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EP0507363A1 - Verfahren zur kontinuierlichen Entschleimung eines Glyceridöles - Google Patents

Verfahren zur kontinuierlichen Entschleimung eines Glyceridöles Download PDF

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Publication number
EP0507363A1
EP0507363A1 EP92200543A EP92200543A EP0507363A1 EP 0507363 A1 EP0507363 A1 EP 0507363A1 EP 92200543 A EP92200543 A EP 92200543A EP 92200543 A EP92200543 A EP 92200543A EP 0507363 A1 EP0507363 A1 EP 0507363A1
Authority
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.)
Granted
Application number
EP92200543A
Other languages
English (en)
French (fr)
Other versions
EP0507363B1 (de
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
Original Assignee
Vandemoortele International NV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
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/de
Application granted granted Critical
Publication of EP0507363B1 publication Critical patent/EP0507363B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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.
  • a process for the continuous removal of a gum phase from triglyceride oil is described in EP 0 348 004. This process involves in a first stage degumming the oil by any conventional degumming method causing phosphatides to be hydrated, and, in a second stage, separating the undissolved and originally non-centrifugable particles from the degummed oil after optional agglomeration, by microfiltration, filtration, centrifugation, sedimentation or decantation.
  • the main disadvantage of this process is the important loss of triglyceride oil entrained during removal of both gum phases.
  • 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 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 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 4,049,686.
  • US 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 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 0.5 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 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 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 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 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.
  • 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 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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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Microbiology (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Fats And Perfumes (AREA)
  • Peptides Or Proteins (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Centrifugal Separators (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)
EP92200543A 1991-04-02 1992-02-26 Verfahren zur kontinuierlichen Entschleimung eines Glyceridöles Expired - Lifetime EP0507363B1 (de)

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 true EP0507363A1 (de) 1992-10-07
EP0507363B1 EP0507363B1 (de) 1993-05-19

Family

ID=8206595

Family Applications (1)

Application Number Title Priority Date Filing Date
EP92200543A Expired - Lifetime EP0507363B1 (de) 1991-04-02 1992-02-26 Verfahren zur kontinuierlichen Entschleimung eines Glyceridöles

Country Status (13)

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

Cited By (9)

* 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 (de) * 1992-08-19 1995-02-01 Vandemoortele Int Nv Kontinuierliches Raffinierungsverfahren mit erniedrigten Abfallströmen.
WO1997024933A1 (en) * 1996-01-05 1997-07-17 Grow Green Pty. Ltd. Protein feedstock, compositions and methods and apparatus for the production thereof
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
WO2002062157A2 (en) * 2001-02-02 2002-08-15 Ip Holdings, L.L.C. Methods for treating phosphatide-containing mixtures
US6844458B2 (en) 1998-11-20 2005-01-18 Ip Holdings, L.L.C. Vegetable oil refining
WO2009132463A1 (en) * 2008-05-02 2009-11-05 Neptune Technologies & Bioressources Inc. New deodorization method and organoleptic improvement of marine oil extracts
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
CN107011991A (zh) * 2017-04-12 2017-08-04 西北大学 一种油脂的阳离子树脂脱磷方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2002322233C1 (en) 2001-07-27 2014-02-13 Aker Biomarine Antarctic As Natural marine source phospholipids comprising flavonoids, polyunsaturated fatty acids and their applications
AR078850A1 (es) 2009-10-29 2011-12-07 Acasti Pharma Inc Composiciones terapeuticas concentradas de fosfolipidos
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
WO2021124444A1 (ja) * 2019-12-17 2021-06-24 株式会社Ｉｈｉ原動機 植物原油の脱ガム装置
WO2021124443A1 (ja) * 2019-12-17 2021-06-24 株式会社Ｉｈｉ原動機 発電システム

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE507650A (de) *
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
EP0077528A1 (de) * 1981-10-15 1983-04-27 Cpc International Inc. Raffiniertes geniessbares Öl und Verfahren zur Herstellung desselben
EP0349718A2 (de) * 1988-07-06 1990-01-10 N.V. Vandemoortele International Verfahren zur kontinuierlichen Entfernung der Gumphase aus Triglyceride-Öl

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE507650A (de) *
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
EP0077528A1 (de) * 1981-10-15 1983-04-27 Cpc International Inc. Raffiniertes geniessbares Öl und Verfahren zur Herstellung desselben
EP0349718A2 (de) * 1988-07-06 1990-01-10 N.V. Vandemoortele International Verfahren zur kontinuierlichen Entfernung der Gumphase aus Triglyceride-Öl

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
REVUE FRANCAISE DES CORPS GRAS vol. 27, no. 7, 1980, PARIS pages 333 - 339; G. DEVINAT ET AL.: 'SUR LA RAFFINABILITE DES HUILES. I. CONSIDERATIONS GENERALES ET ASPECTS TECHNOLOGIQUE ET ANALYTIQUE' *
THE JOURNAL OF THE AMERICAN OIL CHEMISTS' SOCIETY vol. 24, 1947, pages 261 - 264; H.J. DUTTON ET AL.: 'THE FLAVOR PROBLEM OF SOYBEAN OIL. I. A TEST OF THE WATER WASHING-CITRIC ACID REFINING TECHNIQUE' *
THE JOURNAL OF THE AMERICAN OIL CHEMISTS' SOCIETY vol. 61, no. 8, 1984, pages 1380 - 1382; E.G. LATONDRESS: 'ENERGY SAVING TECHNIQUES IN CONTINUOUS DEGUMMING AND REFINING' *

Cited By (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 (de) * 1992-08-19 1995-02-01 Vandemoortele Int Nv Kontinuierliches Raffinierungsverfahren mit erniedrigten Abfallströmen.
WO1997024933A1 (en) * 1996-01-05 1997-07-17 Grow Green Pty. Ltd. Protein feedstock, compositions and methods and apparatus for the production thereof
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
US6407271B1 (en) 1997-07-09 2002-06-18 Etienne Deffense Method for eliminating metals from fatty substances and gums associated with said metals
US6844458B2 (en) 1998-11-20 2005-01-18 Ip Holdings, L.L.C. Vegetable oil refining
WO2002062157A2 (en) * 2001-02-02 2002-08-15 Ip Holdings, L.L.C. Methods for treating phosphatide-containing mixtures
WO2002062157A3 (en) * 2001-02-02 2002-10-03 Ip Holdings Llc Methods for treating phosphatide-containing mixtures
WO2009132463A1 (en) * 2008-05-02 2009-11-05 Neptune Technologies & Bioressources Inc. New deodorization method and organoleptic improvement of marine oil extracts
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
CN107011991A (zh) * 2017-04-12 2017-08-04 西北大学 一种油脂的阳离子树脂脱磷方法
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

Also Published As

Publication number Publication date
PL294068A1 (en) 1992-12-14
MX9201460A (es) 1992-10-01
HUT62646A (en) 1993-05-28
ES2055634T3 (es) 1994-08-16
DK0507363T3 (da) 1993-08-30
EP0507363B1 (de) 1993-05-19
CZ289672B6 (cs) 2002-03-13
SK279220B6 (sk) 1998-08-05
CS95792A3 (en) 1992-10-14
HU212977B (en) 1997-01-28
HU9201094D0 (en) 1992-06-29
DE69200004D1 (de) 1993-06-24
JPH05117685A (ja) 1993-05-14
ATE89599T1 (de) 1993-06-15
CA2063929A1 (en) 1992-10-03
RU2008328C1 (ru) 1994-02-28
PL169760B1 (en) 1996-08-30
DE69200004T2 (de) 1993-09-09

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