EP0457401A1 - Production d'une fraction intermédiaire par cristallisation fractionnée avec recyclage des fractions de stéarine et d'oléine vers interestérification - Google Patents

Production d'une fraction intermédiaire par cristallisation fractionnée avec recyclage des fractions de stéarine et d'oléine vers interestérification Download PDF

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Publication number
EP0457401A1
EP0457401A1 EP19910201120 EP91201120A EP0457401A1 EP 0457401 A1 EP0457401 A1 EP 0457401A1 EP 19910201120 EP19910201120 EP 19910201120 EP 91201120 A EP91201120 A EP 91201120A EP 0457401 A1 EP0457401 A1 EP 0457401A1
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EP
European Patent Office
Prior art keywords
fraction
topping
olein
bottoming
fractional crystallization
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.)
Withdrawn
Application number
EP19910201120
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German (de)
English (en)
Inventor
Rob Zoet
Cornelis Nicolaas Maria Keulemans
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.)
Unilever PLC
Unilever NV
Original Assignee
Unilever PLC
Unilever 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 Unilever PLC, Unilever NV filed Critical Unilever PLC
Publication of EP0457401A1 publication Critical patent/EP0457401A1/fr
Withdrawn legal-status Critical Current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
    • 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
    • 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
    • C11B7/0008—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of solubilities, e.g. by extraction, by separation from a solution by means of anti-solvents
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
    • C11C3/10—Ester interchange

