KR100844288B1 - Method and device for the separation of dust particles - Google Patents

Abstract

The apparatus for separating particles MP from flue gas flow F has a horizontal flue that passes while flue gas flow F passes from first position P1 to second position P2 substantially horizontally. It has a gas duct 18. In a first position P1 the device 16 has a baffle device 32 comprising at least one plate 34, 36, 38, wherein the at least one plate carries particles MP in the flue gas duct 18. Inclined to deflect the particles MP into the lower portion 42, and is installed in the flue gas duct 18. In the second position P2, the device 16 flues to collect particles MP deflected downwardly by plates 34, 36, 38 into the lower portion 42 of the flue gas duct 18. It has a collecting means 40 which is installed in the lower part 42 of the gas duct 18.

Dust, particle, flue gas, flow, duct, baffle device, SCR reactor

Description

METHOD AND DEVICE FOR THE SEPARATION OF DUST PARTICLES

The present invention relates to a method for separating particles from a flue gas flow passed from a first position to a second position substantially horizontally within a flue gas duct.

The invention also relates to an apparatus for separating particles from a flue gas flow, the apparatus having a horizontal flue gas duct through which flue gas passes from a first position to a second position substantially horizontally.

Above all, flue gas purification plants for coal-fired and oil-fired power plants, waste incinerators, etc. often have what are called SCR reactors. Selective Catalytic Reduction (SCR) reactors include reactors in which selective reduction of nitrogen oxides induced by catalytic reactions occurs. SCR reactors often have a catalyst composed of a honeycomb or multiple adjacent plates to provide the maximum reaction surface. A disadvantage for many SCR reactors is that fine dust formed, for example when burning coal, oil, and waste, gets stuck in the SCR reactor and hinders operation.

Kaneko et al., US Pat. No. 5,687,656, disclose a method of reaching the SCR reactor to reduce the amount of dust impeding operation. In the method according to US Pat. No. 5,687,656, the flue gas first passes through the horizontal flue gas duct, then through the vertical flue gas duct, and then passes through a porous plate having a smaller pore size than the particles.

The process according to US 5,687,656 can reduce the amount of dust leading to the SCR reactor. However, a problem with this porous plate is that there is a risk of being blocked by dust particles. This failure increased operating pressure by increasing pressure drop.

It is an object of the present invention to provide a method of separating particles from flue gas, which completely or partially eliminates these disadvantages.

The object is a method of separating particles from a flue gas flow that is delivered substantially horizontally from a first position to a second position in a flue gas duct, wherein in the first position, the particles are disposed underneath the flue gas duct. Deflected downward in the portion, and in the second position, the particles are collected in the lower portion of the flue gas duct.

The advantage of this method is that the deflection in the first position, which can be provided by simple means and a low pressure drop can be provided, surprisingly provides a significant up-concentration of the particles in the lower part of the duct. In particular, large particles, such as particles larger than about 1 mm, are highly deflected so that they are not redispersed in the flue gas flow. Collection in the second location takes place in the lower part of the flue gas duct, i.e. where the particles are collected. This means that the collection only needs to occur from the partial flow of the flue gas flow in which particles are collected, not from the entire flue gas flow.

In a preferred embodiment, the particles are deflected downwards at an angle of 40 to 70 ° with respect to the horizontal plane. It is known that an angle of 40-70 ° provides the optimum deflection of the particles. At angles less than about 40 °, the deflection does not occur large enough, so that the particles do not collect in the lower part of the flue gas duct but redisperse in the flue gas. At angles greater than about 70 °, the pressure drop increases. The deflection is also so great that there is a risk that the particles will reflect off the bottom of the flue gas duct and redisperse in the flue gas flow.

In a preferred embodiment, the flue gas flow F is divided into a first partial flow and a second partial flow in a second position, the first partial flow comprising the deflected particles and collected deflected from the lower portion of the flue gas duct It is delivered downward into the chamber. The first partial flow provides a simple and reliable method of removing some removable portions of particles collected in the lower portion of the flue gas duct from the flue gas flow.

