EDIBLE FATS

Abstract: Hardstock fat for margarine and like emulsion food products is prepared by enzyme rearrangement of a mixture of fatty reactants distinguished from one another by fatty acids of different chain length, and if necessary including hydrogenation and fractionation steps. In particular a mix­ ture may consist of palmitic and lauric fats or their consti­ tuent acids, and also very short chain saturated fatty acids to provide asymmetric glycerides for improving margarine quality.

Description: EDIBLE FATS This invention relates to edible fats particularly for use in emulsion food spreads such as margarine. Margarine and other emulsion food spreads, and also fat blends such as are used in shortenings, are customarily composed of a base stock, often of a liquid or at any rate very soft consistency at ambient temperature, eg, 18 C, and a hardstock fat, the two being blended together in judicious proportions to give the best possible consistency requirements for packing, handling and consumption. In particular, the base stock may be selected for dietary purposes from oils, particularly of vegetable origin, which are rich in polyunsaturated fatty acid glycerides. By contrast, the triglycerides of hard stock fat is composed of substantial amounts of saturated fatty acids, generally of C18 fatty acid triglycerides, an important exception to this generally being hardstock derived from palm oil, almost half the fatty acid residues of which are composed of palmitic acid. Hardstock fats may also contain a proportion of the so-called lauric fats, containing 50% or more of the shorter-chain range of saturated fatty acids Cl0 - C14, and a relatively low degree of unsaturation particularly coconut and palm kernel oils. Most other vegetable oils from which hardstock fats are prepared are normally liquid and are hydrogenated and/or fractionated for this purpose. When saturated they yield substantial amounts of tristearin, i.e. tristearoyl triglyceride of other fatty acids. Hardstock fats may also be prepared from animal sources of fats. They usually exhibit solids content of at least 20 at 200C measured by MNR methods; somewhat harder examples show a dilatation at 200C of at least 500. In addition to fractionation and hydrogenation edible fats and oils may be modified by interesterification, a process in which fats and oil are composed, are rearranged to provide in effect a different melting characteristics, and often also different polymorphism often having quite profound effects on the organoleptic response to the fat and products on which it is based. The present invention provides an improved process for the production of interesterified fats suitable for use in emulsion and other fat-based food products such as margarine. It provides a process for the production of improved fat suitable for use in margarine and like foodspreads wherein a mixture of fat or glyceride oil preferably vegetable with a fatty reactant comprising a fatty acid residue is interesterified in the presence of an active enzyme lipase interesterification catalyst under conditions of water activity in which the catalyst remains active consistent with minimum hydrolysis until the fat mixture is substantially interesterified and removing the catalyst to provide a hardstock fat preferably having a dilatation of at least 500 at 200C, the product or reactant glycerides being hardened or fractionated if necessary. Enzyme interesterification of fats is disclosed in our patent Cases-A.171 and A.189. The process may be carried out in a water-immiscible solvent such as hexane or in liquid phrase withop$ a solvent. The process may be operated batch-wise or continuously. Preferably the solvent comprises an aliphatic liquid boiling at not more than about 1000C, particularly saturated paraffins such as hexane, or other water-immiscible solvents. The interesterification may also be carried out under pressure using solvents normally boiling at ambient conditions. In the process of the present invention interesterification and fractionation steps may be carried out in organic solvent in which the fat, enzyme, water to activate the enzyme, and enzyme dispersant material are distributed and from which pre-selected glycerides are fractionated. The solvent must be substantially water immiscible in the interesterification reaction. The temperature of the interesterification reaction should be maintained at limits between which the catalyst remains active, preferably from 200 to 800 C, more particularly from 400C to 700C. Lower temperatures than this may nevertheless be suitable and enable fractionation by crystallisation to be performed in situ with the reaction, for example at 50 to 200C, for the purpose of directing fat cbmpositions in an interesterification introducing high yields of pre-determined glycerides. The enzyme catalyst is preferably used in conjunction with a dispersant or support for example, an inorganic particulate material which is inert to the reaction, such as kieselguhr, eg, Celite, or a synthetic resin. The catalyst may be prepared on a Celite or similarly inert support in accordance with the description given in our British patent specification no. 1,577,933. Enzyme catalysts are preferably activated for use in the process of the invention, by contact with