WO2000025932A1 - Procede et dispositif pour la separation mecanique d'un systeme disperse - Google Patents

Procede et dispositif pour la separation mecanique d'un systeme disperse Download PDF

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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
Application number
PCT/EP1999/008097
Other languages
German (de)
English (en)
Inventor
Günter Slowik
Jürgen Kohlmann
Original Assignee
Slowik Guenter
Kohlmann Juergen
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE19920237A external-priority patent/DE19920237B4/de
Application filed by Slowik Guenter, Kohlmann Juergen filed Critical Slowik Guenter
Priority to AU12661/00A priority Critical patent/AU1266100A/en
Priority to DE59906973T priority patent/DE59906973D1/de
Priority to CA002348385A priority patent/CA2348385A1/fr
Priority to AT99955886T priority patent/ATE249282T1/de
Priority to EP99955886A priority patent/EP1124641B1/fr
Publication of WO2000025932A1 publication Critical patent/WO2000025932A1/fr

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.

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  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Centrifugal Separators (AREA)
  • Cyclones (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)

Abstract

L'invention concerne un procédé pour la séparation mécanique, dans un séparateur centrifuge, d'un système dispersé en deux ou plusieurs systèmes dispersés ayant des propriétés différentes, ainsi qu'un dispositif convenant à la réalisation du procédé. Partant des inconvénients liés à l'état connu de la technique, l'invention vise à créer un procédé du type en question permettant, sans modifications structurelles importantes, de faire varier de manière importante le degré de séparation indépendamment du débit de fluide et d'influer sur la maille et la précision de séparation. A cet effet, on partage les flux partiels (7, 8) en conduits d'alimentation (1, 2) se distinguant par la superficie de leur section au niveau des points d'entrée (S1, S2) dans le séparateur centrifuge. En cas de partage des flux partiels en plus de deux conduits d'alimentation tangentiels (1, 2, 12, 13), on calcule les superficies de section (2 et 13 ou 1 et 12) en additionnant les superficies des sections des conduits d'alimentation reliés au flux partiel correspondant (7 ou 8), les sommes des superficies des sections des flux partiels respectifs (7 ou 8) différant ainsi aux points d'entrée (S2, S13 ou S1, S12) dans le séparateur centrifuge.
PCT/EP1999/008097 1998-10-29 1999-10-27 Procede et dispositif pour la separation mecanique d'un systeme disperse WO2000025932A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU12661/00A AU1266100A (en) 1998-10-29 1999-10-27 Method and device for mechanically separating a disperse system
DE59906973T DE59906973D1 (de) 1998-10-29 1999-10-27 Verfahren und vorrichtung zum mechanischen trennen eines dispersen systems
CA002348385A CA2348385A1 (fr) 1998-10-29 1999-10-27 Procede et dispositif pour la separation mecanique d'un systeme disperse
AT99955886T ATE249282T1 (de) 1998-10-29 1999-10-27 Verfahren und vorrichtung zum mechanischen trennen eines dispersen systems
EP99955886A EP1124641B1 (fr) 1998-10-29 1999-10-27 Procede et dispositif pour la separation mecanique d'un systeme disperse

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE19849645 1998-10-29
DE19849645.1 1998-10-29
DE19920237.0 1999-05-03
DE19920237A DE19920237B4 (de) 1998-10-29 1999-05-03 Verfahren und Vorrichtung zum mechanischen Trennen eines dispersen Systems

Publications (1)

Publication Number Publication Date
WO2000025932A1 true WO2000025932A1 (fr) 2000-05-11

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Application Number Title Priority Date Filing Date
PCT/EP1999/008097 WO2000025932A1 (fr) 1998-10-29 1999-10-27 Procede et dispositif pour la separation mecanique d'un systeme disperse

Country Status (6)

Country Link
EP (1) EP1124641B1 (fr)
CN (1) CN1121909C (fr)
AT (1) ATE249282T1 (fr)
AU (1) AU1266100A (fr)
CA (1) CA2348385A1 (fr)
WO (1) WO2000025932A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007071373A2 (fr) * 2005-12-20 2007-06-28 Slowik Guenter Procede et dispositif de deshuilage des gaz de ventilation d'un carter de vilebrequin d'un moteur a combustion interne
CN103785550A (zh) * 2012-10-29 2014-05-14 中国石油化工股份有限公司 气流式颗粒分选器和流化床反应器及其应用
CN113798071A (zh) * 2021-08-23 2021-12-17 鞍钢集团矿业有限公司 一种单入口多通道式进料体水力旋流器

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2520468C1 (ru) * 2013-02-05 2014-06-27 Виктор Александрович Рудницкий Способ очистки газового потока от твердых взвесей
CN103861326B (zh) * 2013-11-13 2016-08-17 中石化石油工程设计有限公司 一种立体多点位续推式旋流布水结构
CN104907189A (zh) * 2015-07-02 2015-09-16 泸州北方化学工业有限公司 颗粒物料气固分离器
TWI687258B (zh) * 2019-05-10 2020-03-11 頂程國際股份有限公司 過濾裝置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1009165A (fr) * 1950-01-26 1952-05-26 Perfectionnements aux dispositifs de dépoussiérage des gaz
DE875753C (de) * 1941-11-29 1953-05-07 Kohlenscheidungs Ges Mit Besch Einrichtung zum Abscheiden fester, in einem Gasstrom schwebender Gutteile
DE1292478B (de) * 1959-10-20 1969-04-10 Maschf Augsburg Nuernberg Ag Fliehkraft-Trockenabscheider in Zyklonbauweise
US3507397A (en) * 1969-04-09 1970-04-21 William R Robinson Hydrocyclone unit
DE3936078A1 (de) * 1989-10-30 1991-05-02 Leuna Werke Veb Drallerzeuger fuer zyklonabscheider

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE875753C (de) * 1941-11-29 1953-05-07 Kohlenscheidungs Ges Mit Besch Einrichtung zum Abscheiden fester, in einem Gasstrom schwebender Gutteile
FR1009165A (fr) * 1950-01-26 1952-05-26 Perfectionnements aux dispositifs de dépoussiérage des gaz
DE1292478B (de) * 1959-10-20 1969-04-10 Maschf Augsburg Nuernberg Ag Fliehkraft-Trockenabscheider in Zyklonbauweise
US3507397A (en) * 1969-04-09 1970-04-21 William R Robinson Hydrocyclone unit
DE3936078A1 (de) * 1989-10-30 1991-05-02 Leuna Werke Veb Drallerzeuger fuer zyklonabscheider

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007071373A2 (fr) * 2005-12-20 2007-06-28 Slowik Guenter Procede et dispositif de deshuilage des gaz de ventilation d'un carter de vilebrequin d'un moteur a combustion interne
WO2007071373A3 (fr) * 2005-12-20 2007-09-07 Guenter Slowik Procede et dispositif de deshuilage des gaz de ventilation d'un carter de vilebrequin d'un moteur a combustion interne
CN103785550A (zh) * 2012-10-29 2014-05-14 中国石油化工股份有限公司 气流式颗粒分选器和流化床反应器及其应用
CN113798071A (zh) * 2021-08-23 2021-12-17 鞍钢集团矿业有限公司 一种单入口多通道式进料体水力旋流器

Also Published As

Publication number Publication date
EP1124641A1 (fr) 2001-08-22
CN1325324A (zh) 2001-12-05
ATE249282T1 (de) 2003-09-15
CN1121909C (zh) 2003-09-24
AU1266100A (en) 2000-05-22
EP1124641B1 (fr) 2003-09-10
CA2348385A1 (fr) 2000-05-11

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