CN112267002A - Flue gas micron-level particle separation device - Google Patents
Flue gas micron-level particle separation device Download PDFInfo
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- CN112267002A CN112267002A CN202011266084.5A CN202011266084A CN112267002A CN 112267002 A CN112267002 A CN 112267002A CN 202011266084 A CN202011266084 A CN 202011266084A CN 112267002 A CN112267002 A CN 112267002A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 239000003546 flue gas Substances 0.000 title claims abstract description 114
- 239000002245 particle Substances 0.000 title claims abstract description 114
- 238000000926 separation method Methods 0.000 title claims abstract description 41
- 238000004062 sedimentation Methods 0.000 claims description 15
- 239000000428 dust Substances 0.000 abstract description 27
- 239000000779 smoke Substances 0.000 abstract description 15
- 230000005484 gravity Effects 0.000 abstract description 14
- 230000009471 action Effects 0.000 abstract description 6
- 239000007787 solid Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 238000004880 explosion Methods 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 239000002918 waste heat Substances 0.000 description 5
- 230000000712 assembly Effects 0.000 description 4
- 238000000429 assembly Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000008187 granular material Substances 0.000 description 3
- 238000009628 steelmaking Methods 0.000 description 3
- 241000234295 Musa Species 0.000 description 2
- 235000018290 Musa x paradisiaca Nutrition 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 239000011362 coarse particle Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000001535 kindling effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
- C21C5/28—Manufacture of steel in the converter
- C21C5/38—Removal of waste gases or dust
- C21C5/40—Offtakes or separating apparatus for converter waste gases or dust
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- Environmental & Geological Engineering (AREA)
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- Organic Chemistry (AREA)
- Separating Particles In Gases By Inertia (AREA)
Abstract
The invention provides a flue gas micron-level particle separation device which is arranged in a settling zone of a flue and comprises at least one set of settling components, wherein each settling component comprises at least two layers of inclined plates which are parallel and arranged at intervals, the inclined plates are obliquely arranged towards the top wall of the flue along the flow direction of flue gas, and the included angle between each inclined plate and the top wall of the flue is 5-70 degrees. The flue gas particle separation device can settle the micron-level particle smoke dust in the flue gas by utilizing the gravity action so as to achieve the aim of separating particles in the flue gas.
Description
Technical Field
The invention relates to the technical field of steel making, in particular to a flue gas micron-level particle separation device.
Background
With the gradual enhancement of energy-saving and environment-friendly consciousness, the research on the full waste heat recovery of the converter flue gas and the search of a real dry dedusting process become the attention points of a plurality of steel plants. An important link influencing the development of the converter full-dry method waste heat recovery process is how to solve the explosion-proof problem of the converter flue gas in the process. Three factors causing the explosion of the converter gas are CO concentration of 12.5-75%, temperature below 610 ℃ and fire species with enough energy respectively. To prevent the occurrence of an explosion, it is necessary to consider from these three requirements, and if one of the requirements is restricted, the occurrence of an explosion is restricted.
Converter steelmaking is an intermittent production mode. In the normal smelting production stage of the converter, the flue gas temperature is high, the flue gas volume is large, the dust content is large, the flue gas flow velocity in the pipeline is high, and the CO content is high; in order to prevent the smoke from being exploded due to the ignition of the carried large-particle high-temperature kindling, the separation of large high-temperature particles, especially large particles with a particle size not smaller than 50 μm, needs to be completed before the waste heat recovery, so as to ensure that no explosion occurs in the whole waste heat recovery stage. In the preparation activity stage of the converter, the flue gas temperature is reduced, the flue gas volume is small, the dust content is also reduced, the flue gas flow velocity of the pipeline is small, the CO content is between the upper and lower explosion limit concentration range, if large particle seeds with enough energy exist at the same time, explosion is likely to be caused, and therefore the capture of the large particles in the stage is also important.
