CN116829267A - Cyclone dust collecting apparatus and dust collecting method using the same - Google Patents
Cyclone dust collecting apparatus and dust collecting method using the same Download PDFInfo
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- CN116829267A CN116829267A CN202280013530.2A CN202280013530A CN116829267A CN 116829267 A CN116829267 A CN 116829267A CN 202280013530 A CN202280013530 A CN 202280013530A CN 116829267 A CN116829267 A CN 116829267A
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- 239000000428 dust Substances 0.000 title claims abstract description 227
- 238000000034 method Methods 0.000 title claims description 7
- 238000011084 recovery Methods 0.000 claims abstract description 104
- 238000000926 separation method Methods 0.000 claims abstract description 34
- 239000002245 particle Substances 0.000 description 75
- 239000007787 solid Substances 0.000 description 40
- 230000014759 maintenance of location Effects 0.000 description 23
- 230000000717 retained effect Effects 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 230000007423 decrease Effects 0.000 description 5
- 239000000571 coke Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000004088 simulation Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
Abstract
The cyclone dust collector 1 collects dust DT from a gas TG to be processed including the dust DT, and includes: a dust separator 3 for rotating the gas TG to be processed about a horizontal rotation axis to separate dust from the gas TG to be processed; a dust recovery unit 4 connected to the outlet side of the dust separation unit 3, for recovering dust DT separated by the swirl of the gas TG to be processed by the dust separation unit 3; and a gas recovery unit 5 having an inlet provided in the dust recovery unit 4 and recovering the gas TG to be treated after separating the dust DT, wherein a first ratio L/Dout of a distance L from an outlet of the dust separation unit 3 to the inlet of the gas recovery unit 5 to an outlet diameter Dout of the dust separation unit 3 is not less than 0.4 and not more than 1.0.
Description
Technical Field
The present invention relates to a cyclone dust collector for collecting dust contained in a gas to be processed and a dust collecting method using the cyclone dust collector.
Background
For example, in a vertical iron melting furnace such as a blast furnace, high-temperature air is blown from a tuyere provided in the lower portion of the furnace in a state where an iron source and a heat source such as coke are alternately put into a layer. The air blown from the tuyere reacts with carbon in the coke to generate heat, and the iron source is melted by the heat. The air rises in the furnace. The gas reaching the vicinity of the furnace roof is discharged in a state containing dust formed by coke, solid particles of various sizes generated from the refractory in the furnace, and the like. Therefore, it is necessary to separate and collect dust formed of solid particles from exhaust gas of a blast furnace or the like.
Conventionally, various methods have been used for separating dust from a gas to be processed, and cyclone dust collecting apparatuses have been known as an example thereof. The cyclone dust collector rotates the gas to be processed, thereby separating dust from the gas to be processed by centrifugal force. As a type of cyclone dust collecting apparatus, a vertical type cyclone dust collecting apparatus and a horizontal type cyclone dust collecting apparatus are known. Among them, a horizontal cyclone dust collector with a small pressure loss may be used depending on the nature of the gas to be treated, the installation environment, and the like (for example, see patent documents 1 and 2).
Patent document 1 discloses a horizontal cyclone dust collector in which a gas to be processed is swirled along the circumferential direction of an inner wall portion in an inner space and moved in the axial direction, thereby separating dust. When the gas to be processed swirls, dust in the gas to be processed collides with the inner wall portion by centrifugal force. At this time, the movement component (whirling movement component) of the dust, which whirls along the inner wall portion, and the movement component (axial movement component) which moves in the axial direction disappear, and the dust is separated from the gas to be processed.
Patent document 2 discloses a horizontal cyclone dust collector including a protruding portion formed to protrude from an inner wall portion toward a radial inner side of an inner space, and extending along a circumferential direction of the inner wall portion.
