EP0507363B1 - Procédé pour l'élimination continue des gommes d'une huile glycéridique - Google Patents

Procédé pour l'élimination continue des gommes d'une huile glycéridique Download PDF

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Publication number
EP0507363B1
EP0507363B1 EP92200543A EP92200543A EP0507363B1 EP 0507363 B1 EP0507363 B1 EP 0507363B1 EP 92200543 A EP92200543 A EP 92200543A EP 92200543 A EP92200543 A EP 92200543A EP 0507363 B1 EP0507363 B1 EP 0507363B1
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EP
European Patent Office
Prior art keywords
oil
stage
gum phase
centrifugal separator
process according
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
Application number
EP92200543A
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German (de)
English (en)
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EP0507363A1 (fr
Inventor
Bernard Cleenewerck
Leo Bevernage
Frans Dewulf
Albert Jan Dijkstra
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Vandemoortele International NV
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Vandemoortele International NV
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Publication date
Application filed by Vandemoortele International NV filed Critical Vandemoortele International NV
Priority to AT92200543T priority Critical patent/ATE89599T1/de
Publication of EP0507363A1 publication Critical patent/EP0507363A1/fr
Application granted granted Critical
Publication of EP0507363B1 publication Critical patent/EP0507363B1/fr
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    • 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
    • C11B3/00—Refining fats or fatty oils
    • C11B3/006—Refining fats or fatty oils by extraction
    • 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
    • C11B3/00—Refining fats or fatty oils
    • C11B3/16—Refining fats or fatty oils by mechanical means

