EP2015871B1 - Séparateur à trois phases avec un disque d'épluchage et des ouvertures de sortie de matières solides - Google Patents
Séparateur à trois phases avec un disque d'épluchage et des ouvertures de sortie de matières solides Download PDFInfo
- Publication number
- EP2015871B1 EP2015871B1 EP06724790.8A EP06724790A EP2015871B1 EP 2015871 B1 EP2015871 B1 EP 2015871B1 EP 06724790 A EP06724790 A EP 06724790A EP 2015871 B1 EP2015871 B1 EP 2015871B1
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- EP
- European Patent Office
- Prior art keywords
- drum
- separator
- phase
- disk
- solid
- Prior art date
- Legal status (The legal status 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 status listed.)
- Active
Links
- 239000007787 solid Substances 0.000 title claims description 27
- 239000012071 phase Substances 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 27
- 239000007788 liquid Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 24
- 239000007791 liquid phase Substances 0.000 claims description 20
- 239000010779 crude oil Substances 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000000839 emulsion Substances 0.000 claims description 8
- 238000005191 phase separation Methods 0.000 claims description 6
- 239000007790 solid phase Substances 0.000 claims description 5
- 238000005352 clarification Methods 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 238000011109 contamination Methods 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- 230000008569 process Effects 0.000 description 13
- 238000010276 construction Methods 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 238000006073 displacement reaction Methods 0.000 description 3
- 230000012447 hatching Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 235000019198 oils Nutrition 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000012937 correction Methods 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 210000003027 ear inner Anatomy 0.000 description 1
- 235000021323 fish oil Nutrition 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B11/00—Feeding, charging, or discharging bowls
- B04B11/08—Skimmers or scrapers for discharging ; Regulating thereof
- B04B11/082—Skimmers for discharging liquid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
- B04B1/04—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with inserted separating walls
- B04B1/08—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with inserted separating walls of conical shape
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
- B04B1/10—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with discharging outlets in the plane of the maximum diameter of the bowl
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B11/00—Feeding, charging, or discharging bowls
- B04B11/02—Continuous feeding or discharging; Control arrangements therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B13/00—Control arrangements specially designed for centrifuges; Programme control of centrifuges
- B04B2013/006—Interface detection or monitoring of separated components
Definitions
- the invention relates to a separator according to the preamble of claim 1 as from WO 96/34693 is known and a method for three-phase separation with such a separator.
- Such separators have been known for a long time.
- the liquid discharges are provided with so-called peeling discs, in which the effect is exploited that the rotational energy of the incoming liquid is converted into a back pressure in the discharge line.
- peeling discs have proven themselves.
- a well-known three-phase separator is in Fig. 3 shown. If one or both of the two fluid outlets from the drum are assigned a paring disc and the further outlet is nozzle-like, the result is an area delta LP within which the paring disc permits a displacement of the separation zone in the drum by throttling (see, eg, US Pat WO 86/01436 ).
- the range of displaceability of the separation zone is still relatively low and it is not readily possible to move the separating zone in operation fast enough about the peeling discs.
- the shift also does not always lead to stable process conditions, since the variation of the throttling of the peeling disk processes directly affects several parameters of the process.
- the invention has the object of developing the generic separator such that in a simple manner during operation, a displacement of the separation zone within the drum over a larger radial range is possible, with an improved adjustability of the position of the separation zone should be possible.
- a method for operating such a separator is also to be proposed.
- Throttle devices also on the type in operation non-rotating annular discs are known from the field of solid bowl screw centrifuges known per se - so from the DE 102 09 925 A1 or the DE 102 03 652 A1 , However, the drums of these centrifuges are stored in the region of both axial ends and not oscillating like centrifuges. This results in the difference that the drums of the decanter or solid bowl centrifuges rotate about a defined axis, while the Separatortrommeln Perform a certain precession movement, so that it was assumed that the conditions at the drain ring gap are not constant enough to achieve a defined adjustment of the separation zone between light and heavy phase and a shift of the drainage radius of the heavy liquid phase by means of an adjustable throttle plate. This assumption has not been confirmed. Contrary to expectations, stable conditions also occur at the outlet gap of the separator at the throttle disk. Rather, the throttle disc improves process efficiency as well as fine tuning and process stability.
- the separator is suitable for a wide variety of three-phase separation tasks, in particular crude oil processing, in which the crude oil is clarified by solids and water is separated from the crude oil.
