瑞典专利SE1550297A1 Cyclone separator arrangement and method

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24 ABSTRACT A CyClone separator (10) Comprises a pressure Chamber (20), an ínlet (30) foran incomíng ﬂow of a mixture of gas and particles, a gas outlet (50) foroutgoing gas arranged through a top wall (26) of the pressure Chamber and apartiC1e outlet (40) for outgoing particles arranged in a lower part (22) of thepressure Chamber. The pressure Chamber has a main rotation symmetricshape. The inlet is arranged through a side Wall (28) of an upper part (24) ofthe pressure Chamber for directing the incoming ﬂow With a main VelocityComponent in a tangential direction. The inlet Comprises an inlet tube (36)protruding through the side Wall of the upper part into the pressure Chamber,whereby an inner end (38) of the inlet tube is provided at a position interior ofthe pressure Chamber. A method for operating a Cyclone separator is also disclosed. (rig. 3A)
公开号:SE1550297A1
申请号:SE1550297
申请日:2015-03-12
公开日:2016-09-13
发明作者:Pettersson Patrik；Lindberg Johan
申请人:Valmet Oy；
IPC主号:

专利说明:

lO CYCLONE SEPARATOR ARRANGEMENT AND METHOD TECHNICAL FIELD The present invention relates in general to methods and arrangement forseparating particles from a stream of gas, and in particular to cyclone separator arrangements and methods.
BACKGROUND Cyclonic separation used for separating particles from a gas or liquid streamis utilized in many different applications, such as sawmills, oil refineries orWhen processing biomaterial. In a bioreactor for producing prehydrolyzedparticles from plant material, a stream of hot gas comprising particles ofprehydrolyzed biomaterial is produced. In order to separate the particles from the hot gas, a cyclone separator is typically utilized.
A problem by using cyclonic separation is that sharp particles may erode theinside of the cyclone separator Chamber side Wall. In the application ofbiomaterial processing, it is quite common to have e.g. sand particles mixedWith the plant material. Several approaches, having reinforced surfaces of thecyclone separator chamber side Wall, have been proposed, but such specialtreatments are typically expensive to provide and do not improve the situation in a decisive manner.
Another proposed solution Within prior art is to provide an additional, particle-free, gas stream at or just before the side Wall sections exposed for erosion.This additional gas tends to prohibit the original gas stream to reach the sideWall and the erosion is thereby reduced. However, for gas streams comprisingrelatively large amounts of particles, such as in typical biomaterial applications, the amount of additional gas that is required for mitígating the lO 2 erosion is large. Both the additional arrangements and the gas that is bled into the cyclone separator Will involve increased costs and complexity.
The amount of erosion is strongly dependent on the Velocity, With which theparticles hit the cyclone Chamber side Wall. One idea for reducing the erosionis then to reduce the Velocity of the gas streaming into the cyclone separator.In the published international patent application WO 02/ 18056, a cycloneseparator inlet nozzle is disclosed, which reduces the inlet speed of the gasstream entering into the cyclone separator. Hovvever, a lower entrance speedof the gas reduces the efficiency of the cyclone separation. In a crudeapproximation, the separation efficiency varies With the square of thetangential Velocity, Which means that With a lower tangential Velocity, thecyclone separation has to operate for a longer time to achieve the same effect.This may to a part be compensated by reduce the mean streaming speed alongthe symmetry axis of the cyclone separator, thereby increasing the time thegas spends in the cyclone separator. If the entrance Velocity is reduced evenfurther, the entire cyclone Whirl may even disappear completely and all cyclone separation Vanish.
In the abstract and drawings of the published Korean patent applicationKR20l400568l3A, a cyclone separator is disclosed. The cyclone separatorcomprises an inlet Which is formed in a side of the upper part of the cycloneseparator, a scroll part of the cyclone separator where the outlet of gas issupplied and a supporting part Which is formed between a side of the insideof the inlet and the scroll part. This arrangement prohibits erosion of the scroll part.
Prior art approaches for limiting erosion of the cyclone separator side walls While maintaining a reasonable separation effect still have to be improved. lO SUMMARY A general object of the present technology is to provide arrangements andmethods allowing for reducing erosion of the cyclone separator side walls Whilemaintaining a satisfactory separation effect. The above object is achieved bydevices and methods according to the independent claims. Preferred embodiments are defined in dependent claims.
In general words, in a first aspect, a cyclone separator comprises a pressurechamber, an inlet for an incoming ﬂoW of a mixture of gas and particles, a gasoutlet for outgoíng gas arranged through a top Wall of the pressure chamberand a particle outlet for outgoíng particles arranged in a lower part of thepressure chamber. The pressure chamber has a main rotation symmetricshape. The inlet is arranged through a side Wall of an upper part of thepressure chamber for directing the incoming ﬂow With a main Velocitycomponent in a tangential direction With respect to the rotation symmetricshape. The inlet comprises an inlet tube protruding through, in the tangentialdirection, the side wall of the upper part of the pressure chamber into thepressure chamber, whereby an inner end of the inlet tube is provided at a position interior of the pressure chamber.
