CA1120778A - Processing of food fat - Google Patents

Abstract

Process for the treatment of edible fatty substances, and more particularly of a palm oil or of a fraction of palm oil having a saturated / unsaturated ratio of between approximately 0.3 and approximately 1.2, for the production of one or more edible fractions, one of these fractions being constituted by an edible oil having a high content of unsaturated fatty acids and if necessary another of these fractions being constituted by a concrete fraction usable as a base for butter substitute cocoa. The method is characterized in that for obtaining the oil or the oil fraction to be treated or an intermediate fluid fraction which has already been subjected to a preliminary treatment, in the presence of an appropriate interesterification catalyst , at a temperature of between 20 and 80.degree.C, the interesterification reaction being followed and if necessary, preceded by at least one fractionation using suitable fat fractionating solvents at temperatures between - 20 and + 35.degree.C, to obtain a fluid fraction of iodine index greater than 75 preferably greater than 80, essentially containing unsaturated triglycerides having a triinsaturated triglyceride content> 20% devoid of trans isomers, and exhibiting the properties of edible oils such as peanut oil and olive oil. .

Description

'7 ~ 7 ~
'~.
The present invention relates to a method for the production of a plurality of edible fractions to from fatty coxps such as oils or fats, and more particularly smoothly from palm oil, with a high content in saturated fatty acids and in particular from ~ ir of materials natural fats with a saturated / unsaturated ratio ranging from about 0.3 to about 1.2 ~. The invention also relates to edible fractions obtained by this process.
As we know, natural fats are usually complex mixtures of triglycerides in the compound sition from which saturated (solid) and unsaturated fatty acids enter turés (fluids) of different lengths of chalne. The composition into fatty acids and the distribution of these within triglyceride molecules are specific to each type of oil and determine the melting point of ~ them. However ~ in the mixtures which constitute natural fats, intersolubility phenomena occur.
Regarding the composition of palm oil currently ~ t on the market ~ we can observe a certain balance between the total content of saturated and unsaturated fatty acids, with a predominance of one or the other according to the countries of origin and the variety. However the distribution of fatty acids in the molecule makes it difficult to clearly separate into two fractions:
the amounts of triinsaturated triglycerides (has three fatty acids unsaturated) and trisaturated (three saturated fatty acids) are weak while the disaturated ~ monounsaturated and the monosaturated-diinsatu-res are found for the ~ current ~ discount ~ in almost quantities about 45% which will be able to evolve in the future with new varieties of palm trees, for example the hybrid of Guineensis-Melanococca. However, to obtain an oil comparable to commercial vegetable oils, it is necessary to separate from palm oil, the most unsaturated triglycerides (two double bonds or more) corresponding mainly to trigly-cerides having two or three unsaturated fatty acids in the molecule.
Given the growing interest in palm oil on the world market, a lot of research has been done to develop methods for separating oil from palm and other gra ~ se ~ material with physical properties ques and a chemical composition voi ~ ines, in concrete fractions high melting point, rich in saturated fatty acid and frac-~ 1 ~
7i ~
.
fluid, low melting, rich in unsaturated fatty acids turés.
It turned out that the fractionation processes of the natural fat used9 does not allow to obtain fractions in which the sharing of fatty acids saturated in concrete fractions and unsaturated fatty acids in fluid fractions is perfectly satisfactory: in effect. the chemical structure of the fatty substance, palm oil, the occurrence, is a limiting factor of separation rates pective so that whatever the fractionation processes some of the unsaturated fatty acids remain in the solid fraction.
The consequence was that a satisfactory sharing doing can only be achieved by attacking the chemical structure that of the palm oil triglyceride molecule, to move the unsaturated fatty acids found in the trigly-cerides composed of two saturated acids and one unsaturated acid, towards a triinsaturated or at least monosaturated-diunsaturated formation ~
. One of the most important and most flexible which allows to modify the chemical structure of fatty substances so as to preferably recover the total amount of unsaturated fatty acids they contain, is represented by interesterification, which can be defined as modifying fication of the glyceridic structure of fatty substances, by rearrangement molecular settlement of fatty acids on glycerol, by rupture and reestablishment of ester links.
This is how the researchers were led to develop processes combining ~ ractioning with inter.
esterification.
The methods known in the prior art are aimed generally obtaining a preponderant fraction having specific characteristics; depending on whether they aim to get essentially a fluid fraction or a concrete fraction, these processes use fractionation and inter-higher or lower esterification; this is how we know, for example, processes for obtaining a fraction solid of mixed triglycerides by cooling the oil to treat at 4-5 ~ C for 1 to 5 days, ~ then ~ interesterification at the same temperature, for a period of around 3 to 5 days 4 ~. Followed by fractional crystallization in an appropriate solvent Q7 ~
at a temperature of 20-21 ~ C (American Patent n ~ 2,442,535) 0 From even a solid fraction containing fine triglyceride crystals saturated wrinkles (SSS) can be obtained by crystallization and simultaneous interesterification at increasing temperatures gradually from 21 to 38 ~ C ~ American Patent n ~ 2,875,066) o Other known methods essentially aim to obtaining a fluid fraction: this is in particular the case of U.S. Patent No. 2,442,539 in which interesterification is carried out at a temperature of the order of 49 ~ C and is followed fractionation at 18 ~ C, in a solvent present in a proportion of 4/1 compared to the treated oil, ~ t includes stages of recycling the solid fractlon obtained at the end of the fractionation at the same time as the fluid fraction O This is also the case of the process described in the publication BABIN (OLE ~ GINEUX, lS 29th year, n ~ 7, July 1974, pages 375-378) which realizes a fractionation by centrifugation in the presence of a surfactant active to obtain a concrete fraction and a fluid fraction which is subject to interesterification at 33-36 ~ C, the order of two stages of this process which can be reversed to improve the proportion and quality of the fluid fraction obtained. A method aimed at obtaining a fluid fraction has also been proposed, which performs a palm oil transesterification reaction with a fatty acid ester of a C1 to C3 alkanol (Patent French n ~ 7S 35 734). It does not appear from the prior art that a same process can obtain a fluid fraction of indic ~
iodine greater than 75 and two or more solid fractions all of which can be used in the food industry.
The object of the present invention is to provide a process for producing an edible oil from fat with high fatty acid content saturated which responds better to the necessities of practice than aiming processes. for the same purpose proposed in the prior art, in particular-in that it allows a fluid oil to be obtained with properties analogous to those of edible oils ~ commercial, such as peanut oil and olive oil, in particular, and in particular physico-chemical characteristics analogous to those of these oils, using exclusively processes authorized by the Legislation of many countries, and presenting ~ in in addition, an extremely unsaturated tocopherol / fatty acid ratio 4 ~ favorable on the nutritional level and superior to that of oils above edible.
The present invention is given for the purpose of achieving ~
to achieve this objective by developing a treatment process palm oil or a fraction of palm oil having a saturated / unsaturated ratio of between approximately 003 and approximately 102 for the production of a QU several edible fractions, one of these fractions being constituted by an edible oil with a high content of unsaturated fatty acids O process characterized in that ~ for obtaining edible oil ~ on performs an interesterification reaction of the oil or fraction of oil to be treated or an intermediate fluid fraction having already been subjected to a preliminary treatment in the presence of a interesterification catalyst suitable for 7 + temperature between 20 and ~ 0 ~~ the interesterification reaction being followed and if necessary preceded by at least one fractionation at using suitable fat-breaking solvents for temperatures between ~ -20 and + 35 ~ C to obtain a fluid fraction of iodine index greater than 75 preferably greater than 80 containing essentially unsatu triglycerides ~ -res has a triinsaturated triglyceride content ~ 20% devoid of trans isomers and presenting the properties of edible oils ~
wheat such as peanut oil and olive oil According to an advantageous embodiment of the method5 object of the present invention, it is carried out directly during from a first step the interesterification of fat to treat, at temperatures between ao and 80 ~ C ~ in the presence of an appropriate interesterification catalyst, and subjected to during a second stage of the interest fat process rified to at least one fractionation using a solvent of appropriate fat fractionation at a temperature between -20 and + 35 ~ C.
According to another advantageous embodiment of the process which is the subject of the invention, the fractionation step is carried out in a single operation, using a solvent taken from the group that includes trichlorotrifluoroethane ~
hexane at temperatures between -20 ~ C and -10 ~ C, fat / solvent weight ratio being between 1/2 and 1/7 ~
According to another advantageous embodiment of the method of the present invention ~ the fractionation step comprises at least two successive fractionation operations, namely: a first fractionation of the fat interesterified, using a solvent for ~ reactivation of appropriate fats, taken from the group which includes, preferably, txichlorotri: Eluoroethane, hexane, isopropanol, acetone, present in an oil / solvent weight ratio between 1 / 0.5 and 1/7, for 2 to ~ hours at a temperature included between 0 and -t35 ~ C, followed by a second fractionation of the fraction fluid obtained a]. 'from the first fractionation in a . 10 suitable yeast fractionation solvent, preferably rence taken from the group which includes trichlorotrifluoethane andhexane, present in an oil / solvent weight ratio between 1/2 and 1/7, for 2 to 4 hours, at temperatures erasures between -10 and -20 ~ C, to obtain a fraction edible fluid essentially constituted by triglycerides unsaturated having a triinsature triglyceride content > 20 ~ which is recovered by separation of the concrete fraction also obtained.
According to a provision of this embodiment of the proceed, the concrete fraction obtained at the end of the second fractionation is recycled at the top of the process, in the fat to be treated, to be joint interesterified-lie with the latter.
According to a particularly advantageous variant of the method according to the invention, the reaction of interesteri ~ ication is carried out on an intermediate fluid fraction having already has been subjected to at least one splitting e-tape.
In this case, the method according to the invention comprises stages of fractionation of the fat to be treated, using suitable fat fractionating solvents, present in a proportion of 0.5 to 7 faiths.s the weight of the gralsse, at temperatures between + ~ 5 ~ C and -20 ~ C, to obtain . 5 -one or two concrete fractions and a fluid fraction between medium, and a step of interesterification of the fraction intermediate fluid, which is carried out in the presence of a ~ suitable interesterification catalyst, at a temperature between 20 and 80 ~ C, these main milking stages ment being associated with a complementary fractionation stage keep silent about the interesterified intermediate fraction and can be combined with complete fractionation stages of the concrete fraction (s), these stages of lo additional fractionation using a solvent of appropriate fat splitting, to get four frac - ~
6 ~ 7 ~
presentarlt of the properties of ~ edible raisses O namely:
