EP0981593B1 - Method and device for obtaining stearin from animal or vegetable fats - Google Patents
Method and device for obtaining stearin from animal or vegetable fats Download PDFInfo
- Publication number
- EP0981593B1 EP0981593B1 EP98917043A EP98917043A EP0981593B1 EP 0981593 B1 EP0981593 B1 EP 0981593B1 EP 98917043 A EP98917043 A EP 98917043A EP 98917043 A EP98917043 A EP 98917043A EP 0981593 B1 EP0981593 B1 EP 0981593B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- nozzle
- nozzles
- centrifuge
- stearin
- capacity
- 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.)
- Expired - Lifetime
Links
- 0 C(C1)C2C=C=*C1C2 Chemical compound C(C1)C2C=C=*C1C2 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B7/00—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils
- C11B7/0075—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of melting or solidifying points
-
- 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
- B04B1/12—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 with continuous discharge
Definitions
- the invention relates to a method for obtaining stearin from fats of animal or vegetable origin, in which the fat is heated to a Temperature is liquefied at which there are no crystals in the liquid and in which a gradual cooling then takes place to form crystals and the crystallized oil into the inlet of a plate pack Centrifuge is introduced.
- the invention further relates to an apparatus for performing this method.
- the invention has for its object a method of the aforementioned Kind as well as a device for performing this method so that the selectivity between the stearin phase during the duration of a production and the oil phase for optimal stearin quality and stearin yield constant can be held.
- This object is achieved in that the cooling of the crystallized oil up to to a temperature in the temperature range of 40 ° C and below, but above 10 ° C and the crystallized oil in the inlet of a not self-draining, with a plate pack and a stationary gripping device for the oil phase equipped nozzle centrifuge is introduced and the solid phase led through flow spaces tapering to the nozzles and through the Nozzles is discharged, the to achieve a high selectivity Ratio between the feed rate in l / h and the nozzle rate in l / h in the Range between 2: 1 and 4: 1 is set.
- the crystallized Cooling oil By using a nozzle centrifuge, it is sufficient that the crystallized Cooling oil to a temperature in the temperature range from 10 ° C to 40 ° C, before it is inserted into the centrifuge inlet.
- the nozzles arranged in the peripheral area of the centrifugal drum tapered flow spaces are limited by segment inserts that are made up of Stainless steel. These segment inserts ensure a predetermined Guiding the solid phase from the outside of the plate pack to the nozzles. Deposits of solid particles between two neighboring nozzles and also the occurrence of mixed phases in the solid space are avoided.
- a device for performing the method according to the invention is in the Drawings shown and will be described below.
- crystallizer 1 a fat of animal or vegetable origin except for one Liquefied temperature at which there are no crystals in the liquid. This is followed by gradual cooling to form crystals.
- the crystallizer 1 has a receptacle 2 for the fat to be liquefied on, which is equipped with an agitator 3, which is driven by a motor 4 becomes.
- the receptacle is in its peripheral and in its bottom area equipped with a jacket 5 of a heat exchange medium.
- This coat will in the bottom area by a heat insulation layer 6 and in the peripheral area a heat insulation layer 7 covered on the outside.
- Heat exchange medium circulated by a pump 8.
- Heat exchange medium is used water, either through a steam operated heat exchanger 9 heated or by one with ice water operated heat exchanger 10 can be cooled.
- the crystallizer 1 e.g. Butter oil heated to 55 ° C by means of hot water from the jacket 5 and over a period of 30 min. kept at this temperature while the agitator rotates at 8 rpm. This ensures that the entire Oil is in liquid, uncrystallized form.
- the oil is then cooled with a temperature difference of 15 ° C until the water has reached 32 ° C. Then one takes place at constant water temperature further cooling of the oil until a product temperature of 36 ° C is reached. On this is to prevent too much oil from spontaneously crystallizing out. It many, uniformly sized crystals are formed.
- the agitator runs at 8 Rpm at.
- the next goal is to reach the required fractionation temperature.
- this embodiment is with a temperature difference of 6 ° C and a Agitator speed of 8 rpm worked until the fractionation temperature is achieved.
- the temperature control in the crystallizer is different.