Preferably, the first partial flow is made to spin rapidly in the collection chamber, whereby particles exit from the first partial flow and are separated in the collection chamber. Removing particles by centrifugal force from the first partial flow has the advantage that nets, porous plates and other means that can be easily clogged are not required to separate the particles. This provides considerable reliability in operation.

In a preferred embodiment, as the flue gas flow is transferred from the first position to the second position, the velocity of the flue gas flow is reduced by a factor of 1.2 to 2.5. An advantage of this is that particles deflected from the first position to the lower part of the flue gas duct are not redispersed into the flue gas flow as they are transferred from the first position to the second position. On the other hand, the decreasing gas velocity causes more particles to collect in the lower part of the duct due to the settling effect.

The present invention also aims to provide an apparatus for effectively separating particles from flue gas, which completely or partially overcomes the above mentioned disadvantages.

This object is achieved by a device of the type defined in the manner of the introduction, which comprises a baffle arrangement in a first position and a collecting means in a second position, the baffle apparatus being At least one plate inclined to deflect the particles into the lower portion of the flue gas duct, the collecting means being disposed in the flue gas duct by the plate into the lower portion of the flue gas duct It is disposed in the lower part of the flue gas duct to collect particles deflected in the downward direction. The advantage of this device is that it allows effective separation of particles that are expected to clog the SCR reactor without causing a high pressure drop or the risk of failure of the device.

In a preferred embodiment, the at least one plate forms an angle α of 40 to 70 ° with respect to the horizontal plane. This angled plate allows the particles to be effectively reflected to the lower portion of the flue gas duct.

Preferably, the collecting means has a deflection wall, the deflection wall extending into the flue gas duct opposite the flow direction of the flue gas flow in the lower part of the flue gas duct, terminated by a deflection line on the bottom of the flue gas duct And to deflect a partial flow comprising deflected particles from the flue gas flow and to be delivered into a collection chamber contained in the collecting means. The deflection wall makes it possible to collect particles deflected in the first position effectively without causing a high pressure drop or the risk of failure.

Suitably, the collection chamber has a collection wall, which extends from the portion of the collection chamber located closest to the first position to the deflection wall at a level below the deflection line. The advantage of the collection wall is that it improves the removal of particles from the partial flow and reduces the risk of already separated particles in the collection chamber entering the flue gas flow.

The baffle device suitably comprises at least three beveled plates. The baffle device may be provided with at least three inclined plates, have a low pressure drop, and cause a small risk of passing the baffle device without particles being reflected off the plate and deflected into the lower portion of the flue gas duct. Depending on the height in the vertical direction of the flue gas duct, it may be convenient to use more plates, such as 4, 5 or 6 or more plates.

In a preferred embodiment, the cross-sectional area of the horizontal flue gas duct is 1.2 to 2.5 times larger in the second position than in the first position. This relationship between the cross-sectional areas means that the velocity of the flue gas is reduced, which improves the separation of particles at the second location. The cross-sectional area of the flue gas duct in the second location should be at least 1.2 times the cross-sectional area of the flue gas duct in the first location, to prevent particles deflected into the lower portion of the flue gas duct from redispersing into the flue gas. In an area relationship larger than 2.5 times, separation of very small particles is also provided, which does not pose a risk of clogging, for example, but rather separates in a dust separator placed after the SCR reactor.

Preferably, the length of the flue gas duct from the first position to the second position is at least twice the characteristic cross sectional dimension, such as the diameter or height at the first position. This length also gives particles located close to the top end of the flue gas duct when deflected by the baffle device to provide sufficient time to move to the lower part of the flue gas duct to be separated in the collecting means. If the cross sectional area of the flue gas duct increases from the first position to the second position, the above-mentioned length also needs to take time for the flue gases to spread over the increased cross sectional area, in which case a reduction in the required speed occurs. .

In addition, the features and advantages of the present invention will become apparent from the following description and the accompanying drawings.

The invention will be described in more detail by reference to the accompanying drawings, in which: FIG.

1 is a schematic side view of a power plant in which a device according to the invention is installed;

2 shows a side view of the device according to the invention in more detail.