- a fluid fraction of higher iodine index ~ 80 containing essentially unsaturated triglycerides ayarlt a content of triinsaturated triglycerides ~ 20% present the properties of edible oils such as peanut oil and olive oil;
- a concrete iraction of iodine index between ~ 1 and 43, mainly containing 2 ~ oleo ~ 1/3 - dipalmitin ~ usable as a substitute base for cocoa beu ~ re; - a fraction iodine value concrete between 33 and 43l containing mixed triglycerides ~ usable in different sectors the food industry and notably ~ in margarinerieO ~ a concrete fraction with iodine value less than 20, containing essential tially saturated triglyceridesl usable preferably in lipochemistry or in different sectors of the food industry According to an advantageous embodiment of the method o ~ jet of the present invention, a first step of fractioning ~
ment is carried out at a temperature between 0 and ~ 35 ~ C for obtain a concrete fraction essentially constituted by saturated triglycerides, iodine value less than 2 ~ and a concrete intermediate fraction which is subject to a new fractionation treatment at a temperature between ~ 15 and -20 ~ C in 2 to 7 times its weight of fractionation solvent, to obtain a concrete fraction essentially constituted by 2-oleo ~ 1,3-dipalmitine which can be used as a base for cocoa butter tut and an intermediate i-luide Eraction ~ ui is subject to interesterification in the presence of a catalyst suitable, at a temperature of the order of 80nC for 30 to 60 minutes, followed by further fractionation in a solvent of fractionation preferably taken from the group which includes the trichlorotrifluoroethane and hexane ~ present up to 7 times the weight of the interesteric fluid fraction. ~ Iée to be treated, a a temperature ranging from ~ to -20 ~ C, to collect a fraction essentially consisting of mixed triglycerides 7 of iodine value between 33 and 431 and a fluid fraction essentially consisting of unsaturated triglycerides having triinsaturated triglyceride content ~ 20% iodine value greater than 80, presents the properties of edible oils such as peanut oil and olive oil D
~ according to another advantageous embodiment ~ of ~ 0 process object of the present invention, the first step of 7 ~ 7 ~
fractionation of the fat to be treated is carried out at a temperature between + 20 ~ C and -20 ~ C depending on whether the weight of fractionation solvent varies from 1 to 7 ~ iis the weight of the matter to be treated to give rise to: - on the one hand a reaction concrete which is subject to a new fractionation in the middle solvent, which makes it possible to recover a concrete fraction comprising predominantly saturated tr.l of iodine index less than 20 and a second concrete fraction essentially consisting of 2-oleo-1 r 3-dipalmitine, - and on the other hand to an intermediate fluid fraction which is subjected to a Interesterification treatment at an order temperature 80 ~ C, in the presence of an interesterification catalyst appropri.e, following which one obtains by fractionation in a fractionation solvent preferably taken from the group which includes trichlorotrifluoroethane and hexane, present up to 7 times the weight of the fluid fraction interestéri: Eiate to be treated, at a temperature going up to - ~ 0 ~ C, a concrete fraction essentially constituted by mixed triglycerides, with an iodine value between 33 and ~ 3, and a fluid fraction essentially constituted by unsaturated triglycerides having a triglyceride content triinsaturated> 20 ~ iodine index greater than ~ 0, having the properties of edible oils such as oil peanut and olive oil.
In accordance with the invention the fractional solvent nement implemented can be advantageously chosen from the group which includes trichlorotrifluoroethane, hexane, isopropanol and acetone.
Also according to the invention the different your process fractionation steps are carried out by putting into operation one or more fractionation solvents, notably chosen from the group which has just been mentioned 7 ~ 7 ~
upper.
According to an advantageous embodiment ~ u process object of the invention, the fractionation operations are carried out using quantities of solvent which represent from 0.5 to 7 times the weight of the yrasse material or of the fraction treated, the temperature of the fractionation being between - ~ 35 ~ C and -20 ~ C depending on the proportion of solvent with respect to the fat or the fraction treated, used for fractionation, and the type of soil ~ ant artwork.
According to another advantageous embodiment of the process object of the present invention, the interesterification is a free interesterification, carried out in the oil phase, a a temperature between 60 and 30 ~ C, in prese ~ this dlun suitable interesterification catalyst, preferably chosen in the group of alkaline alcoholates, for a period 30 to 60 minutes.
According to another advantageous provision of the invention tion, llinteres-terification is a directed interesterification, performed in the oil phase at a temperature of around 20 to 40 ~ C, in the presence of a ~ dlintereskerification catalyst appro ~
pray, preferably chosen from the group of alcoholates alca-lins, for a period of 1 to 6 hours, and preferably from 1 to 3 hours 5.
According to another d: ispositi.on still of the process object of the invention, interesterification is an intereste ~
ri-fi.cation diri.gee, carried out in solvent phase, at a temperature around 20 to ~ 0 ~ C approximately, in the presence of a catalyst appropriate interesterification, prefixed in the group of alkaline alcoholates for ~ 6 hours, and preference for 1 to 3 hours the solvan ~ etan-t present in the proportion of 0.05 ~ to 0, ~ part by weight relative to the 24 ~ 778 fat to be treated.
The quantity of catalyst used is preferably of the order of 0.2 to 0.4% by weight of the weight of the fraction subject to interesterification / catalyst u ~ llise possibly ~ for example sodium methylate.
'The interesterification reaction is stopped at due time, by destruction of the catalyst in a known manner in itself, and in particular by introducing water at the rate of About 3% of the weight of the interesterified fraction, or of acid acetic at a rate of approximately 1% of the weight of the ~ racti.on interesterified.
The method according to the invention therefore makes it possible to obtain four edible fractions with specific characteristics, from natural fats presenting a ratio satures / insatures included in ~ re about 0.3 and about 1.2;
this process makes it possible to achieve yields particularly interesting in these four frac ~ ions, since the yield fluid fraction comparable to peanut or olive oil is higher, for current varieties, than 30 ~ and can even reach 70 ~, while the yield. in concrete fraction can be used as a substitute for cocoa butter e ~ t of at least 10 ~ and can even reach 45%, the yield in ~ concrete reaction essentially ... ..
9: ~ .2 ~ 77 ~
consisting of mixed triglycerides is on the order of 10 to 30% and the yield in concrete fraction esserltiel.lement consti-killed by saturated triglycerides is usually between 1 and 15%. Such returns allow maximum u ~ e maximum valuation of the fat used.
Among the fractions obtained by the process according to the invention ~ the fluid fraction is particularly interesting since it is essentially made up of triglysers unsaturated with triinsaturated triglyceride content> 20%
whose iodine index is greater than 75 and preferably 80 whose]
cloud end point is in ~ er at 12 ~ C ~ whose content tocopherols is greater than 0 ~ 035% ~ and whose tocopherol ratio in mg per 100 g of fat / polyunsaturated fatty acids in% 9 is greater than 0 ~ 6, with yields greater than 30% and up to 54% for current varieties and for varieties of palm oil rich in unsaturated for example the hvbride Guineensis ~ Melanococca, up to 75 ~.
To allow a better understanding of the notion of "end point of trouble" or PFT ~ ~ we will give below ~
a brief description of the methods for measuring the PFT: a ~ .lon fat sample (about 50 rnl) is placed in a.
test tube immersed in a precision thermometer7 and surrounded by a dust jacket; the sample is cooled overnight -20 ~ C; it is then placed in a tank containing a water bath thermostatically controlled to a temperature chosen from a range included between - ~ 25 and + 40 ~ C; as soon as the oil has become limpid and we read at the precision thermometer the temperature at which this last became clear, this temperature being called "trouble point" 0 The implementation of the process according to the present inven-tion, presents particularly important avantayes in the treatment of palm oil because the process conforms to the invention allows optimal development of palm oil.
Indeed, palm oil is extracted from the palm fruit at oil found in tropical tropical countries, Sumatra, Malaysia, tropical America) 0 It is distinguished by its relatively high content of palmitic acid which is, as we know it, a fatty acid saturated in C16 t42% approximately for the current varieties) and its significantly low acid content olelque, C18 unsaturated fatty acid (around 38% for the same . . , 10 ~ 7 ~
varieties), while peanut oil and olive oil contain approximately 10% and approximately 15% acid respectively palrnitiquel and about 55% and about 65% oleic acidO This relatively high palmitic acid content is responsible for the poor resistance to cold of palm oil and the impossibility lity in which one is to use it as it is as than salad oil in temperate or cold climates of countries from Europe, North America or Japan ~
In addition to the benefits of valuing palm oil according to the invention, another advantage of process according to the present invention is to concentrate and enrich the fluid fraction with natural tocopherols (Vitamin E) which are of great interest because of their anti oxygen and biological. This is illustrated in the following TabLeau:
lS Palm oil Fluid oil _ departure _ rech_rché_ Tocopherol content (x) in mg / 100 g of oil 58 95 (x) The contents of tocopherols are determined by redox, then colorimetry according to classical methods and expressed in equivalent of ~ -tocopherolO
The figures in the table above relate to fatty substances at the same stage of refining (incoming oil in deodorization).
Concentration in the fluid oil of tocopherols present in palm oil, offers the following advantages:
a) Maintenance of taste properties: it is desirable for the most unsaturated oil fraction to be enriched in ~ natural antioxidants, since it is the most sensitive to oxyclationO
From this point of view, the method makes it possible to obtain a fluid oil suitably protected by its antioxidants ~ natural genes and requiring no addition of synthetic antioxidants such as, for example, BHA and BHT9 whose employment in the food industry is currently being questioned.
The fractions ~ o ~ ides, less oxidizable, contain sufficient quantities of tocopherols for this type of product.
b) Balance of vitamin E / polyunsaturated fatty acids:
recent trays (see; ~ he Role of f, ats in, human n ~ trition - edited by ~ -J-Vergroesen ,, Ch.9: "Lin, oleic aci ~ intake and vitamin E requirement "from ~ '.C. ~ ayer, pages 381-425 - Academic Press, ed. ] .975 demonstrated the importance of tocopherols during of acid ingestion ~ low polyunsaturated and particular linoleic acid ~
~ this title ~ palm oil appears as having a very good balance of vitamin E / polyin fatty acids saturated (see fiyure, page 425, from the opening cited above).
The process according to the present invention provides the advantage enrich the fluid fraction with linoleic acid, yras acid essential, while concentrating the tocopherols, which will in the direction of maintaining the correct initial balance, maintaining which is not ensured by the prior art procedures for an equivalent level of linoleic acid.
If the process conforms to the present invention is of particular interest in its application to trafficking palm oil belonging to the current varieties, it also applies equally to the treatment of new varieties as well as any other fat in which the proportion of saturated fatty acids is too high for ensure satisfactory fluidity in temperate climates.
In addition, the split modalities:
used in the process according to the invention, perme-tten, t to obtain a symmetrical triglyceride 1-3 saturated, 2 unsaturated, with industrlessly interesting yields for obtaining A good cocoa butter substitute compatibili-te with the latter.
For the implementation of the process con ~ orme a 3 ~ the present invention, llon operates in accordance with the terms; ~
which will follow f ~ i-tes with reference to the following drawings:
- fiyure 1 ~ a) represen-te a diagram of .9 ~ J