- crystallizer 1 is followed by a nozzle centrifuge 11, which in the Figures 2 and 3 shows the crystal size distribution in the starting material relatively unimportant, so that there are shorter crystallization times than in the Carrying out the separation of the solid phase and the liquid phase under Use of filter devices.
- the crystallized oil processed in the crystallizer 1 is the inlet 12 of the Centrifuge 11 supplied and from there passes through a distributor 13 in the Rising channels 14 of a plate pack 15. In the separation spaces between the individual Plates of the plate pack are separated from the stearin phase from the oil phase instead of.
- the oil phase flows to the center of the centrifuge and is via a stationary one Gripping device 16 and a nozzle 17 discharged from the centrifuge.
- the stearin phase flows through the solid space 18 of the centrifugal drum 19 and is distributed evenly around the circumference of the centrifugal drum Nozzles 20 discharged into a collecting space 21.
- the nozzles 20 preferably have a nozzle diameter of 0.5 or 0.6 mm on.
- the nozzle output of a nozzle is approx. 150 l / h.
- the ratio between the centrifuge feed rate and the nozzle rate lies in the range between 2: 1 and 4: 1.
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Fats And Perfumes (AREA)
- Edible Oils And Fats (AREA)
- Centrifugal Separators (AREA)
Description
Die Erfindung bezieht sich auf ein Verfahren zur Gewinnung von Stearin aus Fetten tierischer oder pflanzlicher Herkunft, bei dem das Fett durch Erwärmen auf eine Temperatur verflüssigt wird, bei der keine Kristalle in der Flüssigkeit vorhanden sind und bei dem anschließend zur Kristallbildung eine stufenweise Abkühlung erfolgt und das kristallisierte Öl in den Einlauf einer mit einem Tellerpaket ausgerüsteten Zentrifuge eingeführt wird.The invention relates to a method for obtaining stearin from fats of animal or vegetable origin, in which the fat is heated to a Temperature is liquefied at which there are no crystals in the liquid and in which a gradual cooling then takes place to form crystals and the crystallized oil into the inlet of a plate pack Centrifuge is introduced.
Die Erfindung betrifft ferner eine Vorrichtung zur Durchführung dieses Verfahrens.The invention further relates to an apparatus for performing this method.
Es ist bekannt, zur Trennung der festen (Stearin) von der flüssigen Phase Vakuum-Bandfilter oder Filterpressen einzusetzen. Schwierigkeiten treten bei einem Verstopfen der Filterporen insbesondere dann auf, wenn sich diese Filterporen auch durch eine Dampfbehandlung nicht wieder öffnen lassen.It is known to separate the solid (stearin) from the liquid phase vacuum belt filter or use filter presses. Difficulties arise with constipation of the filter pores in particular when these filter pores are also visible do not let steam treatment open again.
Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art sowie eine Vorrichtung zur Durchführung dieses Verfahrens so zu gestalten, daß während der Dauer einer Produktion die Trennschärfe zwischen der Stearinphase und der Ölphase für eine optimale Stearinqualität und Stearinausbeute konstant gehalten werden kann.The invention has for its object a method of the aforementioned Kind as well as a device for performing this method so that the selectivity between the stearin phase during the duration of a production and the oil phase for optimal stearin quality and stearin yield constant can be held.
Diese Aufgabe wird dadurch gelöst, daß die Abkühlung des kristallisierten Öls bis auf eine Temperatur im Temperaturbereich von 40 °C und darunter, jedoch oberhalb 10 °C vorgenommen und das kristallisierte Öl in den Einlauf einer nicht selbstentleerenden, mit einem Tellerpaket und einer ortsfesten Greifeinrichtung für die Ölphase ausgestatteten Düsenzentrifuge eingeführt wird und die Feststoffphase durch sich zu den Düsen verjüngende Strömungsräume geführt und durch die Düsen ausgetragen wird, wobei zur Erzielung einer hohen Trennschärfe das Verhältnis zwischen der Zulaufleistung in l/h und der Düsenleistung in l/h in dem Bereich zwischen 2 : 1 und 4 : 1 eingestellt wird. This object is achieved in that the cooling of the crystallized oil up to to a temperature in the temperature range of 40 ° C and below, but above 10 ° C and the crystallized oil in the inlet of a not self-draining, with a plate pack and a stationary gripping device for the oil phase equipped nozzle centrifuge is introduced and the solid phase led through flow spaces tapering to the nozzles and through the Nozzles is discharged, the to achieve a high selectivity Ratio between the feed rate in l / h and the nozzle rate in l / h in the Range between 2: 1 and 4: 1 is set.