3 is a side view showing how particles are deflected and collected in the apparatus shown in FIG.

4 is a side view showing how particles are deflected and collected in an alternative embodiment of the device according to the invention.

5 is a side view illustrating a baffle arrangment according to an alternative embodiment.

6 is a side view showing a baffle device according to another alternative embodiment.

Figure 7 is a side view showing another alternative embodiment of the present invention.

1 shows a power plant 1. The power plant 1 has a boiler 2, which is burned by contact with air supplied with fuel such as coal, oil, and waste. The flue gases F and particles formed during combustion are passed through the duct 4 to a flue gas cooler 6, also called an economiser. As the flue gases pass vertically downward through the package 8 of tubes, indirect contact with the feed water of the boiler 2 takes place, whereby heat is extracted from the flue gases in the flue gas cooler 6. The flue gas cooler 6 has in its lower part 10 a dust hopper 12 which collects coarse particles. The discharge device 14 is used to remove these collected coarse particles. In the lower part 10 of the flue gas cooler 6 the flue gases change from a vertical flow to a horizontal flow and are delivered to the device 16 according to the invention.

The device 16 has a horizontal flue gas duct 18 that delivers flue gases from a first location P1 to a second location P2 in a substantially horizontal direction, where the first location P1 is a flue gas duct. 18 is located at the point where it is connected to the lower part 10 of the flue gas cooler 6, and the second position P2 is the flue gas duct 20 in which flue gases are vertically changed so that the flue gases are changed vertically. ) Is the vertically upward point. The flue gas is then turned 180 degrees and delivered to the SCR reactor 22 for the selective catalytic reduction of nitrogen oxides. In the illustrated embodiment, the SCR reactor 22 has three catalyst layers 24, 26, 28 including a catalyst formed in a honeycomb structure. Flue gases pass through a number of narrow ducts with openings typically of 4 mm x 4 mm cross section into the catalyst, while the nitrogen oxide content of the flue gas is reduced. The flue gases leave the SCR reactor 22 through the gas duct 30 and are then further purified in the electrostatic precipitator and flue gas desulfurization plant, not shown in FIG. 1, and released into the atmosphere.

The particles collected in the dust hopper 12 are only the coarsest particles. Thus the flue gas leaving the lower part 10 of the flue gas cooler 6 contains a very large number of particles of very small size, if they reach the catalyst layers 24, 26, 28 they are of a honeycomb structure. It will block narrow ducts and cause increased pressure drop and attenuation of nitrogen oxides. In order to avoid these problems, the device 16 has three inclined plates 34, 36, 38 in one position P1 and a baffle device having a collecting means 40 in the second position P2. arrangement 32 has been provided.

2 shows the device 16 in more detail. As mentioned above, the baffle device 32 arranged in the first position P1 has three plates 34, 36, 38. These plates, which are arranged vertically in turn, are inclined to deflect flue gases in the form of flue gas flow F, in particular the lower part 42 of the flue gas duct 18 by means of a "bouncing effect". Deflect downward). As can be clearly understood from FIG. 2, the plates 34, 36, 38 are inclined at an angle α of about 45 ° with respect to the horizontal plane seen in the flow direction of the flue gas flow F, thus When viewed in the flow direction of the flue gas flow (F) is directed downward. As shown in FIG. 2, the flue gas duct 18 has an upper wall 44 which is tilted upward at an angle β with respect to the horizontal plane when viewed in the flow direction of the flue gas flow F. As shown in FIG. The angle β is about 10 degrees. This angle means that the cross-sectional area A2 of the flue gas duct 18 at the second position P2 is about 1.5 times the cross-sectional area at the first position P1. The flue gas duct 18 has a length L, which is about 3.5 times the dimension D of the flue gas duct 18, which may be height or diameter depending on the shape of the duct at the first location P1.