Prior art literature
Patent literature
Patent document 1: japanese patent laid-open No. 2008-6315
Patent document 2: japanese patent application laid-open No. 2011-218250
Disclosure of Invention
Problems to be solved by the invention
However, in the cyclone dust collectors of patent documents 1 and 2, it is difficult to separate dust having a small particle diameter (mass) from the gas to be processed. Therefore, there is a problem that the recovery rate of fine dust in the cyclone dust collector is reduced.
The present invention has been made in view of the above problems, and an object of the present invention is to provide a cyclone dust collector and a dust collecting method using the cyclone dust collector, which can improve the recovery rate of fine dust.
Means for solving the problems
[1] A cyclone dust collector for collecting dust from a gas to be processed, the cyclone dust collector comprising: a dust separation unit for rotating the gas to be processed with a horizontal rotation axis to separate dust from the gas to be processed; a dust recovery unit connected to an outlet side of the dust separation unit, for recovering the dust separated by the swirling of the gas to be processed by the dust separation unit; and a gas recovery unit having an inlet provided in the dust recovery unit, wherein the gas recovery unit recovers the gas to be treated after separating the dust, and a first ratio L/Dout of a distance L from an outlet of the dust separation unit to the inlet of the gas recovery unit to an outlet diameter Dout of the dust separation unit is 0.4 to 1.0.
[2] The cyclone dust collecting apparatus as recited in [1], wherein the dust separating section comprises: a main body portion having a gas flow path extending in a lateral direction; and a rectifying member provided in the gas flow path of the main body portion and configured to flow the gas to be treated in a lateral direction while swirling along an inner wall of the main body portion.
[3] The cyclone dust collecting apparatus as described in [1] or [2], wherein a second ratio Dd/Dout of an inlet diameter Dd of the gas recovery portion to an outlet diameter Dout of the dust separation portion is not less than 0.4 and not more than 0.5.
[4] The cyclone dust collecting apparatus as recited in any one of [1] to [3], wherein the gas recovery portion is formed so that a diameter thereof becomes wider from an inlet side of the gas to be processed toward a traveling direction.
[5] A dust collecting method using the cyclone dust collecting apparatus as described in any one of the above [1] to [4 ].
Effects of the invention
According to the cyclone dust collector of the present invention, the first ratio L/Dout of the outlet diameter Dout of the dust separating unit to the distance L from the outlet of the dust separating unit to the inlet of the gas to be treated collecting unit is set to 0.4 to 1.0, whereby the retention of dust in the separating unit and the increase in pressure loss can be suppressed, and the recovery rate of dust containing small solid particles can be improved.
Drawings
Fig. 1 is a schematic view showing a preferred embodiment of the cyclone dust collecting apparatus of the present invention.
Fig. 2 is a schematic diagram showing an example of a dust separating unit in the cyclone dust collecting apparatus of fig. 1.
FIG. 3 is a graph showing the relationship between the first ratio L/Dout and the dust DT recovery rate when solid particles having a particle diameter of 75 μm are caused to flow in.
FIG. 4 is a graph showing the relationship between the first ratio L/Dout and the dust DT recovery rate when solid particles having a particle diameter of 25 μm are caused to flow in.
FIG. 5 is a graph showing a first ratio L/Dout when solid particles having a particle diameter of 75 μm are caused to flow in, and a retention rate of dust retained at an inlet of the dust collection unit.
FIG. 6 is a graph showing a first ratio L/Dout when solid particles having a particle diameter of 25 μm are caused to flow in, and a retention rate of dust retained at an inlet of the dust collection unit.
Fig. 7 is a graph showing the relationship between the second ratio Dd/Dout of the outlet diameter Dout of the dust separating section to the inlet diameter Dd of the gas recovering section 5 and the pressure loss.
FIG. 8 is a graph showing the relationship between the second ratio Dd/Dout and the recovery rate when solid particles having a particle diameter of 75 μm are caused to flow in.
FIG. 9 is a graph showing the relationship between the second ratio Dd/Dout and the recovery rate when solid particles having a particle diameter of 25 μm are caused to flow in.