Definitions

  • the present invention relates to a process for the continuous removal of a gum phase from triglyceride oil resulting in a gum phase with low oil content and a degummed oil which after bleaching may be physically refined.
  • the present process comprises the following stages:
  • Crude triglyceride oils as obtained by pressing and/or extracting oil seeds or animal matter contain several compounds other than triglycerides. Some of these compounds such as phosphatides, free fatty acids, odours, colouring matter, waxes and metal compounds must be removed because they adversely affect taste, smell, appearance and keepability of the refined oil.
  • the process disclosed in FR-A-1.108.998 is a process for refining crude triglyceride oil in which, in a first stage, the crude oil is water-degummed with water comprising salts and one centrifuge, and in a second stage the water-degummed oil is alkali refined with sodium hydroxide and one centrifuge.
  • the soapstock resulting from the second stage is discarded while the wet gum phase resulting from the first stage is fed to a holding tank in which the gums are separated from the water comprising salts by gravity.
  • the effluent water is finally recycled for subsequent degumming.
  • the degumming stage itself is operated by one single centrifugal separator.
  • the invention relates to a process for the continuous removal of a gum phase from triglyceride oil resulting in a gum phase with low oil content and a degummed oil which after bleaching may be physically refined.
  • the process according to the invention is a process for the continuous removal of a gum phase from triglyceride oil, comprising the following stages:
  • the process according to the invention can advantageously be used in the degumming process according to US-A-4,698,185.
  • water degummed vegetable oils are treated with finely dispersed aqueous acid whereupon this acid is partially neutralised so that a gum phase is formed. If such oils containing a gum phase are processed according to the present invention, the oils thus obtained may be physically refined.
  • the process according to the invention can advantageously be applied to degum oils treated by the process according to GB-A-1 565 569.
  • This process entails adding an acid to crude oil, allowing a contact time of approximately 10 min., partially neutralising this acid with a base and then allowing an extended contact time for the development of a separate gum phase which is finally to be removed from the oil.
  • the process according to the invention can also advantageously be applied to degum oils treated by the process according to US-A-4,049,686.
  • US-A-4,049,686 a process is described in which oil is treated with an acid and cooled to below 40°C whereupon the nonhydratable phospholipids form gums in a form that can be removed from the oil e.g. by centrifuge.
  • the type of oil to be degummed by the process according to the invention is not critical.
  • edible triglyceride oils like soybean oil, sunflowerseed oil, rapeseed oil, palm oil and other vegetable oils as well as animal oils and fats can all be successfully processed provided the gum phase has been successfully developed before the oil is fed to the first centrifugal separator.
  • the washing water to be mixed into the oil obtained from the first centrifugal separator can be water, diluted non-toxic acid, e.g. citric acid, water containing salts, demineralized water or effluent water resulting from the optional washing stage.
  • the amount of washing water to be mixed into the oil leaving the first centrifugal separator generally ranges from 0.05 to 10 wt.%, preferably between 1 and 5 wt.%.
  • the oil - washing water mixture is then optionally passed to a holding vessel.
  • This holding time generally ranges from 10 seconds to 30 minutes, preferably from 0.5 to 15 minutes.
  • the temperature in said holding vessel is preferably between 60 and 110 °C.
  • the whole process according to the present invention is preferably operated at a temperature ranging from 60 to 110°C, even more preferable at a temperature in the range of 80 to 100°C.
  • the centrifugal separators to be used in the process according to the invention can be disc centrifuges, decanters or other equipment capable of continuously separating a gum phase from an oil phase.
  • the performance of such equipment can commonly be adjusted to yield either a gum stream with low oil content or an oil stream with low gum content as set out in EP-A-349 718.
  • the oil phase obtained by the process according to the invention may further be dried and bleached with commonly known bleaching means prior to being physically refined or refined by alkali neutralisation.
  • the feed consisted of water-degummed soybean oil having a temperature of approximately 90°C, a residual phosphorus content of approximately 120 ppm and an iron content of approximately 1.15 ppm.
  • the separate gum phase was formed according to US-A-4,698,185 applying 0.20 vol.% phosphoric acid of 80 % strength, a contact time equal to 2.5 min. (at a throughput of 9.3 tons/h.) and a 50 % neutralization of the phosphoric acid with 12°Bé caustic soda.
  • the soybean oil comprising a separate gum phase was, in the first stage of the process according to the invention, fed to a centrifugal separator, resulting into a gum phase having a triglyceride oil content of approximately 19 wt.% (calculated on dry matter) and triglyceride oil which still contained a fraction of the phosphatides originally present in the feed.
  • the above table also shows that the moisture content of oil resulting from the second centrifugal separator does not increase when operating in accordance with the invention. It also demonstrates, that the first centrifugal separator is able to remove the extra water introduced into the oil at the stage in between the centrifugal separators.
  • the feed consisted of partially water-degummed rapeseed oil having a temperature of approximately 90°C, a residual phosphorus content of approximately 158 ppm and an iron content of approximately 1.58 ppm.
  • the separate gum phase was formed according to US-A-4,698,185 applying 0.16 vol.% phosphoric acid of 80 % strength, a contact time equal to 2.5 min. (at a throughput of 9.0 tons/h.) and a 50 % neutralization of the phosphoric acid with 12°Bé caustic soda.
  • the rapeseed oil comprising a separate gum phase was, in the first stage of the process according to the invention, fed to a centrifugal separator, resulting into a gum phase having a triglyceride oil content of approximately 14 wt.% (calculated on dry matter) and triglyceride oil which still contained a fraction of the phosphatides originally present in the feed.
  • the same rapeseed oil, in which the separate gum phase was formed as mentioned above, was treated by the process according to EP-A-0 349 718, including two washing stages.
  • the oil content of the gum phase obtained by the process according to EP-A-349 718 was approximately 12.6 % (calculated on dry matter).
  • oils thus obtained were bleached with 0.5 wt.% bleaching earth ( Tonsil ACCFF, Süd Chemie, Kunststoff, Germany) at 100°C under vacuum for 30 minutes whereupon the oil was allowed to cool to below 90°C before the bleaching earth was filtered off. Subsequently, the bleached oils were physically refined at 240°C for 2 hours at a vacuum below 400 Pa (30 mmHg). Both oils had a bland neutral taste and showed excellent keepability.
  • Tonsil ACCFF Tonsil ACCFF, Süd Chemie, Kunststoff, Germany
  • the above table 2 clearly illustrates that the residual phosphorus content of the oil resulting from the second centrifugal separator is much lower when operating in accordance to the invention rather than according to EP-A-0 349 718. Furthermore, the above table shows that the oil according to the invention can, after drying, be bleached with the usual amount of bleaching earth in order to obtain a high quality refined oil.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Microbiology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Fats And Perfumes (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Peptides Or Proteins (AREA)
  • Centrifugal Separators (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)

Claims (7)