Durch die Verwendung einer Düsenzentrifuge ist es ausreichend, das kristallisierte Öl bis auf eine Temperatur im Temperaturbereich von 10 °C bis 40 °C abzukühlen, bevor es in den Einlauf der Zentrifuge eingeführt wird.By using a nozzle centrifuge, it is sufficient that the crystallized Cooling oil to a temperature in the temperature range from 10 ° C to 40 ° C, before it is inserted into the centrifuge inlet.
Die sich zu den im Umfangsbereich der Schleudertrommel angeordneten Düsen verjüngenden Strömungsräume werden durch Segmenteinsätze begrenzt, die aus Edelstahl gefertigt sind. Diese Segmenteinsätze gewährleisten eine vorgegebene Führung der Feststoffphase aus dem Außenbereich des Tellerpakets zu den Düsen. Ablagerungen von Feststoffteilchen zwischen zwei benachbarten Düsen und auch das Auftreten von Mischphasen im Feststoffraum werden vermieden.The nozzles arranged in the peripheral area of the centrifugal drum tapered flow spaces are limited by segment inserts that are made up of Stainless steel. These segment inserts ensure a predetermined Guiding the solid phase from the outside of the plate pack to the nozzles. Deposits of solid particles between two neighboring nozzles and also the occurrence of mixed phases in the solid space are avoided.
Durch diesen Segmenteinsatz kann eine Trennschärfe zwischen der Stearinphase und der Ölphase erzielt werden, die besser ist als die der übrigen heute eingesetzten Technologien.By using this segment, a distinction between the stearin phase and the oil phase, which is better than that of the others used today Technologies.
Weitere Merkmale der Erfindung ergeben sich aus den Unteransprüchen.Further features of the invention emerge from the subclaims.
Eine Vorrichtung zur Durchführung des erfindungsgemäßen Verfahrens ist in den Zeichnungen dargestellt und wird im folgenden beschrieben.A device for performing the method according to the invention is in the Drawings shown and will be described below.
Es zeigen:
- Figur 1
- einen Kristallisator in schematischer Darstellung,
Figur 2- eine dem Kristallisator nachgeschaltete Düsenzentrifuge, teilweise im Vertikalschnitt und
- Figur 3
- einen schematischen, horizontalen Schnitt nach der Linie III-III durch die Düsentrommel.
- Figure 1
- a crystallizer in a schematic representation,
- Figure 2
- a nozzle centrifuge downstream of the crystallizer, partly in vertical section and
- Figure 3
- a schematic, horizontal section along the line III-III through the nozzle drum.
In dem Kristallisator 1 wird ein Fett tierischer oder pflanzlicher Herkunft bis auf eine Temperatur verflüssigt, bei der in der Flüssigkeit keine Kristalle vorhanden sind. Anschließend erfolgt zur Kristallbildung eine stufenweise Abkühlung.In the crystallizer 1, a fat of animal or vegetable origin except for one Liquefied temperature at which there are no crystals in the liquid. This is followed by gradual cooling to form crystals.
