CN211611952U - Rectifying device for improving physical agglomeration effect - Google Patents
Rectifying device for improving physical agglomeration effect Download PDFInfo
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- CN211611952U CN211611952U CN201922249865.2U CN201922249865U CN211611952U CN 211611952 U CN211611952 U CN 211611952U CN 201922249865 U CN201922249865 U CN 201922249865U CN 211611952 U CN211611952 U CN 211611952U
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Abstract
The utility model relates to a fairing for improving physics reunion effect belongs to flue gas rectification technical field. The rectifying device is arranged between the coalescence device and the dust removing equipment to improve the physical agglomeration effect of the flue gas; the vortex breaking device comprises a vortex breaking section and a flow stabilizing section which are connected in sequence, wherein the interior of the vortex breaking section is divided into a plurality of vortex breaking chambers with the same cross section shape, the cross sections of any one vortex breaking chamber are the same in shape and size, and balance holes are distributed between adjacent vortex breaking chambers; the shape and the size of the cross section of any position of the steady flow section are the same, and the shape and the size of the cross section of any position of the steady flow section are the same as those of the cross section of any position of the crushed vortex section; at least one layer of flow stabilizing net is arranged in the flow stabilizing section. The utility model discloses a combined action of garrulous whirlpool section and stationary flow section has reduced the turbulence degree and the vortex intensity of upper reaches flue gas, has guaranteed that physics reunites the effect of gathering of device to all have positive effects to improving dust collecting equipment efficiency, extension dust collecting equipment life and reduction running resistance.
Description
Technical Field
The utility model belongs to flue gas rectification field, more specifically relates to a fairing for improving physics reunion effect.
Background
At present, dust removing equipment of industrial facilities such as coal-fired power plants and the like mainly comprises an electrostatic dust collector and a bag type dust collector, but due to the existence of a penetration window, the two types of equipment are difficult to effectively capture ultrafine particles with the particle size range of 0.1-1 mu m for a long time, and the efficiency of the dust removing equipment is low. Along with the improvement of national flue gas emission standards, the requirements on the dust removal efficiency of various dust removers are getting tighter and tighter.
A physical agglomeration device (also called a coalescer) is additionally arranged in front of the dust removing equipment, so that ultrafine particles can be agglomerated and grown up, the ultrafine particles are easy to be trapped by the subsequent dust removing equipment, and the method is a reliable and effective method for solving the problem that the ultrafine particles are difficult to be trapped and adsorbed. The technology shows a development trend at present, and the mode does not need to carry out a large amount of modification on the existing dust removal equipment of a power plant, and has strong operability.
The blade that has special shape in the ware that gathers, dusty flue gas can produce the torrent outdated, and the interact can take place for the granule, and superfine granule will collide with the large granule, realizes that the granule increases on the large granule surface, and then avoids follow-up dust remover escape window, improves the efficiency of dust remover. Because the particle growth of the coalescence device is realized by turbulent vortex, the outlet flue gas still has certain turbulence, and the outlet flue gas is free to flow to easily generate vortex. However, the pipeline after the outlet is not provided with special blades, the turbulence vortex does not meet the agglomeration requirement, large particles which are already well agglomerated in the agglomerator can be dispersed into small particles, the effect of the agglomerator is reduced, and the efficiency of the dust remover is not improved favorably.
At present, the coalescer is not widely applied, so that the research on the solution of the problem that outlet smoke contains a large amount of vortexes is less. At present, a long empty pipeline is generally left behind the coalescence device, and the smoke is allowed to flow freely to dissipate vortex energy, but the method has limited vortex breaking effect, cannot reduce the turbulence to a specified value within a limited length, and cannot maintain the coalescence effect of the coalescence device.
