Cyclone dust collecting device and dust collecting method using the same

Abstract

The cyclone dust collection device 1 collects dust DT from the treated gas TG containing dust DT. The aforementioned cyclone dust collection device includes: a dust separation section 3 that rotates the treated gas TG with the transverse direction as the rotation axis to separate dust from the treated gas TG; a dust recovery section 4 connected to the outlet side of the dust separation section 3 to recover the dust DT separated by the rotation of the treated gas TG caused by the dust separation section 3; and a gas recovery section 5 with the inlet provided in the dust recovery section 4 to recover the treated gas TG after the separation of dust DT. The first ratio L of the distance L from the outlet of the dust separation section 3 to the inlet of the gas recovery section 5 to the outlet diameter Dout of the dust separation section 3, L / Dout, is 0.4 or more and 1.0 or less.

Description

Technical Field

[0001] This invention relates to a cyclone dust collection device for collecting dust contained in a gas being processed, and a dust collection method using the cyclone dust collection device. Background Technology

[0002] For example, in a vertical iron-melting furnace such as a blast furnace, hot air is blown into the furnace through tuyeres located at the bottom, with heat sources such as iron and coke being alternately introduced in layers. The air blown from the tuyeres reacts with the carbon in the coke to generate heat, which melts the iron. The air rises within the furnace. The gas reaching the vicinity of the furnace top is discharged as dust containing various sizes of solid particles from coke and refractory materials within the furnace. Therefore, it is necessary to separate and collect the dust formed from the exhaust gas from the blast furnace.

[0003] In the past, various methods have been used to separate dust from gases being treated, and cyclone dust collectors are known as one example. Cyclone dust collectors separate dust from the gas being treated by causing it to swirl, thereby utilizing centrifugal force. Vertical and horizontal cyclone dust collectors are known types. Depending on the properties of the gas being treated and the installation environment, horizontal cyclone dust collectors with lower pressure loss are sometimes used (see, for example, Patent Documents 1 and 2).

[0004] Patent Document 1 discloses a horizontal cyclone dust collection device that causes the gas to be processed to swirl circumferentially along the inner wall of the internal space and move axially, thereby separating dust. As the gas swirls, the dust particles in it collide with the inner wall due to centrifugal force. At this time, the swirling motion component (swirling motion component) and the axially moving motion component (axial motion component) of the dust disappear, thus separating the dust from the gas being processed.

[0005] Patent document 2 discloses a horizontal cyclone dust collection device, which has a protrusion formed to extend radially inward from the inner wall toward the inner space and to extend circumferentially along the inner wall.

[0006] Existing technical documents

[0007] Patent documents

[0008] Patent Document 1: Japanese Patent Application Publication No. 2008-6315

[0009] Patent Document 2: Japanese Patent Application Publication No. 2011-218250 Summary of the Invention

[0010] The problem that the invention aims to solve

[0011] However, in the case of the cyclone dust collection devices described in Patent Documents 1 and 2, it is difficult to separate small dust particles (mass) from the gas being processed. Therefore, there is a problem of reduced recovery rate of fine dust in the cyclone dust collection device.

[0012] The present invention was made in view of the above-mentioned problems, and its object is to provide a cyclone dust collection device and a dust collection method using the cyclone dust collection device that can improve the recovery rate of fine dust.

[0013] Methods for solving problems

[0014] [1] A cyclone dust collection device that collects dust from a gas being processed. The cyclone dust collection device includes: a dust separation section that rotates the gas being processed with a transverse axis to separate dust from the gas being processed; a dust recovery section connected to the outlet side of the dust separation section to recover the dust separated by the rotation of the gas being processed caused by the dust separation section; and a gas recovery section whose inlet is provided in the dust recovery section to recover the gas being processed after the dust has been separated. The first ratio L of the distance L from the outlet of the dust separation section to the inlet of the gas recovery section to the outlet diameter Dout of the dust separation section is 0.4 or more and 1.0 or less.

[0015] [2] The cyclone dust collection device described in [1] includes: a main body having a gas flow path extending laterally; and a rectifier disposed in the gas flow path of the main body, so that the gas being processed flows laterally while swirling along the inner wall of the main body.

