a significant impact on both the performance parameters and the energy saving performance of the device. And w=1/2 mv according to the kinetic energy theorem formula 2 The energy loss is square to the gas flow rate and therefore the gas flow rate in the hopper area needs to be controlled.
According to the C section velocity cloud picture, under different structures of the guide plate and the air inlet channel 9, the gas movement velocity in the ash bucket area is obviously different, and obvious high-speed areas exist at the sections 1, 2 and 3 of the basic model section C velocity cloud picture. The large flow guide plate model disperses air flow through the design of the flow guide plate for the purpose of air inlet uniform distribution, avoids the flow field characteristics of jet flow, forms obvious energy consumption in the early stage, has certain improvement on the flow field characteristics compared with the original model, but still has a higher speed flow field in the bottom area of the cloth bag, and forms obvious impact on the cloth bag. The dissipation case model has the main purpose of energy consumption, the flow field characteristic of the dissipation case model is that the high-speed area in the section C speed cloud chart is obviously reduced, and the highest speed is obviously reduced, which shows that a great amount of turbulence and vortex in the air inlet channel 9 effectively play a role in energy consumption.
Therefore, the design thought of conventional air inlet uniform distribution is used for enhancing the air inlet kinetic energy dissipation in the early stage to a certain extent in the air inlet uniform distribution process, but the kinetic energy consumption is still insufficient, a large amount of ineffective gas flows still exist, and the ineffective gas flows can cause impact on cloth bags and difficult particle blanking. Based on the design thought of the dissipation box, the purpose of the dissipation box is to realize the consumption of air inlet energy through turbulent flow and vortex flow, so that a more stable flow field is obtained, the ineffective flow of gas is fundamentally reduced, and better flow field performance can be obtained.
In the aspect of particle movement, the flow field characteristics of a basic air inlet channel 9 model, an air inlet uniform distribution model and a dissipation box model are compared and analyzed, and the influence difference of flow fields generated under different air inlet kinetic energy conditions on blanking performance is evaluated.
In order to more intuitively understand the influence of the improved structure on the dust accumulation and blanking performance of the cloth bag, discrete phase particle trajectory analysis (DPM) is performed on the basis of fluent fluid simulation, and the number proportion of low-speed particles in the final flow field area is calculated to judge the proportion of the particles falling into the dust hopper. The particle diameter range of 0-100% of the blanking ratio was analyzed for the original equipment model and the dissipative tank model, as shown in fig. 13, the particle diameter of the original model particles blanking to the coal dust particle corresponding to approximately 100% blanking was 150-1200 μm, the particle diameter of the large baffle model starting blanking to the particle corresponding to approximately 100% blanking was 50-800 μm, and the particle diameter of the dissipative tank model starting blanking to the particle corresponding to approximately 100% blanking was 50-400 μm. The method is characterized in that although air inlet uniform distribution is beneficial to blanking, a large amount of gas kinetic energy is inevitably consumed in the ash bucket and cloth bag area if the gas kinetic energy cannot be consumed in the air inlet channel 9, the consumption form of the gas kinetic energy is mainly the ineffective flow of the gas, and the dissipation box model is used for realizing the consumption of the gas energy to a great extent in the dissipation box and air inlet channel 9 area, so that the gas kinetic energy is obviously reduced in the ash bucket and cloth bag area, and the particle sedimentation efficiency is obviously improved.
In terms of experimental testing:
under the condition that the air inflow of the dissipation box model is increased by 20%, the cloth bag differential pressure rising rate which is the same as that of the original model can be obtained, and under the condition that the air inflow of the dissipation box model is reduced by 15%, the cloth bag differential pressure rising rate which is the same as that of the original model can be obtained. That is, it is shown that the adoption of the dissipative tank model can obtain higher gas throughput without increasing the number of spraying and accelerating times and the cloth bag impact friction for the cloth bag dust collector 11 equipment with the same volume.
Therefore, from the angles of mathematical theory, flow field simulation results, particle simulation results and experimental tests, the adopted dissipation box model designed by the thought of turbulence and vortex dissipation of the air inlet energy has lower air kinetic energy in the ash bucket and cloth bag area, so that low cloth bag impact and sedimentation efficiency is obtained, the blowing times and cloth bag abrasion are reduced, and the service life of the cloth bag is prolonged or the air flow is improved under the same condition.
The embodiments of the invention are intended to embrace all such alternatives, modifications and variances which fall within the broad scope of the appended claims. Therefore, any omission, modification, equivalent replacement, improvement, etc. of the present invention should be included in the scope of the present invention.