SUMMERY OF THE UTILITY MODEL
The utility model provides an among the prior art gather the flue gas of ware export and can not realize fine garrulous whirlpool, can't reduce the turbulence scale in limited length, can not maintain the technical problem of gathering and effect of gathering of ware. The utility model provides a rectifying device for improving the effect of a coalescence device, which is correspondingly provided with a crushed vortex section and a steady flow section, wherein balance holes are distributed between adjacent crushed vortex chambers and are used for pressure exchange between the crushed vortex chambers and vortex energy transmission between the crushed vortex chambers; the utility model discloses can realize garrulous whirlpool betterly, reduce the turbulence scale, maintain the coalescence effect of coalescence ware, can effectively solve the great problem of rectification process pressure drop, be applicable to dust collecting equipment especially suitable for thermal power generating unit.
According to the purpose of the utility model, a rectifying device for improving the physical agglomeration effect is provided, which is arranged between the agglomeration device and the dust removing equipment to improve the physical agglomeration effect of the flue gas; the rectifying device comprises a vortex breaking section and a flow stabilizing section which are sequentially connected, wherein the vortex breaking section is internally divided into a plurality of vortex breaking chambers with the same cross section shape, and the vortex breaking chambers are used for subdividing the upstream flue gas into a plurality of strands, so that the flue gas is guided straight and the attenuation of vortices in the flue gas is accelerated; the cross sections of any one vortex breaking chamber are the same in shape and size; balance holes are distributed between adjacent vortex breaking chambers and are used for pressure exchange between the vortex breaking chambers and vortex energy transfer between the vortex breaking chambers; the shape and the size of the cross section of any position of the flow stabilizing section are the same, and the shape and the size of the cross section of any position of the flow stabilizing section are the same as those of the cross section of any position of the whole crushed vortex section; and at least one layer of current stabilizing net is arranged in the current stabilizing section and used for improving the rectification effect.
Preferably, the shape of the cross section of the vortex breaking chamber is square, round or regular hexagon.
Preferably, the cross-sectional area of the vortex breaking chamber close to the center in the vortex breaking section is larger than that of the vortex breaking chambers at the periphery.
Preferably, the length of the vortex breaking section is 5-10 times of the section diameter or equivalent diameter of the vortex breaking chamber with the smallest cross section area.
Preferably, the length of the steady flow section is 3-5 times that of the length of the vortex breaker.
Preferably, the whole cross-sectional area of the vortex breaking section is 30-50 times of the cross-sectional area of the vortex breaking chamber with the smallest cross-sectional area.
Preferably, the spacing of the balance holes is 2 to 4 times of the cross-sectional diameter or equivalent diameter of the vortex breaking chamber with the smallest cross-sectional area.
Preferably, the open porosity of the flow-stabilizing net is in the range of 0.5-0.6.
Preferably, the flow stabilizing nets are 3 layers which are sequentially arranged, wherein the distance between the flow stabilizing net closest to the vortex breaking section and the outlet of the vortex breaking section is 2-4 times of the length of the vortex breaking section, and the distance between the next layer of flow stabilizing net behind and the previous layer of flow stabilizing net is 1-2 times of the length of the vortex breaking section.
Generally, through the utility model above technical scheme who thinks compares with prior art, mainly possesses following technical advantage:
(1) the utility model discloses a combined action of garrulous whirlpool section and stationary flow section can reduce the turbulence degree and the vortex intensity of upper reaches flue gas, makes the flue gas flow more stable to reduce the offend to the pipe wall, can guarantee that the granule of having gathered together can not be because of reasons such as collision, entrainment broken, guaranteed gathering and effect of gathering and the ware, all have positive effect to dust collecting equipment raising efficiency, reduction resistance, increase of service life.
(2) If the flue gas distributes unevenly, unstable states such as serious torrent, swirl can appear, not only reduces dust collecting equipment's efficiency, still can erode the sack and reduce life, increases the running resistance simultaneously, makes the draught fan exert oneself the increase. The utility model discloses the flue gas speed, the concentration of export are more even, consequently all have positive effect to improving dust collecting equipment efficiency, extension dust collecting equipment life, reduction running resistance.