Der Kristallisator 1 weist einen Aufnahmebehälter 2 für das zu verflüssigende Fett
auf, der mit einem Rührwerk 3 ausgerüstet ist, das über einen Motor 4 angetrieben
wird. Der Aufnahmebehälter ist in seinem Umfangs- und in seinem Bodenbereich
mit einem Mantel 5 eines Wärmetauschermediums ausgestattet. Dieser Mantel wird
im Bodenbereich durch eine Wärmeisolierschicht 6 und im Umfangsbereich durch
eine Wärmeisolierschicht 7 nach außen abgedeckt. In dem Mantel 5 wird das
Wärmetauschermedium durch eine Pumpe 8 umgewälzt. Als
Wärmetauschermedium wird Wasser benutzt, das entweder durch einen mit Dampf
betriebenen Wärmetauscher 9 aufgeheizt oder durch einen mit Eiswasser
betriebenen Wärmetauscher 10 abgekühlt werden kann.The crystallizer 1 has a
Im Kristallisator 1 wird z.B. Butteröl auf 55 °C mittels Heißwasser des Mantels 5 aufgeheizt
und über einen Zeitraum von 30 min. auf dieser Temperatur gehalten, während
das Rührwerk mit 8 U/min umläuft. Hierdurch wird erreicht, daß das gesamte
Öl in flüssiger unkristallisierter Form vorliegt.In the crystallizer 1 e.g. Butter oil heated to 55 ° C by means of hot water from the
Das Öl wird dann mit einer Temperaturdifferenz von 15 °C so lange abgekühlt, bis das Wasser 32 °C erreicht hat. Dann erfolgt bei konstanter Wassertemperatur eine weitere Abkühlung des Öls, bis eine Produkttemperatur von 36 °C erzielt wird. Auf diese Weise soll verhindert werden, daß zuviel Öl spontan auskristallisiert. Es kommt zur Bildung vieler, gleichmäßig großer Kristalle. Das Rührwerk läuft mit 8 U/min um.The oil is then cooled with a temperature difference of 15 ° C until the water has reached 32 ° C. Then one takes place at constant water temperature further cooling of the oil until a product temperature of 36 ° C is reached. On this is to prevent too much oil from spontaneously crystallizing out. It many, uniformly sized crystals are formed. The agitator runs at 8 Rpm at.
Hat das Produkt 36 °C erreicht, so wird für eine Dauer von 420 min mit einer konstanten Temperaturdifferenz von 3 °C langsam abgekühlt. Es findet nun die hauptsächlich, schonende Kristallbildung statt. Das Rührwerk läuft mit 4 U/min um.When the product has reached 36 ° C, it remains constant for a period of 420 min Temperature difference of 3 ° C slowly cooled. Now it mainly finds gentle crystal formation instead. The agitator rotates at 4 rpm.
Nach diesem Verfahrensschritt ist die Kristallbildung weitgehend abgeschlossen. Das nächste Ziel ist das Erreichen der erforderlichen Fraktionierungstemperatur. Bei diesem Ausführungsbeispiel wird mit einer Temperaturdifferenz von 6 °C und einer Rührwerksdrehzahl von 8 U/min gearbeitet bis die Fraktionierungstemperatur erreicht wird.After this process step, crystal formation is largely complete. The next goal is to reach the required fractionation temperature. at this embodiment is with a temperature difference of 6 ° C and a Agitator speed of 8 rpm worked until the fractionation temperature is achieved.
Bei Pflanzenölen und anderen Fetten erfolgt eine andere Temperaturführung im Kristallisator.For vegetable oils and other fats, the temperature control in the crystallizer is different.
Sofern dem Kristallisator 1 eine Düsenzentrifuge 11 nachgeschaltet ist, die in den Figuren 2 und 3 aufgezeigt ist, ist die Kristallgrößenverteilung im Ausgangsmaterial relativ unwichtig, so daß sich kürzere Kristallisationszeiten ergeben als bei der Durchführung der Trennung der Feststoffphase und der Flüssigkeitsphase unter Verwendung von Filtereinrichtungen.If the crystallizer 1 is followed by a nozzle centrifuge 11, which in the Figures 2 and 3 shows the crystal size distribution in the starting material relatively unimportant, so that there are shorter crystallization times than in the Carrying out the separation of the solid phase and the liquid phase under Use of filter devices.