reaction steps of the process according to the in ~ ention for the treatment of a semi-refined palm oil by interest ~ -rification followed by a fractionation to obtain a fluid fraction A and a concrete fraction B rich in SSS and SSI;
- Figure 1 (b) shows a diagram of reaction stages of the process according to the invention for the treatment of a semi-refined palm oil by interes-terification and first fractionation to obtain a concrete action rich in SSS and an inter-fraction mediary which will be subject to a second fractionation for obtain a fluid fraction A and a rich concrete fraction D
in SSI which can be recycled by returning to the beginning of the process;
- Figure 2 represents a diagram of the stages reaction of the process according to the invention for the treatment ment of a semi-refined palm oil subjected to a first fractionation to obtain a concrete fraction Cl rich in SSS and an intermediate fluid fraction Fl which is by the following subject to a second fractionation to obtain a conc.rete fraction C2 rich in POP and a fluid fr ~ ction intermediary F2 which is subsequently subject to an intereste-rification and a fractionation to obtain a fraction concrete C3 and a fluid fraction F3; and - Figure 3 represents a diagram of the e-steps reaction of the process according to. the invention for the ment of a semi-refined palm oil subjected to a first fractionation to obtain a fraction ~ luide interme.diaire which is subsequently interesterified and fractionated dQn.ner a concrete fraction C3 and a fluid fraction F3, and a fraction intermediate concrete tion which is then fractionated to obtain a concrete fraction ~ 1 rich in SSS and a concrete fraction C2 rich in POP.
11 a -: ~ 2 (~ 8 I ~ IN ACCORDANCE WITH DIAGRAMS 1a and 1b PES APPENDIX PINS
Palm oil, preferably semi-refined born, is subject to an interesterification reaction.
a) The interesteri ~ ication reaction can be free ~ at random); in this case, it is performed by presenting ce from 0 ~ 1 to 0.2% by weight of an interesterified catalyst suitable cation, for example pre- sodium methylate ference, or metallic sodium or a Na-K alloy, has a temperature between about 60 ek about 80UC ~ during 30 to 60 minutes, with stirring and 50US vacuum Oll under atmos-inert father ~
"~ .Z ~
b) The interesterification reaction can be directed; in this case, it can be carried out in phase ~ oil or in a solvent such as trichlorofluoroethane preferably or in hexane in an oil / solvent proportion between 1 / 0.05 to 1 / 0.4, in the presence of 0.2 to 0.4% in weight of a suitable catalyst, for example methylate of sodium, or metallic sodium or a Na-K alloy, has a temperature between 30 and 40 ~ C, for 1 hour to 24 hours, preferably 1 to 3 hours, with shaking and vacuum or under an inert atmosphere ~
Once the interesteri. ~ Ication, free or directed, carried out at the end sought after the time indicated above, the catalyst is inactive by adding 2 to 3% by weight of water or 1% glacial acetic acid, and eliminates by all appropriate means.
The interesterified fat is then ready to be split up.
The Erection of the interesterified oil obtained is then carried out sel ~ n one of the following modalities:
1 - In accordance with diagram la:
The fractionation is carried out in a solvent of appropriate fractionation, preferably in trichloro-trifluoroethane or in hexane, the solvent being present at 2 to 7 times the weight of the oil to be fractionated, at a temperature between -10 and -20 ~ C, for 2 to 4 hours, to recover a fluid fraction of iodine index greater than 75, which has the physical and chemicals in commercial edible oils (peanut oil or olive).
II ~ In accordance with diagram lb The fractionation step can e ~ alemen-t be reali-see according to the following modalities:
- ~ - 12 -.
a) a first fractionation is carried out in a fractionation solvent taken from the group which comprises, for example example hexane, trichlorotrifluoroethane, isopropanol, acetone, at temperatures between 0 and + 35 ~ C, the material weight ratio ~ rasse / solvent being between l / 0.5 and 1/7;
b) the intermediate fraction obtained is separated of a concrete reaction also obtained during this fractionation::
ment and is subjected to a second fractionation in solvent phase, the solvent being pre ~ erence trichlorotrifluoroethane or hexane, present at 2 to 7 times the weight of the oil treated, for 2 to 3 hours, at a temperature included between -10 and -20 ~ C. The fluid fraction thus obtained has an iodine index greater than 75.
The concrete fractions obtained are essential-consisting of saturated triglycerides and triglycerides mixed cerides and can be used in lipochemistry and different sectors of the food industry.
The concrete fraction obtained at the end of the second splitting is essential] .ement constituted by tri ~ high school mixed wrinkles. It can be recycled at the head of the pxocédé, ~ ' approximately 50% concrete fraction for About 50% of palm oil to be treated, to be subjected to new to the interesterification process and allow a significant improvement in ~ lobal yield in fluid fraction.

A / Preferably semi-refined palm oil is subjected to a solvent phase fractionation process r at a temperature of the order of 0 to + .35 ~ C, the proportion by weight oil / solvent ~ being between l / 0l5 and 1/7, and preferably between 1 / 0.5 and l / 4 and the duration of the operation of crystallization being from 2 to 15 he ~ res, and preferably from ~,:;.,.