(3) The inside of the vortex breaking section is preferably formed by a plurality of square, round or regular hexagonal small pipelines with equal cross sections in parallel, namely a vortex breaking chamber, and the vortex breaking chamber is mainly used for guiding flue gas to be parallel to the axis of the pipeline, dividing large-scale vortex of the flue gas into small vortices and accelerating the attenuation of the vortices. Meanwhile, the equivalent diameter of the vortex breaking chamber is small, so that the speed difference on the same section is not large, and the speed distribution of the flue gas at the outlet of the vortex breaking section is favorably improved. The balance holes in a certain number are formed in the side wall of the broken vortex chamber, so that internal pressure exchange and vortex energy transmission are facilitated, and airflow at an outlet of the broken vortex section is more uniform, so that the rectification effect of the broken vortex section is enhanced. Because the speed of the part of the vortex breaking section near the wall surface of the flue gas is low, and the speed of the middle part of the vortex breaking section is high, the cross sectional area of the vortex breaking chamber close to the center in the vortex breaking section is larger than that of the vortex breaking chambers at the periphery.
(4) The utility model discloses well stationary flow section is that one section cross-sectional area is unchangeable, has certain length's pipeline simultaneously, and its inside has arranged to open has the net of many fine and close apertures, is called the stationary flow net, and the primary action makes the speed and the direction distribution that come from garrulous vortex room flue gas more even, further reduces torrent and vortex intensity in the flue gas, finally obtains the flue gas that turbulence degree and vortex intensity meet the requirements, guarantees to gather and the good effect of gathering of ware.
(5) The utility model discloses preferably, the stationary flow segment length is 3 ~ 5 times of garrulous vortex segment length, and specific length is confirmed by the number of piles, the interval of stationary flow net, and at this within range, can guarantee to have sufficient distance to arrange the stationary flow net, makes the flue gas speed and the direction distribution that come from garrulous whirlpool room more even, is unlikely to stationary flow segment overlength again, increases along journey resistance, makes the draught fan exert oneself and increases too much.
(6) The utility model discloses preferably, garrulous whirlpool section cross-sectional area is 30 ~ 50 times of the cross-sectional area of garrulous whirlpool room, and in this within range, can guarantee that garrulous whirlpool room quantity is enough, ensures garrulous whirlpool section to the garrulous whirlpool effect of the flue gas of reunion device export for the decay of swirl is unlikely to again garrulous whirlpool room quantity too much, increases the on-way resistance, makes the draught fan exert oneself and increases too much.
(7) The utility model discloses preferably, the interval of balance hole is garrulous whirlpool room cross-section equivalent diameter 2 ~ 4 times, and at this within range, can guarantee to set up the balance hole of a certain amount, the transmission of pressure exchange and vortex energy between the garrulous whirlpool room of being convenient for is unlikely to the trompil again too much, makes the air current mutual interference between the garrulous whirlpool room.
(8) The utility model discloses preferably, the scope of the percent opening of steady flow net is 0.5-0.6, and in this within range, can guarantee steady flow net to come from the rectification effect of garrulous whirlpool room flue gas, make speed and direction distribution more even, be unlikely to the degree of blockage again too big, the air current after the steady flow net is unstable, increases the resistance simultaneously and makes the draught fan output increase too much.
(9) The utility model discloses preferably, the stationary flow net can arrange 1-3 layers, arranges the multilayer when stationary flow section space is sufficient, arranges the individual layer when the space is insufficient. The distance between the steady flow net closest to the broken vortex section and the outlet of the broken vortex section is 2-4 times of the length of the broken vortex section, the distance between the next layer of steady flow net behind and the previous layer of steady flow net is 1-2 times of the length of the broken vortex section, and in the range, the weak turbulence of the smoke at the outlet of the broken vortex section and the previous layer of steady flow net can be fully attenuated, so that a better low turbulence effect can be obtained through the current layer of steady flow net, the length of the steady flow section is not too long, the on-way resistance is increased, and the output of the induced draft fan is increased too much.