Definitions

  • the present invention relates to a method for the production of mid-fraction by fractional crystallization of fatty substances, including fats and glyceride oils.
  • the invention relates to the production of mid-fraction by topping fractional crystallization and bottoming fractional crystallization, in which the stearin topping fraction and olein bottoming fraction formed as byproducts are mixed and interesterified, and the interesterified mixture is recycled as additional feedstock.
  • Natural glyceride oils and fats comprise a great many different triglycerides, the physical properties of which to a large extent are determined by the chain lengths and the degrees of unsaturation of the fatty acid moieties. To make natural glyceride oils or fats more suitable for particular applications it is often required to separate them into fractions characterized by fatty acid glyceride distributions which are homogeneous with respect to the melting behaviour.
  • the fractional crystallization may be carried out on the oils and fats as such (dry fractionation) or after mixing with a solvent (solvent fractionation).
  • solvent fractionation solvent fractionation
  • the oil is cooled to a temperature at which only a higher melting triglyceride fraction crystallizes, followed by separation of the crystallized solids (stearin fraction) from the liquid fraction (olein fraction) e.g. by filtration or centrifugation.
  • the oil or fat is first subjected to a topping fractional crystallization treatment providing a stearin topping fraction and an olein topping fraction.
  • This olein topping fraction is subjected to a bottoming fractional crystallization treatment at a lower crystallization temperature, providing the aimed mid-fraction and an olein bottoming fraction.
  • topping fractional crystallization treatment and the bottoming fractional crystallization treatment may comprise more than one consecutive fractional crystallizations in which the olein fraction and/or stearin fraction are passed to the next or former fractional crystallization.
  • Mid-fraction is a desired starting oil or fat blend for producing margerines.
  • Mid-fraction possesses a good consistency and a good melting performance imparting the margerines obtained good organoleptic properties and a suitable consistency at a temperature within the range of 15-25°C.
  • the production of mid-fraction inevitably results in the formation of two byproducts, namely a stearin topping fraction and an olein bottoming fraction. These fractions are generally less valuable, so that the method for the production of mid-fraction is not optimal from an economic point of view.
  • the invention is based on the finding, that when the feedstock comprising fatty substances, used for the production of mid-fraction has a fatty acid composition of the triglycerides which is similar to that of the mid-fraction produced, and the stearin topping fraction and the olein bottoming fraction are mixed and this mixture is randomly interesterified, this interesterified mixture should have a fatty acid composition similar to that of the feedstock and may be recycled, substantially avoiding the formation of byproducts.
  • the present invention provides a method for the production of mid-fraction by fractional crystallization of fatty substances, in which:
  • a requisite for the method according to the invention is, that the stearin topping fraction and the olein bottoming fraction are subjected to a random interesterification. Therefore, the method according to the invention is not suitable for the production of mid-fraction comprising specific symmetrical or asymmetrical triglycerides.
  • any fatty substance may be used, such as semi-solid glyceride oils and fats of vegetable, animal or marine origin, such as fully or substantially hydrogenated palm oil, palm kernel oil, tallow, butter fats, fish oils, sunflower oil and their solvent or dry fractionated stearin or olein fractions.
  • Preferred feedstock components comprise hydrogenated palm oil, hydrogenated palm kernel oil, fractionated palm oil stearin, sunflower oil, such as palm oil hardened to a melting point of 58°C (C16 40-50%;C18 60-50%), hardened palm oil stearin (C16 50-85%;C18 50-15%), hydrogenated palm kernel oil hardened to a melting point of 39°C (C12 45-55%; C14 12-18%; C16 5-10%; C18 12-25%), hydrogenated palm kernel oil stearin hardened to a melting point of 41°C (C12 50-60%; C14 15-25%; C16 5-10%; C18 5-12%), and sunflower oil hardened to a melting point of 69°C (C16 5-10%;C18 95-90%).
  • palm oil hardened to a melting point of 58°C C16 40-50%;C18 60-50%)
  • hardened palm oil stearin C16 50-85%;C18 50-15%
  • the mid-fraction obtained has a H3 ( ⁇ C50 ) of less than 13, preferably less than 11, and a H2 M value (C44 , C46 , c48 ) which is as large as possible, generally higher than 60, preferably higher than 64, and a H3 +H2 M value which is as large as possible, generally larger than 70.
  • the H3 value is generally less than 16, preferably less than 15.
  • the H2 M value is generally larger than 45, preferably larger than 50.
  • the H3 +H2 M value is generally larger than 65.
  • the interesterification used in the method according to the invention comprises any suitable interesterification process, by which the fatty acids of the triglycerides are randomly exchanged.
  • Any prior art interesterification process might be used, such as the proces disclosed in EP-A-76,682.
  • Preferred is a catalyst comprising an alkaline metal or hydroxide.
  • the catalyst system comprises sodium or sodium hydroxide, glyceride and water in a weight ratio of 1/2/3 to 1/2/7.
  • the catalyst is generally added in a concentration of at least 0.03% by weight sodium hydroxide based on the oil.
  • the information of the European patent application EP-A-76,682 is included by reference.
  • the feedstock as well as the stearin topping fraction and olein topping fraction are subjected to the interesterification.
  • these treatments may comprise more than one, such as two consecutive fractional crystallizations.
  • the topping fraction of crystallization treatment comprises two or more consecutive fractional crystallizations
  • a higher midfraction yield may be obtained when, according to a preferred embodiment the stearin topping fraction originates from the second consecutive topping fractional crystallization, and the olein topping fraction originates from the first consecutive topping fractional crystallization.
  • the bottoming fractional crystallization treatment comprises two consecutive fractional crystallizations, it may be preferred for obtaining better midfraction quality when the olein bottoming fraction originates from the first consecutive bottoming fractional crystallization, and the mid-fraction originates from the second consecutive bottoming fractional crystallization.
  • the olein topping or bottoming fraction comprises a relatively high solid content
  • this fraction is partly recycled to the topping or bottoming fractional crystallization treatment whereby the fraction is diluted.
  • the recycling ratio of the recycled olein fraction is about 10-60%, more preferably 25-50%.
  • the consecutive topping and bottoming fractional crystallizations may be carried out as countercurrent fractional crystallizations, such as disclosed in the earlier European patent application to be included.
  • Impurities present in the feedstock or formed during the production of mid-fraction may accumulate in the recycled stearin topping or olein bottoming fractions. Therefore, it is preferred that intermittantly or continuously a minor part of the stearin topping fraction and/or olein bottoming fraction is not recycled but disposed.
  • the disposed fraction may comprise up to about 5% by weight of the recycled olein topping or bottoming fraction. Alternatively these impurities may be removed intermittantly or continuously from the recycled fractions, for instance by adsorption.
  • Feedstock (F) comprising 47% fully hydrogenated palm oil and 53% fully hydrogenated palm kernel oil was subjected to interesterification (I) using 0.02% by weight metallic sodium.
  • Table 1 shows the fatty acid composition (%) of the mid-fraction and of the feedstock.
  • Feedstock comprising 7% fully hydrogenated, dry fractionated palm oil stearin, 33% fully hydrogenated palm oil and 60% fully hydrogenated palm kernel oil was used for the production of mid-fraction using method B.
  • the fatty acid composition (%) of the mid-fraction obtained and of the feedstock is shown in Table 2.
  • Example II The same process as used in Example II was used, but the olein fractions were recycled at a recycling ratio of 50% on the feed.
  • topping fractional crystallization treatment SPC was 5.4% and in the bottoming fractional crystallization treatment SPC was 12%.
  • the mid-fraction obtained had a H3/H2M value of 15/45.
  • Feedstock comprising 1,5% fully hydrogenated sunflower oil, 46,5% fully hydrogenated palm oil, 26% fully hydrogenated palm kernel oil and 26% fully hydrogenated palm kernel stearin was processed according to method A.
  • topping fractional crystallization treatment the SPC in the crystallizations 1 and 2 was 8%.
  • bottoming fractional crystallization treatment the SPC of the fractional crystallizations 3 and 4 was 16%.
  • the stearin topping fraction and olein bottoming fraction were recycled and mixed with the feedstock in ratio of 62/38. At a separation efficiency of 0.5, the H3/H2M value of the mid-fraction was 12/49.
  • Table 3 shows the fatty acid composition (%) of the mid-fraction and of the feedstock.
  • a feedstock comprising 42% hydrogenated palm kernel stearin, 53% hydrogenated palm oil and 5% hydrogenated sunflower oil, was subjected to solvent fractionation in acetone in a ratio of 1/5 wt/wt.
  • topping fractional crystallization treatment SPC was 29% and the crystallization temperature about 30°C.
  • bottoming fractional crystallization treatment SPC was 33% (on present fat) and the crystallization temperature was about 20°C.
  • the stearin topping fraction 1 and the olein bottoming fraction 2 were recycled and after removal of the acetone, mixed with the feedstock in a ratio of 47.5/52.5, andthereafter interesterified.
  • the fatty acid composition of the mid-fraction resembles closely the composition of the feedstock, see Table 4.
  • the H3/H2M value of the mid-fraction was 14/59. From time to time it was necessery to remove diacylglycerols by adsorption on silica. The time period between the removal procedures of these impurities was depending on the composition of the feedstock.
  • a feedstock comprising 85% palm oil and 15% solvent fractionated palm oil stearin was used in method B.
  • the mid-fraction obtained had a constant composition of 1.2%S3 , 67%S2 0, 6.3%S2 Li and 25,5% others.
  • Midfraction was produced according to method C.
  • Feedstock comprising 43% fully hydrogenated palm kernel oil was subjected to interesterification (I) using 0.02% metallic sodium.
  • the solid particle content (SPC) was 18.5%.
  • the SPC was 30%.
  • the stearin topping fraction and the olein bottoming fraction were recycled to the interesterification and mixed with the feedstock in a ratio of 50/50.
  • the H3/H2M ratio was 12/52.
  • the separation efficiency was kept at 0.5.
  • Table 5 shows the fatty acid composition (%) of the midfraction and of the feedstock.
  • method C may be used in systems in which the SE is still high at a high SPC.