In a second aspect, a method for operating a cyclone separator comprisesintroducing of an incoming ﬂoW of a mixture of gas and particles into apressure chamber having a main rotation symmetric shape. The incoming ﬂoWhas a main Velocity component in a tangential direction With respect to therotation symmetric shape. The introduction of an incoming ﬂoW is performedin the tangential direction at a position interior of the pressure chamber. Gasis exited through a gas outlet of the pressure chamber and particles are exited through a particle outlet of the pressure chamber.
One advantage With the proposed technology is that a cyclone separation operation can be obtained With lower velocities of the incoming ﬂoW of the lO 2245 4 mixture of gas and particles. Other advantages will be appreciated when reading the detailed description.
BRIEF DESCRIPTION OF THE DRAWINGS The invention, together With further objects and advantages thereof, may bestbe understood by making reference to the following description taken togetherwith the accompanying drawíngs, in which: FIG. 1 is an illustration of an example of a lignocellulosic bíomassmaterial treatment arrangement; FIG. 2A illustrates schematically a prior art cyclone separator in apartial cross-sectional view; FIG. 2B schematically illustrates a horizontal cross-sectional view of thecyclone separator of Fig. 2A; FIG. 2C illustrates the equipment of Fig. 2B with a low Velocity enteringgas flow; FIG. 3A illustrates an embodiment of a cyclone separator in a partialcross-sectional view; FIG. SB illustrates schematically a horizontal cross-sectional view of theembodiment of a cyclone separator of Fig. 3A; FIGS. 4A-E illustrate schematic cross-sectional views of otherembodiments of a cyclone separator; FIGS. 5A-D illustrate schematically embodiments of a diffuser 60 thatcan be utilized together with a cyclone separator; FIGS. öA-C schematically illustrate embodiments of diffuserarrangements; FIGS. 7A-D as schematic vertical cross-sections along the ﬂow directionof different embodiments of diffusers; FIGS. 8A-C illustrate schematically embodiments of inlet systems of acyclone separator; and F IG. 9 illustrates a ﬂow diagram of steps of an embodiment of a method for Operating a cyclone separator.
DETAILED DESCRIPTION Throughout the drawings, the same reference numbers are used for similar or corresponding elements.
For a better understanding of the proposed technology, it may be useful tobegin Witha brief overview of a system in Which the proposed technology can be utilized.
Fig. l illustrates a lignocellulosic biomass material treatment arrangement l,cornprising a bioreactor 2, in Which biomass material such as Wood chips,herbaceous plants, straW, bagasse etc. are treated under high pressure andhigh temperature to result in pre-hydrolyzed biomass material. The pre-hydrolysis prepares the biomass material for any following hydrolysis step inconnection with e.g. fermentation of the biomass. Such pre-hydrolyzedbiomass material exits the bioreactor 2 through a transport pipe 5 to a cycloneseparator 10. A blovv Washer arrangement 6 crushes the pre-hydrolyzedbiomass material into biomass particles 8, Which are transported to thecyclone separator 10 in a flow 9 of a mixture 7 of wet and hot gas and theparticles 8, typically also mixed with different types of polluting particles, suchas sand. The main fraction of biomass particles may in a typical case be of asize from some tenths of a millimeter up to a couple of millimeters. HoWever,aggregates of particles may be even larger. The transport is performed With ahigh Velocity for mitigate any deposition of biomass particles on the inside ofthe transport pipe 5. The transport may in a typical case be performed With asteam pressure of 10-15 bar, giving rise to velocities of the gas of somehundred meters per second. The particles and aggregates of particles arecarried With the gas and are typically finally reaching velocities in the same order of magnitude.
The ﬂow 9 of the mixture 7 of gas and particles 8 enters into a pressurechamber 20 of the cyclone separator 10 through an inlet 30 for an incoming ﬂow in the upper part 24 of the pressure chamber 20. In the cyclone separator 6 10, the cyclone action is used to separates out the particles, Which areremoved from the cyclone separator 10 by a particle outlet 40 for outgoíngparticles arranged in a lower part 22 of the pressure Chamber 20. Theremaining cleaned gas exits through a gas outlet 50 for outgoíng gas arranged through a top Wall 26 of the pressure Chamber 20.
When analyzing the prior art approaches for erosion reduction, the approachof utilizing lower velocities than normally applied in the cyclone separator Wasvery attractive, except for the difficulties to maintain the cyclone action insidethe cyclone separator. However, in the here presented technology, means forapproving the Whirl motion are provided, which makes it possible to adapt thegeneral idea of using cyclone separation performed With lower entrance velocities than normally applied.