Drawings
FIG. 1 is a schematic structural diagram of a rectifying device constructed in example 1 for improving physical agglomeration effect;
FIG. 2 is a schematic structural view of a vortex breaker constructed in example 1;
FIG. 3 is an internal schematic view of a vortex breaker section constructed in example 1;
FIG. 4 is a schematic structural view of a steady flow stage constructed in example 1;
FIG. 5 is a schematic structural view of a vortex breaker constructed in example 2;
FIG. 6 is a schematic structural view of a steady flow stage constructed in example 2;
FIG. 7 is a schematic structural view of a vortex breaker constructed in example 3;
FIG. 8 is a schematic structural view of a steady flow segment constructed in example 3;
FIG. 9 is a schematic diagram of the operation of the fairing provided in FIG. 1;
the same reference numbers will be used throughout the drawings to refer to the same or like elements or structures, wherein: 1-a crushing vortex section, 2-a steady flow section, 3-a crushing vortex chamber, 4-a balance hole and 5-a steady flow net.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. Furthermore, the technical features mentioned in the embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.
Example 1
FIG. 1 is a schematic view of a rectifying device for improving physical agglomeration effect in this embodiment; FIG. 2 is a schematic structural view of the vortex breaker section in the present embodiment; FIG. 3 is an internal schematic view of the vortex breaker section of the present embodiment; fig. 4 is a schematic structural diagram of the middle steady flow section of the present invention. The embodiment of the utility model provides a fairing for improving the physical agglomeration effect, which is arranged between an agglomeration device and a dust removal device to improve the physical agglomeration effect of flue gas; the rectifying device comprises a vortex breaking section 1 and a flow stabilizing section 2 which are sequentially connected, wherein the vortex breaking section 1 is internally divided into a plurality of vortex breaking chambers 3 with the same cross section shape, and the vortex breaking chambers 3 are used for subdividing upstream flue gas into a plurality of strands, so that the flue gas is guided straight and the attenuation of vortices in the flue gas is accelerated; the cross sections of all parts in any vortex breaking chamber 3 are the same in shape and size; balance holes 4 are distributed between adjacent vortex breaking chambers 3, and the balance holes 4 are used for pressure exchange between the vortex breaking chambers 3 and vortex energy transfer between the vortex breaking chambers 3; the shape and the size of the cross section of any position of the flow stabilizing section 2 are the same, and the shape and the size of the cross section of any position of the flow stabilizing section 2 are the same as those of the cross section of any position of the vortex crushing section 1; at least one layer of current stabilizing net 5 is arranged in the current stabilizing section 2, and the current stabilizing net 5 is used for improving the rectification effect.
In this embodiment, the vortex chamber 3 is square in shape. The equivalent diameter of the section of the vortex breaking chamber 3 is 100mm, and the calculation method comprises the following steps: d is 4A/L, wherein A is the cross-sectional area (10000 mm)2) And L (400mm) is the cross-sectional perimeter.
The length of the vortex breaking section 1 is 5 times of the cross-section equivalent diameter of the vortex breaking chamber 3.
The length of the steady flow section 2 is 4 times of that of the vortex breaking section 1.
The sectional area of the vortex breaking section 1 is 36 times of that of the vortex breaking chamber 3.
The spacing of the balance holes 4 is 2 times of the equivalent diameter of the section of the vortex breaking chamber 3.
The open pore ratio of the flow stabilizing net 5 is in the range of 0.5.
The number of the flow stabilizing nets 5 is 3, wherein the distance between the flow stabilizing net 5 closest to the crushed vortex section 1 and the outlet of the crushed vortex section 1 is 2 times of the length of the crushed vortex section 1, and the distance between the next layer of flow stabilizing net 5 and the previous layer of flow stabilizing net 5 is 1 time of the length of the crushed vortex section 1.