Das im Kristallisator 1 aufbereitete kristallisierte Öl wird dem Einlauf 12 der
Zentrifuge 11 zugeführt und gelangt von dort über einen Verteiler 13 in die
Steigkanäle 14 eines Tellerpakets 15. in den Trennräumen zwischen den einzelnen
Tellern des Tellerpakets findet die Trennung der Stearinphase von der Ölphase
statt. Die Ölphase strömt zum Zentrum der Zentrifuge und wird über eine ortsfeste
Greifeinrichtung 16 und einen Stutzen 17 aus der Zentrifuge ausgestragen.The crystallized oil processed in the crystallizer 1 is the
Die Stearinphase durchströmt den Feststoffraum 18 der Schleudertrommel 19 und
wird durch am Umfang der Schleudertrommel gleichmäßig verteilt angeordnete
Düsen 20 in einen Auffangraum 21 ausgetragen.The stearin phase flows through the
Zwischen zwei benachbarten Düsen 20 ist jeweils ein aus rostfreiem Stahl
gefertigtes Segment 21 angeordnet und begrenzt einen aus dem Umfangsbereich
des Tellerpakets 15 sich erstreckenden und zur Düse 20 hin sich verjüngenden
Strömungsraum 22 für die Feststoffphase.Between two
Die Düsen 20 weisen vorzugsweise einen Düsendurchmesser von 0,5 oder von 0,6
mm auf. Die Düsenleistung einer Düse beträgt ca. 150 l/h.The
Das Verhältnis zwischen der Zulaufleistung der Zentrifuge und der Düsenleistung liegt im Bereich zwischen 2 : 1 und 4 : 1. The ratio between the centrifuge feed rate and the nozzle rate lies in the range between 2: 1 and 4: 1.
- 11
- KristallisatorCrystallizer
- 22
- Aufnahmebehälterreceptacle
- 33
- Rührwerkagitator
- 44
- Motorengine
- 55
- Mantelcoat
- 66
- Wärmeisolierschichtthermal insulating layer
- 77
- Wärmeisolierschichtthermal insulating layer
- 88th
- Pumpepump
- 99
- Wärmetauscherheat exchangers
- 1010
- Wärmetauscherheat exchangers
- 1111
- Zentrifugecentrifuge
- 1212
- Einlaufenema
- 1313
- Verteilerdistributor
- 1414
- Steigkanalrising channel
- 1515
- TellerpaketDisc stack
- 1616
- Greifeinrichtunggripper
- 1717
- StutzenSupport
- 1818
- FeststoffraumSolid space
- 1919
- Schleudertrommelcentrifugal drum
- 2020
- Düsejet
- 2121
- Segmentsegment
- 21a21a
- Auffangraumstaging area
- 2222
- Strömungsraumflow chamber
Claims (5)
- Method of obtaining stearin from fats of animal or vegetable origin, in which the fat is liquefied by heating to a temperature at which there are no crystals in the liquid and in which crystallisation is followed by gradual cooling and the crystallised oil is introduced into the inlet of a centrifuge equipped with a stack of discs, characterised in that the crystallised oil is cooled to a temperature in the region of 40°C and lower, but higher than 10°C and the crystallised oil is introduced into the inlet (12) of a non-self-draining nozzle-type centrifuge and the solid phase is guided through flow chambers (22) which taper toward the nozzles (20) and is discharged through the nozzles (20), the ratio between the feed capacity in l/h and the nozzle capacity in l/h being adjusted in the range between 2 : 1 and 4 : 1 for achieving precise separation.
- Apparatus for carrying out the method according to claim 1 comprising a crystalliser for the heating and subsequent gradual cooling of the fat of vegetable or animal origin and a subsequent centrifuge equipped with a stack of discs, characterised in that the centrifuge is constructed as a non-self-draining nozzle-type centrifuge (11) with solid phase flow chambers (22) which taper towards the nozzle (20) and are limited by inserted segments (21) arranged in its centrifugal drum (19) and the ratio between the inlet capacity and the nozzle capacity is in the range between 2 : 1 and 4 : 1.
- Apparatus according to claim 2, characterised in that the segments (21) provided in the centrifugal drum (19) are produced from stainless steel.
- Apparatus according to claim 3, characterised in that the segments (21) extend from the outer region of the stack of discs (15) to the nozzles (20).