In order to understand the conditions Within the cyclone separator, a generaldescription of a prior-art cyclone separator is ﬁrst given. Fig. 2A illustrates acyclone separator 10 in a partial cross-sectional vieW. The pressure chamber20 has an upper part 24, a lower part 22 and a top Wall 26. The inlet 30 istypically provided as an outer pipe 34 attached around a hole 32 in a side Wall28 of the upper part 24 of the pressure chamber 20. The hole 32 is typicallyprovided offset from a center line in order to provide the inﬂowing gas mixturewith a velocity directed mainly in the tangential direction, i.e. the inﬂoWinggas mixture has a significant tangential Velocity component. By interactionwith the walls of the pressure chamber 20, this tangential Velocity componentgives rise to a Whirl of gas mixture Within the pressure chamber 20. Thegenerally heavier and denser particles, compared to the other components inthe gas mixture, move in average outwards in the Whirl, towards the Walls ofthe pressure chamber 20. The generally less dense gas or steam presentsinstead a net motion inWards Within the Whirl towards the center, thusperforming a separation of the particles and the gas, respectively, generally referred to as a cyclone action. lO The smaller the particles are in the whirl, the less is the separation efficiencyby the cyclone action. To that end, in this example, and which is typical formany cyclone separators, the lower part 22 of the pressure Chamber 20 has ashape as a frustum of a cone, in order to sharpen up the cyclone action closerto the bottom for separating as ﬁne particles as possible. The particle outlet40 for outgoing particles is provided at the bottom of the pressure chamber 20in a lower part 22 of the pressure chamber 20. The gas outlet 50 for outgoinggas is arranged through a top wall 26 of the pressure chamber 20 andcomprises an outlet tube 52 protruding downwards from the top wall 26. Theoutlet tube 52 collects the cleaned gas that is intended to exit the cyclone separator 10.
Fig. 2B schematically illustrates a horizontal cross-sectional View comprisingthe inlet 30. Here, it is easily seen that the outer pipe 34 is attached to thehole 32 in the side wall 28 displaced from a center direction. This results inthat a Velocity 17 at the entrance has a significant tangential Velocitycomponent 19, which causes the Whirl 12 within the pressure chamber 20.The radial Velocity component 18 is typically relatively small, however, nottotally neglectable. For high Velocities, the creation of the whirl 12 will assist in maintaining the whirl 12 despite the radial Velocity component 18.
The radial Velocity component 18 differs across the hole 32. At the upper edge,as illustrated, of the hole 32, the radial Velocity component 18 is neglectable,however, at the lower edge, as illustrated, of the hole 32, the radial Velocitycomponent 18 may be Very significant, at least for holes 32 that have adiameter that is non-neglectable compared to the diameter of the pressure chamber 20.
Fig. 2C illustrates a similar equipment, but where the entering gas flow has alower Velocity than in earlier examples. Here the Velocity in the whirl 12becomes less, and when the whirl has traVelled around the pressure chamber20 one full turn, the force in the whirl is not enough for dampening the radial Velocity component 18. The incoming ﬂow therefore has a tendency to spread '30 8 out and a part stream can even flow on the opposite side of the outlet tube 52 than intended. The Whirl action may even be lost completely.
A basic idea of the present invention is to use the Velocity of the incoming flowto more efficiently create the Whirl. By introducing the incoming flow in anessentially pure tangential direction and at a position in the interior of the pressure chamber, a Whirl can be maintained by much slower inlet gas flows.
Fig. 3A illustrates an embodiment of a cyclone separator 10 in a partial cross-sectional view. The cyclone separator 10 comprises a pressure chamber 20.The pressure chamber has a main rotation symmetric shape. The cycloneseparator 10 further comprises an inlet 30 for an incoming ﬂow 9 of a mixtureof gas and particles 8. The inlet 30 is arranged through a side wall 28 of anupper part 24 of the pressure chamber 20. This arrangement is intended fordirecting the incomíng ﬂow 9 with a main Velocity component 17 in atangential direction T with respect to the rotation symmetric shape. The gasoutlet 50 and the particle outlet 40 are arranged essentially in the samemanner as described above. The inlet 30 here comprises an inlet tube 36protrudíng through the side wall 28 of the upper part 24 of the pressurechamber 20 into the pressure chamber 20. This protrusion takes place in atangential direction, as Will be discussed in further detail further below. Aninner end 38 of the inlet tube 36 is provided at a position interior of thepressure chamber 20. Furthermore, due to the upper and lower walls of the inlet tube 36, ﬂows in the vertical direction is made more difficult.
In a particular embodiment, where the cyclone separator is utilized in abiomass treatment arrangement, an outer end of the inlet tube 36 is connected to an outlet from a bioreactor, as described further above.
Fig. 3B schematically illustrates a horizontal cross-sectional view comprisingthe inlet 30 of the embodiment of Fig. 3A. Here, it can be seen that the inlettube 36 protrudes into the interior 23 of the pressure chamber 20. The inner end 38 is in this embodiment positíoned at a center line 21. The center line 21 is a line that is perpendicular to the tangential direction and that passesthrough a center of the pressure Chamber 20. The Velocity 17 at the entranceinto the pressure Chamber 20 has then a pure tangential direction. This istrue regardless if the gas exists in the top or bottom part, as illustrated, of theinlet tube. Furthermore, since the inner end 38 at least to a part has passedthe outlet tube 52, any ﬂow in an opposite Whirl direction becomes veryunlikely. The Whirl movement within the pressure chamber 20 can thereby be maintaíned by means of lower velocities of the entering gas ﬂows.