The inside of the vortex breaking section 1 is divided into a plurality of vortex breaking chambers 3 with the same cross section shape, smoke can be guided straight to be parallel to the axis of the pipeline, large-scale vortex of the smoke is divided into small vortices, and attenuation of the vortices is accelerated. And balance holes 4 are distributed between the adjacent vortex breaking chambers 3, so that internal pressure exchange and vortex energy transfer are facilitated, and airflow at an outlet of the vortex breaking section is more uniform, thereby enhancing the rectification effect of the vortex breaking section.
The steady flow section 2 is internally provided with a steady flow net 5 provided with a plurality of fine small holes, which mainly has the functions of making the speed and direction distribution of the flue gas from the vortex breaking chamber 3 more uniform, further reducing the turbulence and the vortex intensity in the flue gas, finally obtaining the flue gas with the turbulence degree and the vortex intensity meeting the requirements, and maintaining the coalescence effect of the upstream coalescence device.
Example 2
FIG. 5 is a schematic structural diagram of a vortex breaker constructed according to the present embodiment; fig. 6 is a schematic structural diagram of the steady flow section constructed in the embodiment. The embodiment of the utility model provides a fairing for improving the physical agglomeration effect, which is arranged between an agglomeration device and a dust removal device to improve the physical agglomeration effect of flue gas; the rectifying device comprises a vortex breaking section 1 and a flow stabilizing section 2 which are sequentially connected, wherein the vortex breaking section 1 is internally divided into a plurality of vortex breaking chambers 3 with the same cross section shape, and the vortex breaking chambers 3 are used for subdividing upstream flue gas into a plurality of strands, so that the flue gas is guided straight and the attenuation of vortices in the flue gas is accelerated; the cross sections of all parts in any vortex breaking chamber 3 are the same in shape and size; balance holes 4 are distributed between adjacent vortex breaking chambers 3, and the balance holes 4 are used for pressure exchange between the vortex breaking chambers 3 and vortex energy transfer between the vortex breaking chambers 3; the shape and the size of the cross section of any position of the flow stabilizing section 2 are the same, and the shape and the size of the cross section of any position of the flow stabilizing section 2 are the same as those of the cross section of any position of the vortex crushing section 1; at least one layer of current stabilizing net 5 is arranged in the current stabilizing section 2, and the current stabilizing net 5 is used for improving the rectification effect.
In this embodiment, the vortex chamber 3 is circular and has the same size. The vortex chamber 3 has a cross-sectional diameter of 100 mm.
The length of the vortex breaking section 1 is 10 times of the cross-section equivalent diameter of the vortex breaking chamber 3.
The length of the steady flow section 2 is 5 times of that of the vortex breaking section 1.
The cross-sectional area of the vortex breaking section 1 is 50 times of that of the vortex breaking chamber 3.
The spacing of the balance holes 4 is 4 times of the equivalent diameter of the section of the vortex breaking chamber 3.
The open pore ratio of the flow stabilizing net 5 is in the range of 0.6.
The number of the flow stabilizing nets 5 is 3, wherein the distance between the flow stabilizing net 5 closest to the crushed vortex section 1 and the outlet of the crushed vortex section 1 is 2 times of the length of the crushed vortex section 1, and the distance between the next layer of flow stabilizing net 5 and the previous layer of flow stabilizing net 5 is 1.5 times of the length of the crushed vortex section 1.