2 a ~ hours.
The solvent is advantageously chosen from the group which includes trichlorotrifluoroethane, hexane, iso-propanol and acetone, and is preferably trichloro-trifluoroethane.
The temperature to which the mixture is subjected palm oil and solvent, is sufficiently low for cause proper cooling to cause crystallization saturation triglycerides at very high melting points, mainly tripalmitin. The mixture is maintained at the above temperature under slow agitation.
duration indicated above, at the end of which the content of saturated triglyceride crystals stabilize r the fraction crystallized concrete (C1) is separated from the Eluide fraction (Fl ~ by a known solid-liquid separation process, by example by pressure filtration on a filter cloth ~ e, in polyamide for example, of porosity 20 ~ 1: the fraction Cl is washed on filter with fresh solvent, miscella lava ~ e obtained is introduced into the filtrate.
The ~ concrete reaction Cl (SSS ~ obtained with a ~ yield of about 1 to 15%, after removal of the solvent, has an iodine value less than 20 and can be used as is.
B / The intermediate fluid fraction, Fl, obtained with a yield of the order of 85 to 95% is subjected to a new fractionation in solvent phase at a higher temperature bass ~ l ~ e that implemented in the first step of fractionation and between +15 and -20 ~ C, the ratio by weight F1 / solvent being preferably between 1/2 and 1/7, and the duration of the crystallization operation being 2 to 15 hours and preferably from ~ to 6 hours.
Preferably the same t ~ vpe of solvent is used ~; - 1 ~ -than during the first fractionation step.
The temperature is chosen low enough to cause crystallization of triglycerides high fusion, mainly disaturated triglycerides-monounsaturated.
Fractionation is continued at temperatures above and for the durations above; the concrete fraction crystallized ~ C2) is then separated from the fluid fraction F2 by filtration and washed on filter as indicated above.
The concrete C2 fraction obtained after elimination solvent is mainly constituted by triglycerides symmetrical monoinsatures-disatures, and more particularly by 2-oleo-1,3-dipalmitine (POP) which constitutes an excellent base of cocoa butter. The C2 fraction, of which the iodine value is between 31 and 43, is obtained with a yield from 10 to 45% and can be used as is.
C / The intermediate fluid fraction F2 is subject has free or directed interesterification treatment.
In the ~ remier case, after elimination of the solvent, the interesterification is carried out in the presence of a catalyst preferably consisting of sodium methylate present in preferably about 0.2% of the weight of F2, during about 30 to 60 minutes, at a temperature of around 60 to 80 ~ C.
In the second case, directed interesterification can be carried out with or without solvent, in the presence of a inter-interxification catalyst preferably taken in the group of alkaline alcoholates, for example, methylate of sodium, at a rate of 0.2 to 0.4% by weight of F2, for a lasts from 1 to 3 hours and at a temperature between 20 and 40 ~ C, the sol ~ ant used being preferably hexane or trichlorotrifluoroethane, in oil /
soil ~ ant between - - - -- 14a -15, ~
1 / 0.05 and 1/04 by weight ~
When the interesterification reaction is ended ~ the catalystD is destroyed by adding 3 ~ / 0 of water or 1% acetic acid for example O
The interest-free fluid fraction thus obtained is washed and dried ~ by usual means, after disposal solvent if applicable D / The interesterified fluid fraction thus treated is then subjected to further fractionation in the solvent phase at a temperature preferably of ~ 20 ~ C ~ the weight ratio fluid / solvent action is preferably of the order of 1/3 to 1/7 and the duration of the operation ~ ation of crystallization being of the order 2 hours after the solvent used is preferably hexane or trichlorotrifluoroethane Once the crystallization operation is complete, we separates ~ by filtration for example ~ a concrete fraction C3 of a fluid fraction F3, Concrete fraction C3 stripped of its solvent is obtained with a yield of 10 to 30% and has an index iodine between 33 and ~ 3; it is essentially made up by mixed triglycerides} usable in different sectors of the food industry t and in particular in margarine factory J after classic refining The fluid fraction F3 ~ freed of its solvent ~
which is obtained with a yield of about 30 to 70% presents a iodine index greater than 80; it is essentially constituted by unsaturated triglycerides has a triglyceride content triinsaturated ~ 20% and has properties comparable to those common edible oils such as peanut oil and oli.ve oil ~ and in particular characteristics of ~ geage and de-icing similar to the latter and are enriched in tocopherols, co ~ a shown in the table below ~:
Concret Oil Concret Concret Oil palm Cl C2 C3 fluid departure (SSS): (POP) (SSI) sought.
Teneux in tocopherols (X) in mg / lOOg of oil 58 15 12 10 95 (X) The contents of tocopherols are determined by redox then colorimized-sorts according to conventional methods and - 40 expressed in equivalent ~ ~ tocopherol .. ~ c ~ ...
~ 6 The figures in the table above relate to fatty substances at the same stage of refining (incoming oil in deodorization).
III - CONFORMS ~ ENT TO THE SCHEME ~ 3 OF THE DRAWINGS ~
A / Preferably semi-refined palm oil is subjected to a solvent phase fractionation process O a a temperature between ~ 20 ~ C and 20 ~ C depending on whether the ratio weight of oil / solvent varies from 1/0? 5 to 1 / 7O The duration of the opera ~
tion of crystallization is preferably about 2 hours 7 and the solvent is advantageously chosen from the group which comprises trichlorotrifluoroethane, hexa ~ e ~ lYisopropanoly l ~ ketone e *
is preferably trichlorotrifluoroethane.
The mixture is kept under slow stirring for the duration indicated above, at the above temperature for cause sufficient cooling to entrain the crystal-trisaturated triglycerides and disatuxed triglycerides monounsaturated which are separated by filtration from a fluid fraction essentially constituted by triglyceride ~ monosaturated-diin-saturated The concrete intermediate fraction? which is obtained with a yield of around 46%, has an iodine value of around 31, and the intermediate fluid fraction O which is obtained with a yield of around 54%, has an iodine value of ~ around 68.
B / The concrete intermediate fraction is subject to further fractionation at a higher temperature than that of the first fractionation stage7 of: the order of ~ 10 ~ CJ
in the solvent phase, the oil / solvent weight ratio possibly ranging ~ up to l / 70 The oil-solvent mixture is stirred slow for about 2 hours after which:
two concrete fractions C1 and C2. The Cl fraction, obtained after solvent distillation with a yield of the order of 10%
has an io ~ e index less than 20. It is essentially constituted by saturated triglycerides (SSS) which can be used what. The fraction C2, obtained after distillation of the solvent with a yield of around 35% has an iodine index of around 40; it is essentially constituted by trigly-symmetric monounsaturated-disaturated cerides? and more particularly-ment by 2-oleo-1,3 dipalmitine, usable as a base cocoa butter substitute C / The intermediate fluid fraction obtained at the end ~ of the first fractionation operation is subject to a process sus of interesterification in the presence of a catalyst consisting of preferably for example by sodium methylate ~ presentO by e ~ ample, in a proportion of 0 ~ 2 ~ 003% by weight of the fraction to interesterify ~ for 30 to 60 minutes at a ~ temperature of around 80 ~ CO interesterification being carried out preferably ~ ence at 80 ~ Ct the interesterification being preferably carried out in phase oil ~ but can also possibly be carried out in phase solvent under the conditions indicated in II.C / above ~
When the reaction is complete, the catalyst is destroyed by any appropriate means known in themselves ~ and in particular ment by adding 3% water or 1% acetic acid glacia].
The fluid .interestified fraction obtained is washed and dried by conventional means after removal of the solvent if it there is The fractionated interesterified fluid thus treated ~
is then subjected to further fractionation in the solvent phase at preferably a temperature of -20 ~ C, the weight ratio fluid / solvent fraction preferably being of the order of 1/3 to 1/7 and the duration of the crystallization operation being of the order 2 hours, the solvent used being preferably hexane or trichlorotrifluoroethane ~
Once the crystal operation] .isation -terminated ~ .on then separates ~ by filtration ~ a concrete fraction C3 of index iodine of the order of 37 ~ e.ssentiellemen-t constituted by trigly--Mixed cerides usable in various industry sectors food and, in particular in margarinerieO and a fluid fraction F3 with an iodine index greater than 80, essentially consisting of unsaturated triylycerides having a tri- triglyceride content unsaturated ~ 20 ~ / ~ which has properties comparable to those ~ UsualIes edible oils, e ~ including characteristics ~ ues of figeaye and de-icing similar to the latter O This fraction fluid F3 is ~ additionally enriched in tocopherols as it has been indicated above ~ -The yield in concrete fraction C3 is around of 18 ~ / ~, and the yield in fluid fraction F3 is of the order of 36%.
Besides the provisions q ~ i precedeO the invention 18 ~ 7 ~
still includes other provisions that will emerge from the ~
following cry ~
The present invention relates more particularly to a process for the production of several edible fractions from natural fatty substances D whose ratio is saturated / unsaturated is between 0 ~ 3 and approximately 1 ~ 2 O and the fractions obtained by implementing this process ~ as well as the means suitable for implementing the process and obtaining said fractions and chalnes of manufacture in ~ uelles said process can possibly be includedO
The invention will be better understood using the complement of description that will follow ~ which refers to these examples of implementation of the process object of the present invention It should be understoodO, however ~ that these examples ples of implementationO are given only by way of illustration tion of ob ~ and invention ~ which they do not constitute way a limitationO
EXAMPLES
EXAMPLE l We start from discolored or deodorized palm oil and we carry out the directed interesterification in the presence of 0.4% sodium methylate at a decreasing temperature of 60 ~ C to 25 ~ C ~ the duration of the interesterification being between 1 and 6 o'clock The interesterification is stopped after this time by removing the catalyst by adding 2% of water followed by two washes with water ~ the oil is dried and fractionated according to the terms below:
a) a first fractionation is carried out in 0 ~ 5 part of trichlo-rotrifluoroethane ~ after 3 to 4 hours of ma-turation at ~ 20 ~ C;
a fluid fraction is separated ~ by filtration6 from a concrete C
~ ui is washed on filter with frals solvent ~ miscella of lava ~ eo ~ held being added to the filtrate;
b ~ the filtrate (fluid fraction ~ solvent) is adjusted to 7 times its weight of trichlorotrifluoroethane relative to the material fatty present, and is. fractional after 2 to 3 hours ~ e matu-ration at -20 ~ C.
L, a fluid fraction essentially constituted by unsaturated triglycerides is separated from a concrete fraction ~, by : ~ 0 ~ iltration ~ The solvent is ~ eliminated from the different fractions by , ~ j all usual means such as evaporation distillation, etc ~ .., The results obtained are shown in table I
clwapresO

__ C ~
E ~ I ~ g ~, ~ ~.
____ _ H ~ C
H
., 1 ~
~ ~ ~.
lo ~ ~ e ~ ~ ~
~ r ~ U!; ~ INO
:: ~ a) a) __ _ _ _ I
1 ~ ~ ~ ~
t ~ H. I Ln Ln Ln ~ H --_ h tg ~
~ e Ln ~ Q ~
O ~ Ln NN
H ¦
~ __ __ _ _.
~ HIN ~ ~ I
__ __ C ~ ~.
, ~
1 ~ ~
~ t ~ o, oo oa U ~ Y
_ ~ -1 H ~ O
., ~ tn ~ O
tn ~ ~ mo ~ _ C4tn ~ ~ 1 '1' n ~ NN
o ~ ~
~ ~
, a, ~ (~ 1 ta

