PREVENTION OF MCPD FORMATION IN TRIACYLGLYCERIDE OILS
20220333036 · 2022-10-20
Inventors
- KORNEL NAGY (Ithaca, NY, US)
- XANTHIPPI THEURILLAT (Linwood, NJ, US)
- MARINE NICOLAS (Morges, CH)
- KARINE MEISSER REDEUIL (Pully, CH)
- SABINE LAHRICHI (Montreux, CH)
Cpc classification
International classification
Abstract
A method is provided for preventing or reducing the formation of monochloropropanediols (MCPDs) or monochloro-propanediol esters (MCPDEs) in triacylglyceride oil, comprising the steps: (a) concentrating insoluble components in liquid starting triacylglyceride oil by (i) applying a centrifugational force on the triacylglyceride oil whilst maintaining the triacylglyceride oil above its melting temperature; and/or (ii) allowing the insoluble components to settle by gravitational force whilst maintaining the triacylglyceride oil above its melting temperature; (b) separating the triacylglyceride oil from the insoluble components; (c) optionally applying additional refining steps and (d) applying heat treatment to the triacylglyceride oil. A purified triacylglyceride oil obtainable by the method of the invention is also provided.
Claims
1. A method for preventing or reducing the formation of monochloropropanediols (MCPDs) or monochloropropanediol esters (MCPDEs) in triacylglyceride oil, comprising the steps: concentrating insoluble components in liquid starting triacylglyceride oil by applying a centrifugational force on the starting triacylglyceride oil whilst maintaining the starting triacylglyceride oil above its melting temperature; and/or allowing the insoluble components to settle by gravitational force whilst maintaining the triacylglyceride oil above its melting temperature; separating the triacylglyceride oil from the insoluble components; and applying heat treatment to the triacylglyceride oil.
2. The method of claim 1 wherein, the starting triacylglyceride oil is melted by heating it to above its melting temperature.
3. The method of claim 1, wherein a centrifugational force is applied on the triacylglyceride oil whilst maintaining the triacylglyceride oil above its melting temperature.
4. The method of claim 1, wherein the starting triacylglyceride oil has a free fatty acid content of at least 0.5 (w/w %).
5. The method of claim 1, wherein the centrifugation is carried out at a g-force above 200 g.
6. The method of claim 1, wherein, in step (a), the insoluble components are allowed to settle by gravitational force whilst maintaining the triacylglyceride oil above its melting temperature.
7-8. (canceled)
9. The method of claim 1, wherein the starting triacylglyceride oil is selected from the group consisting of a plant oil, animal oil, fish oil or algal oil, preferably a plant oil.
10. The method of claim 9 wherein the starting triacylglyceride oil is palm oil or fractions obtained from palm oil.
11. The method of claim 9 wherein the starting triacylglyceride oil is sunflower oil or its high oleic variants.
12. The method of claim 1, wherein the starting triacylglyceride oil has a water content of less than 1%.
13. The method of claim 1, wherein the starting triacylglyceride oil has not been admixed with an acid or alkali.
14. The method of claim 1, wherein the starting triacylglyceride oil is devoid of added crystallization agent.
15. The method of claim 1, wherein the starting triacylglyceride oil has a crystallized triacylglycerol content less than 10% (w/w %).
16. The method of claim 1, wherein the starting triacylglyceride oil has a soap content of less than 1000 ppm.
17. The method of claim 1, wherein the starting triacylglyceride oil has not been admixed with a salt.
18. The method of claim 1, wherein the starting triacylglyceride oil is devoid of any added ionic, cationic and anionic surfactants and/or additives.
19. The method of claim 1, wherein the starting triacylglyceride oil has a bleaching clay content of less than 0.01%.
20. The method of claim 1, wherein the starting triacylglyceride oil has not been cooled below 20° C.
21. A purified triacylglyceride oil obtainable by the method of claim 1.
Description
DESCRIPTION OF THE DRAWINGS
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DETAILED DESCRIPTION OF THE INVENTION
[0114] The terms “comprising”, “comprises” and “comprised of” as used herein are synonymous with “including” or “includes”; are inclusive or open-ended and do not exclude additional, non-recited members, elements or steps. The terms “comprising”, “comprises” and “comprised of” also include the terms “consisting of”, “containing” or “contains”.
[0115] Purification
[0116] The purification is particularly suitable for removing insoluble fraction of oils that may contain chlorine/chloride carrying contaminants (substances that may serve as the chlorine source needed for formation of monochloropropanediols (MCPDs) or monochloropropanediol esters (MCPDEs)) from a starting triacylglyceride oil A starting triacylglyceride oil as used herein throughout is taken to mean the triacylglyceride oil immediately before it is subjected to step (a) or step (e) of the method of the invention).