water. The activated catalyst is then maintained in an active condition by controlling the removal of water from it during the reaction. In accordance with the process described in our patent application A. 194 the water activity of the system in which the catalyst operates is maintained between predetermined limits according to the requirements of the catalyst, to maintain the activity, consistent with the desirability of inhibiting hydrolysis. The process of interesterification may be batchwise or continuous; in the latter event the reactants in liquid phase may be conducted in a continuous stream over a fixed bed of the catalyst. The water activity of the system may then be controlled by careful control of the water content of the stream, according to the extent to which water is miscible in it. Solvents must be selected for this reason from among organic liquids in which water is only slightly miscible, preferably below 1% and more preferably below 0.1%. The feedstock ie, reactants and any solvent may be saturated with water and combined with dry feedstock before use, to provide a stream containing the predetermined amount of water, or the temperature of the saturated stream can be adjusted to give the required water activity. Alternatively, the water content of the feedstock can be controlled by passage through a bed of silica-gel or similar hydrated to a predetermined extent. Preferably the water activity of the feedstock is maintained at 0.4 to 0.85. Other values may be pre-selected in accordance with the characteristics of the catalyst, the period of the interesterification reaction and the degree of hydrolysis that can be tolerated. Enzymes may be used as interesterification catalysts in the process of the invention which are derived from microbial, vegetable or animal sources. Candida cylindracae lipase is non-specific and provides a true randomisation of all fatty acid radicals on all the glyceride positions. Porcine pancreatic lipase, A. niger and Rhizopus enzymes, eg, R. arrhizus and R. japonicus lipases are all specific to the 1,3 terminal acid radicals, giving very little change in any-2-position acid radicals, as are Mucor javanicus, Mucor miehei and Thermomyces lipases. The amount of catalyst present may vary from 0.5 to 10%, but amounts outside these limits may also be used. The catalyst is preferably activated with water before use in the reaction. The catalyst is also preferably used in conjunction with a dispersant for example, an inorganic particulate material which is inert to the reation, such as kieselguhr, eg, Celite or a synthetic resin. The catalyst may be prepared on a Celite support in accordance with the description given in our British patent specification no. 1,577,933. It is preferable activated by contact with water, before participation in the reaction. The catalyst may be random in its effect, catalysing the exchange on all three positions of the glycerides present. Preferably however, the catalyst is selectively reactive in the 1- and 3-positions, eg, Aspergillus niger lipase. The effect of a catalyst which is active selectively according to the positions on the glyceride structure is to limit the number of glyceride species present in the rearranged product, providing important improvements in the fractionation of the product which may then more readily yield fractions more nearly optimal for particular requirements. The number of rearranged glyceride species present'in substantial amount may be further reduced under the influence of positionally selective catalysts, by the use as the fatty reactant of a single fatty acid or its glyceride. Reaction of RHH with an acid M using a 1,3-selective catalyst will produce the glycerides FEH and MHM only, which are more less readily separable from one another and from HH by conventional fractional crystallisation. The invention therefore provides a process comprising the steps of hydrogenating and interesterifying in either order, a mixture of a fat or glyceride oil with a fatty acid reactant in which as interesterification catalyst a 1,3 selective enzyme is used and in which if desired the rearranged product fat is fractionated particularly to recover a mid-fraction. The process of the invention may be applied to vegetable, animal and marine oil, es. sunfldwer,- soya palm groundnut, cottonseed and olive oils, and the so-called lauric fats eg, coconut and palm kernel oils in which substantial amounts of lauric acid residues are present. The fatty reactant may comprise an ester of a mono-hydroxylic or polyhydroxylic alcohol , especially a glyceride, eg, the above fats and their fatty acids. Fatty acids and the fatty acid residues of esters with which the glycerides of C16/Cl8 fats or glyceride oils may be rearranged in accordance with the invention may contain from 3-14 carbon atoms or 20 carbon atoms upwards. A hydrogenation step which may be performed before or after the rearrangement, may be necessary to provide an adequate degree of hardness in the product fat, which may then be fractionated as a further refinement. Highly saturated fat may be less easily reacted in the liquid phase and the hydrogenation step is therefore preferably after the enzyme reaction. In general the arrangement reactants usually include at least on comprising saturated