- the invention also provides a use of a separator according to the invention according to one of the corresponding claims for crude oil treatment in which the crude oil is clarified by solids and water is separated from the crude oil.
- the invention also provides a process for the three-phase separation and clarification of a product to be processed in at least two liquid phases and a solid phase, wherein the processing of the product takes place in a separator according to one of the corresponding claims directed to this, wherein for adjusting the separation zone once in operation adjusting the radius of the light liquid phase LP by means of the paring disc and then adjusting the heavy liquid phase (HP) and thus the separation zone by means of the throttle device, preferably the annular disc takes place.
- Fig.1 to 3 each show separator drums 1, which have a vertically oriented axis of rotation at the radius r 0 .
- the Separatortrommeln 1 are each set to a rotary spindle 2, for example, the type of Fig. 4 driven directly or via a belt (not shown here) or otherwise (eg a gearbox) is.
- the rotary spindle 2 may be designed conically in its upper peripheral region.
- the rotary spindle 2 is mounted with at least one or more bearings 3 on one side of the drum - here below the drum - oscillating and therefore describes in operation due to residual unbalance unlike a decanter a new axis adjusts a kind of precession movement around the vertical r 0 ( please refer Fig. 4 in which the inclination angle ⁇ is shown).
- constructions are also known in which a lower drum is quasi “suspended" on an upper rotary spindle. Again, however, the drum is rotatably mounted oscillating only at one of its ends or subsequent to one of its axial ends.
- the separator drum 1 has a feed pipe 4 for a product P to be hurled, to which a distributor 5 adjoins, which is provided with at least one or more outlet openings 6, through which incoming centrifugal material (crossed hatching) into the interior of the separator drum 1 and the Rising channel 7 of the plate package can be passed.
- a feed through the spindle e.g. from below is also possible.
- the construction is chosen such that the outlet openings 6 below a riser channel 7 in a plate package 8 (outer diameter at reference numeral 8) of conically shaped separating plates 9 are.
- the plate package 8 of a Sheath plate 17 completed, which has a larger diameter than the plate package.
- the Emulionsline or dividing line (also called E line) - forms a separation zone between a lighter liquid phase LP (hatching from the left bottom right top) and a heavier liquid phase HP (hatching to the lower right).
- the lighter liquid phase LP (light phase) is conducted at an inner radius r LP with the aid of a paring disc 10 (also called a gripper) from the drum.
- a paring disc 10 also called a gripper
- the paring disc acts like a pump.
- the peeling disk is downstream of a valve 18 for throttling, for example, outside the separator in its downstream discharge.
- the heavy liquid phase HP flows around the outer circumference of the disc plate 17 through discharge passage 11 to a liquid outlet 12 at the upper axial end of the drum 1 (radius r HP ).
- the constructions of the invention Fig. 1 and 2 are different than the construction of the Fig. 3 provided in the region of the liquid outlet 12 with an adjustable throttle device 13, by means of which the cross section is variable at the liquid outlet.
- this throttle device 13 In order to realize this throttle device 13 structurally in a simple manner, it is proposed according to the type Fig. 2 and 3 to arrange in the axial direction above the liquid outlet 12 outside the drum 1, a kind of annular or throttle plate 19, which is arranged and formed spaced from the at least one liquid outlet opening, wherein the position of the annular disc 19 to the at least one Outlet opening is variable.
- the disc may have a flat surface or be provided with grooves, for example.
- the surface of the annular disc is preferably - but not necessarily - aligned perpendicular to the drum axis.
- the annular disc 19 is e.g. axially displaceable or arranged pivotably on one of its peripheral edges and the annular disc is associated with a drive which is adapted to change the distance between the preferably stationary during operation annular disc 19 and the outlet opening 12.
- the annular disc 19 is designed to be stationary during operation and does not rotate with the drum 1 with.
- the radius of the E-line can be moved within the drum by a certain range.
- the double conical drum in the region of its largest diameter solid discharge nozzles 21, which serve for the continuous discharge of solid particles S from the drum.
- This embodiment is preferred. Embodiments without an additional solids discharge are also conceivable.
- the displaceable annular disc leads to a significant improvement in the adjustability of the emulsion line (E-line) and to a better controllability and controllability of the process. This also results in an enlarged adjustment range of the separation zone.