Example 3
FIG. 7 is a schematic structural diagram of a vortex breaker constructed according to the present embodiment; fig. 8 is a schematic structural diagram of the steady flow section constructed in the present embodiment. The embodiment of the utility model provides a fairing for improving the physical agglomeration effect, which is arranged between an agglomeration device and a dust removal device to improve the physical agglomeration effect of flue gas; the rectifying device comprises a vortex breaking section 1 and a flow stabilizing section 2 which are sequentially connected, wherein the vortex breaking section 1 is internally divided into a plurality of vortex breaking chambers 3 with the same cross section shape, and the vortex breaking chambers 3 are used for subdividing upstream flue gas into a plurality of strands, so that the flue gas is guided straight and the attenuation of vortices in the flue gas is accelerated; the cross sections of all parts in any vortex breaking chamber 3 are the same in shape and size; balance holes 4 are distributed between adjacent vortex breaking chambers 3, and the balance holes 4 are used for pressure exchange between the vortex breaking chambers 3 and vortex energy transfer between the vortex breaking chambers 3; the shape and the size of the cross section of any position of the flow stabilizing section 2 are the same, and the shape and the size of the cross section of any position of the flow stabilizing section 2 are the same as those of the cross section of any position of the vortex crushing section 1; at least one layer of current stabilizing net 5 is arranged in the current stabilizing section 2, and the current stabilizing net 5 is used for improving the rectification effect.
In this embodiment, the vortex breaking chambers 3 are regular hexagons and have the same size. The equivalent diameter of the section of the vortex breaking chamber 3 is 173mm, and the calculation method is as follows: d is 4A/L, wherein A is the cross-sectional area (25981 mm)2) And L (600mm) is the cross-sectional perimeter.
The length of the vortex breaking section 1 is 8 times of the cross-section equivalent diameter of the vortex breaking chamber 3.
The length of the steady flow section 2 is 4 times of that of the vortex breaking section 1.
The cross-sectional area of the vortex breaking section 1 is 40 times of that of the vortex breaking chamber 3.
The spacing of the balance holes 4 is 3 times of the equivalent diameter of the section of the vortex breaking chamber 3.
The open pore ratio of the flow stabilizing net 5 is in the range of 0.55.
The number of the flow stabilizing nets 5 is 3, wherein the distance between the flow stabilizing net 5 closest to the crushed vortex section 1 and the outlet of the crushed vortex section 1 is 2 times of the length of the crushed vortex section 1, and the distance between the next layer of flow stabilizing net 5 and the previous layer of flow stabilizing net 5 is 1 time of the length of the crushed vortex section 1.
Example 4
As shown in FIG. 9, when the rectifying device is in operation, the flue gas from the outlet of the agglomeration device at the upstream flows into the vortex breaking section 1, at this time, the direction and the magnitude of the flue gas velocity are not consistent, and the agglomeration device agglomerates and particles by means of turbulent vortex, and the outlet airflow inevitably contains vortex. After the flue gas is shunted to each vortex breaking chamber 3, the big vortex is directly broken, and the small vortex disappears along with the dissipation of energy in the flow. The balance holes 4 arranged between the adjacent vortex breaking chambers 3 can enable the interior of the vortex breaking section 1 to carry out pressure exchange and vortex energy transfer, so that the airflow at the outlet of the vortex breaking section 1 is more uniform. The direction of the airflow at the outlet of the vortex breaker 1 is substantially parallel to the axis of the pipeline. The smoke continuously flows into the steady flow section 2, the speed and the direction of the smoke are distributed more uniformly under the action of the fine and small holes in the steady flow net 5, the turbulence and the vortex intensity in the smoke are further reduced, the smoke with the turbulence degree and the vortex intensity meeting the requirements is finally obtained, and the coalescence effect of the coalescence device is maintained.
When not installing fairing additional, the coalescence ware only has 20% -30% to the efficiency promotion of dust collecting equipment desorption superfine particle, and install fairing additional after, can reach 50% -60% to the efficiency promotion of dust collecting equipment desorption superfine particle, this because fairing makes the flue gas flow more stable to reduce the clash to the pipe wall, can guarantee that the granule of coalescence can not be because of reasons such as collision, entrainment broken, guaranteed the coalescence effect of coalescence ware.