FIG. 10 is a graph showing the relationship between the second ratio Dd/Dout and the retention rate when solid particles having a particle diameter of 75 μm are caused to flow in.
FIG. 11 is a graph showing the relationship between the second ratio Dd/Dout and the retention rate when solid particles having a particle diameter of 25 μm are caused to flow in.
Fig. 12 is a schematic view showing another embodiment of the cyclone dust collecting apparatus of the present invention.
Detailed Description
Hereinafter, embodiments of the present invention will be described with reference to the drawings. Fig. 1 is a schematic view showing a preferred embodiment of the cyclone dust collecting apparatus of the present invention. The cyclone dust collector 1 in fig. 1 is a horizontal cyclone dust collector that generates a swirling flow about a lateral axis and collects dust DT from a gas TG to be processed. The cyclone dust collector 1 includes: a dust separator 3 for separating dust DT from the gas TG to be processed flowing into the inflow pipe 2; a dust recovery unit 4 for recovering the dust DT separated by the dust separation unit 3; and a gas recovery unit 5 for recovering the gas TG to be treated after separating the dust DT. The case where the inflow pipe 2 is connected to, for example, a blast furnace, a converter, or the like, and the gas TG to be treated is an exhaust gas discharged from the blast furnace, the converter, or the like is exemplified.
Fig. 2 is a schematic view showing an example of a dust separating unit in the cyclone dust collecting apparatus of fig. 1. The dust separator 3 in fig. 2 rotates the gas TG about the transverse axis to separate the dust DT from the gas TG. The dust separating unit 3 includes: a main body portion 3A having a gas flow path extending in the lateral direction; and a rectifying member 3B provided in the gas flow path of the main body 3A and configured to axially move the target gas TG while swirling along the inner wall of the main body 3A.
The main body 3A has a hollow portion, for example, a cylindrical shape or a conical shape, and serves as a gas flow path. In the example shown in fig. 1, the body portion 3A has a conical shape, and the outlet diameter Dout of the body portion 3A is larger than the inlet diameter Din (Dout > Din). Therefore, the diameter of the gas flow path in the body portion 3A gradually increases from the upstream side toward the downstream side. In the following description, the gas flow path of the body 3A may be referred to as an enlarged flow path. The rectifying member 3B is disposed in the hollow portion of the main body 3A, and turns the gas TG to be treated flowing into the main body 3A into a swirling flow. That is, the rectifying member 3B has a shape including a rectifying plate 3C formed in a spiral shape on the outer peripheral side, and the rectifying plate 3C causes the gas TG to be treated flowing in from the inlet side of the main body 3A to flow along the rectifying plate 3C to form a swirling flow.
In particular, since the main body 3A forms an enlarged flow path, the gas TG to be processed becomes a swirling flow (hereinafter, sometimes referred to as an enlarged swirling flow) whose spiral radius becomes wider toward the downstream side (outlet side). Therefore, the swirling flow of the processing gas TG is more likely to be separated from the rectifying plate 3C as it goes downstream in the flow direction of the processing gas TG, and can be swirled easily along the inner wall of the main body 3A. In the example shown in fig. 1, the main body 3A is shown to form an enlarged flow path having an outlet diameter Dout larger than the inlet diameter Din (Dout > Din) of the main body 3A, but the present invention is not limited thereto. The shape of the main body 3A may be a cylindrical shape having an outlet diameter Dout equal to an inlet diameter Din (dout=din) according to the performance required of the cyclone dust collector 1. Alternatively, the body 3A may be formed in a shape in which the outlet diameter Dout is smaller than the inlet diameter Din (Dout < Din), and the diameter gradually decreases from the inlet side to the outlet side. The main body 3A has any shape and can generate swirling flow.