In the embodiment of Fig. 3B, the gas outlet comprises an outlet tube 52protruding downwards from the top wall. A, with respect to the rotationsymmetric shape, radially inner edge 37 of the inner end 38 of the inlet tube36 is provided at a distance D from the outlet tube 52. This preferred detailenables the gas to pass at the radial inner side of the inlet tube 36 when having rotated one or several turns within the pressure chamber 20.
Fig. 4A illustrates a schematic cross-sectional view of another embodiment ofa cyclone separator 10. Also here, the inlet tube 36 protrudes through the sidewall 28 of the upper part of the pressure chamber 20 into the pressurechamber. The inner end 38 of the inlet tube 36 is provided at a position interior23 of the pressure chamber 20, however, in this embodiment, the inner end38 does not reach the entire way to the center line 21. This means that thegas exiting the inner end 38 of the inlet tube 36 at the radially inner side stillhas a small radial Velocity component. However, since the distance to thecenter line 21 is small, this radial Velocity component is also small. It ispreferred if an angle c1 between a line between the center C of the pressurechamber 20 and the radially inner edge 37 of the inner end 38 of the inlet tube36 and the center line 21 is kept below 30°, which ensures that no part of thegas ﬂow enters the pressure chamber 20 with a radial to tangential Velocitycomponent ration that is larger than l/x/š. The closer to the center line 21 theinner end 38 is situated, the smaller becomes the radial Velocity component.
Therefore, more preferably, the angle a is kept below 20°, even more preferably lO below l0°, even more preferably below 5° and most preferably in the Vicinity or at O°.
Fig. 4B illustrates a schematic cross-sectional view of another embodiment ofa Cyclone separator 10. Also here, the inlet tube 36 protrudes through the sideWall 28 of the upper part of the pressure Chamber 20 into the pressureChamber. The inner end 38 of the inlet tube 36 is provided at a position interior23 of the pressure Chamber 20, however, in this embodiment, the inner end38 protrudes beyond the center line 21. This means that the gas exiting theinner end 38 of the inlet tube 36 at the radially inner side has a small radialVelocity component, in this case directed outwards. A radially Velocitycomponent directed outwards will not counteract the whirl formation.However, an outwards directed radially Velocity Component may increase theerosion on the inner side wall of the pressure Chamber 20. It is thereforefalsopreferred to keep such a radial Velocity component small. In analogy with thereasoning above, it is preferred if the angle ß between the line between thecenter C of the pressure Chamber 20 and the radially inner edge 37 of theinner end 38 of the inlet tube 36 and the Center line 21 is kept below 30°,which ensures that no part of the gas flow enters the pressure Chamber 20with a radial to tangential Velocity component ration that is larger than 1 /x/š .The closer to the center line 21 the inner end 38 is situated, the smallerbecomes the outwards directed radial Velocity Component. Therefore, morepreferably, the angle ß is kept below 20°, even more preferably below l0°, even more preferably below 5° and most preferably in the Vicinity or at O°.
Considering both Fig. 4A and Fig. 4B, it is thus preferred if an absolutemeasure of an angle o, ß between a line between the Center C of the pressureChamber 20 and the radially inner edge 37 of the inner end 38 of the inlet tube36 and the center line 21, where the center line 21 is a line that isperpendicular to the tangential direction and that passes through the centerof the pressure Chamber 20, is kept below 30°, more preferably below 20°,even more preferably below l0°, even more preferably below 5° and most preferably in the Vicinity or at O°. 11 In other words, the action of introducing the incoming ﬂow is performed at aposition, for which an absolute measure of an angle a, ß between the linebetween the center C of the pressure Chamber 20 and the position and a centerline 2 1, where the center line 2 1 is a line that is perpendicular to the tangentialdirection T and passes through the center C of the pressure chamber 20, issmaller than 30°, preferably smaller than 20°, even more preferably smaller than lO°, and even more preferably smaller than 5°.
The most preferred embodiment is as anyone skilled in the art realizes if theinner end 38 protrudes at least up to the center line 21, and most preferably not beyond, as illustrated e.g. in Fig. 3B.
Fig. 4C illustrates a schematic cross-sectional view of yet another embodimentof a cyclone separator 10. Also here, the inlet tube 36 protrudes through theside wall 28 of the upper part of the pressure chamber 20 into the pressurechamber. The inner end 38 of the inlet tube 36 is provided at a position interior23 of the pressure chamber 20, and, in this embodiment, the inner end 38 isalso positioned at the center line 21. In this embodiment, however, the inlettube 36 is curved to follow the wall of the pressure chamber 20. The centerline 21 is directed perpendicular to the tangential direction as defined at theinner end 38. This embodiment also provides a good possibility to achieve awhirl action Within the pressure chamber 20 by relatively low entrancevelocities of the gas. A small disadvantage is, however, that the curved shape of the inlet tube 36 increase the complexity in manufacturing.