It will be understood by those skilled in the art that the foregoing is merely a preferred embodiment of the present invention, and is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. The rectifying device is used for being arranged between the coalescence device and the dust removing equipment so as to improve the physical agglomeration effect of the flue gas; the rectifying device comprises a vortex breaking section (1) and a flow stabilizing section (2) which are sequentially connected, wherein the interior of the vortex breaking section (1) is divided into a plurality of vortex breaking chambers (3) with the same cross section shape, and the vortex breaking chambers (3) are used for subdividing upstream flue gas into a plurality of strands, so that the flue gas is guided straight and the attenuation of vortices in the flue gas is accelerated; the cross sections of all parts in any vortex breaking chamber (3) are the same in shape and size; balance holes (4) are distributed between the adjacent vortex breaking chambers (3), and the balance holes (4) are used for pressure exchange between the vortex breaking chambers (3) and vortex energy transfer between the vortex breaking chambers (3); the shape and the size of the cross section of any position of the flow stabilizing section (2) are the same, and the shape and the size of the cross section of any position of the flow stabilizing section (2) are the same as those of the cross section of any position of the whole vortex breaking section (1); at least one layer of current stabilizing net (5) is arranged in the current stabilizing section (2), and the current stabilizing net (5) is used for improving the rectification effect.
2. The fairing for promoting physical agglomeration as recited in claim 1 wherein said vortex chamber (3) has a cross-sectional shape of a square, circle or regular hexagon.
3. A fairing for enhancing the physical agglomeration according to claim 1, wherein the vortex breaker (1) has a vortex breaker chamber (3) with a cross-sectional area closer to the centre than the vortex breaker chambers (3) at the periphery.
4. The fairing for improving physical agglomeration as claimed in claim 1 wherein the length of the vortex breaker section (1) is 5 to 10 times the cross-sectional diameter or equivalent diameter of the vortex breaker chamber (3) of minimum cross-sectional area.
5. The fairing for improving physical agglomeration as recited in claim 1, wherein said flow stabilizer (2) has a length 3 to 5 times the length of the vortex breaker (1).
6. A fairing for improving physical agglomeration as claimed in claim 1, wherein the overall cross-sectional area of the vortex breaker section (1) is 30 to 50 times the cross-sectional area of the vortex breaker chamber (3) of the smallest cross-sectional area.
7. A fairing for improving physical agglomeration as claimed in claim 1, wherein the spacing of said balance holes (4) is 2 to 4 times the cross-sectional or equivalent diameter of the vortex breaker chamber (3) of the smallest cross-sectional area.
8. The fairing device for enhancing physical agglomeration as recited in claim 1, wherein said open porosity of said flow-stabilizing network (5) is in the range of 0.5-0.6.
9. The rectifying device for improving the physical agglomeration effect as claimed in claim 1, wherein the flow stabilizing net (5) is 3 layers arranged in sequence, wherein the distance between the flow stabilizing net (5) closest to the crushed vortex section (1) and the outlet of the crushed vortex section (1) is 2-4 times of the length of the crushed vortex section (1), and the distance between the flow stabilizing net (5) at the next layer and the previous layer is 1-2 times of the length of the crushed vortex section (1).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922249865.2U CN211611952U (en) | 2019-12-16 | 2019-12-16 | Rectifying device for improving physical agglomeration effect |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110841378A (en) * | 2019-12-16 | 2020-02-28 | 华中科技大学 | Rectifying device for improving physical agglomeration effect |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110841378A (en) * | 2019-12-16 | 2020-02-28 | 华中科技大学 | Rectifying device for improving physical agglomeration effect |
| CN110841378B (en) * | 2019-12-16 | 2023-07-04 | 华中科技大学 | Rectifying device for improving physical agglomeration effect |
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Granted publication date: 20201002 Effective date of abandoning: 20230704 |