- Apparatus according to claim any of claims 2 to 4, characterised in that the nozzles (20) have a nozzle aperture with a diameter of about 0.5 or about 0.6 mm.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19719776A DE19719776C1 (en) | 1997-05-10 | 1997-05-10 | Process and device for obtaining stearin from fats of animal or vegetable origin |
| DE19719776 | 1997-05-10 | ||
| PCT/EP1998/001663 WO1998051764A1 (en) | 1997-05-10 | 1998-03-21 | Method and device for obtaining stearin from animal or vegetable fats |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0981593A1 EP0981593A1 (en) | 2000-03-01 |
| EP0981593B1 true EP0981593B1 (en) | 2002-01-16 |
Family
ID=7829189
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP98917043A Expired - Lifetime EP0981593B1 (en) | 1997-05-10 | 1998-03-21 | Method and device for obtaining stearin from animal or vegetable fats |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US6169191B1 (en) |
| EP (1) | EP0981593B1 (en) |
| AR (1) | AR010156A1 (en) |
| AU (1) | AU728509B2 (en) |
| BR (1) | BR9804898A (en) |
| CO (1) | CO5050406A1 (en) |
| DE (1) | DE19719776C1 (en) |
| DK (1) | DK0981593T3 (en) |
| MY (1) | MY118310A (en) |
| NZ (1) | NZ333603A (en) |
| WO (1) | WO1998051764A1 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102010006618A1 (en) * | 2010-02-01 | 2011-08-04 | GEA Westfalia Separator GmbH, 59302 | Fractionation process and fractionation plant |
| DE112022002275T5 (en) | 2021-04-22 | 2024-02-29 | Desmet Belgium | Novel process and system for solvent fractionation |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2807411A (en) * | 1954-10-06 | 1957-09-24 | Sharples Corp | Process of centrifugally separating glycerides from oil |
| US3111490A (en) * | 1959-12-21 | 1963-11-19 | Dorr Oliver Inc | Centrifuge machine |
| US3145223A (en) * | 1961-09-22 | 1964-08-18 | Pennsalt Chemicals Corp | Winterizing glyceride oils |
| DE1482708C3 (en) * | 1964-04-14 | 1973-10-25 | Tscheskoslovenska Akademie Ved., Prag | Device for the independent Ab let thickened fractions from a centrifuge |
| US3797736A (en) * | 1972-04-07 | 1974-03-19 | Westfalia Separator Ag | Method and apparatus for controlling the concentration factor of a discharge |
| ATA93974A (en) * | 1973-03-09 | 1976-08-15 | Westfalia Separator Ag | SHOWER SPIN DRUM WITH FULL PIECES |
| EP0088949B1 (en) * | 1982-03-16 | 1986-05-07 | N.V. Safinco | Process for separating solids from oils |
-
1997
- 1997-05-10 DE DE19719776A patent/DE19719776C1/en not_active Expired - Lifetime
-
1998
- 1998-03-21 WO PCT/EP1998/001663 patent/WO1998051764A1/en active IP Right Grant
- 1998-03-21 AU AU70396/98A patent/AU728509B2/en not_active Ceased
- 1998-03-21 BR BR9804898-8A patent/BR9804898A/en not_active IP Right Cessation
- 1998-03-21 NZ NZ333603A patent/NZ333603A/en not_active IP Right Cessation
- 1998-03-21 US US09/214,735 patent/US6169191B1/en not_active Expired - Lifetime
- 1998-03-21 EP EP98917043A patent/EP0981593B1/en not_active Expired - Lifetime
- 1998-03-21 DK DK98917043T patent/DK0981593T3/en active
- 1998-04-23 CO CO98022509A patent/CO5050406A1/en unknown
- 1998-05-07 AR ARP980102134A patent/AR010156A1/en unknown
- 1998-05-08 MY MYPI98002096A patent/MY118310A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| DK0981593T3 (en) | 2002-04-29 |
| EP0981593A1 (en) | 2000-03-01 |
| CO5050406A1 (en) | 2001-06-27 |
| BR9804898A (en) | 1999-09-08 |
| NZ333603A (en) | 2000-03-27 |
| AR010156A1 (en) | 2000-05-17 |
| AU728509B2 (en) | 2001-01-11 |
| AU7039698A (en) | 1998-12-08 |
| US6169191B1 (en) | 2001-01-02 |
| MY118310A (en) | 2004-09-30 |
| DE19719776C1 (en) | 1998-12-03 |
| WO1998051764A1 (en) | 1998-11-19 |
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