- E-line emulsion line
- the outlet openings 12 may have a round shape in the manner of bores or may be e.g. Wedge-like or step-like widening from the inside out, which increases the control capability in different cases .. It could also be a tube placed in the outlet openings, which would have the advantage that the liquid flow does not attach to the drum.
- This consists of a liquid outlet in the drum upstream disk 15 which extends from the outer periphery of the paring disc 10 to the outside and having a maximum circumferential radius which is greater than the largest radius to which the outlet openings 12 extend.
- the standing still, non-rotating (shutter) disc 15 is in turn connected upstream of the drum 1, a kind of annular disc 16 as the first weir, which extends from the inner periphery of the drum cover of the drum 1 inwardly and whose inner radius is smaller than the largest Radius to which the disc 15 and the outlet openings 12 extend, so that in the region between the annular disc 16 and the outlet openings 12 (as 2nd weir) on the inner circumference of the drum cover of the drum 1, the Hydrohermitikringformat 14 is formed.
- This chamber prevents the uncontrolled escape of gases or steam from the drum through the outlet openings 12 or labyrinths or other gaps or the like, which would cause a short-term instability in the region of the emulsion line - separation zone -.
- the throttling device 13 alone can achieve an adjustability of the discharge radius of the heavy liquid phase of about 336 to 384 mm (ie 48 mm) or a compensation of the density variance (K) of 0.884 to 0.915 (0.031), because either by reaction to shifts or in product changes by changing the gap width of the gap 20 counteracted a displacement of the separation zone to keep them at a constant radius as possible to keep the process stable.
- the peeling disk 10 alone can achieve an adjustment of the radius of the dividing line of 360 to 392 mm (32 mm) or a compensation of the density change (K) of 0.878 to 0.900 (0.022).
- the throttling device 13 and the peeling disk 10 can achieve an adjustment of the separating zone or the radius of the E-line of 336 to 414 mm (corresponding to 78 mm) or a density ratio variance (K) of 0.863 to 0.915 (0.052).
- a separate and independent water supply into the drum (not shown here, feasible, for example, by a concentric supply pipe within the supply pipe 4 for the product and further through the manifold into the drum) to provide in the three-phase separation - without a To exert additional hydraulic load on the stack of plates - to ensure that there is always a sufficient back pressure at the gap 20. If, on the other hand, the gap were not completely traversed, there would possibly be an uncontrolled shift in the e-line.
- the discharge volume flow through the gap 20 is preferably observed and possibly also measured in order to prevent such dry runs and to minimize the volume of water to be added as much as possible.
- the nozzle discharge capacity may be initially determined theoretically based on the machine design and drum rotation speed. This capacity is hereinafter referred to as "nominal" capacity or derivative rate.
- the nozzles 21 will show wear and a period of time within which it is advisable to repair the solids discharge nozzles 21 may be indicated. This is advantageous because it is possible to maximize the time to change nozzles.
- the measured "drain rate" is less than the nominal rate, one can conclude that one or more of the solids discharge nozzles 21 are clogged.
- the system may be configured to automatically correct the effect of nozzle wear when determining whether the solids discharge nozzles are clogged or not.
- the pressure drop across the throttle device depends on the flow rate or quantity and the size of the gap 20.
- the pressure drop over the paring disc 10 depends on the flow rate and the throttling pressure on the valve 20 of the paring disc.
- the pressure drops affect the discharge rates of the heavy and light phases. Combined and considered individually, the discharge line radii also influence the position of the E-line.
- the user can conclude that a greater proportion of heavy phase is in the light phase and vice versa.
- a stable separation process can be maintained although fluctuation in the product feed rate and composition may occur or density fluctuations of the heavy and / or lighter liquid phases LP and HP.
- Such effects occur e.g. in natural products such as fish oil or in the treatment of crude oil (separation of water from the crude oil) or in the treatment of water (in particular separation of oil residues from the water).
- a correction of the flow rate of the solids can be performed by measuring the solids content, since the solids density is a relatively constant parameter.
- the light phase density and finally the density can be measured directly.
- the inflow and outflow rates of the heavy and light phases can be determined.
- This simple expert system can be supplemented by an online measurement of the exact heavy phase composition and the light phases. Neither the heavy nor the light phases typically have a polarity which would make measuring the volumetric concentration easy.
