WO2000025932A1 - Method and device for mechanically separating a disperse system - Google Patents
Method and device for mechanically separating a disperse system Download PDFInfo
- Publication number
- WO2000025932A1 WO2000025932A1 PCT/EP1999/008097 EP9908097W WO0025932A1 WO 2000025932 A1 WO2000025932 A1 WO 2000025932A1 EP 9908097 W EP9908097 W EP 9908097W WO 0025932 A1 WO0025932 A1 WO 0025932A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- centrifugal separator
- cross
- partial
- feed channels
- sectional areas
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/02—Construction of inlets by which the vortex flow is generated, e.g. tangential admission, the fluid flow being forced to follow a downward path by spirally wound bulkheads, or with slightly downwardly-directed tangential admission
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C11/00—Accessories, e.g. safety or control devices, not otherwise provided for, e.g. regulators, valves in inlet or overflow ducting
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/02—Construction of inlets by which the vortex flow is generated, e.g. tangential admission, the fluid flow being forced to follow a downward path by spirally wound bulkheads, or with slightly downwardly-directed tangential admission
- B04C5/04—Tangential inlets
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01M—LUBRICATING OF MACHINES OR ENGINES IN GENERAL; LUBRICATING INTERNAL COMBUSTION ENGINES; CRANKCASE VENTILATING
- F01M13/00—Crankcase ventilating or breathing
- F01M13/04—Crankcase ventilating or breathing having means for purifying air before leaving crankcase, e.g. removing oil
- F01M2013/0422—Separating oil and gas with a centrifuge device
- F01M2013/0427—Separating oil and gas with a centrifuge device the centrifuge device having no rotating part, e.g. cyclone
Definitions
- the invention relates to a method for mechanically separating a disperse system into two or more disperse systems with different properties in a centrifugal separator and a device suitable for carrying out the method.
- Suitable disperse systems are those in which the disperse phase is solid, liquid or gaseous and the dispersant is either liquid or gaseous, that is to say fluid.
- the mechanical separation of such a disperse system of identical particle density in coarse and fine material is referred to as "classifying”. If separation is carried out according to different densities, one speaks of “sorting”. If particles are separated from a liquid or gaseous dispersant surrounding them, this is a separation process. So-called centrifugal separators, also called cyclones, are used to carry out the mechanical separation processes “classifying”, “sorting” and “separating”.
- a generic method and the associated device are known from DE 39 36 078 C2.
- the method intended to control the degree of separation of a fluid multiphase mixture is carried out using a cyclone separator with a swirl generator.
- the entire material flow is divided into at least two partial flows by a first division, or at least two input material flows are used for the cyclone separator, with the size of at least one of the partial flows being changeable.
- the partial streams are optionally further divided and then fed to the feed channels of the swirl generator.
- the swirl generator has a swirl chamber with several tangential feed channels, which have the same cross-sectional area and the number of which is even.
- the invention had for its object to provide a generic method with which it is possible to vary the separation efficiency regardless of the fluid throughput in a large width without major structural changes and to influence the size of the separating particles and the selectivity.
- the object is achieved by the method features specified in claim 1. Suitable embodiments of the procedure are given in claims 2 to 14. A device for performing the method is the subject of claim 15. Suitable design variants of the device are specified in claims 16 to 28.
- the proposed procedure of dividing the partial streams into tangential feed channels with different cross-sectional areas as individual values or as a sum at the entry point in the centrifugal separator leads to a substantial expansion of the control range and to an improved influence on the procedural and qualitative parameters during operation. It is of great advantage that, in comparison to the solutions known from the prior art, the degree of separation can be regulated within a relatively large range independently of the total volume flow. An operating mode with three or four tangential feed channels is sufficient for a large number of application areas.
- centrifugal separators are either arranged directly on the centrifugal separator, evenly distributed over the circumference, or they open into a separate swirl chamber with which the centrifugal separator is additionally equipped.
- a centrifugal separator with such a swirl chamber is described in detail, for example, in DE 39 36 078 C2.
- each partial flow is divided into one or two tangential feed channels, whereby in the case of two tangential feed channels they differ in their cross-sectional area at the entry point in the centrifugal separator , or in the case of more than two tangential feed channels, the sum of the cross-sectional areas is essential as a distinguishing feature, enables a multitude of variations with regard to a different setting of the entry impulses of the individual partial flows to be introduced into the centrifugal separator, which affect the centrifugal acceleration in the separator.