The collecting means 40, which is arranged in the lower part 42 of the flue gas duct 18, is located in the second position P2. The collecting means 40 is arranged in the lower part of the flue gas duct 18 and is in the shape of an isosceles triangle with the center vertex facing down. The walls of the collection chamber 46 form an angle γ of about 60 ° with respect to the horizontal plane. A discharge device 48, which may include a fluid transfer system, is used to periodically empty the collection chamber 46. The collecting means 40 also has a deflection wall 50 extending in the lower portion 42 of the flue gas duct 18 into the flue gas duct 18 in a direction opposite the flow direction of the flue gas flow. As shown in FIG. 2, the wall 50 starts at the end of the collection chamber 46, which is a far end when viewed in the flue gas flow direction, and extends obliquely upwards into the flue gas duct 18. The deflection wall 50 forms an angle δ of about 60 ° with respect to the horizontal plane and is terminated by the deflection line 52 across the flue gas duct 18 extending in the horizontal direction. The rear wall 54 included in the vertical flue gas duct 20 extends from the deflection line 52 in the flue gas flow direction.

The collection chamber 46 also has a collection wall 56, which extends from the wall 58 of the collection chamber 46 to the deflection wall 50 closest to the first position P1 and also in its vertical direction. The level is located below the vertical level of the deflection line 52 located above the sea 60 of the flue gas duct 18.

FIG. 3 shows how flue gases F and medium-sized particles MP can be expected to move within the device 16 during operation. Medium-sized particles herein refer to particles larger than about 1 mm but smaller than about 10 mm, with a particle size of 10 mm is the particle size expected to cause the biggest problems of blocking holes in the catalyst layers 24, 26, 28. . The coarse particles, which refer to particles of about 10 mm or more size, will mostly be separated in the dust hopper 12 of the flue gas cooler 6, but otherwise they will also be separated in the device 16. Fine particles pointing to particles smaller than 1 mm will only be separated to a limited extent in the device 16. As mentioned above, when the flue gas flow F leaves the lower portion 10 of the flue gas cooler 6, it is flowed back in a substantially horizontal flow direction. As the flue gas flow F arrives at the baffle apparatus 32 arranged at the first point P1, the flue gas flow F is deflected downwards so that the lower portion 42 of the flue gas duct 18 Headed to. The velocity of the flue gas flow F in the first position P1 is about 20 m / s. When the flue gas flow F is delivered to the second position P2, the effects of deflection are substantially lost, and the flue gas flow F at the second position P2 has a substantially constant gas velocity profile. Will have Since the cross-sectional area A2 at the second position P2 is larger than the cross-sectional area A1 at the first position P1, the velocity of the flue gas flow F gradually decreases, so that at the second position P2 It will be about 13m / s.

The medium-sized particles MP impinge on the plates 34, 36, 38 and reflect downwardly of the lower portion 42 of the flue gas duct 18, as can be clearly seen from FIG. 3. do. 3 shows the patterns of typical particles for these particles MP in dotted lines. As shown in FIG. 3, some particles MP have an oblique upward upward movement when leaving the lower part of the flue gas cooler 6, but these particles MP also have plates 34, 36. , 38). Thus, after being reflected down into the lower portion 42 of the flue gas duct 18, the medium-sized particles MP are not redispersed into the flue gas flow F and the bottom 60 of the duct 18. Will continue to follow. The baffle device 32 will have an equalizing effect on the velocity profile of the flue gas flow F in the flue gas duct 18 and swirls to swirl the particles MP from the lower portion 42. Will reduce the formation of eddy. The fact that the velocity of the flue gas flow F decreases as it goes from the first position P1 to the second position P2 also indicates that the flue gas flow F retains medium-sized particles MP again. Thereby reducing the tendency to import them. In contrast, the settling effect is achieved due to this decrease in velocity, and the medium-sized particles MP are moved closer to the bottom 60 of the duct 18. In the second position P2, the deflection line 52 in which the stagnation point is formed deflects the first partial flow FP which is transmitted downward into the collection chamber 46 by the deflection wall 50. The deflection line 52 should be located at a level above the floor 60 and the deflection wall 50 should have an angle δ relative to the horizontal plane so that the first partial flow FP is formed in the collection chamber 46. It has a maximum gas velocity of about 5-6 m / s in the stationary vortex. The remaining flue gas flow is deflected into the flue gas duct 20 vertically upwards by the wall 54 as the second partial flow FF. The deflected first partial flow FP carries medium-sized particles MP and presses them downward into the collection chamber 46. In the collection chamber 46, the partial flow FP causes a rapid rotation so that the medium-sized particles MP are separated under pressure by centrifugal force opposite the walls 58 of the chamber 46. The collection wall 56 contributes to the rapid rotation forced by the partial flow FP and also increases the amount of particles MP removed from the partial flow FP. Moreover, collection wall 56 reduces the risk of particles entering the flue gas from collection chamber 46 and redispersing. As can be clearly seen from FIG. 3, the partial flow FP will spin rapidly past the collection wall 56 and again mix with the flue gas flow. Depending on the design of the collecting means 40, the partial flow FP may form a somewhat stable, stationary vortex in the collection chamber 46, which makes a large or small gas exchange with the main flue gas flow. However, regardless of gas exchange, partial flow FP will bring particles MP into collection chamber 46.