The separation and trapping technology of the large particles with the size of a Chinese meter contained in the flue gas is various at present, and mainly comprises wet or semidry separation, cyclone separation, cloth bag separation and the like, and the large particles are separated from the flue gas by utilizing gravity, centrifugal force, inertia force and resistance. The wet or semi-dry separation technique needs additional water consumption and dust particles (the main component is Fe)2O3) The physical and chemical properties are changed under the condition of high temperature and water existence, and the secondary utilization of dust is influenced; vortex flow is easily generated by the flue gas of the cyclone separation technology; the cloth bag separation technique has large pressure loss and is not suitable for high-temperature flue gas. Therefore, it is necessary to develop a method which is efficient, simple and convenient and canThe method is suitable for the dry method neglected-meter large particle trapping technology of high, medium and low temperature, high, medium and low flow rate intermittent conversion.
The Chinese patent with the publication number of CN1148264C discloses a gas-solid cyclone separation method and a device thereof, which can reduce the abrasion, and comprises the following steps: 1. the flue gas with certain flow velocity and carrying smoke dust enters the cylinder of the cyclone separator along the tangential direction through the horizontal flue gas inlet section of the gas-solid separator, and particles carried by the flue gas are thrown to the wall surface at high speed under the action of centrifugal force and inertia force; 2. large particles in the flue gas are gradually gathered towards the opposite side of the inlet in the cylinder to form a dense phase region of the large particles, the large particles in the dense phase region enter a spiral downward coarse particle spiral discharging pipe connected with the outer wall of the cylinder along an opening on the wall surface of the cylinder in the range of the dense phase region, and are directly discharged through a material returning leg of the cyclone separator; 3. the purified flue gas is discharged through the central cylinder of the cyclone separator.
According to the cyclone separation technology, due to the uncertain rotating airflow path, the back-and-forth airflow at the gas-solid separation interface and other factors, the airflow in the cyclone dust collector cannot realize the form of plug flow, the phenomena of vortex and the like can exist, the back-mixing carrying phenomenon of a small amount of large particles can possibly exist, and the hidden danger of explosion of converter smoke is caused.
Chinese patent application publication No. CN10949921A discloses a moving bed granular layer filter, which comprises an inner layer cylinder, a middle cylinder and an outer layer cylinder, wherein a first annular cavity is formed between the inner layer cylinder and the middle cylinder, a filtering granular layer is arranged in the first annular cavity, a flue gas inlet is arranged at the lower part of the filter, a flue gas outlet is arranged at the upper part of the filter, dust-containing flue gas firstly enters the inner cavity of the inner layer cylinder from the flue gas inlet, then is filtered by the filtering granular layer and then enters a second annular cavity between the middle cylinder and the outer layer cylinder, and the filtered purified flue gas is discharged from the flue gas outlet.
Although the moving bed granular layer filter has high dust removal efficiency, the gas-solid contact area of gas flowing through the moving granular layer is large, the flow speed requirement is low, the filter material needs to be updated periodically, the total energy consumption is high, and the operation cost is high.
The utility model discloses a chinese utility model patent that grant publication number is CN209338597U discloses a converter flue gas removes dust and waste heat recovery system, its step is after the vaporization cooling flue, gets into the tower of putting out a fire for the converter flue gas, through the water spray cooling in the tower of putting out a fire, extinguishes the kindling of flue gas, gets rid of the large granule smoke and dust in the flue gas through the mode that gravity subsides simultaneously.
Although the gravity settling separation technology effectively avoids the risk of explosion of converter flue gas, the gravity settling separation technology is a combined separation technology of wet method and gravity settling, on one hand, the high-temperature energy of the flue gas is wasted, and on the other hand, the water consumption is large, and the wastewater needs to be subjected to secondary treatment.
Chinese utility model patent with publication number CN201744260U discloses a pervaporation spray cooling dry dust collector, which comprises the following steps: the smoke enters from the water cooling channel, is mixed with fog drops sprayed by the double-flow spray gun, enters the evaporative cooling tower through the compensator, is evaporated and vaporized by absorbing heat in the evaporative cooling tower, the temperature of the smoke is reduced, coarse particles and part of fine particle dust collide with the fog drops and fall into the banana elbow, the smoke is discharged from an ash outlet of the ash conveyor through an ash discharge valve, and the smoke subjected to temperature reduction and coarse dust removal enters the electrostatic dust collector for fine dust removal from an outlet connecting pipeline of the banana elbow.