3 5 U 0 ~ 1) U
rl ~ r ~ h ~ rl h ~ 1 h rl ~ rl Q) ~ rl a ra ~ $ -1 5-1, S: ~ h ~:
~, Ln ~ ~ n ~
a) v ~ a) ~ a tl) ~ Sl a) h 'aJ 5-1 e H a) ha) ~ a \ rl 'id' ~ I 51 ~ rl ~ h P ~
., __, ~, ~, .. __., ____.__ ~ ~ -_ '7 ~ 78 We proceed co ~ described in Example l ~ to the differ-However, the concrete D (SSI) is subject to rinsing.
ge pushed with pure solvent ~ which improves performance S in sought-after oil, while maintaining a high Iodine Index7 greater than 80, and a satisfactory PFTO The results obtained are shown in Table II below:
c. ', a' ~
7 ~
. ~ ~ l __ __., .............. .
. ~ ~
E ~. ~ u ~ ~
~ 4 ON ~ a). O rl O 1 ~
r-lr ~ l ~ r ~ l ~ rl ~ r ~ r- ~
r ~ l P ~. . rl ~ H rl ~: ~ X ~ a) ~ ~
~ r ~ ~~ I a): ~ H j ~
) '~ rl Lt) H CO ~ a ~ ~ H ~ Ot ~ a) CO
. . _ ~ rl ~ ~. rl --__ a) ~ rl rl ~ ~
~) rl 1 ~ 1 t rl r ~ 4-1 ~) ~ ~ a ~ a ~ a ~ I '~
r ~ ~ r ~ a1 rl N rl N
~ ~ ~ ~ ~ n ~ u ~ ~ n I ~ In P :; (I) ~ (I). __. r ~ ~ I
r ~ u ~ ~ ~
_ _ _ ~ r¦ rl ~ ~ ~ ~ ~ a rt ~ rdrl rl L, a) a) rl rl L. r ¦ t ~ tn G) ~ ~ t ~ ~ ri FF ~ ~ rl h ~ V t ~) rl L ~ ~ -, ~ rl a) HU r ~ ~~ t ~ L ~ rl ~ H h HL ~ L ~ O ~ ~> ~ rl 41 __ _ U_ _ - I
O tV t ~ lN ~ ~ a) - - L ~
; Cc ~ ~. rt. ~ a t ~ ~ r - lt ~) ~ 1 ~ ~ r ~ l ~ 1--1 t ~: JH a) 4 ~ ~ ~ ~ t ~ r ~ l rl ~ N tS ~
f'S '~ N ~ rl HI' CO IN rl E ~~) H ~ a) a) h -1 ~ ~ ¦ U ~ IV - - ~ --_--a) t- ~ a) ~ cL ~
O t ~ ~ (J ~ ~ 1 G tV ~ ir-l 1 ~ H
~ a3 ~ ro. ., rt ~ rt ~ a) ~ ~ ~, rtL ~ 'N t ~, r ~ l ~ ~ rr ~ 00 00 ~ IN
a LO r-ltV U
. __. . L ~ t ~ ~ O. . a) ~ _ _ aj O 00 ~ t 1 ~, ~ rl L ~ 1 ~ 1 L ~ r ~ t ~ a ~
~ IN r-l1 ~ rl tV rl h) ~ 1t ~ In U tl) ~ ro r ~ 1r-l rl ~ t ~ ~~ rh N t tn ~ rd a) L, _. _ ._ .o L ~ rl ULh, a ~ V
~ 1 cor ~ N tV ~ H Or ~ Jr-lt'f) where Lt; O t ~ \ ht ~ a ~ vt ~ l ~ n ~ a tl ~ NNL, s ~ Ll '; t ~ rl.
~ ~ tV h ~ r5 ~ th 5 ~
rl r lt ~ rl ~ D rt r - l ~ D
j ~ ob '~ - ~ J h ~ 1. . -.
~ tv rl r ~ ha ~ r ~ ~ rl rh r ~ l ~ h ah) mt ~ I h 5 ~ Irt a) ~ V
HH ~ ~ L ----_ 1--1 H ~ - 1-1 H

0 ~ 7 ~ 3 ..

1 kg of palm oil is interesterified in phase oil, i.e. ~ free interesterification ~ for 45 minutes at 80 ~ C ~ then fractionates at -20 ~ C in trichlorotrifluoro-ethane present in an oil / solvent proportion of 1 / 7n A fluid fraction of Iodine Index 78D is obtained with a yield of 3 ~%, of PFT equal to 9 ~ C and which has excellent properties freezing / defrosting tees at + 15 ~ C (comparable to peanut oil) O
The above examples make it possible to establish the following conditions and characteristics:
It can be seen that as soon as 20% of SSS ~ is obtained by directed interestérification. ~ a fluid yield of 52%.
We also note that compared to the inter-free rification olein unsaturation is improved by directed interesterificationO However ~ upon obtaining 20% of SSS, we reach the maximum of unsaturation ~
We also note that the unwashed concrete D obtained in Examples 1 and 2, always has a close degree of unsaturation starting palm oil. This allows recycling D if there is center of this fraction at the head of the interesterification cycle in mix 50/50 approximately with whole palm O This recycling has for effect of improving the overall yield in fluid fraction of the process O
There is also a very noticeable improvement of the PFT in the case of the interested ~ directed ification in relation to free interesterification.
FinallyD the degree of sa-tura ~ i.on of the concrete C augrnente with the degree of interestification ~

We start with pa] .me oil interesterified at random II = 52.
500 g of this fat is mixed with 250 g of hexane; cool to ~ 15 ~ C and make them fat crystals for 2 hours. ~ near this time we filter the crystals that we wash.
The filtrate is xepris and diluted so as to have a proportion by weight of oil / solvent of 1 to 30 Cooled at -20 ~ C and the crystals are magnified for

4 hours. After this time ~ we filter e ~ we wash the crystals with "new solvent, and after removing the solvent from each of the : -77 ~

fracti.ons, we get the following results:
~ r Concrete rich in SSS 16 18 Intermediate fraction 60 81 Concrete rich in SSI 41-44 36 Fluid 75-76 45 The PFT of the fluid fraction is 11 and the test is equivalent to peanuts ~
. The content of reducing tocopherols (antioxidants active) of the fluid fraction obtained in accordance with this Example ~
was dosed by colorimetry using the bathophenanthro-line which is based on the oxidation of tocopherols by chloride ferric in alcoholic solution ~ on subsequent formation of the Fe / bathophenanthroline complex, and the measurement at 532 m ~ of the specific extinction of the colored complex O
This assay gave the following results:
fluid fraction ~ before deodorization: 75 mg * / 100 g of oil:
after deodorization: 40 mg * /: 100 g of oil * unit: tocopherols expressed in mg of ~ -tocopherols for 100 g of oil.

We take Guineensis hybrid palm oil Melanococca d ~ 687 which is randomly interesterified and directed way according to the conditions according to the invention To 375 g of this sampleO is added 375 g of trichlorotrifluoroethane; cool to 0 ~ C and leave for 3 hours at this temperature O The crystals that have formed are filtered and washed O
We obtain ~ on the one hand ~ a concrete rich in trisa-30 -turated ~ SSS) ~ and / on the other handO a filtrate containing the fraction intermediate which is adjusted with solvent in a ratio fat / solvent of 1/7 by weight and which is cooled to -20 ~ C; this temperature is left for 3 hours7 The cris-rates obtained, rich in disaturated ~ monounsaturatedO are filtered and washed and the filtrate contains the fluid fraction of the palm, rich in unsaturated triglyceridesO
After removing the solvent from each of the fractions ~
the following results are obtained:
,. . .
~, ' ~ close inter. After inter-directed After inter ~ directed free 1 h ~ to ~ 35 ~ C 6 ho to + 35 ~ C
~ / 0 II -r O / D II ~ r% I ~ Io ____ ____ _ _ ____------ r ---------- ~~~ __ .____. ~ ___ .__._. w_. _______. _ Concrete SSS 9-10 23-24 18 2120-23 32-38 Concrete SSI 19-21 45-47 14 5015-17 50-52 Fluid 69-71 78-79 68 84 61-63 85 _ __ _ ~
10 This Example clearly shows that from a period directed interesterification l hour ~ we get a fr ~ tion fluid equivalent to that obtained after 6 hours of interestéri.fi ~
directed cation, and despite everything more unsafe than that obtained after free interesterification and with a much higher yield lS what you get with Elais type palm oil Guineensis.

1 kg of palm oil is fractionated at -20 ~ C ~ Ratio oil / trichlorotrifluoroethane by weight: 1/7. We get a fluid fraction of Iodine Index 72, with a yield of 43% 0 The freezing and de-icing characteristics of this fluid by measuring the cloud point of ~ in and the stability -at + 15 ~ C, and we compare it to that of other fluids (Table III) ~
2 ~
.
.
77 ~ 3 __ ~, 4 ~ a 6- ~
~ a ~ ~ I
_ _ _ ~~
~ _ _____ _ _ H h ~ _ E ~
~ _ ~ _ ~ _ _ _ ____ ._ ~ i ._ ~
~ ~ ~ ~ ~
___ -, ~ ___ ~ ~ _ '$ ~ ~
o ~ - ~ H
- 26 ~
.27 ~ ~
This table highlights the influence of the step of free or directed interesterification on the characteristics physicochemical of the final fluid fraction sought O
It is indeed found, that after interesterification ~
S the unsaturation of the fluid increases at the same time as the trouble point and improves the de-icing test which becomes comparable to peanut oil In this Table ~ it is remarkable to note that only the fluid of Example 6, obtained SanS interesterification prior, is not satisfactory as to its characteristics The fluids obtained in Examples 1 to 5 above above are comparable to peanut oil So that the fluid fraction can be compared to peanut oil in terms of its freezability / defreability ~ it is necessary that it conforms to the following specifications:
s = saturated SSS ~ ~ l7%
O = oleic acid S ~ O 6 lo%
PFT e 12 ~ C
~ It is necessary ~ moreover, that the defigage test such as defined below is equivalent to that of peanut oil ~
as shown in Table IV below:
T ~ BLEAU IV
SSS S20PFT Defigage Storage + 2 months % '~ / 0 ~ C a ~ 15 ~ C
Interesterification free 0.4 S, l 8 good li ~ pide Interesterification directed 0.1 10 15 baddep8t 30 final fluid Example 2 1 hour 0 ~ 3 4 10 good clear 6 hours 0 ~ 1 3-r 511 good clear We determine the characteristics of freezing and defrosting of the fluid fractions in accordance with the present invention, by measuring their cloud point as indicated above, as well as their stability at 15 ~ Co The freezing test /
de ~ igeage is to cool the oil a night to 0 ~ C ~ and observe the clearing time of the replaced oil at ~ 15 ~ Co Le clearing time is taken when the oil is perfectly clear ~ .'2 ~ 7 ~