- the selectivity and the grain size can be set on a product-specific basis and the part sizes can be changed during operation.
- the required rotational symmetry of the partial streams is not impaired after entering the centrifugal separator.
- the partial flow rate which is introduced into the centrifugal separator at the entry point through the tangential feed channel with the smallest cross-sectional area, is increased by adjusting the pump or throttle device accordingly, and the other partial flow rate is reduced accordingly.
- the total volume flow remains constant.
- the partial flows introduced into the centrifugal separator are mixed very well with one another. This effect can be further improved by the arrangement of the swirl chamber already mentioned, the radial component of the speed vector increasing.
- the partial flow amount that is assigned to the tangential feed channel with the larger cross-sectional area or to the feed channels with the larger sum of the cross-sectional areas should be controllable via a throttle valve integrated in the partial flow line. With this valve, this partial flow can then be influenced in its throughput. With constant throughput, the other partial flow quantity, which is introduced into the centrifugal separator via the feed channel with the smaller cross-sectional area, is then inevitably increased. This already results in a large control range for the degree of separation.
- any irregularities that occur as a result of different input impulses of the two, three or four partial flow quantities can be largely compensated for.
- Internals should be provided in the swirl chamber for a certain positive guidance of the partial flows introduced. It is important that a free selection can be made for the partial flows and that a partial flow does not result from a return and therefore cannot be freely adjusted.
- the partial flows can either be formed from a total volume flow by division or as separate output conveying flows, which originate from one or two storage containers and in which the mass transfer takes place through separate conveying members. A volume flow change to form different partial flows can then be brought about by changing the speed of the pumps used.
- the proposed procedure can also be used for those applications in which the degree of separation is to be kept constant, with variable fluid throughput.
- the achievable control range is considerably restricted in the procedure known from the prior art.
- the two partial flows are arranged symmetrically and tangentially Feed channels introduced into the swirl chamber of the centrifugal separator.
- this solution is only suitable for centrifugal separators with an additional swirl chamber.
- the pressure can be measured in order to influence the degree of separation in the partial stream which is introduced into the centrifugal separator at the entry point via the feed channel with the smallest cross-sectional area. This is kept at a predetermined value by changing at least one of the remaining partial flow quantities.
- a pressure measuring device is integrated in the feed channel with the smallest cross-sectional area at the entry point into the centrifugal separator. This is coupled to a control valve, which is integrated in one of the feed channels for the other partial flows. It is also possible to arrange a control valve in several of the other partial flows, which are then optionally controlled via the pressure measuring device.
- a further embodiment variant consists of measuring or determining selected substance parameters before and / or after the centrifugal separator and, depending on this, the partial flow quantity ratio between two or more partial flows and / or the pressure difference between two defined points, one before and one after the centrifugal separator, to be changed. This measure is used above all when the pressure cannot be used as a parameter for controlling the deposition process.
- the loading of the feed stream can change.
- the property of a material flow is measured and used as the reference variable for the control.
- the particle size distribution in the stream after the centrifugal separator can be measured by means of a measuring device and the pressure upstream of the centrifugal separator and the ratio of the partial flows upstream of the centrifugal separator can be changed. This measure allows, for example, the dust content in the clean gas flow or the average particle size of the centrifugal separator to be kept constant by appropriate control.
- the required actuators for changing the partial flow ratio and / or the pressure difference can be, for example, a pump or a valve, which can also be used in combination if necessary.
- FIG. 1 shows a centrifugal separator with two tangential feed channels, as a longitudinal section along the line B-B in FIG. 2,
- FIG. 2 shows a section along the line A-A in FIG. 1,
- FIG. 3 shows the perspective illustration of the centrifugal separator according to FIG. 1 with a variant for the partial flow division
- FIG. 4 shows a centrifugal separator according to FIG. 1 with an additional one
- FIG. 5 a section along line A-A in FIG. 4,
- FIG. 6 shows a perspective view of a centrifugal separator with three tangential feed channels which open into a swirl chamber
- FIG. 7 shows the centrifugal separator according to FIG. 6 as a longitudinal section
- FIG. 8 shows the top view of the centrifugal separator according to FIG. 6,
- FIG. 9 shows the functional circuit diagram for a variant of the partial flow division of the
- FIG. 10 shows a functional circuit diagram for the division of the partial flows in a centrifugal separator with four tangential feed channels
- FIG. 11 shows a functional circuit diagram for the division of two separately taken partial streams into three tangential feed channels of a centrifugal separator
- FIG. 12 shows a functional circuit diagram for a centrifugal separator with two tangential feed channels and a pressure measuring device.