[0117] The method of the invention subjects the starting triacylglyceride oils to treatment that physically removes the insoluble fraction of oils containing chloride/chlorine carrying substances, which may be an active source of chlorine during oil refining, from the starting (e.g. crude) oils. The treatment may be based on centrifugation or settling in order to allow centrifugational or gravitational force to concentrate the microparticles, segregated droplets and sediments in a narrow space of the storage vessel and subsequently allow the taking off of the upper phase pure oil.
[0118] 3-Halogen-1,2-propandiols, in particular 3-monochloro-1,2-propandiol (3-MCPD), are known contaminants in foods (Food Addit. Contam. (2006) 23: 1290-1298). For example, studies have indicated that 3-MCPD may be carcinogenic to rats if administered at high doses (Evaluation of Certain Food Additives and Contaminants, World Health Organisation, Geneva, Switzerland (1993) 267-285; Int. J. Toxicol. (1998) 17: 47). However, it has also been discovered that refined edible oils may contain 3-MCPD in its fatty acid ester form, while only containing very little amounts of free 3-MCPD (Food Addit. Contam. (2006) 23: 1290-1298). The European Food Safety Authority (EFSA) has recommended that 3-MCPD esters are treated as equivalent to free 3-MCPD in terms of toxicity (European Food Safety Authority (2008)).
[0119] It is well known that dehalogenation reactions can occur during thermal processes. For example, chlorine has been shown to leave chemical components as hydrogen chloride (gas) upon the input of sufficient activation energy, which is abundant during the deodorisation of vegetable oils at high temperatures (e.g. up to 270° C.). The inventors believe that hydrogen chloride may be evolved during oil refining from chlorine-containing compounds inherently present in the starting materials of the triacylglyceride oil refining process, for example plant materials.
[0120] Indeed, it has been suggested that MCPD generation reactions increase exponentially (>150° C.) and go to completion in a short time period.
[0121] Without wishing to be bound by theory, it is suggested that mechanistically, the MCPD di-esters may be formed during oil refinement via the protonation of the terminal ester group of triacylglycerides (TAG), which represent about 88-95% of total glycerides in most vegetable oils, through interaction with hydrogen chloride evolved during oil refining. The formed oxonium cation can then undergo intramolecular rearrangement, followed by nucleophilic substitution of chloride ion and the release of a free fatty acid and an MCPD di-ester.
[0122] Once removed through use of the method of the invention, the potential chlorine source is no longer available for the formation of chlorinated compounds, such as MCPD esters during the heating steps in oil refinement. Purified product oils are thereby obtained that will develop reduced quantity of monochloropropandiols (MCPDs) or monochloropropandiol esters (MCPDEs) when compared to the non-purified refined triacylglyceride oil when they are subjected to various refining practices with heat treatment e.g. deodorization.
[0123] In another embodiment, the quantity monochloropropandiol esters (MCPDEs) is reduced in the purified and heat treated triacylglyceride oil by at least 40%, 50%, 60%, 70%, 80%, 90%, 95% or 99% compared to the starting triacylglyceride oil.
[0124] Refined oils produced using the method of the invention may contain, for example, less than 3 ppm, less than 1 ppm, less than 0.5 ppm, or preferably less than 0.3 ppm MCPDEs.
[0125] In another embodiment, the quantity monochloropropanediols (MCPDs) is reduced in the purified and heat treated triacylglyceride oil by at least 40%, 50%, 60%, 70%, 80%, 90%, 95% or 99% compared to the starting triacylglyceride oil.
[0126] Refined oils produced using the method of the invention may contain, for example, less than 3 ppm, less than 1 ppm, less than 0.5 ppm, or preferably less than 0.3 ppm MCPDs.
[0127] Quantities of MCPDEs may be readily analysed using protocols well known in the art. For example, liquid chromatography/mass spectrometry (LC/MS)-based approaches are suitable for analysing levels of MCPDEs, as shown in the present Examples.
[0128] In one embodiment, the starting triacylglyceride oil input into step (a) or step (e) of the method of the invention is crude triacylglyceride oil.
[0129] The term “crude oil” as used herein may refer to an unrefined oil. For example, in some embodiments, the starting triacylglyceride oil input into step (a) or step (e) of the method of the invention has not been refined, degummed, bleached and/or fractionated. In a preferred embodiment, the starting triacylglyceride oil has not been deodorised before step (a) or step (e).
[0130] In some embodiments, the starting triacylglyceride oil is subjected to preliminary processing before step (a) or step (e), such as preliminary cleaning. However, any processes carried out on the starting triacylglyceride oil before step (a) or step (e) preferably do not involve heating the triacylglyceride oil to a temperature greater than 100° C., 150° C., 200° C. or 250° C. In some embodiments, the triacylglyceride oil is subjected to preliminary refining, fractionation, hydrogenation and/or interesterification before step (a) or step (e).