and is compared to the peanut oil challenge time cooled under the same conditions as the fluid conforming to the invention ~
Table V below gives the chroma composition topographic of fluid fractions ~ types obtained in accordance with the present inventiong compared to that of oils comes =
commercial targets.
~ 3t7 ~ 7 _ I
he .,.
., ",. I
~ ,, ~, . ,, ~ I
r ~ U ~
a) ~ 1 ~ ~ ~ ca o II
h O
a), J ~ I
/ DI
I
~ ua) i ., ~, _ I
h ~ 'i I
~ i ~ q O ~ I
h ~ ~ :: ~ E ~ '' D ~ ~ I ~ oo ~ ~.
U h ~ XI ~ ~ 9 ~~ 1 ' i ~ .... ~
., ~ ~ I
h ~ I
~ a) I
u, oa) a ~ ~ I
a ~
~ u ~ .CXI, ~ o ~ r 'oo ~ m ~ rl rl (UI 1-- ~ ll ') ~ --1 ~ ~ 1 ~
~ 2 0 ~ ~. . ~.
E ~;> ~ ~ i ~ O, - ~ O ~ ~ '7 ~ ~
~ O. ~ ~ ~. OI, O
, ~ ~., ~ ~ I1 '~ ~ 1 U ~ O 0- O ~ r ~
, ~ O ~: OI ~ 1 ~ I
;> ~: r4 ~ n ~ ~~
~ ~ IO ~ ~ U ~ O ~ d ~
~ rl OP ~ ~ 0 ~ I
~ ~~ I
a), ~
rl ~ U ~
~ ~ aha) Io . ~) -I ~ j ~ ri S ~ C ~ S r ~ ¦ r ~
~ _ I 'X
X ~
. ~ ~ 0 . ~ O
. c ~ U v) '~ l u ~ co co c ~ O o u ~ ~ H
771 ~

We proceed according to the diagram of Figure 30 100 kg of refined palm oil with an iodine index of 51, fully melted at a temperature of 50 ~ C ~ are mixed with 700 kg of trichlorotrifluoroethaneO
The mixture, cooled at the speed of OD 1 ~ C / minute up to -10 ~ C ~ is maintained at this temperature for 2 hours ~
after which, it is vacuum-filtered on polyamide canvas of porosity ~ 20 _ ~ lA The filter cake is washed ~ with twice 50 kg of soil ~
selling fresh ~
The intermediate concrete fraction (cfo figure 3 is subject to further fractionation after adjustment of the dilution with 1 part of oil for 7 parts of solvent by weight ~ to ~ 10 ~ C. ~ close filtration ~ rin ~ ages and elimination of the solvent by distillation, the raw material is recovered which comprises two distinct concrete fractions, namely: a concrete fraction Cl, obtained with a yield of ll% which is essentially consisting of saturated triglycerides (SSS) with diiodes index 7, and a concrete fraction C2 ~ obtained with a yield obtained 35% which is mainly made up of oleopalmitin symmetrical and whose iodine index is 390 After removal of the solvent ~ the fluid fraction intermediate (see figure 3) is randomly interesterified during one hour at 80 ~ C! using 0 ~ 2% sodium methoxide as catalystO
After destruction of the catalyst with 3% water ~
centrifugation and washing of the oil, the oil is dried at 90 ~ C under empty and is ready for splitting.
This one. is produced under the same conditions as the first fractionation, except for the temperature of : fractionation which is -20 ~ C ~ ~ close rinsing ~ the fraction fluid F3 and the concrete part C3 obtained are cleared solvent, weighed and studied - from the point of view of chemical composition and physical characteristics, together with the other two previously obtained fractions.
,; ~. ~, ~~~ 3 ~ 77 ~
TABLE VI
fractions: Iodine value: Yield compared to :: whole palm oil ~ _ _ _ _ _ _ _ _ _ _ _ _ ._ _ _ _ _ _ _ _ _ ._ _ _ _. _, _ _ _ _ _ _ ~ _ _ _ _ ._ _._ _ _ _ _ ... _ _ _ _ _ .. _ ... =. ... ~. ._ _ _ _ _ _ _ Intermediate fluid: 68: 54%
Intermediate concrete 31 46 ~ / 0 _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ ._ _ ._ _ _ _ _ _ _ _ _ ._ _ _ _ ._ _ _ _ ~ _ _. . ._ .. _ _ _ ._. . . ~ _ ~ ~. ~ _ ._ ._ _ _ Fluid F3: 83: 36%
10 C3 (SII / SSI) 37 1 ~%
C2 (POP): 39: 35%
Cl (SSS) 11%
~ _ _ _ _ _ _ t We proceed according to the diagram in Figure 30 1 kg of refined palm oil with an iodine index of 51 to 50 ~ C is mixed with 7 kg of trichlorotrifluoroethane which is the temperature of -20 ~ Co The resulting mixture is at the temperature from 0 ~ C approx. This procedure makes it possible to reduce maple cooling time O The rest of the operation is identical to Example 7 ~ except for the temperature of the first fractionation which is -5 ~ Co The following fractions are obtained:
TABLE ~ U VII
- --_.-___.__._.__ ~ _ ~ _.___ .. _._ .. _ ~ _. ~ .__.___.__ Fractions: Indicate iodine: Yield compared to.
:: whole palm oil _ _ ~ _ _ _ _. ~ _ ~ _ _ ~ _ _ ._ _ _ .. _ ~. _. ~ ._ ._ ~ _ _ _ ._ _. _. ._ _ _ _ ._ _. _ ._ ._ _ _ _ .. ~. _ ._ ~ .. _ .. _ ._ .. _. ~, _ _ _ _ _ _ ~ intermediate intermediate: 65: 60%
30 Intermediate concrete 31 ~ 40%
. _ _ _ _ _ _ _ ~ _ _ _ ._ _ _ _. _. ._ ._ _ _ _ _ _ ._ ._ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _,. . _ ~ .. _ _ _ ~ ... ._ ._ _ _ __ _ _ _ ._ Fluid F3: 84: 23%
C3 (SII / SSI) ~ 36 37%
_ _. _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ ~ _ _ ._ _ _ _ _ _ _ _ _ _ _ _ _ ~. _ _ _ _ ._ _ _ _ _ _ _ _. _. ._ _ ._ ._ _ _._ ._ _ _ _ _ 35 C2 (POP): 40: 2 ~%
Cl (SSS) 9 12%
_ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ ._. ~ _ _ _ ._ _ _ _ _ _ ._ _ _ _ _ _ _ _ _ _ _ _. _ _ _ _ _ _ _ _ _ ._ ._ ._ _ _ _ _ _ _ _ _ E ~ EMPLE 9 We proceed according to the diagram in FIG. 3.
40 hexane is used in place of trichlorotrifluoro-.-. ~.,.:
~ 2 ~
ethane ~ Oil dilution ratios and temperatures are for the first split. 1/4 (volO 'oil for volO
- hexane) and ~ 15 ~ C, for the second fractionation. 1/4 and = 20 ~ C;
for the third fractionation: 1/4 and ~ 10 ~ Co The fractions palm oil obtained have the characteristics mentioned in Table VIII belowO L, the other operations remain identical to those of Example 7 ~
TABLE VIII
Fractions: Iodine Index: Yield vs.
. whole palm oil :
Intermediate fluid: 68: 56%
Intermediate concrete - 30 ~ 44, ~ iO
_ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ ~ ~ _ ~ ~ ~ ~ ~ ~ ~ ~ _ _ ~ ~. ~ _ ~ _ ~. ... ~. ~. ~ .. ~ ~ ... ,,. .. ~. ~ .. _. ~ .. ~
::
Fluid F3: 84: 3 ~%
C3 (SSI / SII) '36' 18%
_ _ _ _. _ ._ _ ._ _ _ _ _ _ _ _ _ _ _ _ _ _ _. _ ._ ._ .. O_ ~ ._ ~ .. _ _. ~ ~ _ _ _ ~ .0 ... . _ _ _. . ~ .. ..... ~ .. ~ .. ._. ~ .. ~. . _.
. _ O ... ~ ._ C2 (POP) 38 3 ~%
20 Cl (SSS) not measured 10%
~ _ _ _ _ _ _ _ _ ._ _ _ _ ~ _ ~ _ _ _ ~ _ ~ ~ ._ _ ._ _ _ _ _ _ _ ~. ~. ~ _ _. ~ ~ ~ = _ _ ~ ~ _ ~. . _ ._ ._. ~. . . ~ ~. ~ ~. . , ~. ~. ~. _ _ 95% isopropanol is used for the first fractionation ~ in a 1/3 dilution ratio (vol ~ / vol !. The concrete intermediate fraction obtained has a glycerol composition ~
different from the concrete obtained with the use of solvents apolar previous ~ The content of partial glycerides (diglyceri-des in particular) is lower ~ (see Table IX below ~ below) ~
TABLE IX
Scheme 3: Diylycerides 1-2: Diglycerides 1 ~ 3 % O%
concrete intermediate obtained with solvent 107 ~ 4 ~ 4 apolar (hexane) concrete intermediate obtained with solvent polar (isopropanol). ~ 1 ~ 0 '~ 300 _ _ _ _ _ _ ._ _ _ _ _ _ _ _ _. ~. ~ ~ _ ~ _ _ _ _ _ _ _,. . ~ _ ._. ~ ._ ~ ._. =. ~. . _ _ _. ~. ~. ~ _ .. ~ ._. ~ ~. . ~.,. ~ ~ ~. . ~ ..,. , =,. . ~,. ~ ~ ~
The fluid fraction F1 is interesterified after complete elimination of alcohol and undergoes operations of 6 interes ~
771 ~
same and second fractionation identical to those described in Examples 7 and 9 ~
Table X below gives the acid composition stearic, palmitic ~ oleic and linoleic from fluid fraction F3 obtained in accordance with Examples 7 and 90 PAINTINGS