[0016] [3] In the cyclone dust collection device described in [1] or [2], the second ratio Dd / Dout of the inlet diameter Dd of the aforementioned gas recovery section and the outlet diameter Dout of the aforementioned dust separation section is 0.4 or more and 0.5 or less.

[0017] [4] The cyclone dust collection device described in any of [1] to [3], wherein the aforementioned gas recovery section is formed such that its diameter widens from the inlet side of the gas being processed toward the direction of travel.

[0018] [5] A dust collection method which uses the cyclone dust collection device described in any of [1] to [4] above.

[0019] Invention Effects

[0020] According to the cyclone dust collection device of the present invention, by making the first ratio L / Dout of the outlet diameter Dout of the dust separation section to the distance L from the outlet of the dust separation section to the inlet of the treated gas recovery section 0.4 or more and 1.0 or less, it is possible to suppress the retention of dust in the separation section and the increase of pressure loss, and improve the recovery rate of dust containing small solid particles. Attached Figure Description

[0021] [ Figure 1 [Image 1] is a schematic diagram illustrating a preferred embodiment of the cyclone dust collection device of the present invention.

[0022] [ Figure 2 ] is to show Figure 1 A schematic diagram of an example of the dust separation section in a cyclone dust collection device.

[0023] [ Figure 3 [1] is a graph showing the relationship between the first ratio L / Dout and the recovery rate when solid particles with a diameter of 75 μm flow into the dust recovery section.

[0024] [ Figure 4 [1] is a graph showing the relationship between the first ratio L / Dout and the recovery rate when solid particles with a diameter of 25 μm flow into the dust recovery section.

[0025] [ Figure 5 [This is a graph showing the first ratio L / Dout when solid particles with a diameter of 75 μm flow into the dust collection section and the retention rate of solid particles retained at the inlet of the dust collection section.]

[0026] [ Figure 6 [This is a graph showing the first ratio L / Dout when solid particles with a diameter of 25 μm flow into the dust collection section and the retention rate of solid particles retained at the inlet of the dust collection section.]

[0027] [ Figure 7 [1] is a graph showing the relationship between the second ratio Dd / Dout of the dust separation section outlet diameter Dout and the gas recovery section inlet diameter Dd, and the pressure loss.

[0028] [ Figure 8 [This is a graph showing the relationship between the second ratio Dd / Dout and the recovery rate when solid particles with a diameter of 75 μm flow into the dust recovery section.]

[0029] [ Figure 9 [1] is a graph showing the relationship between the second ratio Dd / Dout and the recovery rate when solid particles with a diameter of 25 μm flow into the dust recovery section.

[0030] [ Figure 10[This is a graph showing the relationship between the second ratio Dd / Dout and the retention rate when solid particles with a diameter of 75 μm flow into the dust recovery section.]

[0031] [ Figure 11 [1] is a graph showing the relationship between the second ratio Dd / Dout and the retention rate when solid particles with a diameter of 25 μm flow into the dust recovery section.

[0032] [ Figure 12 [Image 1] is a schematic diagram illustrating another embodiment of the cyclone dust collection device of the present invention. Detailed Implementation

[0033] Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings. Figure 1 This is a schematic diagram illustrating a preferred embodiment of the cyclone dust collection device of the present invention. Figure 1 The cyclone dust collector 1 is a horizontal cyclone dust collector that generates a swirling flow with the transverse axis to collect dust DT from the treated gas TG. The cyclone dust collector 1 includes: a dust separation section 3 that separates the dust DT from the treated gas TG that flows in from the gravity inlet pipe 2; a dust recovery section 4 that recovers the dust DT separated by the dust separation section 3; and a gas recovery section 5 that recovers the treated gas TG after the dust DT has been separated. It should be noted that the example is exemplified by the case where the inlet pipe 2 is connected to, for example, a blast furnace or converter, and the treated gas TG is exhaust gas discharged from the blast furnace or converter.