In the embodiments presented here above, a, with respect to the rotationsymmetric shape, radially outer edge 39 of the inner end 38 of the inlet tube36 is provided against the side wall 28 of the upper part of the pressurechamber 20 or is integrated with the side wall 28 of the upper part of thepressure chamber 20. Typically, such arrangement will utilíze the spacewithin the pressure chamber 20 in an optimal way. However, as illustrated in the embodiment of Fig. 4D, in manufacturing of the cyclone separator 10, it lO 12 might in certain cases be easier to provide the radially outer edge 39 at adistance d from the side wall 28 of the pressure Chamber 20. The distance dmay in different embodiments be within O and 25% of the diameter of thepressure chamber 20, but is preferably kept small. Thus, preferably, thedistance d is within 0 and 15%, more preferably within 0 and 5% and mostpreferably within 0 and 2.5% of the diameter of the pressure chamber 20 ofthe pressure chamber 20. The efﬁciency of creating the Whirl within thepressure chamber 20 will typically be reduced, however, typically marginally,and this marginal loss in efficiency may instead be compensated by the ease of manufacture.
In Fig. 4E, an embodiment of a cyclone separator 10 is illustrated, having anoutlet tube 52 protruding downwards from the top wall, which outlet tube 52is Wider than in previous embodiments. If also the inlet tube 36 is wider thanin previous embodiments, the inner end 38 of the inlet tube 36 may beprovided against the outlet tube 52. In other words, the, with respect to therotation symmetric shape, radially inner edge of the inner end 38 of the inlettube 36 is provided without any distance from the outlet tube 52. This, non-preferred embodiment, may be operable in some applications, in particularwhere non-sticky particles are to be separated. However, it is believed that inmost cases, there might be problems with solid matter that collects at the outside of the inlet tub 36.
As discussed further above, the here presented technology is very useful inconnection with incoming ﬂows of a mixture of gas and particles that haverelatively low velocities, compared to prior art cyclones, in order to reduce theerosion of the cyclone chamber. However, in a typical case, where a mixtureof gas and particles is to be moved over a distance between e.g. a pre-hydrolyzer and a cyclone chamber, there is no general request to have a lowvelocity of such a flow. At the contrary, low velocities when transporting ﬂowsof a mixture of gas and particles may render into deposition of solid particlesat the inner walls of the transporting tubes. Therefore, high velocities are typically utilized during transporting of ﬂows of a mixture of gas and particles, l0 13 as mentioned above typically in the order of a couple of hundred meters per second.
It is therefore common that there has to be a reduction in Velocity of such aﬂow before letting the ﬂow into a cyclone separator, in order to reduce theerosion of the inner side Walls of the cyclone chamber. Therefore, in a preferredembodiment, the inlet comprises a diffuser. The diffuser is an arrangementthat distributes a ﬂow over an increased area, which results in a decreased average Velocity.
Fig. 5A illustrates schematically an embodiment of a diffuser 60 that can beutilized together With any of the above presented embodiments of a cycloneseparator. In this embodiment, the diffuser 60 comprises a part of the inlettube 36. In this embodiment, the diffuser 60 also comprises a part of the outerpipe 34 of the inlet. The diffuser 60 has a rnonotonically increasing cross-sectional area towards the inner end 38 of the inlet tube 36. The term“monotonically increasing cross-sectional area” is intended to define a cross-sectional area that is non-decreasing in all portions, i.e. only has portions ofincreasing and/ or constant cross-sectional areas towards the inner end 38 ofthe inlet tube 36. Note, however, that the increasing does not necessarily haveto be strictly increasing, i.e. there might also be portions With constant cross-sectional areas. An ingoing cross-sectional area a is increased monotonicallyto an outgoing cross-sectional area A, in this particular embodiment the cross-sectional area is strictly increasing. Preferably, the cross-sectional area of thediffuser 60 increases at least 2 times, more preferably at least 5 times andmost preferably around 10 times from the ingoing cross-sectional area a to theoutgoing cross-sectional area A. On the other hand, the velocity reductioncannot in practice be too large in order to maíntain an efficient cyclone actionand it is therefore preferred if the cross-sectional area of the diffuser 60increases at most 17 times, and more preferably at most 13 times from theingoing cross-sectional area a to the outgoing cross-sectional area A. Theposition of the side wall 28 of the pressure chamber and the hole 32 in the pressure charnber are depicted by broken lines, to increase the understanding 14 of the position of the diffuser 60. In the present embodiment, themonotonically increasing cross-sectional area of the diffuser 60 is provided bya monotonically increased vertical dimension of the diffuser 60 towards theinner end 38 of the inlet tube 36. In particular, the vertical dimension of thediffuser 60 is increased downwards, towards the inner end 38 of said inlettube 36. In other words, the upper wall of the diffuser 60 is essentially horizontal, While the lower wall is sloping downwards.