- the centrifugal separator 10 shown in FIG. 1 consists, in a manner known per se, of a separating space 3, which is connected to a conical lower part 4, and an immersion tube 5, which protrudes from the separating space 3.
- the two feed channels 1, 2 have different cross-sectional areas at their entry points S 1 ( S 2.
- the two tangential feed channels 1, 2 have the same height and each have a rectangular cross-sectional area, and differ only in The width of the feed channel 1 at the entry point Si is wider than that of the other tangential feed channel 2 at the same point S 2.
- the decisive factor is the cross-sectional area directly at the point of entry into the Centrifugal separator 10.
- the tangential feed channels can also have a different cross-sectional profile, for example a conical one.
- the shape or contour of the cross-sectional area does not have to be exclusively rectangular, but can also be circular, for example. The mode of operation of this embodiment variant is explained in more detail with reference to FIG.
- the entire fluid stream of the disperse system to be separated is removed from a storage container and then divided into two partial streams 7 and 8.
- a valve 9 is integrated in the partial flow line for the partial flow 8 before the connection point to the tangential feed channel 1.
- the partial flow 8, which can be changed in its volume flow, is supplied with the larger one via the feed channel 1
- FIGS. 4 and 5 show an embodiment variant which, in comparison to the variant according to FIGS. 1 to 3, is also equipped with an additional swirl chamber 11. This is located above the separating chamber 3 and has a larger diameter than the separating chamber 3.
- the swirl chamber 11 is lower in height than the height of the separating chamber 3.
- the tangential feed channels 1 and 2 open into the swirl chamber 11 on the outer circumference thereof.
- the tangentially introduced partial flows to the central axis of the centrifugal separator 10 are accelerated and made more uniform. This ensures that a particularly high rotational symmetry of the flow is achieved when entering the separating chamber 3.
- FIGS. 6 to 8 show an embodiment variant with three tangential feed channels 1, 2 and 12 with identical cross-sectional areas at the entry points Si, S 2 and S 12 into the swirl chamber 11 of the centrifugal separator 10.
- the entry points S 1f S 2 and S i2 are evenly distributed over the circumference of the swirl chamber 11, and are therefore each at the same distance from one another.
- a component 14 is arranged with a conical surface, the cone tip in the direction of
- Deposition room 3 shows. At the transition point from the swirl chamber 11 into the separating space 3, a distance is provided in parallel in the opposite direction pointing conical or funnel-shaped inlet 15 is arranged. This allows the heavier phase to be pre-separated in the swirl chamber.
- the effect according to the invention only occurs when two tangential feed channels, such as 2 and 12, are fed via one feed line 8 and 5, and the third feed channel, for example 1, is fed via the other feed line 7.
- This circuit variant is shown in FIG. 9.
- the total fluid flow 6 is removed from the storage container by means of a delivery flow pump 16 and divided between the two partial flows 7 and 8.
- the partial flow 7 reaches the centrifugal separator via the tangential feed channel 1 without further influence
- the partial stream 8 is divided into two further sub-streams 8a and 8b, a valve 9 being integrated in the line for the partial stream 8.
- the lower part stream 8a then reaches the centrifugal separator 10 via the tangential feed channel 2 and the lower part stream 8b via the tangential feed channel 12.
- FIG. 10 shows a further embodiment variant according to the invention for an arrangement with four tangential feed channels 1, 2, 12 and 13.
- the feed channels 1 and 12 each have the same cross-sectional area at their entry points Si and S 12 in the centrifugal separator 10 and are arranged opposite one another. Both apply in an analogous manner to the feed
- the partial flow 8 is divided into two further lower partial flows 8a and 8b, which have the larger cross-sectional areas via the tangential feed channels 2 and 13, which have the larger cross-sectional areas at the entry points S 2 and S 13 compared to the two other feed channels 1 and 12 in the centrifugal separator 10 be initiated.