[0034] Figure 2 It is shown Figure 1 A schematic diagram of an example of the dust separation section in a cyclone dust collection device. Figure 2 The dust separation unit 3 rotates the treated gas TG with the transverse axis, separating the dust DT from the treated gas TG. The dust separation unit 3 includes: a main body 3A having a gas flow path extending laterally; and a rectifier 3B disposed in the gas flow path of the main body 3A, which moves the treated gas TG axially while rotating along the inner wall of the main body 3A.

[0035] The main body 3A has a hollow section, which may be, for example, cylindrical or conical in shape, and serves as a gas flow path. Figure 1In the illustrated example, the main body portion 3A has a conical shape, and the outlet diameter Dout of the main body portion 3A is larger than the inlet diameter Din (Dout > Din). Therefore, the diameter of the gas flow path in the main body portion 3A gradually widens from the upstream side toward the downstream side. It should be noted that in the following description, the gas flow path of the main body portion 3A is sometimes referred to as an expanding flow path. The rectifying member 3B is disposed in the hollow portion of the main body portion 3A to make the processed gas TG flowing into the main body portion 3A into a swirling flow. That is, the rectifying member 3B has a shape with a rectifying plate 3C formed in a spiral shape on the outer peripheral side, and the rectifying plate 3C makes the processed gas TG flowing in from the inlet side of the main body portion 3A flow along the rectifying plate 3C to become a swirling flow.

[0036] Especially because the main body portion 3A forms an expanding flow path, the processed gas TG becomes a swirling flow in which the radius of the spiral widens as it moves toward the downstream side (the outlet side) (hereinafter, sometimes referred to as an expanding swirling flow). Therefore, the swirling flow of the processed gas TG is more likely to separate from the rectifying plate 3C as it moves downstream in the flow direction of the processed gas TG, and can easily swirl along the inner wall of the main body portion 3A. It should be noted that in Figure 1 In the illustrated example, a case where the main body portion 3A forms an expanding flow path with the outlet diameter Dout of the main body portion 3A being larger than the inlet diameter Din (Dout > Din) is shown, but it is not limited to this. The shape of the main body portion 3A can be a cylindrical shape with the outlet diameter Dout equal to the inlet diameter Din (Dout = Din) according to the performance required by the cyclone dust collector 1. Alternatively, the shape of the main body portion 3A can be formed such that the outlet diameter Dout is smaller than the inlet diameter Din (Dout < Din), and the diameter gradually decreases from the inlet side toward the outlet side. The main body portion 3A can generate a swirling flow in any shape.

[0037] Figure 1 The dust recovery portion 4 shown in

[0038] The gas recovery unit 5 is the part that recovers the treated gas TG after the separation of dust DT, and is connected to a gas utilization side pipe (not shown). The gas recovery unit 5 is formed, for example, by a pipe with a diameter smaller than the outlet diameter Dout of the dust separation unit 3 and the dust recovery unit 4, and its inlet side is inserted into the dust recovery unit 4. When inserted into the dust recovery unit 4, the gas recovery unit 5 is arranged coaxially, for example, with its central axis aligned with the central axes of the dust separation unit 3 and the dust recovery unit 4. Furthermore, the gas recovery unit 5 is inserted into the dust recovery unit 4 with the dust chute 4B located below it.

[0039] See Figure 1 and Figure 2 An operational example of the cyclone dust collection device 1 will be described. The treated gas TG discharged from a blast furnace or converter flows into the dust separation section 3 via the inlet pipe 2. The treated gas TG becomes an expanded swirling flow due to its flow along the rectifier plate 3C of the dust separation section 3, and then flows into the dust recovery section 4. The dust DT contained in the treated gas TG collides with the inner wall of the main body 3A of the dust separation section 3 or the inner wall of the dust recovery section 4 due to the swirling flow, losing kinetic energy. As a result, the dust DT separates from the swirling flow of the treated gas TG and is recovered into the dust chute 4B. On the other hand, the treated gas TG after the dust DT is separated is recovered by the gas recovery section 5 and flows into a utilization side pipe (not shown).

[0040] Here, using Figure 1 The dust DT recovered by the cyclone dust collector 1 contains solid particles of various sizes. The critical particle size ds for the separation and capture of solid particles in the cyclone dust collector 1 can be obtained by the following formula (1).