This increase in cross-sectional area leads to a reduction of the Velocity of theincoming ﬂow before introducing the incoming ﬂow into the pressure chamber.In the view of the above discussion, preferably, the Velocity reduction is atleast 2 times, more preferably at least 5 times and most preferably around 10times from the ingoing cross-sectional area a to the outgoing cross-sectionalarea A. On the other hand, the Velocity reduction cannot in practice be toolarge in order to maintain an efficient cyclone action and it is thereforepreferred if the Velocity reduction is at most 17 times, and more preferably atmost 13 times from the ingoing cross-sectional area a to the outgoing cross- sectional area A.
Fig. 5B illustrates schematically another embodiment of a diffuser 60 that canbe utilized together With any of the above presented embodiments of a cycloneseparator. This embodiment resembles the embodiment of Fig. 5A e.g. in thatthe monotonically increasing cross-sectional area of the diffuser 60 is providedby a monotonically increased vertical dimension of the diffuser 60 towards theinner end 38 of the inlet tube 36. In this embodiment, however, the upper wall of the diffuser 60 slopes upwards.
Fig. 5C illustrates schematically yet another embodiment of a diffuser 60 thatcan be utilized together with any of the above presented embodiments of acyclone separator. This embodiment resembles the earlier embodiments ofFigs. 5A and 5B e.g. in that the diffuser 60 has a monotonically increasingcross-sectional area towards the inner end 38 of the inlet tube 36. In this embodiment, however, the increased cross-sectional area of the diffuser 60 is lO provided by increasing both the horizontal and vertical dimensions towards the inner end 38.
It is presently believed that the embodiment in Fig. 5A is the preferredembodiment among these alternatives. However, depending on the actualapplication, also the embodiments of Figs. 5B and 5G are operable, providingthe intended technical effect, giving a reduced velocity upon entering thecyclone separator. The embodiment of Fig. 5C has the drawback that it allowsthe mixture of gas and particles in the diffuser 60 to achieve a radial Velocitycomponent. This radial velocity component is typically small compared to thetotal velocity, however, since this is an unwanted feature when the mixtureenters into the cyclone separator, the increase in the horizontal dimension ispreferably kept small compared to the total horizontal dimension at the innerend 38. The embodiment of Fig. 5B allows the mixture of gas and particles inthe diffuser 60 to achieve a small vertical velocity component, directedupwards. In a typical cyclone separator, the inlet is provided relatively closeto the upper wall, and a velocity component directed upwards will only causea generally undesired interaction between the top Wall of the cyclone separatorand the ﬂow of the mixture. Therefore, the presently preferred embodiment has a diffuser with a horizontal upper wall.
The actual shape of the diffuser and/or inlet tube 36 is in general notparticularly important. In the previous embodiments, tubes of rectangularcross-sections have been illustrated. This is typically easy to integrate withcyclone separator pressure chambers having a cylindrical form in the upperpart. Such rectangular cross-sections can therefore in a practicalmanufacturing point of view be considered as advantageous. However, ingeneral, also other types of cross-sectional geometries are feasible. Fig. 5D illustrates one example, where the diffuser 60 has an elliptical cross-section.
As mentioned above, the diffuser could comprise at least a part of the inlettube 36 and/ or at least a part of the outer pipe 34 of the inlet. Fig. 6A schematically illustrates an embodiment of a diffuser arrangement, where the 16 diffuser 60 has one part outside the side wall 28 and one part inside the sidewall 28, i.e. in the interior 23 of the pressure Chamber. The part outside theside Wall 28 then constitutes a part of the outer pipe 34 of the inlet. The partinside the side wall 28 constitutes a part of the inlet tube 36. Fig. 6Bschematically illustrates an embodiment of a diffuser arrangement, where thediffuser 60 is provided entirely inside the side Wall 28, i.e. in the interior 23 ofthe pressure Chamber. The diffuser 60 then constitutes at least a part of theinlet tube 36. Fig. 6C schematically illustrates an embodiment of a diffuserarrangement, Where the diffuser 60 is provided entirely outside the side Wall28. The diffuser 60 then constitutes at least a part of the outer pipe 34 of the inlet.
The behavior of the increase of the diffuser cross-sectional area can bedesigned in different ways. A few non-limiting embodiments are schematicallyillustrated in the figures 7A-7D. In Fig. 7A, the diffuser cross-sectional areadoes not increase continuously, i.e. it is not strictly increasing, but increasesinstead in two separated regions, and thus still presenting a monotonicincrease. In this embodiment, the vertical dimension change of the diffuser 60takes place both upwards and downwards. In this particular embodiment, inthe portions where the diffuser cross-sectional area increases, the verticaldimension increases linearly, i.e. in the cross-sectional view, the upper andlower walls of the diffuser have the form of a straight hä. In Fig. 7B, a similarembodiment is illustrated. However, in this case, the change in the verticaldimension is provided by the lower wall of the diffuser 60. In Fig. 7C, anembodiment of a diffuser 60 having a non-linear increase of the verticaldimension is illustrated. Also in Fig. 7D, an embodiment of a diffuser 60having a non-linear increase of the vertical dimension is illustrated. The non-linear increase of the vertical dimension in Figs. 7 C and 7D can be seen as curved lines.