- the other partial flow 7 branching off from the total volume flow is likewise divided into two further partial flows 7a and 7b, which are introduced into the centrifugal separator 10 via the tangential feed channels 1, 12 with the smaller cross-sectional areas at the entry points Si and S 12 .
- FIG. 11 A further embodiment variant is shown in FIG. 11, in which the total volume flow is formed from two separate sub-streams 7, 8, which are either taken from a container or from two locally separated containers, in each case each sub-stream 7, 8 via a separate delivery flow pump 16 and 17.
- the sub-stream 7 then passes into the centrifugal separator 10 without further division via the tangential feed channel 1 with the smaller cross-sectional area at the entry point Si.
- the other sub-stream 8 is divided into two sub-streams 8a and 8b, which pass through the tangential feed channels 2 and 12 with the larger cross-sectional areas at the entry points S 2 and S 12 into the centrifugal separator 10. It is again crucial that the sum of the cross-sectional areas of the entry points S 2 and S 12 is larger than the remaining cross-sectional area.
- the individual flow rates are regulated exclusively via the speed control of the flow pumps 16 and 17. This variant offers the following advantages:
- Certain disperse systems run the risk of clogging the supply lines, particularly in the area of valves. A risk of clogging can be avoided by the possible regulation of the quantities of material to be supplied exclusively by means of the speed control via built-in pumps. If the centrifugal separator is operated in suction mode, the pump or the compressor is arranged behind the centrifugal separator. An influence on the The flow rate then takes place via the characteristic curve of the pump or via the sucked-in false air (aero cyclone).
- FIG. 12 also shows a centrifugal separator as a functional circuit diagram, the structure of which essentially corresponds to the variant shown in FIG. 3.
- a pressure measuring device 18 is integrated, which is connected via a line 19 to the control valve 9, which in the feed line for the partial flow 8 , which is connected to the feed channel 1, is coupled.
- This variant is used when it is a feed stream whose loading remains almost constant and in which the other material properties do not change.
- the simplest implementation of this measure takes place when the total volume flow, the feed flow, is divided into two partial flows, which are introduced directly into the centrifugal separator 10 via a respective tangential feed channel 1 or 2, as shown in FIG.
- the pressure is measured in the feed channel 2, and the measuring point can also be outside this channel 2, for example in the feed line to this channel.
- the control valve 9 is changed as a function of the measured pressure until the pressure has reached the desired setpoint again. As a result, the ratio of the two partial flows is influenced at the same time.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA002348385A CA2348385A1 (en) | 1998-10-29 | 1999-10-27 | Method and device for mechanically separating a disperse system |
AT99955886T ATE249282T1 (en) | 1998-10-29 | 1999-10-27 | METHOD AND DEVICE FOR MECHANICALLY SEPARATING A DISPERSED SYSTEM |
DE59906973T DE59906973D1 (en) | 1998-10-29 | 1999-10-27 | METHOD AND DEVICE FOR MECHANICALLY SEPARATING A DISPERSE SYSTEM |
AU12661/00A AU1266100A (en) | 1998-10-29 | 1999-10-27 | Method and device for mechanically separating a disperse system |
EP99955886A EP1124641B1 (en) | 1998-10-29 | 1999-10-27 | Method and device for mechanically separating a disperse system |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19849645.1 | 1998-10-29 | ||
DE19849645 | 1998-10-29 | ||
DE19920237A DE19920237B4 (en) | 1998-10-29 | 1999-05-03 | Method and device for mechanically separating a disperse system |
DE19920237.0 | 1999-05-03 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000025932A1 true WO2000025932A1 (en) | 2000-05-11 |
Family
ID=26049807