[0041] [Formula 1]

[0042]

[0043] d s Critical particle size for separation and trapping [m]

[0044] μ: fluid viscosity [Pa·s]

[0045] r1: Inner diameter of rotation [m]

[0046] r2: Outer diameter of rotation [m]

[0047] N: Rotational speed [-]

[0048] v i Speed ​​[m / s]

[0049] ρ p Particle density [kg / m³] 3 ]

[0050] ρ a : Fluid density [kg / m 3

[0051] According to Equation (1), by increasing the motion component (swirling motion component) of the swirling dust DT, the critical separation and capture particle size ds can be reduced. Specifically, in order to reduce the critical separation and capture particle size ds, it is considered to make the denominator of Equation (1) a large value or make the numerator a small value. Here, among the dust DT recovered by the cyclone dust collector 1, the tiny solid particles refer to particles with a particle size of 100 μm or less. However, for example, when the dust DT has a tiny particle size of 100 μm or less, the separation in the dust separation section 3 becomes difficult, and the uncaught tiny solid particles flow into the gas recovery section 5 together with the processed gas TG.

[0052] Therefore, in order to improve the recovery rate of tiny solid particles, while keeping the swirling amount of the processed gas TG in the dust separation section 3 constant, various changes are made to the first ratio L / Dout, and the recovery rate of the tiny solid particles with small mass is studied through simulation. It should be noted that in the simulation, the particle sizes of the tiny solid particles that become the dust DT are set to 75 μm and 25 μm which are 100 μm or less, and the particle Reynolds number of the solid particles is set to about 100. In addition, the above-mentioned L is the distance between the dust separation component 3 and the gas recovery section 5 in the axial direction of the cyclone dust collector 1.

[0053] <s Figure 3 is a graph showing the relationship between the first ratio L / Dout and the recovery rate when solid particles with a particle size of 75 μm flow into the dust recovery section 4. Figure 4 is a graph showing the relationship between the first ratio L / Dout and the recovery rate when solid particles with a particle size of 25 μm flow into the dust recovery section 4. It should be noted that the recovery rate refers to the ratio of the amount of solid particles recovered by the dust chute 4B to the total amount of solid particles flowing in from the inflow pipe 2.

[0054] In Figure 3 when the particle size is 75 μm, the larger the first ratio L / Dout, the smaller the recovery rate. On the other hand, in Figure 4 when the particle size is 25 μm, when the first ratio L / Dout is in the range of 0 or more and 0.75 or less (0 ≤ L / Dout ≤ 0.75), the recovery rate decreases as the first ratio L / Dout increases. In addition, when the first ratio L / Dout is larger than 0.75 (0.75 < L / Dout), the recovery rate increases as the first ratio L / Dout increases. Considering Figure 3 and Figure 4 ​It can be seen that as long as the first ratio L / Dout is less than or equal to 1.0 (L / Dout≤1.0), the dust DT can travel a distance of more than L while maintaining the amount of motion in the direction of separation. Moreover, it is possible to recover tiny solid particles as required by the cyclone dust collection device 1.

[0055] However, simply setting the upper limit of the first ratio L / Dout as described above cannot improve the recovery rate, i.e., it cannot increase the recovery rate. While the dust DT is separated by the swirling flow, it moves towards the dust chute 4B in the direction of the swirling flow. The swirling flow is a complex fluid motion that constantly changes the center of swirling, resulting in sections where countercurrents occur. This tendency is particularly strong in enlarged swirling flows where the diameter of the swirling flow of the treated gas TG increases as it moves downstream because the outlet diameter Dout of the dust separation section 3 is larger than the inlet diameter Din of the dust separation section 3. Small solid particles tend to move in the same direction as the treated gas TG and are retained at the boundary between the dust separation section 3 and the dust recovery section 4 due to the countercurrent, i.e., at the outlet of the dust separation section 3 and the inlet of the dust recovery section 4. The retained solid particles may flow towards the gas recovery section 5 along with the treated gas TG. Therefore, the relationship between the tiny solid particles retained at the inlet of the dust collection unit 4 and the first ratio L / Dout was studied.