[0131] Triacylglyceride Oil
[0132] The term “triacylglyceride” can be used synonymously with “triacylglycerol” and “triglyceride”.
[0133] In these compounds, the three hydroxyl groups of glycerol are each esterified by a fatty acid. Oils that may be purified using the method of the invention comprise triacylglycerides and include plant oil, animal oil, fish oil, algal oil and combinations thereof.
[0134] In a preferred embodiment, the starting triacylglyceride oil is a plant oil. Example, plant oils include sunflower oil, corn oil, canola oil, soybean oil, coconut oil, palm oil, palm kernel oil and cocoa butter.
[0135] In another embodiment, the starting triacylglyceride oil is palm oil or fractionated palm oil such as palm olein, palm stearin, mid-fraction.
[0136] In a preferred embodiment, the starting triacylglyceride oil is a crude plant oil.
[0137] In another preferred embodiment, the starting triacylglyceride oil is crude palm oil or fractionated crude palm oil such crude palm olein, crude palm stearin, crude mid-fraction.
[0138] In one embodiment, the plant oil is crude palm oil. In one embodiment, the plant oil is crude corn oil. In one embodiment, the plant oil is crude sunflower oil. In one embodiment, the plant oil is cold pressed crude canola oil. In one embodiment, the plant oil is crude soybean oil.
[0139] In a preferred embodiment, the plant oil is at least partially solvent extracted. Preferably, the solvent is a mixture of 2-propanol and n-hexane.
[0140] In one embodiment, the plant oil is solvent extracted crude sunflower seed oil.
[0141] In one embodiment, the plant oil is solvent extracted crude canola seed oil.
[0142] Crude Triacylglyceride Oil
[0143] In the case of palm oil, crude oil may be produced from different portions of palm fruit, e.g. from the flesh of the fruit known as mesocarp and also from seed or kernel of the fruit. The extraction of crude palm oil (CPO) from the crushed fruits can be carried out under temperatures ranging for example from 90 to 140° C.
[0144] In other cases, for example sunflower, crude oil may be produced by pressing, by solvent extraction or the combination thereof, for example as described by Gotor & Rhazi in Oilseeds & fats Crops and lipids 2016 (DOI: 10.1051/ocl/2016007).
[0145] Refined Oils
[0146] As used herein, the term “refined” may refer to oils that have been subjected to methods that improve the quality of the oil and include a heat treatment. This heat treatment may be a deodorisation step comprising steam distillation or short path distillation. Such heat treatment can be applied in the 150-300° C. range, more commonly in the 160-260° C. or the 160-240° C. range.
[0147] Heat Treatment
[0148] As used herein, the term “heat treatment” may refer to exposing the oil to temperatures in the 150-300° C. range, more commonly in the 160-260° C. or the 160-240° C. range. The heat treatment may be applied in closed vessels or in ampoules or in combination with vacuum and/or steam as it is done in the industrial setting during deodorization (steam distillation or short path distillation).
[0149] Chlorine and Chloride
[0150] Chlorine is a chemical element with symbol CI and atomic number 17. Chlorine can be found in a wide range of substances both in ionic (e.g. sodium chloride) and covalent form (e.g. polyvinyl chloride). Accordingly, the terms “chlorine” and “chloride” both refer to substances that contain the chlorine element in various forms.
[0151] As used herein, the terms “chlorine containing”, “chloride containing”, “organochlorine”, “chlorine donor”, all refer to substances that in any format contain the chlorine element. This format can be either ionic, polar covalent or covalent.
[0152] Chlorine or Chloride Carrying Substances
[0153] As used herein, the terms “chlorine or chloride carrying substances” refer to substances that in any format contain the chlorine element. This format can be either ionic, polar covalent or covalent.
[0154] Chlorine Donor
[0155] As used herein, the terms “chlorine donor” refer to substances that in any format contain the chlorine element and may release the chlorine in any form for example but not restricted to hydrochloric acid, hypochlorite, chloride anion.
[0156] Acidity and pH
[0157] In chemistry, pH is a scale used to specify how acidic or how basic is a water-based solution. Similarly, as used herein, the term “pH” and the term “acidity” refer to the free acid content of the oil samples. For example when mixing the oil with phosphoric acid can be considered as lowering its pH. Similarly, a neutralization step with the addition of sodium hydroxide to the oil can be considered as increasing the pH of the oil.