4 shows an alternative embodiment in accordance with the present invention in the form of an apparatus 116. The device 116 has a horizontal flue gas duct 118 that carries the flue gas flow F from the first position P1 to the second position P2 in a substantially horizontal direction, the first position P1. ) Is located at the portion where the flue gas duct 118 is connected with the flue gas cooler (not shown in FIG. 4), and the second position P2 is the flue gas duct 120 in which the flue gas flow F is horizontal. Is the point delivered horizontally within the SCR reactor (not shown in FIG. 4). The device 116 also has a baffle device 132 in a first position P1, which has a beveled plate 134, 136, 138, of the same type as the baffle device 32 described above. . In the baffle device 132, the medium-sized particles MP are deflected, ie “bounced” downwards into the lower portion 142 of the flue gas duct 118. In the second position P2, the device 116 has a collecting means 140 having a collecting chamber 146 of the same type as the chamber 46 shown in FIG. 2. The collecting means 140 also extends into the flue gas duct 118 in a direction opposite to the flow direction of the flue gas flow F and is a deflection line 152 located above the bottom 160 of the flue gas duct 118. Has a horizontal deflection wall 150 terminated by. Within the collection chamber 146 is mounted a collection wall 156 of the same type as the collection wall 56 and extending at a level below the deflection wall 150. As shown in FIG. 4, the deflection wall 150 at an angle of 0 ° relative to the horizontal plane thus deflects a partial flow FP that is transmitted down the interior of the chamber 146 in the deflection line 152. Particles MP of size cause a rapid rotation during separation. The remaining flue gas flow, represented by the partial flow FF, continues into the horizontal flue gas duct 120. Partial flow FF also includes flue gases leaving chamber 146, which means that partial flow FF is the same size as flue gas F supplied to flue gas duct 118. There will be. The deflected partial flow FP in the chamber 146 forms a stationary vortex that makes some exchange with the rest of the flue gas flow. The flue gas duct 118, which is the same as the flue gas duct 18 shown in FIG. 2, has a top wall 144 inclined upward with respect to the horizontal plane when viewed in the flow direction of the flue gas flow. Thus, the velocity of the flue gas flow is smaller at the second point P2 compared to the first point P1, which risks the particles MP reflected below the lower portion 142 again dispersing into the flue gas. Decreases. In an alternative embodiment, the deflection wall 150 may be provided with a hinge at its attachment point, thus adjusting the angle of the wall 150 relative to the horizontal plane and thus the appropriate first partial flow FP in FIG. 4. Rotations shown in dotted lines are possible.

5 illustrates a baffle device 232 according to an alternative embodiment. The baffle device 232 arranged in the flue gas duct 218 of the same type as the flue gas duct 18 described above has five inclined plates 234, 235, 236, 237, 238. These plates are inclined at an angle ε of about 45 ° with respect to the horizontal plane, so that when viewed in the flow direction of the flue gas flow F, the line is tilted upwards. Thus, the plates 234, 235, 236, 237, 238 are not positioned one after another vertically upwards. As can be clearly seen from FIG. 5, the plates 234, 235 overlap each other by the distance O when viewed in the horizontal direction (the remaining plates overlap correspondingly with each other). This overlap O reduces the risk that the particles MP can pass through the baffle device 232 without colliding against the plates 234, 235, 236, 237, 238. Two typical travel paths for the medium-sized particles MP are also shown in FIG. 5.