Landscapes
- Centrifugal Separators (AREA)
Claims (19)
- Séparateur avec un tambour de séparateur (1) en forme de cône simple ou double au moins à l'intérieur, qui est supporté avec possibilité de rotation à une seule de ses extrémités axiales et qui présente un axe de rotation vertical ainsi que :a) uniquement à son extrémité inférieure ou à son extrémité supérieure, une broche rotative pour l'entraînement du tambour de séparateur, qui est supportée de façon pendulaire autour d'un point d'articulation (G) ;b) un tuyau d'arrivée (4) pour un produit à traiter ;c) au moins deux sorties de liquide pour une phase légère (LP) et une phase lourde (HP), la sortie de liquide pour la phase légère (LP) étant munie d'une turbine centripète,d) de préférence, des ouvertures d'extraction de solides au niveau de sa plus grande circonférence intérieure,e) un paquet de disques de séparation disposé dans le tambour de séparateur,caractérisé en ce quef) la sortie de liquide (12) de la phase lourde (HP) est suivie d'un dispositif d'étranglement réglable (13) à l'extérieur du tambour, qui présente de préférence un disque annulaire (19) et qui est conçu pour décaler le rayon du liquide R(HP) jusqu'auquel la phase lourde s'étend dans le tambour en modifiant la section de sortie de l'étranglement réalisé pour la phase liquide lourde.
- Séparateur selon la revendication 1, caractérisé en ce que le disque annulaire (19) est disposé au-dessus de la sortie de liquide (12) dans le sens axial, à l'extérieur du tambour (1).
- Séparateur selon l'une des revendications précédentes, caractérisé en ce que le disque annulaire (19) est associé à un dispositif d'entraînement et en ce que le disque annulaire est disposé de façon mobile dans le sens axial, en particulier avec possibilité de translation et/ou de basculement, de sorte que la distance entre le disque annulaire (19) en fonctionnement et l'ouverture de sortie, autrement dit la largeur d'une fente annulaire (20), est modifiable.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce que le disque annulaire (19) est conçu pour ne pas être rotatif en fonctionnement.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce que les ouvertures de sortie des solides sont conformées comme des buses (21) dimensionnées pour évacuer les particules solides du tambour (2) en continu.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce que les buses de sortie des solides (21) peuvent être fermées au moyen d'une soupape à piston.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce que les buses de sortie des solides (21) contiennent des buses et une soupape à piston.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce qu'il comporte un autre tuyau d'arrivée s'étendant dans le tambour pour un liquide tel que de l'eau à ajouter au produit à traiter.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce qu'il comporte au moins un ou plusieurs capteurs pour la mesure des débits de produit au niveau des arrivées et/ou des écoulements.
- Séparateur selon l'une des revendications précédentes, caractérisé en ce que la sortie de liquide (12) pour la phase liquide lourde et le dispositif d'étranglement (13) sont précédés par une chambre annulaire hydrohermétique (14).
- Séparateur selon la revendication 10, caractérisé en ce que la chambre annulaire hydrohermétique (14) se compose d'un disque d'accumulation (15) monté en amont d'une sortie de liquide (12) à l'intérieur du tambour, qui s'étend vers l'extérieur à partir de la circonférence extérieure de la turbine centripète (10) et qui présente un rayon de circonférence maximal qui est plus grand que le plus grand rayon jusqu'auquel les ouvertures de sortie (12) s'étendent, le disque d'accumulation étant précédé d'un disque annulaire (16) qui s'étend à partir de la circonférence extérieure du couvercle du tambour (1) vers l'intérieur et dont le rayon intérieur est plus petit que le plus grand rayon jusqu'auquel s'étendent le disque d'accumulation (15) et les ouvertures de sortie (12), de sorte que la chambre annulaire hydrohermétique (14) est formée dans la zone comprise entre le disque annulaire (16) et les ouvertures de sortie (12) sur la circonférence intérieure du couvercle du tambour (1).
- Procédé pour la séparation et l'épuration de trois phases d'un produit à traiter en au moins deux phases liquides et une phase solide, caractérisé en ce que le traitement du produit a lieu dans un séparateur selon l'une des revendications précédentes, le rayon de la phase liquide légère (LP) étant réglé une fois au moyen de la turbine centripète (10) pour définir la zone de séparation, puis la phase liquide lourde (HP) et ainsi la zone de séparation étant réglées au moyen du dispositif d'étranglement (13) formé par le disque annulaire (19).