Example 7 Example 9 ~ 16 l9 ~ 6 l9 ~ 7 o 3: 2 ~ 4 Cl8- ~ 51 ~ 8 ~ 51 ~ 5 Cl ~ ==. 21.5: 22 ~ 5 Iodine index. 83 84 Performance versus:
to palm palm departure: 36%: 38%
The content of reducing tocopherols (antioxidants active) of the fluid fraction F3 obtained in accordance with the Example 9 was assayed by colorimetry using the bathophenan method throline which is based on the oxidation of tocopherols by the ferric chloride in alcoholic solution O on the subsequent formation quente of the Fe ~ / bathophenanthroline ~ complex and measures it at 532m of the specific extinction of the colored complex formedO
This assay gave the following results:
Fraction F3: before deodorization: 75 mg / 100 g of oil after deodorization: 40 my / lOO g of oil * unit: tocopherols expressed in mg of ~ -tocopherol for 100 g of oil.

! _ We proceed according to the diagram of Figure 2 0 l kg of palm oil is crystallized at 0 ~ C in phase solvent consisting of 7 kg of trichlorotrifluoroethane ~ ratio 1/7) for 2 hours.
Separated by filtratlon on polyamide canvas of ., porosity 20 ~ a concrete fraction Cl SSS of Iodine number 7 ~
usable in lipochemistry ~ of a fluid fraction E'l of index dtIode 54. 3 ~
'7 ~
The latter is split with 7 times its weight of trichlorotrifluoroethane at -15 ~ C for 4 hours, at end of which one separates ~ by filtration on polyamide canvas 20 a concrete fraction C2 POP of Iodine index 43 ~, usable as cocoa butter substitute base O and a fluid fraction F2 of Iodine 737 index which is randomly interesterified during a hour at 80 ~ C ~ in the presence of 0 ~ 3 ~ / 'of sodium methyl.a-te ,.
At the end of this time ~ the interesterification is arxêtée by destruction of the catalyst by introduction of 3%
glacial acetic acidO and the interesterified fluid fraction is fractionated in solvent phase in 7 times its weight of $ richloro-~ trifluoroethane7 for 2 hours at -20 ~ C.
A concrete fraction C3 is filtered off constituted by mixed triglycerides of Iodine index 33 ~ useful sand in particular in margarinerieD and a ~ fluid reaction F3 of indiced'Iodine 85 ~ whose tocopherol content is 79 mg / 100 g before deodorization and 64 mg / 100 g after deodorization The yields obtained in this example. ~ Are the following:
TABLE XI
Fraction Yield over total palm oil Cl 10%
C2 ~ 2%
C3 12%
36%
_ ._ _ _ _ _ _ _ _ _ _ _ ._ ._ .. _ _ ~ _ _ _ _ ._ _ ._ _. ~. _ _ ._ _ .. _ ._ ._ _ ._ ~ ~ _ _ _ _ _ .. _ ._ ._. ~ .. _. _ _ ...... _. _. _. _ The freezing and freezing characteristics of the fluid fraction F3 obtained in accordance with this Example 11, and of: The ~ fluid reaction F3 obtained in accordance with Example 7 ~
have been determined by measuring the cloud end point and the stability at + 15 ~ C. Trouble end point ~ P ~ FT,) is measured as follows: a fat sample (approximately 50 ml) is placed in a test tube in which a thermometer is immersed precision, and. surrounded by a dust jacket; the sample is cooled one night at -20 ~ C; it is then placed in a tank containing a water bath thermostatically controlled at a temperature chosen in a ~ 4 ~, range between +25 and ~ 40 ~ C; as soon as the oil became limpidc, we read with a precision thermometer "the temperature at 3 ~
v ~
which the latter has become limpid, this temperature being called "end of trouble point".
The freezing / challenge test. ~ Eage consists of re ~ stiffening oil a night at 0 ~ C and observe the time of ~ igea ~ e oil returns to + 15 ~ C. The clearing time is taken when the oil is perfectly clear, and is compared to the time of defragrage of the peanut oil re ~ stiffness in the same condi ~
tions that the fluid according to the invention.
The results obtained are given in the Table XII below, by comparison with the results obtained with the oil peanut:
TABLE XII
-Peanut Fluid F3 Fluid F3 Example 7 Example 11 _ ~:
PoF.T. _ 8 ~ C 9 ~ C
_ _, ~.
Stability Defigeage com- Defigeage com- Complete defigeage a + 15 ~ C plet - rest plet at ~ 15 ~ C - a - ~ 15 ~ C - rest limpid to this- remains limpid limpid to this te -temperature at this temperature erasure _ _ ~
II 93.3 83 85 It follows from the foregoing description that, what that soi.ent the modes of implementation ~ re, realization and ap-pl: ication adopted ~ one obt: Slow a process for the production of several ~ edible reactions from natural fatty substances, which presents in relation to ~ procedures aimed at the same goal ante-laughingly known ~ important advantages some of which have was mentioned in the above, and of which other advantages will emerge from the use of said process.
As is apparent from this ~ ui precede, the inven-tion is in no way limited to those of its methods of implementation work, realization and application which have just been '78 described more exp ~ icite; on the contrary, she embraces all the variations that can come to mind of the technician in the ma ~ iere, without departing from the frame, nor the por-tee, the present invention.
- 35a -''

Claims (43)