6 illustrates a baffle device 443 according to another alternative embodiment. The baffle device 332 arranged in the flue gas duct 318 of the same type as the flue gas duct 18 described above has three tiltable plates 334, 336, 338. As shown by each plate indicated by a dashed line in FIG. 6, each plate 334, 336, 338 can be rotated on the accessory horizontal shafts 335, 337, 339. Horizontal shafts 335, 337, 339 are connected to actuator 341, which actuator is schematically illustrated and disposed outside the flue gas duct 318, and guide rail 343 connected to motor 345. It includes. The position of the guide rail 343 in the vertical direction can be set by the motor 345, and consequently the plates 334, 336, 338 can be rotated at a desired angle α with respect to the horizontal plane. Thus, the value of the angle α that sufficiently separates medium-sized particles to prevent clogging the pores of the SCR reactor without causing unnecessary high pressure drop across the baffle device 332 can be determined by experiment. The baffle device 332 can also be configured such that the plates can be rotated at an angle α of 90 with respect to the horizontal plane, in which case the baffle device 332 can also act as a shut-off damper. .

7 illustrates an apparatus 416 according to another alternative embodiment. A device 416 is connected behind the flue gas cooler 406 partially shown in FIG. 7, which is very similar to the device 16 shown in FIG. The flue gas cooler 406 is passed through a vertical flue gas flow F that is directed upwards. At the upper end 410 of the flue gas cooler 406, flue gas flow F is turned in the horizontal flow direction and flows into the apparatus 416. The device 416 has a flue gas duct 418 and a baffle device 432 arranged therein and having three sloped plates 434, 436, 438. As can be clearly seen in FIG. 7, the medium-sized particles MP are reflected on the plates 434, 436, 438 and are highly deflected below the lower portion 442 of the duct 418. . The baffle apparatus 432 also deflects the flue gas flow F and makes the gas velocity profile constant in the duct 418. This reduces the risk of the deflected particles MP being dispersed in the flue gas flow F again. The device 416 also has a collecting means 440 with a deflection wall 450. The deflection wall 450 is in a manner similar to that described with reference to FIG. 3, in which the partial flow FP passes the partial flow FP through which the medium-sized particles MP pass down inside the collection chamber 446. Deflect.

It will be understood that many variations of the foregoing embodiments are possible within the scope of the appended claims.

For example, the separation of particles carried out by the device can be adjusted by selecting the appropriate plates of the baffle device in terms of the angle, size, and number of plates relative to the horizontal plane, so that there is a risk of clogging the pores of the catalyst layers included. Particles separate to the desired degree without unnecessarily raising the pressure drop in the apparatus. The openings in the catalyst have a size that can be designed as d _H. It is known by experience that most of the particles having a size of 0.5 × d _H or more must be separated before they reach the catalyst. In the example shown in FIG. 1, the openings are square with 4 mm sides (ie d _H = 4 mm), which means that particles having a size of at least 2 mm must be separated before the catalyst.

The walls of the collection chamber 46 do not necessarily have to have an angle γ of about 60 degrees with respect to the horizontal plane. The angle γ is selected to such an extent that an adequate flow rate of the partial flow FP in the collection chamber 46 is obtained, and the separated particles slide down the discharge device 48 at the bottom of the collection chamber 46. Can be. In many cases, an angle γ of about 40-70 ° has been found to meet these criteria well.

As is apparent from the foregoing, the deflection walls 50, 150 can achieve different angles δ with respect to the horizontal plane. In many cases, an angle δ of about 0 to 70 ° is desirable to provide a suitable first partial flow FP.