The dust collection unit 4 shown in fig. 1 is connected to the outlet side of the dust separation unit 3, and collects dust DT separated by the swirling of the gas TG to be processed in the dust separation unit 3. The dust collection unit 4 is formed, for example, in a bottomed cylindrical shape having the same diameter as the outlet diameter Dout of the dust separation unit 3. The dust collection unit 4 includes: a swirling space portion 4A provided between the outlet of the dust separating portion 3 and the inlet of the gas recovering portion 5; and a dust chute (durt section) 4B provided at the bottom of the dust collection unit 4 and collecting the dust DT. The swirling space portion 4A is a region where the gas TG to be treated, which is a swirling flow, flows in and the dust DT collides with the inner wall. Then, the dust chute 4B recovers the dust DT separated from the swirling flow.
The gas recovery unit 5 is a part for recovering the gas TG to be treated after separating the dust DT, and is connected to a gas utilization side pipe, not shown. The gas recovery unit 5 is formed of, for example, a pipe having a diameter smaller than the outlet diameter Dout of the dust separation unit 3 and the dust recovery unit 4, and the inlet side is inserted into the dust recovery unit 4. When the gas recovery unit 5 is inserted into the dust recovery unit 4, for example, the gas recovery unit 5 and the dust separation unit 3 are coaxially disposed so that the central axes thereof coincide with each other. The gas recovery unit 5 is inserted into the dust recovery unit 4 such that the dust chute 4B is positioned below the gas recovery unit 5.
An operation example of the cyclone dust collector 1 will be described with reference to fig. 1 and 2. The gas TG to be treated discharged from the blast furnace, the converter, or the like flows into the dust separation section 3 through the inflow pipe 2. The processed gas TG flows along the rectifying plate 3C of the dust separating unit 3 to form an expanded swirling flow, and flows into the dust collecting unit 4. The dust DT contained in the processed gas TG collides with the inner wall of the main body portion 3A in the dust separation portion 3 or the inner wall of the dust recovery portion 4 due to the swirling flow, and loses kinetic energy. As a result, the dust DT is separated from the swirling flow of the gas TG to be processed and recovered to the dust chute 4B. On the other hand, the gas TG to be processed from which the dust DT has been separated is recovered by the gas recovery unit 5 and flows into a utilization-side pipe, not shown.
Here, the dust DT recovered by the cyclone dust collector 1 of fig. 1 includes solid particles having various particle diameters. The separation and collection critical particle diameter ds of the solid particles in the cyclone dust collector 1 can be obtained by the following formula (1).
[ formula 1]
d s : separation and collection critical particle diameter [ m ]]
Mu: fluid viscosity [ Pa.s ]
r 1 : rotation inner diameter [ m ]]
r 2 : outer diameter of rotation [ m ]]
N: rotational speed [ - ]
v i : speed [ m/s ]]
ρ p : particle Density [ kg/m ] 3 ]
ρ a : fluid Density [ kg/m ] 3 ]
According to the formula (1), the separation and collection critical particle diameter ds can be reduced by increasing the kinetic component (swirling kinetic component) of the dust DT. Specifically, in order to reduce the separation/collection critical particle diameter ds, it is considered to make the denominator of the formula (1) a large value or make the numerator a small value. In the dust DT collected by the cyclone dust collector 1, fine solid particles are particles having a particle diameter of 100 μm or less. However, for example, when the dust DT has a fine particle diameter of 100 μm or less, separation by the dust separator 3 becomes difficult, and fine solid particles that have not been captured flow into the gas recovery unit 5 together with the gas TG to be processed.
Therefore, in order to increase the recovery rate of fine solid particles, the recovery rate of fine solid particles having a small mass was studied by simulation while the swirl amount of the gas TG to be treated in the dust separator 3 was kept constant and the first ratio L/Dout was variously changed. In the simulation, the particle diameters of the fine solid particles to be the dust DT were set to 75 μm and 25 μm of 100 μm or less, and the particle reynolds numbers of the solid particles were set to about 100. The distance L is a distance between the dust separating member 3 and the gas recovery unit 5 in the axial direction of the cyclone device 1.