[0158] Melting Temperature
[0159] The term “melting temperature” as used herein may refer to the temperature at which a solid changes state from solid to liquid at a pressure of 100 kPa. For example, the melting temperature may be the temperature at which a solid changes state from solid to liquid at a pressure of 100 kPa when heated at 2° C. per minute.
[0160] The skilled person is readily able to select suitable methods for the determination of the melting temperature of the triacylglyceride oil.
[0161] For example, apparatus for the analysis of melting temperatures may consist of a heating block or an oil bath with a transparent window (e.g. a Thiele tube) and a magnifier. A sample of the solid may be placed in a thin glass tube and placed in the heating block or immersed in the oil bath, which is then gradually heated. The melting of the solid can be observed and the associated melting temperature noted.
[0162] For fats and oils with highly complex triacylglycerol composition, the method of Slip Melting Point is a commonly used reference (AOCS Official method Cc 3-25).
[0163] Centrifugation
[0164] The term “centrifugation” as used herein may refer to the rapid rotation of a vessel including its oil content in order to exert centrifugal force on the vessel and its content.
[0165] Beyond mitigating the formation of MPCDEs, further advantages of the herein described centrifugation step include: [0166] 1) the centrifugation step allows improved removal of residual water from the oil avoiding the need of further vacuum drying as it is common practice in today's industry and thus resulting in energy and cost saving. [0167] 2) the centrifugation step allows improved removal of residual solids from the oil before degumming steps hence allowing the production of better quality gums with less solid content. [0168] 3) the centrifugation step allows improved removal of inorganic sediments allowing the use of lower quantity of clays during the bleaching process in order to reduce cost and waste material of the bleaching process.
[0169] In one embodiment, the centrifugation occurs at elevated temperatures at which the oil is in the liquid state. This temperature can be 30° C., 40° C., 50° C., 60° C., 70° C., 80° C., 100° C. or above for palm oil and 50° C., 60° C., 80° C., 100° C. or above for palm stearin, 15° C., 20° C. or above for palm olein, 5° C. or above for seed oils including sunflower oil, canola/rapeseed oil, corn oil. In a preferred embodiment, the temperature can be between 30° C. and 80° C. for palm oil, preferably between 35° C. and 70° C. In a preferred embodiment, the temperature can be between 5° C. and 20° C. for sunflower oil. In a preferred embodiment, the centrifugation speed is at least 15,000 g for 15 min.
[0170] Settling
[0171] The term “settle” or “settling” as used herein may refer to setting the oil vessel into a movement free or substantially movement free environment, preferably avoiding its disturbance for a period of time that can be at least 4 hours, 6 hours, 1 day, 2 days, a week or a month.
[0172] In one embodiment, the oil vessel is settled into a fixed, movement free environment and its disturbance avoided for a period of time of at least 5 months, for example for crude sunflower oil or crude soybean oil. In one embodiment, the crude oil is heated to at least 60° C. prior to settling.
[0173] In one embodiment, the oil vessel is settled into a fixed, movement free environment and its disturbance avoided for a period of time of at least 4 days, for example for cold pressed crude canola oil.
[0174] Soap
[0175] As used herein, the term “soap” may refer to a variety of cleansing and lubricating products produced from substances with surfactant properties.
[0176] In the vegetable oil refining context and the current context the term “soap” is used to describe alkali carboxylates which are the salt of fatty acids formed by the negatively charged deprotonated fatty acid and a positively charged counter ion e.g. a sodium or a potassium cation. [Bailey's Industrial Oil and Fat Products—6th edition, page 3084—Soap raw materials and their processing page 105; Wikipedia]
[0177] As it is well known in the literature of alkali refining practices, free fatty acids react with alkali e.g. sodium hydroxide or potassium hydroxide to form such soaps [The Lipid Handbook—Third Edition; edited by Frank D. Gunstone; page 178, 191].
[0178] Further Refinement
[0179] As the insoluble oil components along with their chlorine donor substances are depleted by the method of the invention, heating during any subsequent refinement processes will not cause significant generation of unwanted chlorinated compounds, such as the MCPDEs.
[0180] In one embodiment, the method further comprises one or more processes selected from the group consisting of physical or chemical refining, degumming, neutralization and bleaching subsequent to step (d) or step (i).
[0181] In one embodiment, the method further comprises deodorisation subsequent to step (d) or step (i), preferably wherein the deodorisation is vacuum steam deodorisation.
[0182] In one embodiment, the method further comprises fractionation subsequent to step (d) or step (i).
[0183] Processes for carrying out refinement, degumming, bleaching, deodorisation and fractionation are well known in the art.
[0184] By way of example, refinement of plant oil, such as vegetable oil, typically consists of physical refining or chemical refining.