- Procédé selon la revendication 12, caractérisé en ce que la zone de séparation est maintenue à un rayon constant par un procédé de régulation en fonction de la quantité de produit amenée et/ou de la texture.
- Procédé selon la revendication 12 ou 13, caractérisé en ce que les débits dans la conduite d'alimentation en liquide du tambour et de la conduite de sortie de liquide hors du tambour sont déterminés, en particulier mesurés, au niveau de la turbine centripète et du dispositif d'étranglement et en ce que le débit de solides est déterminé à partir de la différence entre ces grandeurs.
- Procédé, en particulier selon la revendication 12, 13 ou 14, caractérisé en ce qu'un changement du débit déterminé pour la phase solide est utilisé pour déduire un changement de l'état des buses d'évacuation des solides, une augmentation du débit signalant une usure des buses et une diminution du débit un colmatage ou un encrassement des buses.
- Procédé selon la revendication 15, caractérisé en ce qu'en cas de formation d'une émulsion, l'ajustement de la turbine centripète et du dispositif d'étranglement permet de déplacer la zone de séparation de telle façon que l'émulsion soit évacuée à travers la turbine centripète ou la fente du dispositif d'étranglement.
- Procédé selon l'une des revendications 12 à 16, caractérisé en ce que la teneur en solides du produit amené dans le tambour de séparateur est mesurée.
- Procédé selon l'une des revendications 12 à 17, caractérisé en ce que le volume d'écoulement de la phase liquide légère est déterminé, en particulier mesuré.
- Utilisation d'un séparateur selon l'une des revendications précédentes pour la préparation d'huile brute, dans laquelle l'huile brute est épurée des solides et l'eau est séparée de l'huile brute.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/EP2006/004414 WO2007131515A1 (fr) | 2006-05-11 | 2006-05-11 | Séparateur à trois phases avec un disque d'épluchage et des ouvertures de sortie de matières solides |
Publications (2)
Publication Number | Publication Date |
---|---|
EP2015871A1 EP2015871A1 (fr) | 2009-01-21 |
EP2015871B1 true EP2015871B1 (fr) | 2017-04-26 |
Family
ID=37547697
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP06724790.8A Active EP2015871B1 (fr) | 2006-05-11 | 2006-05-11 | Séparateur à trois phases avec un disque d'épluchage et des ouvertures de sortie de matières solides |
Country Status (6)
Country | Link |
---|---|
US (1) | US8192342B2 (fr) |
EP (1) | EP2015871B1 (fr) |
CN (1) | CN101189068B (fr) |
CA (1) | CA2619883C (fr) |
NO (1) | NO341606B1 (fr) |
WO (1) | WO2007131515A1 (fr) |
Families Citing this family (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2007131515A1 (fr) * | 2006-05-11 | 2007-11-22 | Westfalia Separator Ag | Séparateur à trois phases avec un disque d'épluchage et des ouvertures de sortie de matières solides |
EP2091656A1 (fr) * | 2006-11-15 | 2009-08-26 | Westfalia Separator Australia Pty.Ltd. | Ensemble de centrifugeuse autonettoyante continue |
DE202007009212U1 (de) * | 2007-06-30 | 2008-12-11 | Gea Westfalia Separator Gmbh | Drei-Phasen-Trennseparator |
SE535959C2 (sv) * | 2010-01-29 | 2013-03-05 | Alfa Laval Corp Ab | System innefattande centrifugalseparator samt metod för kontroll av detsamma |
EP2366457B1 (fr) * | 2010-03-19 | 2013-03-06 | Alfa Laval Corporate AB | Dispositif et procédé pour la surveillance et l'ajustement de la position radiale d'une couche d'interface dans un séparateur centrifugal. |