Fig. 3 is a graph showing a relationship between the first ratio L/Dout and the recovery rate of the dust DT when solid particles having a particle diameter of 75 μm are caused to flow into the dust recovery unit 4. Fig. 4 is a graph showing a relationship between the first ratio L/Dout and the recovery rate of the dust DT when solid particles having a particle diameter of 25 μm are caused to flow into the dust recovery unit 4. The recovery rate is a ratio of the amount of solid particles recovered by the dust chute 4B to the amount of total solid particles flowing in from the inflow pipe 2.
In the case of the particle size of 75 μm in FIG. 3, the larger the first ratio L/Dout, the smaller the recovery rate. On the other hand, in the case where the particle diameter of FIG. 4 is 25. Mu.m, when the first ratio L/Dout is in the range of 0 to 0.75 (0.ltoreq.L/Dout.ltoreq.0.75), the recovery rate decreases with an increase in the first ratio L/Dout. When the first ratio L/Dout is larger than 0.75 (0.75 < L/Dout), the recovery rate increases with an increase in the first ratio L/Dout. From a combination of fig. 3 and 4, it is understood that if the first ratio L/Dout is 1.0 or less (L/Dout is 1.0 or less), the dust DT can travel a distance equal to or greater than the distance L while maintaining the amount of movement in the separable whirling direction. Further, the collection of fine solid particles required as the cyclone dust collector 1 can be performed.
However, merely determining the upper limit of the first ratio L/Dout as described above cannot achieve improvement in recovery rate, that is, cannot achieve increase in recovery rate. The dust DT is separated by the swirling flow and moves to the position of the dust chute 4B in the traveling direction of the swirling flow. The swirling flow is a complex fluid motion that always travels while changing the center of swirling, and a portion that is counter-current to the traveling direction is generated. In particular, in an expanded swirling flow in which the diameter of the swirling flow of the gas TG increases as the gas TG advances downstream because the outlet diameter Dout of the dust separating portion 3 is larger than the inlet diameter Din of the dust separating portion 3, this tendency is stronger and a backflow phenomenon is likely to occur. The small solid particles tend to move in the same manner as the flow of the gas TG to be processed, and remain in the boundary portion between the dust separation unit 3 and the dust recovery unit 4, that is, in the portion which is the outlet of the dust separation unit 3 and the inlet of the dust recovery unit 4, due to the influence of the reverse flow. The retained solid particles may flow together with the gas TG to be processed to the gas recovery unit 5. Therefore, the relationship between the fine solid particles retained in the inlet of the dust collection unit 4 and the first ratio L/Dout was studied.
Fig. 5 is a graph showing a first ratio L/Dout when solid particles having a particle diameter of 75 μm are caused to flow in, and a retention rate of dust DT retained at an inlet of the dust collection unit 4. Fig. 6 is a graph showing a first ratio L/Dout when solid particles having a particle diameter of 25 μm are caused to flow into the dust recovery unit 4, and a retention rate of the dust DT retained at the inlet of the dust recovery unit 4. The retention rate is a ratio of the amount of solid particles retained in the inlet of the dust recovery unit 4 (i.e., the outlet of the dust separation unit 3) to the amount of total solid particles flowing in from the inflow pipe 2.
When the particle diameter of the solid particles in FIG. 5 is 75. Mu.m, the larger the first ratio L/Dout is, the lower the retention rate is. As shown in fig. 5, the overall ratio L/Dout is kept low regardless of the magnitude of the first ratio L/Dout. On the other hand, when the particle diameter of the solid particles in fig. 6 is 25 μm, the retention of the dust DT at the inlet of the dust recovery section 4 by the reverse flow increases as the first ratio L/Dout becomes smaller. Considering the retention rate in fig. 5 and 6, it is understood that the retention of the dust DT at the inlet of the dust recovery unit 4 is not problematic as long as the first ratio L/Dout is 0.4 or more. This is because if the first ratio L/Dout is 0.4 or more, the extreme pressure distribution after passing through the dust separating unit 3 can be eliminated, and a sufficient space for preventing the backflow can be ensured. Therefore, the first ratio L/Dout is set to 0.4 or more. In particular, in fig. 6, when the first ratio L/Dout is 0.5 or more, the retention rate can be suppressed to 5% or less, which is more preferable.