  1. Procédé pour l'élimination en continu d'une phase gomme d'une huile triglycéridique, caractérisé en ce qu'il comprend les étapes suivantes :
    a) au cours d'une première étape, on soumet une phase gomme séparée à une séparation centrifuge dans un premier séparateur centrifuge pour obtenir une phase gomme à teneur en huile minimale et une huile qui contient encore une fraction des gommes présentes à l'origine dans la charge,
    b) au cours d'une seconde étape, on mélange une proportion de 0,05 à 10% en poids, de préférence 1 à 5% en poids, d'eau de lavage à l'huile obtenue à partir du premier séparateur centrifuge, le mélange ainsi obtenu étant éventuellement envoyé dans un réservoir de retenue.
    c) au cours d'une troisième étape, on soumet le mélange obtenu à l'étape b) à une séparation par centrifugation dans un second séparateur centrifuge pour obtenir une huile à teneur en gomme résiduelle minimale et une phase gomme humide à teneur en huile bien supérieure à celle de la phase gomme obtenue à l'étape a),
    d) au cours d'une quatrième étape, on recycle la phase gomme obtenue à l'étape c) dans le courant d'huile introduit dans le premier séparateur centrifuge.
  2. Procédé suivant la revendication 1, caractérisé en ce que l'on choisit l'eau de lavage dans le groupe formé par l'eau, un acide atoxique dilué et de l'eau contenant des sels.
  3. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que l'eau de lavage est de l'eau déminéralisée.
  4. Procédé suivant la revendication 1 ou 2, caractérisé en ce que l'eau de lavage est constituée par un acide atoxique, de préférence l'acide citrique, dilué.
  5. Procédé suivant la revendication 1, caractérisé en ce que l'eau de lavage est l'effluent provenant du traitement de l'huile obtenue à l'étape c) dans une étape de lavage à l'eau subséquente.
  6. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que l'on fait passer le mélange de l'étape b) par un récipient de retenue et on l'y laisse reposer pendant une période variant de 10 secondes à 30 minutes, de préférence 0,5 à 15 minutes.
  7. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que la température varie de 60 à 110°C, de préférence de 80 à 100°C, au cours du traitement.
EP92200543A 1991-04-02 1992-02-26 Procédé pour l'élimination continue des gommes d'une huile glycéridique Expired - Lifetime EP0507363B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT92200543T ATE89599T1 (de) 1991-04-02 1992-02-26 Verfahren zur kontinuierlichen entschleimung eines glyceridoeles.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP91105198 1991-04-02
EP91105198 1991-04-02

Publications (2)

Publication Number Publication Date
EP0507363A1 EP0507363A1 (fr) 1992-10-07
EP0507363B1 true EP0507363B1 (fr) 1993-05-19

Family

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EP92200543A Expired - Lifetime EP0507363B1 (fr) 1991-04-02 1992-02-26 Procédé pour l'élimination continue des gommes d'une huile glycéridique

Country Status (13)

Country Link
EP (1) EP0507363B1 (fr)
JP (1) JPH05117685A (fr)
AT (1) ATE89599T1 (fr)
CA (1) CA2063929A1 (fr)
CZ (1) CZ289672B6 (fr)
DE (1) DE69200004T2 (fr)
DK (1) DK0507363T3 (fr)
ES (1) ES2055634T3 (fr)
HU (1) HU212977B (fr)
MX (1) MX9201460A (fr)
PL (1) PL169760B1 (fr)
RU (1) RU2008328C1 (fr)
SK (1) SK279220B6 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8278351B2 (en) 2001-07-27 2012-10-02 Neptune Technologies & Bioressources, Inc. Natural marine source phospholipids comprising polyunsaturated fatty acids and their applications
US8586567B2 (en) 2009-10-29 2013-11-19 Acasti Pharma, Inc. Concentrated therapeutic phospholipid compositions