The velocity of the flue gas flow in the flue gas ducts 18 and 118 can vary within a wide range. However, it is particularly preferred that the velocity of the flue gas flow F in the first position P1 is about 13-25 m / s, since the velocity in this range is medium-sized particles MP, 34, 36, etc., so that they effectively fall below the lower portions 42, 142 of the flue gas ducts 18; 118.

Claims (13)

To separate particles MP from flue gas flow F, which is transmitted substantially horizontally from first position P1 to second position P2 in flue gas duct 18; 118. In In the first position P1, the particles MP are deflected downward to the lower portion 42; 142 of the flue gas duct 18; 118, In the second position (P2), the particles (MP) are collected in the lower part (42; 142) of the flue gas duct (18; 118). The method of claim 1, wherein the particles (MP) are deflected downwards at an angle of 40 to 70 ° with respect to a horizontal plane. The flue gas flow (F) according to claim 1 or 2 is divided into a first partial flow (FP) and a second partial flow (FF) at the second position (P2), The first partial flow includes the particles MP deflected and is separated from the lower portions 42, 142 of the flue gas duct 18; 118 and delivered into the collection chamber 46; 146. Way. 4. The method of claim 3, wherein the first partial flow FP is rapidly rotated in the collection chambers 46 and 146, whereby the particles MP exit from the first partial flow FP. Particle Separation Method Separation in Collection Chamber (46; The speed of the flue gas flow (F) according to claim 1 or 2, while the flue gas flow (F) is transferred from the first position (P1) to the second position (P2). Particle separation method reduced by a factor of 2.5.  From the flue gas flow F having a horizontal flue gas duct 18; 118, in which flue gas flow F is transmitted from the first position P1 to the second position P2 substantially horizontally therethrough. In the particle separation device (16; 116) for separating the particles (MP), The particle separation device 16; 116 in the first position P1 includes a baffle arrangement 32; 132 comprising at least one plate 34, 36, 38; 134, 136, 138. Wherein the at least one plate is inclined to deflect the particles MP below the lower portion 42; 142 of the horizontal flue gas duct 18; 118, and the flue gas duct 18; 118), The particle separation device 16; 116 in the second position P2 is the plate 34, 36, 38; 134, 136 into the lower portion 42; 142 of the flue gas duct 18; 118. Collecting means (40; 140) installed in the lower portion (42; 142) of the flue gas duct (18; 118) to collect the particles (MP) that are deflected downwards by (138). Particle separation apparatus, characterized in that. 7. Particle separator according to claim 6, wherein the at least one plate (34, 36, 38; 134, 136, 138) forms an angle α of 40 to 70 ° with respect to the horizontal plane. 8. The collecting means (40; 140) according to claim 6 or 7, having a deflection wall (50; 150), The deflection wall 50; 150 is opposed to the flow direction of the flue gas flow F in the lower portion 42; 142 of the flue gas duct 18; 118. The particles MP, which extend inwardly and are terminated by deflection lines 52 and 152 above the bottom 60 and 160 of the flue gas duct 18 and 118 and deflected from the flue gas flow F A particle separation device arranged to deflect and transfer the partial flow (FP) comprising a chamber into a collection chamber (46; 146) contained within the collecting means (40; 140). 9. The collection chamber (46, 146) has collection walls (56; 156), The collection wall is provided at the level below the deflection line 52; 152 from portions 58 and 158 of the collection chambers 46 and 146 located closest to the first position P1. 50; 150). 8. A particle separation device according to claim 6 or 7, wherein the baffle device (32; 132) comprises at least three beveled plates (34, 36, 38; 134, 136, 138). 8. The cross-sectional area (A1; A2) of the horizontal flue gas duct (18; 118) according to claim 6 or 7, is 1.2 to 2.5 times larger than the first position (P1) than in the second position (P2). Larger particle separation device. 8. The length L of the flue gas duct 18; 118 from the first position P1 to the second position P2 is at the first position P1. At least twice the characteristic cross-sectional dimension (D), which is the diameter or height of the particles. 8. A particle separator according to claim 6 or 7, wherein the baffle device (332) is provided with an actuator (341) for setting an angle (α) of the plate (334, 336, 338) with respect to a horizontal plane.

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