Here, as shown in fig. 3 and 4, from the viewpoint of the recovery rate, the smaller the first ratio L/Dout, the larger the recovery rate. As shown in fig. 5 and 6, from the viewpoint of the retention rate, the higher the first ratio L/Dout, the smaller the retention rate. From the viewpoints of retention rates in fig. 5 and 6, the retention rate can be suppressed to 5% or less as long as the first ratio L/Dout is 0.45 or more. Therefore, the lower limit of the first ratio L/Dout is preferably 0.45. On the other hand, as shown in fig. 4, even when the particle diameter of the dust DT is 25 μm, the recovery rate increases with a decrease in the first ratio L/Dout as long as the first ratio L/Dout is 0.75 or less. Therefore, the upper limit of the first ratio L/Dout is preferably 0.75. As shown in fig. 3, if the first ratio L/Dout is 0.65 or less, the recovery rate of dust DT having a particle diameter of 75 μm can be maintained at 50% or more. Therefore, the upper limit of the first ratio L/Dout is more preferably 0.65.
As described above, the outlet diameter Dout of the dust separating section 3 and the distance L between the dust separating section 3 and the gas recovery section 5 are set so that the first ratio L/Dout is 0.4 or more and 1.0 or less. This can suppress the retention of fine dust, improve the recovery rate, and suppress the mixing of fine dust into the gas recovery unit 5.
In the cyclone dust collector 1 according to the embodiment of the present invention, the first ratio L/Dout may be set to a range of 0.4 or more and 1.0 or less (0.4. Ltoreq.l/Dout. Ltoreq.1.0), but the following configuration is preferable in order to further improve the recovery rate. That is, it is preferable to construct: the first ratio L/Dout is set to the above-described range, and the second ratio Dd/Dout of the outlet diameter Dout of the dust separating portion 3 to the inlet diameter Dd of the gas recovery portion 5 is considered. In the case of using the horizontal cyclone dust collecting apparatus 1, it is assumed that the capacity of the exhaust fan is not large. Therefore, the increase in pressure loss causes a decrease in dust collection performance. As shown in fig. 1, the gas recovery unit 5 has a smaller diameter than the dust separation unit 3 and the dust recovery unit 4, and generates a pressure loss when recovering the gas. Therefore, the influence of the pressure loss caused by the inlet diameter Dd of the gas recovery section 5 and the outlet diameter Dout of the dust separation section 3 on the recovery rate of the minute dust DT was studied.
Fig. 7 is a graph showing the relationship between the second ratio Dd/Dout and the pressure loss. In fig. 7, it is seen that when the second ratio Dd/Dout is smaller than 0.4 (Dd/Dout < 0.4), the pressure loss increases sharply with a decrease in the second ratio Dd/Dout. Therefore, from the viewpoint of pressure loss, the second ratio Dd/Dout is desirably 0.4 or more.
On the other hand, it is considered that the second ratio Dd/Dout approaching 1.0 indicates that the inlet diameter Dd of the gas recovery unit 5 and the outlet diameter Dout of the dust separation unit 3 have the same diameter, and the dust DT contained in the swirling flow directly flows into the gas recovery unit 5. Therefore, similarly to fig. 3 to 6, the relationship between the second ratio Dd/Dout and the recovery rate and the retention rate was studied.
Fig. 8 is a graph showing the relationship between the second ratio Dd/Dout and the recovery rate when solid particles having a particle diameter of 75 μm are caused to flow into the dust recovery unit 4. Fig. 9 is a graph showing the relationship between the second ratio Dd/Dout and the recovery rate when solid particles having a particle diameter of 25 μm are caused to flow into the dust recovery unit 4. In fig. 8 and 9, the first ratio L/Dout is fixed to 0.75.