[0185] In efforts aimed at increased sustainability, oil refineries have modified their plant oil processing lines in the past few decades for the minimisation of energy expenditure (economisers) and the reduction of waste. However, the steps of these two refining processes have essentially remained the same.
[0186] Physical refining is essentially an abridged form of chemical refining and was introduced as the preferred method of palm oil refining in 1973. It may be a three step continuous operation where the incoming oil is pre-treated with acid (degumming), cleansed by being passed through adsorptive bleaching clay, and then subjected to steam distillation. This process allows for the subsequent deacidification, deodorisation and decomposition of carotenoids unique to palm oil (i.e. the crude oil is deep red in colour, unlike other vegetable oils). Given the lack of neutralisation step in physical refining, refined bleached (RB) oil produced from a physical refinery contains nearly the same free fatty acid (FFA) levels as found in the crude oil.
[0187] Neutralised bleached (NB) oil from a chemical refinery and RB palm oil are comparable pre-deodorisation in every other aspect.
[0188] The heat bleaching unit operation is the main source of loss in the oil refining process resulting in 20-40% reduction in oil volume post filtration. The process typically lasts for about 30-45 min and typically takes place under 27-33 mbar vacuum at a temperature of 95-110° C.
[0189] Heat bleached oil may then be rerouted in piping to a deaerator that aides in the removal of dissolved gases, as well as moisture, before being sent to a deodorisation tower.
[0190] A bleaching step may comprise heating the oil and cleaning the oil by passing it through adsorptive bleaching clay.
[0191] A deodorisation step may comprise steam distillation.
[0192] The skilled person will understand that they can combine all features of the invention disclosed herein without departing from the scope of the invention as disclosed.
[0193] Preferred features and embodiments of the invention will now be described by way of non-limiting examples.
[0194] The practice of the present invention will employ, unless otherwise indicated, conventional techniques of chemistry, biochemistry, molecular biology, microbiology and immunology, which are within the capabilities of a person of ordinary skill in the art. Such techniques are explained in the literature. See, for example, Sambrook, J., Fritsch, E. F. and Maniatis, T.
[0195] (1989) Molecular Cloning: A Laboratory Manual, 2nd Edition, Cold Spring Harbor Laboratory Press; Ausubel, F. M. et al. (1995 and periodic supplements) Current Protocols in Molecular Biology, Ch. 9, 13 and 16, John Wiley & Sons; Roe, B., Crabtree, J. and Kahn, A. (1996) DNA Isolation and Sequencing: Essential Techniques, John Wiley & Sons; Polak, J. M. and McGee, J. O'D. (1990) In Situ Hybridization: Principles and Practice, Oxford University Press; Gait, M. J. (1984) Oligonucleotide Synthesis: A Practical Approach, IRL Press; and Lilley, D. M. and Dahlberg, J. E. (1992) Methods in Enzymology: DNA Structures Part A: Synthesis and Physical Analysis of DNA, Academic Press. Each of these general texts is herein incorporated by reference.
EXAMPLES
Analytical Procedures Used in the Examples
[0196] Sample Preparation
[0197] Oil samples were diluted stepwise prior to injection. [0198] 1) Firstly, 100 μL of each sample was transferred into a vial and 900 μL of a mixture of n-Hexane:Acetone (1:1 v/v) was added. The sample was vortexed for 5-10 s. [0199] 2) In the second step, 50 μL of this solution was further diluted by mixing it with 950 μL of acetone. The obtained solution was vortexed for 5-10 s. [0200] 3) 100 μL of this latter solution was mixed with 90 μL of methanol and 10 μL of internal standard mix solution. (the internal standard mix solution contained at 2 ng/μL concentration the following stable isotope labeled compounds solubilized in methanol: 1-oleoyl 2-linoleoyl 3-chloropropanediol-.sup.2H.sub.5 (OL), 1-2-dipalmitooyl 3-chloropropanediol-.sup.2H.sub.5 (PP), 1-palmitoyl 2-oleoyl 3-chloropropanediol-.sup.2H.sub.5 (PO), 1-palmitoyl 2-linoleoyl 3-chloropropanediol-.sup.2H.sub.5 (PL), 1-2-dilinoleoyl 3-chloropropanediol-.sup.2H.sub.5,(LL),), 1-2-oleoyl 3-chloropropanediol-.sup.2H.sub.5,(OO)).
[0201] LC Conditions
[0202] Ultra high performance liquid chromatography was performed using either a Thermo UltiMate 3000 system or a Waters Acquity H-class system equipped with a silica based octadecyl phase (Waters Acquity HSS C18, 1.7 μm; 2.1×150 mm). The applied solvent gradient is summarised in Table 3.
