EP0981593B1 - Verfahren und vorrichtung zur gewinnung von stearin aus fetten tierischer oder pflanzlicher herkunft - Google Patents
Verfahren und vorrichtung zur gewinnung von stearin aus fetten tierischer oder pflanzlicher herkunft 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
- 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.
- 1
- Kristallisator
- 2
- Aufnahmebehälter
- 3
- Rührwerk
- 4
- Motor
- 5
- Mantel
- 6
- Wärmeisolierschicht
- 7
- Wärmeisolierschicht
- 8
- Pumpe
- 9
- Wärmetauscher
- 10
- Wärmetauscher
- 11
- Zentrifuge
- 12
- Einlauf
- 13
- Verteiler
- 14
- Steigkanal
- 15
- Tellerpaket
- 16
- Greifeinrichtung
- 17
- Stutzen
- 18
- Feststoffraum
- 19
- Schleudertrommel
- 20
- Düse
- 21
- Segment
- 21a
- Auffangraum
- 22
- Strömungsraum
Claims (5)
- 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, dadurch gekennzeichnet, 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 (12) einer nicht selbstentleerenden Düsenzentrifuge eingeführt wird und die Feststoffphase durch sich zu den Düsen (20) verjüngende Strömungsräume (22) geführt und durch die Düsen (20) ausgetragen wird, wobei zur Erzielung einer hohen Trennschärfe das Verhältnis zwischen der Zulaufleistung in l/h und der Düsenleistung in l/h in den Bereich zwischen 2 : 1 und 4 : 1 eingestellt wird.
- Vorrichtung zur Durchführung des Verfahrens nach Anspruch 1 mit einem Kristallisator zur Erwärmung und anschließenden stufenweisen Abkühlung des Fetts pflanzlicher oder tierischer Herkunft und einer nachgeschalteten, mit einem Tellerpaket ausgestatteten Zentrifuge, dadurch gekennzeichnet, daß die Zentrifuge als nicht selbstentleerende Düsenzentrifuge (11) ausgebildet ist, in deren Schleudertrommel (19) sich zu den Düsen (20) verjüngende, durch eingesetzte Segmente (21) begrenzte Strömungsräume (22) für die Feststoffphase angeordnet sind und das Verhältnis zwischen der Einlaufleistung und der Düsenleistung in dem Bereich zwischen 2 : 1 und 4 : 1 liegt.
- Vorrichtung nach Anspruch 2, dadurch gekennzeichnet, daß die in der Schleudertrommel (19) vorgesehenen Segmente (21) aus rostfreiem Stahl gefertigt sind.
- Vorrichtung nach Anspruch 3, dadurch gekennzeichnet, daß die Segmente (21) sich vom Außenbereich des Tellerpakets (15) bis zu den Düsen (20) erstrecken.
- Vorrichtung nach einem der Ansprüche 2 bis 4, dadurch gekennzeichnet, daß die Düsen (20) eine Düsenöffnung mit einem Durchmesser von ca. 0,5 oder ca. 0,6 mm aufweisen.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19719776A DE19719776C1 (de) | 1997-05-10 | 1997-05-10 | Verfahren und Vorrichutng zur Gewinnung von Stearin aus Fetten tierischer oder pflanzlicher Herkunft |
DE19719776 | 1997-05-10 | ||
PCT/EP1998/001663 WO1998051764A1 (de) | 1997-05-10 | 1998-03-21 | Verfahren und vorrichtung zur gewinnung von stearin aus fetten tierischer oder pflanzlicher herkunft |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0981593A1 EP0981593A1 (de) | 2000-03-01 |
EP0981593B1 true EP0981593B1 (de) | 2002-01-16 |
Family
ID=7829189
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP98917043A Expired - Lifetime EP0981593B1 (de) | 1997-05-10 | 1998-03-21 | Verfahren und vorrichtung zur gewinnung von stearin aus fetten tierischer oder pflanzlicher herkunft |
Country Status (11)
Country | Link |
---|---|
US (1) | US6169191B1 (de) |
EP (1) | EP0981593B1 (de) |
AR (1) | AR010156A1 (de) |
AU (1) | AU728509B2 (de) |
BR (1) | BR9804898A (de) |
CO (1) | CO5050406A1 (de) |
DE (1) | DE19719776C1 (de) |
DK (1) | DK0981593T3 (de) |
MY (1) | MY118310A (de) |
NZ (1) | NZ333603A (de) |
WO (1) | WO1998051764A1 (de) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102010006618A1 (de) * | 2010-02-01 | 2011-08-04 | GEA Westfalia Separator GmbH, 59302 | Fraktionierungsverfahren und Fraktionierungsanlage |
DE112022002275T5 (de) | 2021-04-22 | 2024-02-29 | Desmet Belgium | Neuartiges Verfahren und Anlage zur Lösungsmittelfraktionierung |
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 (de) | 1964-04-14 | 1973-10-25 | Tscheskoslovenska Akademie Ved., Prag | Einrichtung zum selbständigen Ab lassen von verdickten Fraktionen aus einer Zentrifuge |
US3797736A (en) * | 1972-04-07 | 1974-03-19 | Westfalia Separator Ag | Method and apparatus for controlling the concentration factor of a discharge |
ATA93974A (de) | 1973-03-09 | 1976-08-15 | Westfalia Separator Ag | Dusenschleudertrommel mit fullstucken |
EP0088949B1 (de) | 1982-03-16 | 1986-05-07 | N.V. Safinco | Verfahren zur Trennung von Feststoffen aus Ölen |
-
1997
- 1997-05-10 DE DE19719776A patent/DE19719776C1/de not_active Expired - Lifetime
-
1998
- 1998-03-21 US US09/214,735 patent/US6169191B1/en not_active Expired - Lifetime
- 1998-03-21 EP EP98917043A patent/EP0981593B1/de not_active Expired - Lifetime
- 1998-03-21 NZ NZ333603A patent/NZ333603A/xx not_active IP Right Cessation
- 1998-03-21 DK DK98917043T patent/DK0981593T3/da active
- 1998-03-21 BR BR9804898-8A patent/BR9804898A/pt not_active IP Right Cessation
- 1998-03-21 WO PCT/EP1998/001663 patent/WO1998051764A1/de active IP Right Grant
- 1998-03-21 AU AU70396/98A patent/AU728509B2/en not_active Ceased
- 1998-04-23 CO CO98022509A patent/CO5050406A1/es unknown
- 1998-05-07 AR ARP980102134A patent/AR010156A1/es unknown
- 1998-05-08 MY MYPI98002096A patent/MY118310A/en unknown
Also Published As
Publication number | Publication date |
---|---|
MY118310A (en) | 2004-09-30 |
DK0981593T3 (da) | 2002-04-29 |
CO5050406A1 (es) | 2001-06-27 |
US6169191B1 (en) | 2001-01-02 |
AU7039698A (en) | 1998-12-08 |
BR9804898A (pt) | 1999-09-08 |
AR010156A1 (es) | 2000-05-17 |
EP0981593A1 (de) | 2000-03-01 |
DE19719776C1 (de) | 1998-12-03 |
NZ333603A (en) | 2000-03-27 |
WO1998051764A1 (de) | 1998-11-19 |
AU728509B2 (en) | 2001-01-11 |
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