CN102179315A (zh) * | 2010-09-20 | 2011-09-14 | 辽宁双联化工制药机械有限公司 | 油田老化油处理用碟式分离机 |
DE102010038195A1 (de) * | 2010-10-14 | 2012-04-19 | Gea Mechanical Equipment Gmbh | Verfahren zur Phasentrennung eines Produktes mit einer Zentrifuge |
US8317672B2 (en) * | 2010-11-19 | 2012-11-27 | Kensey Nash Corporation | Centrifuge method and apparatus |
CN203425926U (zh) * | 2013-06-27 | 2014-02-12 | 国宇新兴(北京)技术发展有限公司 | 离心真空复合分离机 |
CN103316782A (zh) * | 2013-07-05 | 2013-09-25 | 安徽赛而特离心机有限公司 | 一种三相碟式分离机转鼓组 |
CA2870910C (fr) * | 2013-11-12 | 2017-09-19 | Syncrude Canada Ltd. | Procede de detection et de controle de perte de ligne de separation |
CN103962248A (zh) * | 2014-05-07 | 2014-08-06 | 江苏巨能机械有限公司 | 三相碟式分离机 |
ES2807592T3 (es) * | 2015-04-24 | 2021-02-23 | Alfa Laval Corp Ab | Separador centrífugo y métodos relacionados con el mismo |
SE538912C2 (sv) * | 2015-05-27 | 2017-02-07 | Apparatus for cleaning crank case gases | |
BR102015028129B1 (pt) | 2015-11-09 | 2021-11-03 | Delp Engenharia Mecânica S.A. | Separador centrífugo |
DE102018105586A1 (de) * | 2018-03-12 | 2019-09-12 | Hengst Se | Rotor eines Zentrifugalabscheiders und Zentrifugalabscheider |
EP3666388A1 (fr) * | 2018-12-10 | 2020-06-17 | Alfa Laval Corporate AB | Système et procédé de séparation centrifuge |
CN115379902A (zh) | 2020-02-06 | 2022-11-22 | 波特研究公司 | 离心机以及有关系统和方法 |
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US3179334A (en) * | 1961-09-15 | 1965-04-20 | Pennsalt Chemicals Corp | Centrifuge discharge means |
DE1220012B (de) | 1963-07-24 | 1966-06-30 | Lohmann & Welschehold Kg | Schnurschalter mit Glimmlampe |
US4042172A (en) | 1976-04-14 | 1977-08-16 | Andrei Stepanovich Nozdrovsky | Bowl centrifuge rotor |
DE2617692A1 (de) | 1976-04-23 | 1977-11-03 | G P I Nii Gipronikel | Schleudertrommel einer absetzzentrifuge |
DE2707111C3 (de) | 1977-02-18 | 1979-08-23 | Flottweg-Werk Dr. Georg Bruckmayer Gmbh & Co Kg, 8313 Vilsbiburg | Vollmantel-Schneckenzentrifuge zur Trennung eines Feststoff-Flüssigkeitsgemisches |
DE3014315C2 (de) | 1980-04-15 | 1985-07-18 | Klöckner-Humboldt-Deutz AG, 5000 Köln | Verfahren und Vorrichtung zum Entfernen von Metallen aus Metallsalzlösungen |
DE3104578A1 (de) | 1980-04-15 | 1982-10-28 | Klöckner-Humboldt-Deutz AG, 5000 Köln | Verfahren zum entfernen von metallen aus metallsalzloesungen |
SE8302215D0 (sv) * | 1983-04-20 | 1983-04-20 | Alfa Laval Marine Power Eng | Centrifugalseparator |
DK410284A (da) | 1984-08-28 | 1986-03-01 | Alfa Laval Zeta As | Fremgangsmaade til styring af graensefladen mellem olie og vand ved slamudtoemning fra en centrifuge til separering af olie og vand og slam |
SE456801B (sv) * | 1987-03-19 | 1988-11-07 | Alfa Laval Separation Ab | Utloppsanordning vid centrifugalseparator |
DE3728901C1 (en) | 1987-08-29 | 1988-11-17 | Westfalia Separator Ag | Weir for adjusting the level of liquid in solid-bowl centrifuge drums of worm centrifuges |
DE3822983A1 (de) | 1988-07-07 | 1990-01-11 | Hiller Gmbh | Vollmantel-schneckenzentrifuge |
DE3921327A1 (de) | 1989-06-29 | 1991-01-03 | Kloeckner Humboldt Deutz Ag | Wehr zum einstellen des fluessigkeitsstandes in vollmantelzentrifugen |
DE4132029A1 (de) | 1991-09-26 | 1993-04-01 | Westfalia Separator Ag | Wehrscheibe zum einstellen des fluessigkeitsstandes in vollmantelschleudertrommeln von schneckenzentrifugen |