TABLE-US-00001 TABLE 3 Details of the applied LC gradient (solvent A was 1 mM ammonium-formate in methanol; and solvent B was 100 μM ammonium-formate in isopropanol). Time [min] Solvent A [%] Solvent B [%] Flow rate [μL/min] 0 100 0 400 15.0 100 0 300 18.0 50 50 200 25.0 0 100 200 32.5 0 100 180 33.0 0 100 150 35.0 100 0 150 40.0 100 0 400 42.0 100 0 400
[0203] MS Conditions
[0204] Monitoring of monochloropropandiol (MCPD) esters was performed using Thermo Fisher high resolution mass spectrometers (Q Exactive Hybrid Quadrupole-Orbitrap, Orbitrap Fusion™ Lumos™ Tribrid™ and Orbitrap Elite Hybrid). These platforms enabled highly selective mass analysis at a routine mass accuracy of ˜2 ppm. MCPD esters were monitored in ESI positive ion mode (ESI+). Under these conditions the observed MCPD precursor ion was [M-H].sup.−, whereas the monitored MCPD ester ions were the [M+NH.sub.4].sup.+ and [M+Na].sup.+ adducts.
[0205] Data Interpretation
[0206] The relative quantification of MCPDE was performed by first extracting the ion chromatograms of the [M+NH.sub.4].sup.+ and [M+Na].sup.+ adducts at their respective m/z value in a 10 ppm mass window and then integrating the resulting peak areas at the corresponding chromatographic retention time. The abbreviations of the monitored MPCDEs are as following: PP: dipalmitoyl MCPD ester; PO: palmitoyl-oleyl MCPD ester; OO: dioleyl MCPD ester; OL: oleyl-linoleyl MPCD ester; LL: dilinoleyl MPCD ester; PL: palmitoyl-linoleyl MPCD ester.
[0207] For every experiment, the peak areas of the most abundant MPCDEs detected in the control samples were set as 100% and the results found in the mitigated samples were expressed as a relative % compared to the non-mitigated control samples.
[0208] In-Ampoulle Heat Treatment of the Samples
[0209] The heat treatment of crude oil samples was performed in sealed glass ampoules under nitrogen for 2 h at 230° C. in a Thermo Scientific Heraeus oven (series 6100). The glass ampoules were fabricated from glass Pasteur pipettes by flushing them with nitrogen and sealing them using a Bunsen gas burner. These conditions were chosen in order to mimic the thermal conditions used during edible-oil deodorisation.
Example 1
[0210] Solvent Extracted Crude Palm Oil
[0211] Production of Solvent Extracted Crude Palm Oil
[0212] 1.8 kg frozen, whole, intact palm fruit was thawed at room temperature. The kernels were removed from the fruit manually using a scalpel. 4 L of extraction solution was prepared by mixing 2 L of 2-propanol and 2 L of n-hexane. 1.4 kg of palm pulp including the fruit flesh and skin was mixed, pureed and homogenised with 2 L of extraction solution using a commercial immersion blender mixer (Bamix Gastro 200). The resulting slurry was mixed and further homogenised with the remaining 2 L of extraction solution using a polytron (Kinematica Polytron PT 10 35 GT). The resulting slurry solution was aliquoted into 1 L polypropylene tubes (Sorvall 1000 mL) and centrifuged at 4000 g for 15 min at 30° C. in a Thermo Scientific Heraeus Cryofuge 8500i centrifuge. The organic phases were filtered through filter paper (Whatman 595 1/2) and were combined. The organic solvent was then evaporated from the oil using a Büchi Rotavapor R-300 system at 60° C. (B-300 heating bath, I-300 vacuum controller, V-300 pump and P-314 recirculating chiller operated at 4° C.). The vacuum was stepwise adjusted until it reached 10 mbar to avoid boiling of the sample.
[0213] Different batches of crude palm oils were subjected to centrifugation, in order prevent the formation of MPCDEs during heat treatment.
[0214] Centrifugation of Solvent Extracted Crude Palm Oil
[0215] 1 L of crude palm oil prepared as described above was melted by heating to 80° C. in a water bath. The oil was homogenized by manual shaking. 40 mL aliquots were transferred into 50 mL Falcon test tubes. The tubes were inserted into an Eppendorf 5810 centrifuge pre-heated to 40° C. and were centrifuged at 15000 g for 15 min at 40° C.