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  • 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)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Fats And Perfumes (AREA)
EP19910201120 1990-05-17 1991-05-09 Production d'une fraction intermédiaire par cristallisation fractionnée avec recyclage des fractions de stéarine et d'oléine vers interestérification Withdrawn EP0457401A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP90109334 1990-05-17
EP90109334 1990-05-17

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EP0457401A1 true EP0457401A1 (fr) 1991-11-21

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EP (1) EP0457401A1 (fr)
AU (1) AU7708291A (fr)
CA (1) CA2042828A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0651046A1 (fr) * 1993-11-02 1995-05-03 N.V. Vandemoortele International Procédé de fractionnement à sec de matières grasses
WO2009012982A3 (fr) * 2007-07-25 2009-03-19 Loders Croklaan Bv Procédé
US8414943B2 (en) 2007-12-21 2013-04-09 Loders Croklaan B.V. Process for producing a palm oil product

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB590916A (en) * 1945-02-13 1947-07-31 Procter & Gamble Process for improving fats and fatty oils for food and other purposes
EP0109721A2 (fr) * 1982-11-22 1984-05-30 Unilever N.V. Mélange gras pour margarines
EP0185524A2 (fr) * 1984-12-17 1986-06-25 Unilever Plc Graisses comestibles

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB590916A (en) * 1945-02-13 1947-07-31 Procter & Gamble Process for improving fats and fatty oils for food and other purposes
EP0109721A2 (fr) * 1982-11-22 1984-05-30 Unilever N.V. Mélange gras pour margarines
EP0185524A2 (fr) * 1984-12-17 1986-06-25 Unilever Plc Graisses comestibles

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0651046A1 (fr) * 1993-11-02 1995-05-03 N.V. Vandemoortele International Procédé de fractionnement à sec de matières grasses
WO2009012982A3 (fr) * 2007-07-25 2009-03-19 Loders Croklaan Bv Procédé
US8414943B2 (en) 2007-12-21 2013-04-09 Loders Croklaan B.V. Process for producing a palm oil product

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Publication number Publication date
AU7708291A (en) 1991-11-21
CA2042828A1 (fr) 1991-11-18

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