[0056] Figure 5 This is a graph showing the first ratio L / Dout when solid particles with a diameter of 75 μm flow into the dust collection section 4 and the retention rate of solid particles retained at the inlet of the dust collection section 4. Figure 6 This is a graph showing the first ratio L / Dout when solid particles with a diameter of 25 μm flow into the dust collection section 4, and the retention rate of solid particles retained at the inlet of the dust collection section 4. It should be noted that the retention rate refers to the ratio of the amount of solid particles retained at the inlet of the dust collection section 4 (i.e., the outlet of the dust separation section 3) to the total amount of solid particles flowing in from the inlet pipe 2.

[0057] Figure 5 When the particle size of the solid particles is 75 μm, the larger the first ratio L / Dout, the lower the retention rate. Additionally, as... Figure 5 As shown, the overall performance is suppressed to a low level regardless of the magnitude of the first ratio L / Dout. On the other hand, Figure 6 When the particle size of the solid particles is 25 μm, as the first ratio L / Dout decreases, the retention of solid particles at the inlet of the dust collection unit 4 due to backflow increases. Considering... Figure 5 and Figure 6Based on the retention rate, it can be seen that as long as the first ratio L / Dout is 0.4 or higher, there is no problem with the retention of dust DT at the inlet of the dust collection section 4. This is because as long as the first ratio L / Dout is 0.4 or higher, the extreme pressure distribution after passing through the dust separation section 3 can be eliminated, ensuring sufficient space to prevent backflow. Therefore, the first ratio L / Dout is set to 0.4 or higher. Especially... Figure 6 In the case where the first ratio L / Dout is 0.5 or higher, the retention rate can be suppressed to below 5%, which is therefore preferred.

[0058] Here, as Figure 3 and Figure 4 As shown, from a recovery rate perspective, the smaller the first ratio L / Dout, the greater the recovery rate. Figure 5 and Figure 6 As shown, from the perspective of retention rate, the larger the first ratio L / Dout, the smaller the retention rate. According to... Figure 5 and Figure 6 From the perspective of retention rate, as long as the first ratio L / Dout is 0.45 or higher, the retention rate can be suppressed to below 5%. Therefore, the lower limit of the first ratio L / Dout is preferably 0.45. On the other hand, as described above... Figure 4 As shown, even when the particle size of dust DT is 25 μm, the recovery rate increases as the first ratio L / Dout decreases, provided that the first ratio L / Dout is 0.75 or less. Therefore, the upper limit of the first ratio L / Dout is preferably 0.75. Moreover, as... Figure 3 As shown, as long as the first ratio L / Dout is below 0.65, the recovery rate of DT dust with a particle size of 75 μm can be maintained at over 50%. Therefore, the upper limit of the first ratio L / Dout is more preferably 0.65.

[0059] As described above, the outlet diameter Dout of the dust separation unit 3 and the distance L between the dust separation unit 3 and the gas recovery unit 5 are set such that the first ratio L / Dout is 0.4 or higher and 1.0 or lower. This suppresses the retention of fine dust particles and improves the recovery rate, while also preventing fine dust particles from mixing into the gas recovery unit 5.

[0060] Here, in the cyclone dust collection device 1 according to the embodiment of the present invention, the first ratio L / Dout can be set in the range of 0.4 or more and 1.0 or less (0.4 ≤ L / Dout ≤ 1.0), but in order to further improve the recovery rate, the configuration described below is preferred. That is, it is preferred that the first ratio L / Dout is set in the above-mentioned range, and a second ratio Dd / Dout is considered, taking into account the outlet diameter Dout of the dust separation section 3 and the inlet diameter Dd of the gas recovery section 5. In the case of using the horizontal cyclone dust collection device 1, the capacity of the exhaust fan is assumed to be not large. Therefore, the increase in pressure loss becomes the cause of the decrease in dust collection performance. Figure 1 As shown, the gas recovery unit 5 has a smaller diameter than the dust separation unit 3 and the dust recovery unit 4, resulting in pressure loss during gas recovery. Therefore, the influence of the pressure loss caused by the inlet diameter Dd of the gas recovery unit 5 and the outlet diameter Dout of the dust separation unit 3 on the recovery rate of minute dust DT was investigated.