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1999/008097 WO2000025932A1 (en) | 1998-10-29 | 1999-10-27 | Method and device for mechanically separating a disperse system |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP1124641B1 (en) |
CN (1) | CN1121909C (en) |
AT (1) | ATE249282T1 (en) |
AU (1) | AU1266100A (en) |
CA (1) | CA2348385A1 (en) |
WO (1) | WO2000025932A1 (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2007071373A2 (en) * | 2005-12-20 | 2007-06-28 | Slowik Guenter | Method and device for separating oil from crankcase breather gases from an internal combustion engine |
CN103785550A (en) * | 2012-10-29 | 2014-05-14 | 中国石油化工股份有限公司 | Pneumatic particle separator, and fluidized bed reactor and its application |
CN113798071A (en) * | 2021-08-23 | 2021-12-17 | 鞍钢集团矿业有限公司 | Single-inlet multi-channel feed body hydrocyclone |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2520468C1 (en) * | 2013-02-05 | 2014-06-27 | Виктор Александрович Рудницкий | Scrubbing of gas flow from suspended solids |
CN103861326B (en) * | 2013-11-13 | 2016-08-17 | 中石化石油工程设计有限公司 | A kind of three-dimensional multi-point continues pushing-type eddy flow cloth water-bound |
CN104907189A (en) * | 2015-07-02 | 2015-09-16 | 泸州北方化学工业有限公司 | Particle material gas-solid separator |
TWI687258B (en) * | 2019-05-10 | 2020-03-11 | 頂程國際股份有限公司 | Filter apparatus |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1009165A (en) * | 1950-01-26 | 1952-05-26 | Improvements to gas dedusting devices | |
DE875753C (en) * | 1941-11-29 | 1953-05-07 | Kohlenscheidungs Ges Mit Besch | Device for separating solid good parts suspended in a gas flow |
DE1292478B (en) * | 1959-10-20 | 1969-04-10 | Maschf Augsburg Nuernberg Ag | Centrifugal dry separator in cyclone design |
US3507397A (en) * | 1969-04-09 | 1970-04-21 | William R Robinson | Hydrocyclone unit |
DE3936078A1 (en) * | 1989-10-30 | 1991-05-02 | Leuna Werke Veb | Vortex chamber for cyclone dust separator - has tangential inlet ducts arranged in rotational symmetry |
-
1999
- 1999-10-27 EP EP99955886A patent/EP1124641B1/en not_active Expired - Lifetime
- 1999-10-27 WO PCT/EP1999/008097 patent/WO2000025932A1/en active IP Right Grant
- 1999-10-27 CA CA002348385A patent/CA2348385A1/en not_active Abandoned
- 1999-10-27 CN CN99812887.2A patent/CN1121909C/en not_active Expired - Fee Related
- 1999-10-27 AT AT99955886T patent/ATE249282T1/en not_active IP Right Cessation
- 1999-10-27 AU AU12661/00A patent/AU1266100A/en not_active Abandoned
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE875753C (en) * | 1941-11-29 | 1953-05-07 | Kohlenscheidungs Ges Mit Besch | Device for separating solid good parts suspended in a gas flow |
FR1009165A (en) * | 1950-01-26 | 1952-05-26 | Improvements to gas dedusting devices | |
DE1292478B (en) * | 1959-10-20 | 1969-04-10 | Maschf Augsburg Nuernberg Ag | Centrifugal dry separator in cyclone design |
US3507397A (en) * | 1969-04-09 | 1970-04-21 | William R Robinson | Hydrocyclone unit |
DE3936078A1 (en) * | 1989-10-30 | 1991-05-02 | Leuna Werke Veb | Vortex chamber for cyclone dust separator - has tangential inlet ducts arranged in rotational symmetry |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2007071373A2 (en) * | 2005-12-20 | 2007-06-28 | Slowik Guenter | Method and device for separating oil from crankcase breather gases from an internal combustion engine |
WO2007071373A3 (en) * | 2005-12-20 | 2007-09-07 | Guenter Slowik | Method and device for separating oil from crankcase breather gases from an internal combustion engine |
CN103785550A (en) * | 2012-10-29 | 2014-05-14 | 中国石油化工股份有限公司 | Pneumatic particle separator, and fluidized bed reactor and its application |
CN113798071A (en) * | 2021-08-23 | 2021-12-17 | 鞍钢集团矿业有限公司 | Single-inlet multi-channel feed body hydrocyclone |
Also Published As
Publication number | Publication date |
---|---|
CA2348385A1 (en) | 2000-05-11 |
CN1325324A (en) | 2001-12-05 |
ATE249282T1 (en) | 2003-09-15 |
CN1121909C (en) | 2003-09-24 |
AU1266100A (en) | 2000-05-22 |
EP1124641B1 (en) | 2003-09-10 |
EP1124641A1 (en) | 2001-08-22 |
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