Although the evaporation spray cooling dry-type dust removal technology can achieve the purposes of rapid cooling and coarse dust removal, a large amount of circulating water is still needed, the technology is not a real dry-type dust removal method, the high-temperature energy of smoke is wasted, and the problem that the inner wall of an evaporation cooler is easy to scale in the using process is also solved.
Disclosure of Invention
The invention aims to provide a flue gas micron-grade particle separating device which is low in energy consumption and can separate micron-grade particles in flue gas.
In order to achieve the purpose, the invention provides a flue gas-grade particle separation device which is arranged in a settling zone of a flue, and the flue gas-grade particle separation device comprises at least one set of settling components, each settling component comprises at least two layers of inclined plates which are arranged at intervals, the inclined plates are obliquely arranged towards the top wall of the flue along the flow direction of flue gas, and the included angle between each inclined plate and the top wall of the flue is 5-70 degrees.
The flue gas-grade particle separating device comprises a plurality of inclined plates, wherein the distance between every two adjacent inclined plates is 10-350 mm.
The flue gas neglected particle separating device comprises a plurality of inclined plates, wherein the inclined plates are arranged at equal intervals.
The flue gas-grade particle separating device comprises a sloping plate, wherein the sloping plate is 600-2500 mm long.
The flue gas neglected particle separating device is characterized in that the length of each inclined plate is equal.
According to the flue gas neglected particle separating device, the inclined plates of the two adjacent layers are arranged in parallel.
The flue gas-grade particle separating device comprises a flue gas inlet, a flue gas outlet, a sloping plate, a flue gas inlet, a flue gas outlet, a flue gas inlet, a flue gas outlet, a flue gas inlet, a flue gas.
The flue gas-grade particle separating device comprises a plurality of inclined plates, wherein the inclined plates are flat plates with uniform thickness.
The flue gas neglected particle separating device comprises a flue gas inlet, a flue gas outlet, a flue gas inlet, a flue gas outlet, a flue gas.
The flue gas-grade particle separating device comprises a settling component, wherein the settling component is arranged between the settling component and the inclined plate, and the distance between the settling component and the inclined plate is 1100mm, and the width of the inclined plate is 4500 mm.
Compared with the prior art, the invention has the following advantages:
the flue gas particle separation device utilizes the full dry method gravity sedimentation, has low energy consumption, does not interfere the physicochemical property of dust-containing particles from the outside, can keep unchanged, and is beneficial to secondary utilization of dust.
According to the flue gas micron-level particle separation device, the multilayer inclined plates are arranged, so that high-temperature flue gas carrying particles can be divided into a plurality of flat and thin air flows to form multilayer flow flue gas, the specific gravity of solid particles is far higher than that of the flue gas, the solid particles fall under the action of self gravity, and the inclined plates are obliquely arranged towards the top wall of the flue along the flow direction of the flue gas, so that the falling distance of the solid particles is shortened, the solid particles can more quickly contact the inclined plates, the micron-level particles are separated, and the separation purpose is achieved.
Drawings
The drawings are only for purposes of illustrating and explaining the present invention and are not to be construed as limiting the scope of the present invention. Wherein:
FIG. 1 is a first schematic diagram of the flue gas-neglected particle separating device of the invention;
FIG. 2 is a second schematic diagram of the flue gas-neglected particle separating device of the invention;
fig. 3 is a schematic structural view of the swash plate.
The reference numbers illustrate:
100. a flue; 101. an inlet; 102. an outlet; 110. a settling zone;
200. a sedimentation component; 210. a sloping plate; 211. a flow guide surface; 212. a shunt side; 213. connecting the side surfaces.