[0061] Figure 7 This is a graph showing the relationship between the second ratio Dd / Dout and pressure loss. Figure 7 As can be seen from the data, when the second ratio Dd / Dout is less than 0.4 (Dd / Dout < 0.4), the pressure loss increases sharply as the second ratio Dd / Dout decreases. Therefore, from the perspective of pressure loss, it is desirable for the second ratio Dd / Dout to be above 0.4.

[0062] On the other hand, it is assumed that a second ratio Dd / Dout close to 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 are the same diameter, and the dust DT contained in the swirling flow flows directly into the gas recovery unit 5. Therefore, with Figures 3-6 Similarly, the relationship between the second ratio Dd / Dout and the recovery and retention rates was studied.

[0063] Figure 8 This is a graph showing the relationship between the second ratio Dd / Dout and the recovery rate when solid particles with a diameter of 75 μm flow into the dust recovery section 4. Figure 9 This is a graph showing the relationship between the second ratio Dd / Dout and the recovery rate when solid particles with a diameter of 25 μm flow into the dust recovery section 4. It should be noted that... Figure 8 and Figure 9 In this case, the first ratio L / Dout is fixed at 0.75.

[0064] like Figure 9 As shown, with a solid particle size of 25 μm, the recovery rate is in the range of 6 ± 2% independent of the second ratio Dd / Dout. On the other hand, as... Figure 8As shown, when the solid particle size is 75 μm, a recovery rate of over 70% can be ensured when the second ratio Dd / Dout is 0.5 or less (Dd / Dout ≤ 0.5). Furthermore, it is known that when the second ratio Dd / Dout is greater than 0.5 (Dd / Dout > 0.5), the recovery rate decreases sharply. Therefore, it is desirable to set the second ratio Dd / Dout to 0.5 or less.

[0065] Figure 10 This is a graph showing the relationship between the second ratio Dd / Dout and the retention rate when solid particles with a diameter of 75 μm flow into the dust recovery section 4. Figure 11 This is a graph showing the relationship between the second ratio Dd / Dout and the retention rate when solid particles with a diameter of 25 μm flow into the dust collection section 4. (See figure) Figure 10 and Figure 11 As shown, when the second ratio Dd / Dout is 0.4 or higher, the retention rate of small solid particles is suppressed to a low level, below 10%. As described above, considering the reduction of pressure loss, the improvement of recovery rate and retention rate, it is preferable that the second ratio Dd / Dout is 0.4 or higher and 0.5 or lower (0.4 ≤ Dd / Dout ≤ 0.5).

[0066] Figure 12 This is a schematic diagram illustrating another embodiment of the cyclone dust collection device of the present invention. It should be noted that, in Figure 12 In the cyclone dust collection device 100, for the... Figure 1 The cyclone dust collection device 1 has parts with the same structure marked with the same reference numerals and their descriptions are omitted. Figure 12 Cyclone dust collection device 100 and Figure 1 The difference between the cyclone dust collection device 1 and the gas recovery unit 105 is that the diameter of the gas being processed TG increases from upstream to downstream in the flow direction.

[0067] Figure 12 The gas recovery section 105 is formed by a diffuser tube whose diameter increases from the inlet side towards the downstream. The cone angle θ of the gas recovery section 105 is preferably an angle at which the flow of the treated gas TG does not detach from the inner wall of the gas recovery section 105. Considering the general jet divergence angle, it can be 15° or less, and more preferably 12.5° or less. Thus, the gap between the flow of the treated gas TG flowing into the gas recovery section 105 from the inlet and the inner wall of the gas recovery section 105 can suppress the generation of turbulence and eddies that would increase pressure loss.

[0068] Right now, Figure 1The gas recovery unit 5 shown is sometimes connected to a utilization-side pipe (not shown), the diameter of which is larger than the inlet diameter Dd of the gas recovery unit 5. In this case, a sharp step difference occurs in the pipe cross-section at the connection between the gas recovery unit 5 and the utilization-side pipe. At the connection, the airflow detaches from the wall of the gas recovery unit 5, increasing the pressure loss. Therefore, by making the gas recovery unit 5... Figure 12 The diffuser (gas recovery unit 105) shown in the diagram can suppress the increase in pressure loss caused by the gas flow detaching from the wall of the gas recovery unit 5.