As shown in fig. 9, in the case where the particle diameter of the solid particles is 25 μm, the recovery rate is in the range of 6±2% independently of the second ratio Dd/Dout. On the other hand, as shown in FIG. 8, when the particle diameter of the solid particles is 75. Mu.m, the recovery rate can be maintained at 70% or more when the second ratio Dd/Dout is 0.5 or less (Dd/Dout. Ltoreq.0.5). Further, it is found that when the second ratio Dd/Dout is larger than 0.5 (Dd/Dout > 0.5), the recovery rate is drastically reduced. Therefore, it is desirable to set the second ratio Dd/Dout to 0.5 or less.
Fig. 10 is a graph showing a relationship between the second ratio Dd/Dout and the retention rate when solid particles having a particle diameter of 75 μm are caused to flow into the dust collection unit 4. Fig. 11 is a graph showing a relationship between the second ratio Dd/Dout and the retention rate when solid particles having a particle diameter of 25 μm are caused to flow into the dust collection unit 4. As shown in fig. 10 and 11, when the second ratio Dd/Dout is in the range of 0.4 or more, the retention rate of fine solid particles is suppressed to be 10% or less. As described above, the second ratio Dd/Dout is preferably 0.4 to 0.5 (0.4. Ltoreq.Dd/Dout. Ltoreq.0.5) in view of the reduction of pressure loss, the improvement of recovery rate and the retention rate.
Fig. 12 is a schematic view showing other embodiments of the cyclone dust collecting apparatus of the present invention. In the cyclone dust collecting apparatus 100 of fig. 12, the same reference numerals are given to the parts having the same configuration as the cyclone dust collecting apparatus 1 of fig. 1, and the description thereof is omitted. The cyclone dust collecting apparatus 100 of fig. 12 is different from the cyclone dust collecting apparatus 1 of fig. 1 in that the gas recovery portion 105 has a shape in which the diameter widens from the upstream toward the downstream in the flow direction of the gas TG to be processed.
The gas recovery portion 105 of fig. 12 is formed of a diffuser pipe having a diameter that increases from the inlet side toward the downstream. The taper angle θ of the gas recovery unit 105 is preferably an angle at which the flow of the target gas TG does not separate from the inner wall of the gas recovery unit 105. In view of a general jet beam divergence angle, the angle may be 15 ° or less, and more preferably 12.5 ° or less. In this way, the occurrence of turbulence and vortex can be suppressed in the gap between the gas flow of the target gas TG flowing in from the inlet of the gas recovery unit 105 and the inner wall of the gas recovery unit 105, and the pressure loss can be increased.
That is, the gas recovery unit 5 shown in fig. 1 may be connected to a use-side pipe, not shown, and the diameter of the use-side pipe may be larger than the inlet diameter Dd of the gas recovery unit 5. In this case, a sharp step is generated in the pipe cross section of the connection portion between the gas recovery unit 5 and the use-side pipe, and the gas flow is separated from the wall surface of the gas recovery unit 5 at the connection portion, thereby increasing the pressure loss. Therefore, by making the gas recovery unit 5 a diffuser pipe (gas recovery unit 105) shown in fig. 12, an increase in pressure loss due to detachment of the gas flow from the wall surface of the gas recovery unit 5 can be suppressed.
Even in the cyclone dust collector 100 shown in fig. 12, the recovery rate of fine dust can be improved by setting the first ratio L/Dout to 0.4 to 1.0 (0.4. Ltoreq.l/Dout. Ltoreq.1.0) in the same manner as the cyclone dust collector 1 of fig. 1. Further, the recovery rate can be further improved by setting the second ratio Dd/Dout to 0.4 to 0.5 (0.4. Ltoreq.dd/Dout. Ltoreq.0.5).
The present invention is not limited to the above embodiments, and various modifications can be made. In the above embodiments, the case where the gas TG to be processed is the exhaust gas from a blast furnace, a converter, or the like has been exemplified, but the application is not limited as long as the gas is a gas that separates dust DT contained in the object to be processed. In fig. 2, the dust separating unit 3 is illustrated as having the rectifying member 3B having the rectifying plate 3C at the center in the main body 3A, but the present invention is not limited thereto, and the dust separating unit 3 may be configured to generate a swirling flow. For example, the rectifying member 3B may be constituted by a rectifying plate attached to the inner wall surface of the main body 3A.