Detailed Description
In order to clearly understand the technical solution, the purpose and the effect of the present invention, a detailed description of the present invention will be described with reference to the accompanying drawings. Where the adjective or adverbial modifiers "inner" and "outer" are used merely to facilitate relative reference between groups of terms, and do not describe any particular directional limitation on the modified terms. In the description of the present invention, "a plurality" means two or more unless otherwise specified. In fig. 1 and 2, the solid short arrows indicate the flow direction of the flue gas, and the "high temperature" means 650 to 800 ℃.
As shown in fig. 1 and fig. 2, the present invention provides a flue gas hop-level particle separation device, which is disposed in a settling zone 110 of a flue, and comprises at least one set of settling assemblies 200, wherein:
the sedimentation component 200 comprises at least two layers of inclined plates 210 arranged at intervals from top to bottom, so as to be beneficial to the arrangement of the inclined plates 210, a flue gas circulation channel is formed between every two adjacent inclined plates 210, the inclined plates 210 are obliquely arranged towards the top wall of the flue 100 along the flowing direction of flue gas, and the included angle alpha between the inclined plates 210 and the top wall of the flue 100 is 5-70 degrees, so that when particles flow along with the flue gas in the flue gas circulation channel, the falling distance is shortened, the inclined plates 210 can be quickly touched, and the particles are separated.
When the device is used, as shown in figures 1 and 2, high-temperature flue gas generated in the smelting process of the converter mainly cools the flue gas to about 800 ℃ by radiation heat exchange through a converter flue positioned above the converter, and the concentration of particles carried in the flue gas can reach 200g/Nm3The flue gas carries particles with the particle size of the micron order or below to enter the flue 100 from the inlet 101, the particles with the particle size of the micron order or below are settled on each inclined plate 210 under the action of the multilayer inclined plates 210, namely, the separation of the particles with the particle size of the micron order is completed, and the collected particles are collected and then discharged in the preparation stage of converter steelmaking.
According to the flue gas-grade particle separating device, the multilayer inclined plates 210 are arranged, so that high-temperature flue gas carrying particles can be separated into a plurality of flat and thin air flows by the multilayer inclined plates 210 to form multilayer flow flue gas, the solid particles fall under the action of self gravity due to the fact that the specific gravity of the solid particles is far higher than that of the flue gas, the inclined plates 210 are obliquely arranged towards the top wall of the flue 100 along the flowing direction of the flue gas, the falling distance of the solid particles is shortened, the solid particles can rapidly contact the inclined plates 210, the particles in the grade of the particles are separated, the separating purpose is achieved, in addition, the included angle between the inclined plates 210 and the top wall of the flue 100 ranges from 5 degrees to 70 degrees, cleaning and sliding of accumulated ash are facilitated, and when the inclined angles of the inclined plates 210 are larger than the repose angles of the particles, the ash.
Further, adjacent two-layer swash plate 210 parallel arrangement each other to make the multilayer stream flue gas that forms more even, thereby more be favorable to coming out the neglected meter level granule separation.
Further, the distance h between two adjacent inclined plates 210 is 10 mm-350 mm, and such a distance can not only enable the smoke to smoothly pass through the smoke circulation channel, but also shorten the falling distance of particles, thereby enabling the smoke to more quickly contact the inclined plates 210.
Further, the length L of the inclined plate 210 is 600 mm-2500 mm, and the particles carried by the flue gas can fully contact the inclined plate 210 due to the length L, so that the separation effect is improved.
Still further, each inclined plate 210 has an equal length to facilitate installation of the settling assembly 200 in a pipe.
Further, the width of the inclined plate 210 is 2000 mm-5000 mm, and the width can ensure the contact area of the flue gas and the inclined plate 210, thereby ensuring the separation effect.
In one embodiment of the present invention, as shown in fig. 3, the inclined plate 210 includes two opposite flow guide surfaces 211, two opposite connection side surfaces 213 and two opposite flow diversion side surfaces 212, and the two connection side surfaces 213 are fixedly connected to the inner surface of the flue 100, so that the inclined plate 210 does not affect the flow of the flue gas.
The two connecting side surfaces 213 may be welded to the inner surface of the flue 100, or may be fixed by bolts or rivets.