[0069] Even the Figure 12 The cyclone dust collection device 100 shown in the figure, through communication with... Figure 1 Similarly, by setting the first ratio L / Dout to 0.4 or more and 1.0 or less (0.4 ≤ L / Dout ≤ 1.0), the recovery rate of fine dust can also be improved. In addition, by setting the second ratio Dd / Dout to 0.4 or more and 0.5 or less (0.4 ≤ Dd / Dout ≤ 0.5), the recovery rate can be further improved.

[0070] This invention is not limited to the embodiments described above and various modifications are possible. In the embodiments described above, the treated gas TG is exemplified as exhaust gas from a blast furnace or converter, but its application is not limited as long as it is a gas used to separate dust DT contained in the object being treated. Furthermore, Figure 2 The example shown illustrates a dust separation unit 3 with a rectifier component 3B having a rectifier plate 3C at its center within the main body 3A. However, this is not a limitation; the dust separation unit 3 can be configured to generate a swirling flow. For example, the rectifier component 3B can be a rectifier plate mounted on the inner wall of the main body 3A.

[0071] Explanation of reference numerals in the attached figures

[0072] 1. 100 Cyclone Dust Collection Device

[0073] 2 Inflow pipe

[0074] 3 Dust Separation Section

[0075] 3A Main Body

[0076] 3B rectifier components

[0077] 3C rectifier board

[0078] 4. Dust Recovery Department

[0079] 4A Rotation Space Section

[0080] 4B Dust Chute

[0081] 5. 105 Gas Recovery Unit

[0082] DT dust

[0083] Dd gas recovery unit inlet diameter

[0084] Dout dust separation unit outlet diameter

[0085] TG processed gas

Claims

1. A cyclone dust collection device for collecting dust from the gas being treated discharged from a blast furnace or converter, the cyclone dust collection device comprising: Inflow pipe, which is connected to the blast furnace or converter; A dust separation section is connected to the inflow pipe and rotates the gas being treated that flows in from the inflow pipe with the transverse direction as the axis of rotation, thereby separating the dust from the gas being treated. A dust recovery unit, formed as a bottomed cylindrical section, is connected to the outlet side of the dust separation unit to recover the dust separated by the swirling of the treated gas caused by the dust separation unit; and A gas recovery unit, with its inlet located within the dust recovery unit, recovers the treated gas after the dust has been separated. The first ratio of the distance L from the outlet of the dust separation unit to the inlet of the gas recovery unit to the outlet diameter Dout of the dust separation unit, L / Dout, is 0.4 or more and 1.0 or less. The dust recovery unit includes: a swirling space disposed between the outlet of the dust separation unit and the inlet of the gas recovery unit; and a dust chute, which is directly connected to the downstream side of the swirling space of the dust recovery unit in the flow direction of the gas being processed and is disposed at the bottom of the dust recovery unit. The dust separation section, the swirling space section, and the gas recovery section are arranged along the swirling axis. The dust separation section is configured such that its inner diameter gradually widens from the upstream side to the downstream side in the flow direction of the gas being processed. The inner diameter of the swirling space section is set to be the same as the outlet diameter Dout of the dust separation section. The dust separated by the swirling of the gas being processed collides with the inner wall of the swirling space and is then recovered by the dust chute.

2. The cyclone dust collection device as described in claim 1, wherein, The dust separation unit includes: a main body having a gas flow path extending laterally; and a rectifier disposed within the gas flow path of the main body, causing the gas to be processed to flow laterally while swirling along the inner wall of the main body.

3. The cyclone dust collection device as described in claim 1 or 2, wherein, The second ratio of the inlet diameter Dd of the gas recovery section to the outlet diameter Dout of the dust separation section, Dd / Dout, is 0.4 or more and 0.5 or less.

4. The cyclone dust collection device according to any one of claims 1 to 3, wherein, The gas recovery section is configured such that its diameter widens from the inlet side of the gas being processed toward the direction of travel.

5. A dust collection method, wherein the cyclone dust collection device according to any one of claims 1 to 4 is used.

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