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0560121A3 (en) * 1992-03-09 1994-07-27 Vandemoortele Int Nv Method for refining glyceride oil
EP0583648A3 (fr) * 1992-08-19 1995-02-01 Vandemoortele Int Nv Procédé de raffinage en continu avec des effluents réduits.
WO1997024933A1 (fr) * 1996-01-05 1997-07-17 Grow Green Pty. Ltd. Charge d'alimentation de proteines; compositions, procedes et dispositif de production associes
WO1999002630A1 (fr) * 1997-07-09 1999-01-21 Crystallisation And Degumming Sprl Procede d'elimination des metaux des corps gras et des gommes associes a ces metaux
US6844458B2 (en) 1998-11-20 2005-01-18 Ip Holdings, L.L.C. Vegetable oil refining
US6426423B1 (en) * 1998-11-20 2002-07-30 I.P. Holdings Methods for treating phosphatide-containing mixtures
WO2009132463A1 (fr) * 2008-05-02 2009-11-05 Neptune Technologies & Bioressources Inc. Nouveau procédé de désodorisation et amélioration organoleptique d'extraits d'huile d'animal marin
DE102008048009A1 (de) 2008-09-19 2010-03-25 Rmenergy Umweltverfahrenstechnik Gmbh Vorrichtung zur dezentralen Aufbereitung nativer Öle und Fette zur Nutzung als Kraftstoff oder als Rohstoff für die Biodieselherstellung
JP6801958B2 (ja) * 2015-12-24 2020-12-16 日清オイリオグループ株式会社 焙煎油の製造方法、及び食用油脂組成物の製造方法
CN107011991B (zh) * 2017-04-12 2021-04-13 西北大学 一种油脂的阳离子树脂脱磷方法
WO2021124444A1 (fr) * 2019-12-17 2021-06-24 株式会社Ｉｈｉ原動機 Dispositif de démucilagination d'huile végétale brute
WO2021124443A1 (fr) * 2019-12-17 2021-06-24 株式会社Ｉｈｉ原動機 Système de génération d'énergie

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE507650A (fr) *
GB481580A (en) * 1935-06-29 1938-03-11 Sharples Specialty Co Improvements in or relating to the treatment of fatty oils
FR1108998A (fr) * 1954-07-10 1956-01-19 Separation Sa Franc Pour La Perfectionnements au traitement des huiles végétales
MX7580E (es) * 1981-10-15 1989-11-23 Cpc International Inc Procedimiento para la refinacion de aceites vegetales crudos
US4927544A (en) * 1988-07-06 1990-05-22 N.V. Vandemoortele International Process for the continuous removal of a gum phase from triglyceride oil

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8278351B2 (en) 2001-07-27 2012-10-02 Neptune Technologies & Bioressources, Inc. Natural marine source phospholipids comprising polyunsaturated fatty acids and their applications
US8383675B2 (en) 2001-07-27 2013-02-26 Neptune Technologies & Bioressources, Inc. Natural marine source phospholipids comprising polyunsaturated fatty acids and their applications
US8680080B2 (en) 2001-07-27 2014-03-25 Neptune Technologies & Bioressources, Inc. Natural marine source phospholipids comprising polyunsaturated fatty acids and their applications
US10028968B2 (en) 2001-07-27 2018-07-24 Aker Biomarine Antarctic As Natural marine source phospholipids comprising polyunsaturated fatty acids and their applications
US8586567B2 (en) 2009-10-29 2013-11-19 Acasti Pharma, Inc. Concentrated therapeutic phospholipid compositions
US9475830B2 (en) 2009-10-29 2016-10-25 Acasti Pharma Inc. Concentrated therapeutic phospholipid compositions
US10130644B2 (en) 2009-10-29 2018-11-20 Acasti Pharma Inc. Concentrated therapeutic phospholipid compositions
US10617702B2 (en) 2009-10-29 2020-04-14 Acasti Pharma Inc. Concentrated therapeutic phospholipid compositions

Also Published As

Publication number Publication date
EP0507363A1 (fr) 1992-10-07
CA2063929A1 (fr) 1992-10-03
HU9201094D0 (en) 1992-06-29
RU2008328C1 (ru) 1994-02-28
HUT62646A (en) 1993-05-28
JPH05117685A (ja) 1993-05-14
CS95792A3 (en) 1992-10-14
DE69200004D1 (de) 1993-06-24
ATE89599T1 (de) 1993-06-15
HU212977B (en) 1997-01-28
PL169760B1 (en) 1996-08-30
DE69200004T2 (de) 1993-09-09
PL294068A1 (en) 1992-12-14
SK279220B6 (sk) 1998-08-05
DK0507363T3 (da) 1993-08-30
ES2055634T3 (es) 1994-08-16
CZ289672B6 (cs) 2002-03-13
MX9201460A (es) 1992-10-01

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