Further, each of the inclined plates is a flat plate with uniform thickness, so that smoke can smoothly pass through between two adjacent inclined plates 210 to form a smoke circulation channel.
In one embodiment of the present invention, as shown in fig. 1, two sets of settling assemblies 200 are disposed in the flue 100 at intervals, so that the flue gas is discharged after two-stage settling, thereby improving the effect of separation of the micron-scale particles.
Further, the distance H between two sedimentation components 200 is 1100mm to make the flue gas after the first grade is depositd, speed reduces and carries out second grade sedimentation again, thereby further improves the effect of the separation of the micron grade granule.
Of course, more than two sets of settling assemblies 200 are disposed in the flue 100 at intervals, such as three, six, or nine sets of settling assemblies 200, which will not be described herein again.
The use process of the flue gas micron-grade particle separation device is specifically described below with reference to the accompanying drawings:
as shown in figure 1, a set of sedimentation components are arranged in the flue 100, the included angle between the inclined plate 210 and the top wall of the flue 100 is 45 degrees, the length of the inclined plate 210 is 1414mm, the width of the inclined plate 210 is 4500mm, the temperature of flue gas entering the flue 100 is 700 ℃, the flow velocity range of the flue gas is 1.5-7 m/s, and the concentration of dust-containing particles in the flue gas is 120g/Nm3The particle size range of the particles within the statistical range of analysis is 20-100 μm.
Through simulation and calculation analysis, the separation and collection effect of the flue gas micron-sized particle separation device on dust-containing particles in flue gas is calculated and analyzed, and statistical results show that the collection rate of the sedimentation component on 20 mu m particle size particles is not lower than 70%, the collection rate on 30 mu m particle size particles is not lower than 96.2%, and the collection rate on 50 mu m and above particle size particles can reach 100% when the flow rate of the flue gas is within the range of 1.5-7 m/s.
As shown in figure 2, two sets of sedimentation components are arranged in the flue 100, each set of sedimentation component comprises four layers of inclined plates 210, the distance between two adjacent inclined plates is 45mm, the included angle between the inclined plates 210 and the top wall of the flue 100 is 11 degrees, the length of the inclined plates 210 is 1100mm, the width of the inclined plates 210 is 4500mm, the temperature of the flue gas entering the flue 100 is 700 ℃, the flow velocity range of the flue gas is 1.5-7 m/s, and the concentration of dust-containing particles in the flue gas is 120g/Nm3The particle size range of the particles within the statistical range of analysis is 20-100 μm.
Through simulation, the separation and trapping effects of the flue gas micron-sized particle separation device on dust-containing particles in flue gas are calculated and analyzed, and statistical results show that when the flow velocity of the flue gas is 7m/s, the trapping rate of the inclined plate sedimentation area on 20-micron-sized particles is 37.3%, the trapping rate on 30-micron-sized particles is 71.6%, and the trapping rate on 50-micron-sized particles and above is 100%; the lower the flue gas flow velocity is, the higher the capture rate of the inclined plate sedimentation area on particles with corresponding particle sizes is; when the flow velocity of the flue gas is 1.5m/s, the collection rate of the inclined plate sedimentation zone on particles with the particle size of 20 mu m is 64.4 percent, and the collection rate on particles with the particle size of 30 mu m or more is 100 percent.
In conclusion, the flue gas particle separation device provided by the invention utilizes the full-dry method gravity sedimentation, is low in energy consumption, does not interfere with the physicochemical properties of dust-containing particles from the outside, can keep unchanged, and is beneficial to secondary utilization of dust.
According to the flue gas micron-level particle separation device, the multilayer inclined plates are arranged, so that high-temperature flue gas carrying particles can be divided into a plurality of flat and thin air flows to form multilayer flow flue gas, the specific gravity of solid particles is far higher than that of the flue gas, the solid particles fall under the action of self gravity, and the inclined plates are obliquely arranged towards the top wall of the flue along the flow direction of the flue gas, so that the falling distance of the solid particles is shortened, the solid particles can more quickly contact the inclined plates, the micron-level particles are separated, and the separation purpose is achieved.