[0216] Following the treatment via centrifugation, the resulting oil and the starting material (without centrifugation) have been subjected to heat treatment as described above in order to mimic the thermal conditions used during edible-oil deodorisation. The resulting samples have been analysed for their MPCDE content by LC-MS. The beneficial effect of the centrifugation based mitigation is shown in
Example 2
[0217] Solvent Extracted Crude Sunflower Oil
[0218] Production of Solvent Extracted Crude Sunflower Seed Oil
[0219] 1.2 kg of sunflower seeds were crushed and homogenised with 1.5 L of extraction solution (2-propanol:n-hexane, 1:1 v/v) using a commercial immersion blender mixer (Bamix Gastro 200). The homogenate was mixed with a further 1.5 L of extraction solution and further homogenised using a polytron (Kinematica Polytron PT 10 35 GT). The resulting slurry was aliquoted into 1 L polypropylene tubes (Sorvall 1000 mL) and centrifuged at 4000 g for 15 min at 22° C. in a Thermo Scientific Heraeus Cryofuge 8500i centrifuge. The organic phases were filtered through filter paper (Whatman 595 1/2) and were combined. The organic solvent was then evaporated from the oil using a Büchi Rotavapor R-300 system at 60° C. (B-300 heating bath, I-300 vacuum controller, V-300 pump and P-314 recirculating chiller operated at 4° C.). The vacuum was stepwise adjusted until it reached 10 mbar to avoid boiling of the sample.
[0220] Crude solvent extracted sunflower oil (produced as described above) was subjected to centrifugation in order to prevent the formation of MCPDEs during heat treatment.
[0221] Centrifugation of Solvent Extracted Crude Sunflower Oil
[0222] 1 L of crude sunflower oil prepared as described above was homogenized by manual shaking. 40 mL aliquots were transferred into 50 mL Falcon test tubes. The tubes were inserted into an Eppendorf 5810 centrifuge and were centrifuged at 15000 g for 15 min at 23° C.
[0223] Following the treatment via centrifugation, the resulting oil and the starting material (without centrifugation) have been subjected to heat treatment in triplicates as described above in order to mimic the thermal conditions used during edible-oil deodorisation. The resulting samples have been analysed for their MPCDE content by LC-MS. The beneficial effect of the centrifugation based mitigation is shown in
[0224] Overall, the data show substantial reduction in the levels of monochloropropandiol esters (MCPDEs) after the mitigation compared to the levels observed in the absence of treatment for each of the studies on crude sunflower oil and crude palm oil.
Example 3
[0225] Industrially Produced Crude Palm Oil
[0226] Industrially produced crude palm oil was purchased from Nutriswiss (Lyss, Switzerland). The oil was subjected to mitigation trials by centrifugation.
[0227] 1 L of crude palm oil was melted by heating to 80° C. in a water bath. The oil was homogenized by manual shaking. 40 mL aliquots were transferred into 50 mL Falcon test tubes. The tubes were inserted into an Eppendorf 5810 centrifuge pre-heated to 40° C. and were centrifuged at 15000 g for 15 min at 40° C.
[0228] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the centrifugation on the resulting MCPDE levels are shown in
Example 4
[0229] Long-Term Settling of Industrially Produced Crude Corn Oil
[0230] Industrially produced crude corn oil was purchased from VFI GmbH (Wets, Austria).
[0231] The crude oil was first heated in a 2-L pyrex bottle at 60° C. in the water bath and was homogenized by vigorous manual shaking, then was left on the bench at room temperature without any disturbance for 5 months.
[0232] After the 5-month time period, 40-mL aliquots were taken from the upper phase and from the bottom phase, called “upper phase” and “lower phase” respectively.
[0233] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the long term settling on the resulting MCPDE levels are shown in
Example 5
[0234] Long-Term Settling of Industrially Produced Crude Sunflower Oil
[0235] Industrially produced crude bio sunflower oil was purchased from VFI GmbH (Wets, Austria).
[0236] The crude oil was first heated in a 2-L pyrex bottle at 60° C. in the water bath and was homogenized by vigorous manual shaking, then was left on the bench at room temperature without any disturbance for 5 months.
[0237] After the 5-month time period, 40-mL aliquots were taken from the upper phase and from the bottom phase, called “upper phase” and “lower phase” respectively.
[0238] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the long term settling on the resulting MCPDE levels are shown in
Example 6
[0239] Short Term Settling of Cold Pressed Crude Canola Oil
[0240] 7.9 kg of canola seeds were pressed using a home electrical oil press (OP 700, Rommelsbacher, Germany) resulting in ˜2.4 kg of pressed oil and ˜5.5 kg of remaining solid residue (cake). The pressed oil was then filtered through filter paper (Whatman 595%) at 65° C. in the oven.
[0241] 2 L of crude oil was then left on the bench at room temperature without any disturbance for 4 days for settling.
[0242] After the 4-days time period, a 20-mL aliquot was taken from both the upper phase and from the bottom phase, called “upper phase” and “lower phase” respectively.
[0243] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the short term settling on the resulting MCPDE levels are shown in
Example 7
[0244] Long-Term Settling of Industrially Produced Crude Soybean Oil
[0245] Industrially produced crude bio soybean oil was purchased from VFI GmbH (Wets, Austria).