The embodiments of the invention, about which an exclusive right of property or privilege is claimed, are defined as follows: 1. Process for the treatment of edible fatty substances for the production of one or more edible fractions, one of these fractions being constituted by an edible oil wheat with a high content of unsaturated fatty acids, process characterized in that for obtaining the oil edible, an interesterification reaction of the oil or fraction of oil to be treated or a fraction intermediate fluid which has already been subjected to a treatment beforehand, in the presence of an interesterification catalyst suitable, at a temperature between 20 and 80 ° C, the interesterification reaction being followed by at least one fractionation using fractionation solvents greases suitable for temperatures between -20 and + 35 ° C, to obtain a fluid fraction with a higher iodine index 75, containing mainly unsaturated triglycerides having a triinsaturated triglyceride content> 20% without of trans isomers, and having the properties of oils edible. 2. Method according to claim 1, characterized in what said dietary fats are chosen from in the group consisting of palm oil or a fraction palm oil with a saturated / unsaturated ratio between about 0.3 and about 1.2. 3. Method according to claim 1, characterized in that two or more edible fractions are pro-picks and that one of these fractions is constituted by a edible oil with a high content of fatty acids unsaturated, and that another of these fractions is made up by a concrete fraction usable as a substitute for cocoa butter. 4. Method according to claim 1, characterized in that the interesterification reaction is preceded by at minus a fractionation using fractionating solvents appropriate fats. 5. Method according to claim 1 or 4, characterized in that after said fat fractionation step, the resulting fluid fraction has an iodine index greater than 80. 6. Method according to claim 1, characterized in that said fluid fraction of iodine index greater than 75 presents the properties of edible oils chosen from the group including peanut oil and olive oil. 7. Method according to claim 1, characterized in that one performs the interesterification on the oil or the fraction of oil to be treated, and in that we submit the fat interesterified to at least one fractionation, so as to obtain a fluid fraction whose end point cloudiness is less than 12 ° C and has a content of trisaturated triglycerides less than 0.6%, a content of monounsaturated disaturated triglycerides less than 10%, one de-icing test similar to that of peanut oil, and whose concentration in tocopherols is enriched compared the tocopherol content of the palm oil used, while maintaining the favorable tocopherol / fatty acid ratio polyunsaturated from the latter. 8. Method according to claim 7, characterized in that the fractionation step comprises at least two successive fractionation operations, i.e. a first fractionation of the interesterified fat, using an appropriate fat fractionating solvent, followed a second fractionation of the fluid fraction obtained at the outcome of the first fractionation in a fractionation solvent appropriate fat, to obtain a fluid fraction comes-target essentially constituted by unsaturated triglycerides which is recovered by separation of the concrete fraction also-obtained. 9. Method according to claim 8, characterized in what for the first fractionation of the fat interesterified, said appropriate fat fractionating solvent is chosen from the group constituted by trichlorotrifluoro-ethane, hexane, isopropanol and acetone, present in a oil / solvent weight ratio between 1 / 0.5 and 1/7, for a period of between 2 and 4 hours and at temperatures erasures between 0 and + 35 ° C. 10. Method according to claim 8, characterized in that for the second fractionation of the fluid fraction obtained after the first fractionation, said solvent appropriate fractionation is selected from the group comprising trichlorotrifluoroethane and hexane, present in a oil / solvent weight ratio between 1/2 and 1/7, for a period of between 2 and 4 hours and at temperatures erasures between -10 and -20 ° C. 11. Method according to claim 8, characterized in that the concrete fraction obtained at the second outcome fractionation is recycled at the head of the process in the material fatty to be treated, to be interesterified jointly with the latter. 12. Method according to claim 1, characterized in that the oil or the fraction of oil to be treated is subjected at least one fractionation step using solvents of fractionation of the appropriate fats present in a proportion of 0.5 to 7 times the weight of the oil, at temperatures erasures between + 35 ° C and -20 ° C, to obtain a frac-concrete tion and an intermediate fluid fraction that we submit to the interesterification reaction followed by additional fractionation steps of the fluid fraction interesterified intermediary, these main stages of treatment which can be associated with fractionation stages complementary to concrete fractions, these stages of additional fractionation using a solvent of proper fat splitting, to get four fractions with edible fat properties, chosen from the group constituted by the fluid fraction containing essentially unsaturated triglycerides, the concrete fraction iodine value between 31 and 43, containing essential-2-oleo-1,3 dipalmitine, usable as a base cocoa butter substitute, the concrete index fraction iodine between 33 and 43, containing triglycerides mixed, usable in different industry sectors food, and the concrete fraction of lower iodine index to 20, containing mainly saturated triglycerides having the character of a usable food product. 13. Method according to claim 12, characterized in that said concrete fraction of iodine value between 33 and 43, containing mixed triglycerides can be used in margarinerie. 14. Method according to claim 12, characterized in that said concrete fraction of index less than 20 can be used in lipochemistry or in different sectors of the food industry. 15. Method according to claim 12, characterized in that a first fractionation step is carried out at a temperature between 0 and + 35 ° C for ratios oil / solvent between 1 / 0.5 and 1/7, to give a concrete fraction essentially constituted by trigly-saturated cerides with an iodine index of less than 20, retaining the character of food products, usable in different food industry and lipochemistry sectors, and a intermediate fluid fraction which is subjected to a new fractionation treatment at a temperature between +15 and -20 ° C in 2 to 7 times its weight of fraction solvent-to lead to a concrete fraction essentially consisting of 2-oleo-1,3-dipalmitine usable as as a cocoa butter substitute base and at a fraction intermediate fluid which is subject to interesterification in the presence of an appropriate catalyst, at a temperature of around 20 to 80 ° C, for a time between 0:30 hour and approximately 6 hours, followed by further fractionation in a fractionation solvent to collect a fraction crete essentially consisting of mixed triglycerides, iodine value between 33 and 43, usable in different sectors of the food industry and a fraction fluid essentially constituted by triglycerides unsaturated with a triinsaturated triglyceride content> 20%, iodine index greater than 80, having the properties edible oils. 16. Method according to claim 15, characterized in that the fractionation of said intermediate fluid which previously subjected to an interesterification in the presence of a suitable catalyst, at a temperature of 20 to 80 ° C for between 0:30 and 6 hours, takes place in a fractionation solvent chosen from the group consisting of trichlorotrifluoroethane and hexane, rightly present up to 7 times the weight of said interesterified fluid fraction to be treated, at a temperature of up to -20 ° C. 17. Method according to claim 12, characterized in that the first step of fractionation of the oil to be treated at a temperature between + 20 ° C and -20 ° C depending on whether the weight of the fractionating solvent varies from 1 to 7 times the weight of the oil to be treated, to give rise to on the one hand to a concrete fraction which is subject to a new fractionation in a solvent medium which makes it possible to recover a concrete fraction essentially comprising triglycerides saturated, iodine value less than 20, retaining the character-type of food, usable in different food industry and lipochemistry sectors, and a second contrite fraction essentially consisting of 2-oleo-1,3-dipalmitine, usable as a base for cocoa butter substitute, and secondly to a fraction intermediate fluid which is subjected to an interes-verification at a temperature of the order of 20 to 80 ° C, in presence of an appropriate interesterification catalyst, the result of which a concrete fraction is obtained comprising mainly mixed triglycerides, of iodine index for before reaching 43, usable in different sectors of the food industry and a fluid fraction of iodine index greater than 80, which has properties similar to oils edible. 18. Method according to claim 12, characterized in that the fractionation solvent (s) used are chosen from the group consisting of trichlorotri-fluoroethane, hexane, isopropanol and acetone. 19. Process according to claim 18, characterized in that for the stages of obtaining the fluid fraction iodine index greater than 80, the solvent (s) of frac-implemented are chosen from the group made up with trichlorotrifluoroethane and hexane. 20. Method according to claim 12, characterized in that the different process fractionation steps are carried out using one or more solvents fractionation, used separately or in mixtures. 21. Method according to claim 12, characterized in that the fractionation operations are carried out in using quantities of solvent which represent 0.5 to 7 times the weight of the oil or fraction treated, the fractionation temperature being between + 35 ° C and -20 ° C, depending on the proportion of solvent relative to the oil or treated fraction used for the fraction-and the type of solvent used. 22. Method according to claim 1, characterized in that interterterification is interesterification free, carried out in the oil phase, at a temperature included between 60 and 80 ° C approximately, for 30 to 60 minutes, in the presence of an appropriate interesterification catalyst. 23. Method according to claim 1, characterized in that interesterification is interesterification directed, carried out in oil phase, at a temperature of the order from 20 to 40 ° C approximately, for 1 to 24 hours in the presence of a suitable interesterification catalyst. 24. Method according to claim 23, characterized in that said directed interesterification is carried out for 1 to 3 hours. 25. The method of claim 1, characterized in that interesterification is interesterification directed, performed in solvent phase, at a temperature between 20 and 40 ° C approximately, for 1 to 24 hours, in the presence of an appropriate interesterification catalyst. 26. Method according to claim 25, characterized in that said directed interesterification is carried out for 1 to 3 hours. 27. Method according to claim 25, characterized in that directed interesterification is carried out in a solvent taken from the group constituted by hydrocarbons halogenated or not. 28. The method of claim 27, characterized in that said halogenated or non-halogenated hydrocarbons are chosen in the group consisting of trichlorotrifluoroethane and hexane. 29. Method according to claim 25 or 27, characterized in that the solvent is used in a fat / solvent weight ratio between 1 / 0.05 and 1 / 0.4. 30. Method according to claim 1, characterized in that the interesterification catalyst is chosen in the group consisting of alkali alcoholates, the catalyst being present in an amount of 0.1 to 0.4% by weight relative to the weight of the product to be treated. 31. Method according to claim 30, characterized in that the interesterification catalyst is chosen in the group consisting of sodium methylate, sodium metallic and sodium-potassium alloys. 32. Method according to claim 1 or 7, character-laughed at in that the fractionation step is carried out in one single operation using a solvent taken from the group consisting of trichlorotrifluoroethane and hexane, at temperatures between -20 ° C and -10 ° C, the ratio by weight of fat / solvent being between 1/2 and 1/7. 33. Fluid fraction obtained by implementing the method according to claim 1, characterized in that it consists essentially of unsaturated triglycerides having a triinsaturated triglyceride content> 20% index iodine equal to or greater than 75, in that it is devoid of of trans isomers, and in that it conforms to the specifica-following:
cloud end point: below 12 ° C
trosaturated triglyceride content: less than 0.6%
disaturated-monounsaturated triglyceride content: less than 10%
de-icing test: equivalent to that of peanut oil, tocopherol content: of the order of 0.038% by weight, tocopherol ratio expressed in mg per 100 g of material fatty / polyunsaturated fatty acids%: greater than 0.6. 34. Fluid fraction according to claim 33, characterized in that said unsaturated triglycerides having a content of triinsaturated triglycerides> 20% have an index iodine greater than 80%. 35. Fractions of fatty substances obtained by putting implementing the method according to claim 1, characterized in that they are chosen from the group comprising the fluid fraction of iodine index greater than 80, containing essentially unsaturated triglycerides having a content > triinsaturated triglycerides> 20% without trans isomers and exhibiting the properties of edible oils; the frac-concrete iodine value between 31 and 43, containing essentially 2-oleo-1,3-dipalmitine, usable in as a substitute base for cocoa butter; fraction iodine value concrete between 33 and 43, containing mixed triglycerides, usable in different areas of the food industry; and the concrete index fraction iodine less than 20, containing mainly triglycerides saturated wrinkles, presenting the character of a food product and usable in different sectors of the food industry keep quiet and in lipochemistry. 36. Fractions of fatty substances according to claim 35, characterized in that said properties of oils edible are those of peanut oil or olive oil. 37. Fat fraction according to claim 35, characterized in that said concrete fraction of index iodine between 33 and 43, containing triglycerides mixed can be used in margarine. 38. Fractions according to claim 35, character-ridiculous in that they are obtained with yields which are around 30 to 70% for the fluid fraction, comparable with edible natural fluid oils, from 10 to 45% approximately for the concrete POP fraction usable as a base of cocoa butter substitute, about 10 to 30% for the SSI / SII concrete fraction usable in different sectors of the food industry, and from 1 to 15% approximately for the concrete SUS fraction usable in different sectors of food industry and lipochemistry. 39. Fractions according to claim 38, characterized in that said concrete SSI / SII fraction is usable in margarinerie. 40. Fluid fraction according to claim 35 or 38, characterized in that it is devoid of trans isomers, in that it has an iodine value greater than 80, a content in tocopherols greater than 30 mg / 100 g of the fluid fraction, a cloud end point below 12 ° C, an SSS content less than 0.6%, an SSI content less than 10%, and a defogging test similar to that of peanut oil. 41. Concrete fraction according to claim 35 or 38, characterized in that it contains predominantly symmetrical oleodipalmitin (POP) in that it has a iodine value between 31 and 43, and in that it is usable as a substitute base for cocoa butter. 42. Concrete fraction according to claim 35 or 38, characterized in that it is essentially constituted by mixed SSI / SII triglycerides with iodine value included between 33 and 43, and in that it can be used in different food industry sectors. 43. Concrete fraction according to claim 35 or 33, characterized in that it is essentially constituted by SSS saturated triglycerides with an iodine value of less than 20 and in that it is usable in different sectors of food industry and lipochemistry.