It can be noted that when a ﬂow of a mixture of a gas and particles enters acyclone separator with a low Velocity, the separation efficiency is generally lower compared to a case Where a high entrance velocity is used. The cyclone 17 action increase in general with increasing Velocity in the Whirl. This reducedefficiency may at least to a part be compensated by allowing the gas/ particlemixture to spend more time in the cyclone separator, thus travelling moreturns around the pressure chamber before they are exiting from the cyclone.One way to do that is to try to reduce the vertical Velocity induced whenentering of the ﬂow of the mixture from the outer pipe into the pressurechamber. If the mixture is entered with a pure horizontal Velocity, themovement downwards is only caused by the gravity, typically on the particles,and the gas pressure from the subsequent entered mixture. The mixture willtherefore be kept in a Whirl motion as long as possible, which increase the separation efficiency.
Such operation can at least to a part be made more difficult to obtain if themixture already at the instant of entering the pressure chamber has adownwards directed Velocity component. It is therefore concluded thatapproaches of entering the mixture through the top wall, thereby deliberately giving a large vertical Velocity component are basically unsuitable.
Also the provision of a diffuser may, as brieﬂy mentioned above, give a minorvertical Velocity component. However, by an appropriate design of the diffuser,such effects can be reduced. One possibility is to provide the actual diffuseraction a distance before the inner end of the inlet tube, and providing aconstant cross-sectional area part of the inlet tube closest to the inner end.
The embodiments of Figs. 7A, 7B and 7D are examples of such designs.
During experiments with cyclone separators Operating with low entranceVelocities, as compared with typical prior art cyclones, it has been found thatthere is a tendency for the particles in the mixture entering the pressurechamber to stick to the top wall and/ or the side wall above the entering level.This has been particularly frequent for sticky particles. In many applications,remaining quantities of particles in the cyclone pressure chamber aredisadvantageous. In Fig. 8A an embodiment of an inlet system of a cyclone separator is illustrated schematically. The inlet tube 36 is here provided with 18 a bafﬂe plate 70. The bafﬂe plate 70 is arranged horizontally and is attachedto an upper part of the inner end 38 of the inlet tube 36 and protrudes in thetangential direction T of the incoming mixture of gas and particles. Thisarrangement of the bafﬂe plate '70 guides the streaming mixture towards tothe opposite side wall of the pressure chamber. Any particles having anupwards directed vertical velocity component is thereby prevented to reachthe top of the pressure Chamber. This arrangement of the bafﬂe plate 70 isadvantageously combined with e.g. the diffuser described in otherembodiments further above, and may even mitigate the disadvantages ofcertain embodiments providing upwards directed vertical Velocity components, e.g. as could be provided by the embodiment of Fig. 5B.
In Fig. SB another embodiment of an inlet system of a cyclone separator isillustrated schematically. Here the horizontal bafﬂe plate 70 protrudes in thetangential direction T all the way to the side wall of the pressure chamber 20.Such an arrangement provides for that most of the particles are caught by theWhirl motion before they have any opportunity to deviate upwards towards the top.
In certain applications, as e.g. in the embodiment of Fig. 8C, the inlet 30 canbe provided juxtaposed to the top wall 26 or a divisional top wall of thepressure chamber 20. The horizontal bafﬂe plate 70 is then preferablyintegrated in the top wall 26 of the pressure chamber 20.
Fig. 9 illustrates a ﬂow diagram of steps of an embodiment of a method forOperating a cyclone separator. The procedure starts in step 200. In step 220,an incoming ﬂow of a mixture of gas and particles is introduced into a pressurechamber having a main rotation symmetric shape. The incoming ﬂow has amain velocity component in a tangential direction with respect to the rotationsymmetric shape. The step 220 comprises a part step 222 in which theintroduction of the incoming flow is performed in the tangential direction at aposition interior of the pressure chamber. ln a preferred embodiment, the step of introducing an incoming ﬂow is performed, in the tangential direction, at or lO 19 behind a center line. The center line is defined as a line that is perpendicularto the tangential direction and that passes through a center of the pressureChamber. In step 230, gas is exited through a gas outlet of the pressurechamber and in step 240, particles are exited through a particle outlet of the pressure Chamber. The procedure ends in step 299.
In a preferred embodiment, the method for Operating a cyclone separatorcomprises the further step 210 of reducing a Velocity of the incoming ﬂow before the step of introducing the incoming ﬂow into the pressure chamber.
The embodiments described above are to be understood as a few illustrativeexamples of the present invention. It will be understood by those skilled in theart that various modifications, combinations and changes may be made to theembodiments Without departing from the scope of the present invention. Inparticular, different part solutions in the different embodiments can becombined in other configurations, Where technically possible. The scope of the present invention is, however, defined by the appended claims.