[0246] The crude oil was first heated in a 2-L pyrex bottle at 60° C. in the water bath and was homogenized by vigorous manual shaking, then was left on the bench at room temperature without any disturbance for 5 months.
[0247] After the 5-month time period, 40-mL aliquots were taken from the upper phase and from the bottom phase, called “upper phase” and “lower phase” respectively.
[0248] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the long term settling on the resulting MCPDE levels are shown in
Example 8
[0249] Long-Term Settling of Solvent Extracted Crude Sunflower Oil
[0250] Production of solvent extracted crude sunflower seed oil is described above.
[0251] 1 L of this crude oil was subjected to long term settling trial by leaving it on the bench at room temperature without any disturbance for 5 months.
[0252] After the 5-month time period, 40-mL aliquots were taken from the upper phase and from the bottom phase, called “upper phase” and “lower phase” respectively.
[0253] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the long term settling on the resulting MCPDE levels are shown in
Example 9
[0254] Industrially produced crude palm oil was purchased from Nutriswiss (Lyss, Switzerland). The oil was subjected to mitigation trials by centrifugation.
[0255] 1 L of crude palm oil was melted by heating to 40° C. in a water bath. The oil was homogenized by manual shaking. 30 mL aliquots were transferred into 50 mL Falcon test tubes. The tubes were inserted into an Eppendorf 5810 centrifuge pre-heated to 40° C. and were centrifuged at 15000 g for 15 min at 40° C.
[0256] The resulting samples were subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The benefits of the centrifugation on the resulting MCPDE levels are shown in
Example 10
[0257] Industrially produced crude palm oil was purchased from Nutriswiss (Lyss, Switzerland). The same batch of crude oil was subjected to mitigation trials by two different centrifugation experiments.
[0258] The crude palm oil was melted by heating to 80° C. in a water bath. The oil was homogenized by manual shaking.
[0259] One aliquot of the oil was transferred into 40 mL Falcon tubes and was subjected to centrifugation at 15000 g for 15 min at 40° C. in an Eppendorf 5810 centrifuge pre-heated to 40° C.
[0260] The other aliquot was transferred into 1 L reservoirs and was subjected to centrifugation at 4000 g for 15 min at 40° C. in a Thermo Scientific Heraeus Cryofuge 8500i centrifuge pre-heated to 40° C.
[0261] Following centrifugation, the upper 10% (v/v %) and lower 10% (v/v %) phases were separated into different tubes. These aliquots corresponding to the purified oil (upper 10%) and the sediment-rich oil (low 10%) were then subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The concentration effect of the centrifugation on the resulting MCPDE levels is shown in
Example 11
[0262] Industrially produced crude palm oil was purchased from Nutriswiss (Lyss, Switzerland). The crude oil was first heated at 80° C. and then centrifuged at 15′000 g for 15 min at 40° C. The lower 10 v/v % liquid phase rich in sediments was used for degumming.
[0263] Degumming of this oil was performed by first heating this oil to 80° C. and adding 0.02% phosphoric acid 85% (v/v). Then this mixture was sheared with a shear mixer (Silverson L5M-A) at 1000 rpm for 2 min while maintaining the crude oil at 85° C. Then the mixture was mixed with 2% MilliQ water (v/v) and again sheared at 1000 rpm for 2 min. In order to separate the oil from the gums, the mixture was centrifuged at 3′000 g for 5 min at 40° C. and the upper 95% liquid phase was used further work as the degummed oil.
[0264] The centrifugation based mitigation was applied to this degummed oil by subjecting it to centrifugation at 15000 g for 15 min at 40° C. in an Eppendorf 5810 centrifuge pre-heated to 40° C.
[0265] Following centrifugation, the upper 10% (v/v %) and lower 10% (v/v %) phases were separated into different tubes. These aliquots corresponding to the purified degummed oil (upper 10%) and the sediment-rich degummed oil (low 10%) were then subjected to heat treatment in ampoules in order to simulate the formation of MCPDEs and were analysed by LC-MS for their MCPDE content accordingly. The concentration effect of the centrifugation on the resulting MCPDE levels is shown in
[0266] All publications mentioned in the above specification are herein incorporated by reference. Various modifications and variations of the disclosed methods, uses and products of the invention will be apparent to the skilled person without departing from the scope and spirit of the invention. Although the invention has been disclosed in connection with specific preferred embodiments, it should be understood that the invention as claimed should not be unduly limited to such specific embodiments. Indeed, various modifications of the disclosed modes for carrying out the invention, which are obvious to the skilled person are intended to be within the scope of the following claims.