DE4320265C2 (de) | 1993-06-18 | 1995-08-03 | Westfalia Separator Ag | Wehr für Vollmantelschleudertrommeln |
DE19500600C1 (de) | 1995-01-11 | 1996-02-08 | Westfalia Separator Ag | Vollmantelzentrifuge |
SE505440C2 (sv) | 1995-05-02 | 1997-08-25 | Alfa Laval Ab | Förfarande och centrifugalseparator för separering av två vätskor |
US5643169A (en) | 1995-06-06 | 1997-07-01 | Baker Hughes Incorporated | Decanter centrifuge with adjustable gate control |
US5695442A (en) | 1995-06-06 | 1997-12-09 | Baker Hughes Incorporated | Decanter centrifuge and associated method for producing cake with reduced moisture content and high throughput |
SE9600299D0 (sv) * | 1996-01-29 | 1996-01-29 | Tetra Laval Holdings & Finance | Utloppsanordning och en centrifugalseparator försedd med en sådan utloppsanordning |
US6368264B1 (en) | 1999-03-29 | 2002-04-09 | M-I L.L.C. | Centrifuge control system and method with operation monitoring and pump control |
SE521432C2 (sv) * | 1999-06-03 | 2003-11-04 | Alfa Laval Corp Ab | Sätt att ställa in ett gränsskikts radiella nivå i en centrifugalseparator |
US6572524B1 (en) | 2000-07-14 | 2003-06-03 | Alfa Laval Inc. | Decanter centrifuge having a heavy phase solids baffle |
EP1232794B1 (fr) | 2001-02-08 | 2004-06-09 | Westfalia Separator AG | Procédé pour la séparation d'un mélange à phases multiples et système de centrifugeuse décanteuse pour la mise en oeuvre dudit procédé |
DE10203652B4 (de) | 2002-01-30 | 2006-10-19 | Westfalia Separator Ag | Vollmantel-Schneckenzentrifuge mit einem Wehr |
DE10209925B4 (de) | 2002-03-07 | 2010-06-17 | Gea Westfalia Separator Gmbh | Dreiphasen-Vollmantel-Schneckenzentrifuge, Vollmantel-Schneckenzentrifuge und Verfahren zum Betreiben einer Dreiphasen-Vollmantel-Schneckenzentrifuge |
DE10223802B4 (de) | 2002-05-29 | 2005-06-09 | Westfalia Separator Ag | Vollmantel-Schneckenzentrifuge |
CN2756319Y (zh) * | 2004-08-19 | 2006-02-08 | 上海航发机械有限公司 | 悬吊转鼓碟式分离机 |
SE528387C2 (sv) | 2005-03-08 | 2006-10-31 | Alfa Laval Corp Ab | Centrifugalseparator och förfarande för separering av en produkt i åtminstone en relativt tung fas och en relativt lätt fas |
WO2007131515A1 (fr) * | 2006-05-11 | 2007-11-22 | Westfalia Separator Ag | Séparateur à trois phases avec un disque d'épluchage et des ouvertures de sortie de matières solides |
DE202007009212U1 (de) * | 2007-06-30 | 2008-12-11 | Gea Westfalia Separator Gmbh | Drei-Phasen-Trennseparator |
-
2006
- 2006-05-11 WO PCT/EP2006/004414 patent/WO2007131515A1/fr active Application Filing
- 2006-05-11 EP EP06724790.8A patent/EP2015871B1/fr active Active
- 2006-05-11 CN CN2006800197761A patent/CN101189068B/zh not_active Expired - Fee Related
- 2006-05-11 CA CA2619883A patent/CA2619883C/fr active Active
- 2006-05-11 US US11/922,495 patent/US8192342B2/en active Active
-
2008
- 2008-12-10 NO NO20085146A patent/NO341606B1/no not_active IP Right Cessation
Non-Patent Citations (1)
Title |
---|
None * |
Also Published As
Publication number | Publication date |
---|---|
NO341606B1 (no) | 2017-12-11 |
CA2619883C (fr) | 2014-04-15 |
CA2619883A1 (fr) | 2007-11-22 |
NO20085146L (no) | 2008-12-10 |
WO2007131515A1 (fr) | 2007-11-22 |
US8192342B2 (en) | 2012-06-05 |
CN101189068A (zh) | 2008-05-28 |
CN101189068B (zh) | 2011-09-28 |
EP2015871A1 (fr) | 2009-01-21 |
US20090298666A1 (en) | 2009-12-03 |
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