权利要求:
Claims (18)
[1] 1. A cyclone separator (10), Comprising: a pressure Chamber (20) having main rotation symmetric shape; an inlet (30) for an incoming ﬂow (9) of a mixture (7) of gas and particles(8), said inlet (30) being arranged through a side Wall (28) of an upper part (24)of said pressure Chamber (20) for directing said incoming ﬂow (9) with a mainVelocity component in a tangential direction (T) with respect to said rotationsymmetric shape; a gas outlet (50) for outgoing gas arranged through a top wall (26) ofsaid pressure Chamber (20); and a particle outlet (40) for outgoing particles arranged in a lower part (22)of said pressure Chamber (20),characterized in that said inlet (30) comprises an inlet tube (36) protruding through, in saidtangential direction (T), said side wall (28) of said upper part (24) of saidpressure Chamber (20) into said pressure Chamber (20), whereby an inner end(38) of said inlet tube (36) is provided at a position interior (23) of said pressure Chamber (20).
[2] 2. The cyclone separator according to Claim 1, characterized in that anabsolute measure of an angle (d, ß) between a line between a center (C) of saidpressure Chamber (20) and a radially inner edge (37) of said inner end (38) ofsaid inlet tube (36) and a Center line (21), said center line (21) being a line thatis perpendicular to said tangential direction (T) and passing through saidCenter (C) of said pressure Chamber (20), is smaller than 30°, preferablysmaller than 20°, even more preferably smaller than 10°, and even more preferably smaller than 5°.
[3] 3. The Cyclone separator according to claim 2, characterized in that saidinlet tube (38) protrudes into said interior (23) of said pressure Chamber (20) up to said center line (21). 21
[4] 4. The cyclone separator according to any of the claims 1 to 3,characterized in that a, with respect to said rotation symmetric shape,radially outer edge (39) of said inner end (38) of said inlet tube (36) is providedagainst said side Wall (28) of said upper part (24) of said pressure Chamber(20) or is integrated With said side Wall (28) of said upper part (24) of said pressure Chamber (20).
[5] 5. The cyclone separator according to any of the claims 1 to 4,characterized in that said gas outlet (50) comprises an outlet tube (52) protrudingdovvnwards from said top Wall (26); and Wherein a, with respect to said rotation symmetric shape, radially inneredge (37) of said inner end (38) of said inlet tube (36) is provided at a distance(D) from said outlet tube (52).
[6] 6. The cyclone separator according to any of the claims 1 to 5, characterized in that said inlet (30) comprises a diffuser (60).
[7] 7. The cyclone separator according to claim 6, characterized in that saiddiffuser (60) comprises a part having a monotonically increasing cross- sectional area towards said inner end (38) of said inlet tube (36).
[8] 8. The cyclone separator according to claim 7, characterized in that across-sectional area of said diffuser (60) increase at least 2 times, preferablyat least 5 times, also preferably at most 17 times, more preferably at most 13times and most preferably 10 times from an ingoing cross-sectional area (a) to an outgoing cross-sectional area (A).
[9] 9. The cyclone separator according to claim 7 or 8, characterized in thatsaid monotonically increasing cross-sectional area of said diffuser (60) isprovided by a monotonically increased vertical dimension of said diffuser (60) towards said inner end (38) of said inlet tube (36). lO 22
[10] 10. The cyclone separator according to claim 9, characterized in that saidvertical dimension of said diffuser (60) is increased doWnWards, towards said inner end (38) of said inlet tube (36).
[11] 11. The cyclone separator according to any of the claims 1 to 10,characterized by further comprising a horizontal bafﬂe plate (70) attached toan upper part of said inner end (38) of said inlet tube (36) and protruding in said tangential direction (T).
[12] 12. The cyclone separator according to claim 11, characterized in thatsaid horizontal bafﬂe plate (70) protrudes in said tangential direction (T) all the Way to said side Wall (28) of said pressure chamber (20).
[13] 13. The cyclone separator according to claim 12, characterized in thatsaid horizontal bafﬂe plate (70) is integrated in said top Wall (26) of said pressure chamber (20).
[14] 14. The cyclone separator according to any of the claims 1 to 13,characterized in that an outer end of said inlet tube (36) is connected to an outlet from a bioreactor (2).
[15] 15. A method for operating a cyclone separator, comprising the steps of: - introducing (220) an incoming ﬂoW of a mixture of gas and particlesinto a pressure chamber having main rotation symmetric shape, saidincoming ﬂoW having a main Velocity component in a tangential direction withrespect to said rotation symmetric shape; - exiting gas (230) through a gas outlet of said pressure chamber; and - exiting particles (240) through a particle outlet of said pressurechamber, characterized in that said step of introducing (220) an incoming flow isperformed (222) in said tangential direction at a position interior of said pressure chamber. 23
[16] 16. The method according to claim 15, characterized in that said step ofintroducing (220) an incoming ﬂow is performed at a position, for which anabsolute measure of an angle (d, ß) between a line between a center (C) of saidpressure Chamber (20) and said position and a center line (21), said centerline (21) being a line that is perpendicular to said tangential direction (T) andpassing through said center (C) of said pressure chamber (20), is smaller than30°, preferably smaller than 20°, even more preferably smaller than lO°, and even more preferably smaller than 5°.
[17] 17. The method according to claim 16, characterized in that said step ofintroducing (220) an incoming ﬂow is performed, in said tangential direction, at said center line.
[18] 18. The method according to any of the claims 15 to 17, characterized bythe further step of:- reducing (210) a Velocity of said incoming ﬂow before said step of introducing said incoming ﬂow into said pressure Chamber.

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同族专利:

公开号 | 公开日

BR112017019183A2|2018-04-24|

US20180056307A1|2018-03-01|

EP3268133A1|2018-01-17|

SE538760C2|2016-11-15|

WO2016144231A1|2016-09-15|

EP3268133A4|2018-11-14|

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法律状态:

优先权:

申请号 | 申请日 | 专利标题

SE1550297A|SE538760C2|2015-03-12|2015-03-12|Cyclone separator arrangement and method|SE1550297A| SE538760C2|2015-03-12|2015-03-12|Cyclone separator arrangement and method|

US15/556,015| US20180056307A1|2015-03-12|2016-02-15|Cyclone separator arrangement and method|

EP16762051.7A| EP3268133A4|2015-03-12|2016-02-15|Cyclone separator arrangement and method|

PCT/SE2016/050115| WO2016144231A1|2015-03-12|2016-02-15|Cyclone separator arrangement and method|

BR112017019183A| BR112017019183A2|2015-03-12|2016-02-15|cyclone separator arrangement and method for operating a cyclone separator|

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