The above description is only an exemplary embodiment of the present invention, and is not intended to limit the scope of the present invention. Any equivalent changes and modifications that can be made by one skilled in the art without departing from the spirit and principles of the invention should fall within the protection scope of the invention. It should be noted that the components of the present invention are not limited to the above-mentioned whole application, and various technical features described in the present specification can be selected to be used alone or in combination according to actual needs, so that the present invention naturally covers other combinations and specific applications related to the invention.
Claims (10)
1. The flue gas-grade particle separation device is used for being arranged in a settling zone of a flue and is characterized by comprising at least one set of settling components, each settling component comprises at least two layers of inclined plates arranged at intervals, the inclined plates are obliquely arranged towards the top wall of the flue along the flowing direction of flue gas, and the included angle between each inclined plate and the top wall of the flue ranges from 5 degrees to 70 degrees.
2. The flue gas hop-class particle separating device according to claim 1,
the distance between two adjacent sloping plates is 10 mm-350 mm.
3. The flue gas hop-class particle separating device according to claim 2,
the inclined plates are arranged at equal intervals.
4. The flue gas hop-class particle separating device according to claim 1,
the length of the inclined plate is 600 mm-2500 mm.
5. The flue gas hop-class particle separating device according to claim 4,
the lengths of the inclined plates are equal.
6. The flue gas hop-class particle separating device according to claim 1,
the adjacent two layers of the inclined plates are arranged in parallel.
7. The flue gas hop-class particle separating device according to claim 1,
the inclined plate comprises two oppositely arranged flow guide surfaces, two oppositely arranged connecting side surfaces and two oppositely arranged flow distribution side surfaces, and the two connecting side surfaces are fixedly connected with the inner surface of the flue.
8. The flue gas hop-class particle separating device according to claim 1,
each inclined plate is a flat plate with uniform thickness.
9. The flue gas hop-by-hop particle separation device according to any of claims 1 to 8,
two groups of sedimentation components are arranged in the flue at intervals.
10. The flue gas hop-class particle separating device according to claim 9,
the distance between the two sedimentation components is 1100mm, and the width of the inclined plate is 4500 mm.
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| CN202011266084.5A CN112267002A (en) | 2020-11-13 | 2020-11-13 | Flue gas micron-level particle separation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP4371643A1 (en) * | 2022-11-16 | 2024-05-22 | CERI Environment Protection Technology Co. Ltd. | Shallow incline plate settlement apparatus and particle trapping method |
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| CN103372349A (en) * | 2013-05-30 | 2013-10-30 | 浙江天地环保工程有限公司 | Demisting device for outlet flue of desulfurization tower |
| CN203469671U (en) * | 2013-09-03 | 2014-03-12 | 浙江天地环保工程有限公司 | Combined demister of outlet flue of desulfurization tower |
| CN206577585U (en) * | 2017-01-18 | 2017-10-24 | 富民薪冶工贸有限公司 | A kind of lead smelting exhaust processing system |
| CN107737492A (en) * | 2017-11-25 | 2018-02-27 | 邹德学 | A kind of waste gas complex dust collector |
| CN112206588A (en) * | 2020-11-13 | 2021-01-12 | 北京京诚科林环保科技有限公司 | Flue gas particle separation device |
| CN112246015A (en) * | 2020-11-13 | 2021-01-22 | 北京京诚科林环保科技有限公司 | High-temperature flue gas particle separation device |
| CN112263878A (en) * | 2020-11-13 | 2021-01-26 | 北京京诚科林环保科技有限公司 | Multi-settling high-temperature flue gas particle separation device |
| CN213835408U (en) * | 2020-11-13 | 2021-07-30 | 北京京诚科林环保科技有限公司 | Flue gas micron-level particle separation device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| EP4371643A1 (en) * | 2022-11-16 | 2024-05-22 | CERI Environment Protection Technology Co. Ltd. | Shallow incline plate settlement apparatus and particle trapping method |
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