Claims (7)
1. An intake device of a pulse bag-type dust collector based on intake energy dissipation, comprising: dissipation case, preliminary screening device and intake duct; the method is characterized in that: the dissipation box is of a cube structure and is provided with a gas inlet, so that the flow direction plane of gas flowing into the dissipation box from the gas inlet is vertical to the flow direction plane of gas flowing out of the dissipation box, and the gas makes high-speed vortex motion in the dissipation box to realize energy dissipation; one end of the dissipation box is connected with a primary screening device, the other end of the dissipation box is connected with an air inlet channel with a wedge-shaped structure, a V-shaped baffle plate group is arranged at the connection area of the dissipation box and the primary screening device, and the primary screening device realizes particle air separation through an impeller and an impeller bin; the dissipation box is communicated with the air inlet, a fixed guide plate and a plurality of movable assemblies are respectively connected in the air inlet, the movable guide plate is arranged on the movable assembly, and the movable assembly is used for controlling the movable guide plate to move up and down to obtain an optimized flow field of the air inlet;
the air inlet is provided with equidistant stiffening beams, the movable guide plates are vertically arranged, the movable guide plates are of arc plate structures, the intrados of the arc plate structures faces one end, connected with the dissipation box, of the air inlet, and the height of the movable guide plates accounts for 15% -25% of the longitudinal height of the air inlet; each movable guide plate is sequentially distributed at equal intervals from one end, close to the dissipation box, in the air inlet channel to the other end, two ends of each movable guide plate are connected with movable assemblies, and the movable assemblies are fixedly connected with the air inlet channel reinforcing beam;
the moving assembly comprises a screw, a sleeve, a bearing, a base, a sealing ring, a limit switch and a motor; the two ends of the movable guide plate are respectively connected with a sleeve, a screw rod is penetrated in the sleeve, the screw rod is in threaded connection with the sleeve, and the two ends of the sleeve are respectively provided with a sealing ring; the two ends of the screw rod are respectively and rotatably connected with a base through bearings, the base is connected with a reinforcing beam, and a limit switch is arranged on one side, close to the sleeve, of the base; the motor is connected with the end parts of the screw rods through the coupler, and the motors connected with the two screw rods of the same moving assembly are connected in parallel, so that synchronous movement is realized.
2. The pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation according to claim 1, wherein the length and the width of a dissipation box are respectively matched with the sizes of a box body and an air inlet channel in the bag-type dust collector, the installation and the operation are convenient, the thickness of the dissipation box accounts for 1/15-1/10 of the total length of the box body, and the thickness of the dissipation box is reasonably designed according to the filtering speed interval of the bag-type dust collector.
3. The pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation according to claim 1, wherein a dissipation box air inlet is arranged on the rear end face of the dissipation box and is connected with an air inlet pipeline at a position with a high centering; the connection position of the dissipation box and the primary screening device is arranged at the front end of the dissipation box and is opposite to the direction of the gas inlet; the connection position of the dissipation box and the air inlet channel is arranged on the side face of the dissipation box, and the width and the height of the opening are consistent with those of the air inlet channel.
4. The pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation according to claim 1, wherein two ends of a fixed guide plate are fixedly connected with an air inlet channel, the fixed guide plate comprises a flat guide plate and an inclined guide plate, the flat guide plate is positioned at the bottom of an inlet of the air inlet channel, the inclined guide plate is fixedly connected with the flat guide plate and two sides of the air inlet channel, the inclined guide plate is inclined by 45 degrees, and the lengths of the flat guide plate and the inclined guide plate are close to those of the adjacent movable guide plates.
5. The pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation according to claim 1, wherein the primary screening device comprises a particle channel and a V-shaped baffle, one end of the particle channel is communicated with the end part of the dissipation box, and the other end of the particle channel is communicated with a particle collecting device at the bottom of an ash bucket of the bag-type dust collector; the V-shaped baffle plate group is arranged in the connection area of the dissipation box and the primary screening device.
6. The pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation according to claim 5, wherein the V-shaped baffle group comprises an upper V-shaped baffle group and a lower V-shaped baffle group, the upper V-shaped baffle group is arranged above the lower V-shaped baffle group, and the V-shaped baffles in the upper V-shaped baffle group and the V-shaped baffles in the lower V-shaped baffle group are distributed at equal intervals from top to bottom; the V-shaped baffles in the upper V-shaped baffle group are inclined downward toward one end of the gas inlet, and the V-shaped baffles in the lower V-shaped baffle group are inclined upward toward one end of the gas inlet.
7. The pulse bag-type dust collector air inlet device based on air inlet kinetic energy dissipation according to claim 5, wherein the primary screening device further comprises an impeller bin, an impeller and a driving motor, the impeller bin is arranged on the particle channel, the impeller is fixed in the center of the impeller bin through an impeller shaft and is driven by the driving motor to intermittently rotate, the impeller bin wraps the impeller, at least 2 impeller blades are ensured to be in contact with the impeller bin at the same time, and the gas pressure of the upper space and the lower space of the impeller bin are independent; the impeller bin is communicated with the dissipation box and the collecting port at the bottom of the ash bucket through the particle channel, so that particles pass through and gas does not pass through.
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| CN116502360A (en) * | 2023-04-27 | 2023-07-28 | 宝武水务科技有限公司 | Optimization method for flow guiding structure of bag type dust collector |
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| CN101648094A (en) * | 2009-08-25 | 2010-02-17 | 洁华控股股份有限公司 | Double-inlet turbulence mixing type bag dust remover and dust removing method thereof |
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