Description of the reference numerals
1. 100 cyclone dust collector
2 inflow pipe
3 dust separation part
3A main body
3B rectifying component
3C rectifying plate
4 dust recovery unit
4A convolution space part
4B dust chute
5. 105 gas recovery unit
DT dust
Inlet diameter of Dd gas recovery section
Outlet diameter of Dout dust separation section
TG treated gas
Claims (5)
1. A cyclone dust collector that collects dust from a gas to be processed, the cyclone dust collector comprising:
a dust separation unit for rotating the gas to be processed with a horizontal rotation axis to separate dust from the gas to be processed;
a dust recovery unit connected to an outlet side of the dust separation unit, the dust recovery unit being configured to recover the dust separated by the swirling of the gas to be processed by the dust separation unit; and
a gas recovery unit having an inlet provided in the dust recovery unit, the gas recovery unit recovering the gas to be treated after separating the dust,
a first ratio L/Dout of a distance L from an outlet of the dust separating section to an inlet of the gas recovery section to an outlet diameter Dout of the dust separating section is 0.4 to 1.0.
2. The cyclone dust collecting apparatus as claimed in claim 1, wherein the dust separating part comprises: a main body portion having a gas flow path extending in a lateral direction; and a rectifying member provided in the gas flow path of the main body portion and configured to flow the gas to be treated in a lateral direction while swirling along an inner wall of the main body portion.
3. The cyclone dust collecting apparatus as claimed in claim 1 or 2, wherein a second ratio Dd/Dout of an inlet diameter Dd of the gas recovery section to an outlet diameter Dout of the dust separating section is 0.4 to 0.5.
4. A cyclone dust collecting apparatus as claimed in any one of claims 1 to 3, wherein the gas recovery portion is formed so that a diameter becomes wider from an inlet side of the gas to be treated toward a traveling direction.
5. A dust collecting method using the cyclone dust collecting apparatus as claimed in any one of claims 1 to 4.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2021-058065 | 2021-03-30 | ||
| JP2021058065 | 2021-03-30 | ||
| PCT/JP2022/014337 WO2022210345A1 (en) | 2021-03-30 | 2022-03-25 | Cyclone dust collecting device, and dust collection method employing cyclone dust collecting device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116829267A true CN116829267A (en) | 2023-09-29 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202280013530.2A Pending CN116829267A (en) | 2021-03-30 | 2022-03-25 | Cyclone dust collecting apparatus and dust collecting method using the same |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JP7435794B2 (en) |
| CN (1) | CN116829267A (en) |
| WO (1) | WO2022210345A1 (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0344749B1 (en) * | 1988-06-02 | 1995-02-01 | Cyclofil (Proprietary) Limited | Vortex tube separating device |
| CA1327948C (en) * | 1988-06-02 | 1994-03-22 | Willem Johannes Christian Prinsloo | Vortex tube separating device |
| JP3323781B2 (en) * | 1996-09-05 | 2002-09-09 | 日揮株式会社 | Gas transfer piping |
| US6280502B1 (en) * | 1998-12-31 | 2001-08-28 | Shell Oil Company | Removing solids from a fluid |
-
2022
- 2022-03-25 CN CN202280013530.2A patent/CN116829267A/en active Pending
- 2022-03-25 JP JP2022542338A patent/JP7435794B2/en active Active
- 2022-03-25 WO PCT/JP2022/014337 patent/WO2022210345A1/en active Application Filing
Also Published As
| Publication number | Publication date |
|---|---|
| WO2022210345A1 (en) | 2022-10-06 |
| JPWO2022210345A1 (en) | 2022-10-06 |
| JP7435794B2 (en) | 2024-02-21 |
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