fatty acid residues in the form of a free fatty acid or ester, including glycerides. An important aspect of rearrangement of ;hardstock fats in accordance with the invention is the modification of palm oil. This oil contains substantial amounts of palmitic acid in glycerides and exhibits very slow crystallisation rates, with the result that post-crystallisation develops during storage in margarine containing palm oil and its derivatives, leading to an undesirable condition known as graininess. This condition may be modified by rearrangement with lauric fats or C12/C14 fatty acids, in accordance with the present invention. By means of the invention, hardstock fats can be obtained containing from 40-75% of glycerides of carbon number 46-48, giving superior melting profiles to margarine in which they are included in amounts as little as 8-158 in blends with high PUFA vegetable oils. Another important feature of the present invention is the provision of the process for the preparation of asymmetric glycerides MHH in which H = C16/C18 preferably saturated fatty acid residue of much shorter chain length less than 8 carbon atoms and preferably from 2 to 6, particularly C4. These triglycerides may be used as components in margarines and emulsion food spreads to provide textural and/or melting characteristics to food spreads akin to butter. Highly unsaturated marine oil is hydrogenated to confer flavour stability for edible purposes and the resulting increase in melting characteristics may be improved by interesterification of the hardened oil or blends with other fats, in accordance with the invention to provide margarine hardstock fats. The grainy texture observed on storing fat mixtures containing high levels of lard, may be eliminated by interesterification in accordance with the invention to provide compositions with improved plastic range which are suitable for use in shortening and as margarine fats. Blends of palm oil with lauric fats or their hardened derivatives may be improved by interesterification in accordance with the invention, for example equal parts of hardened palm oil and hardened palm kernel oil. An effective hardstock for margarine may also be obtained by interesterification of soya bean oil and hardened lauric fat eg. hardened coconut oil. This interesterified product may be blended as a hardstock, with as much as 80% highly unsaturated oil, giving a good margarine fat with essential fatty acid content and a low trans content. Similarly a blend of hardened lauric fat and liquid oils containing longer chain fatty acids eg. fish oil or rapeseed oil, may be interesterified using lipase enzymes as catalyst in accordance with the invention, to provide hardstock for margarine and other emulsion food products particularly low fat spreads. Hardstock fats made in accordance with the invention may also be used in artificial creams and ice-cream. Although fatty acids of 14 or less carbon atoms which are found in nature are generally saturated, it should be understood that the present invention is not confined to the preparation of saturated triglycerides, but extends to the preparation of unsaturated triglycerides, in which a shorter-chain acid is introduced, to provide asymmetric or symmetric unsaturated triglycerides. EXAMPLE I A mixture of one part soyabean oil with 0.45 parts of lauric acid was dissolved in 2.9 parts by weight of hexane and the solution percolated at a feed rate of 4.3 kilogrammes per hour, corresponding to 1.0 kilogrammes per hour of soyabean oil, down a reactor column maintained by a heating jacket at 400C and containing a packed bed of a 1,3-selective interestification catalyst, comprising Mucor Miehei lipase supported on Celite. The catalyst was pre-wetted to a water content of 10% and conditioned by slurrying in a mixture of hexane with soyabean oil before use. The feed rate provided a residence time in the reactor of about 20 minutes. The feed was pre-wetted by passage through silica gel with added water giving a water activity A of 0.85. The reactor effluent collected over 100 hours was distilled to remove solvent, extracted with methanol to remove free fatty acid and hydrogenated using an active nickel catalyst to an iodine alue less than 2. The substantially saturated product (A) was fractionated from acetone solution with removal of a stearine fraction to recover from the solution an olein fraction (B) in 73% yield of (A). Margarine was made by conventional methods, from blends of sunflower oil with 8 and 10% of (B) as hardstock. Tests showed that with only 8% a satisfactory product was obtained, with a required hardness after 4 days, determined by Penetrometer measurements at 5-200C and "thinness" measured by viscosity at 340C on unstabilised fat. At 10% level a much harder, less thin product was obtained. Comparison of solids content of the olein (B) with a mid-fraction (C) recovered from it in 60% yield by acetone fractionation, indicated that even less (C) would be required to achieve comparable results in similarly prepared margarine. Results are tabulated in Table 1 with a comparison margarine made by similar methods using as hardstock (D), a randomised mixture of equal parts of palm kernel oil hardened to 390C and palm oil hardened to 580C by hydrogenation using a non-selective active catalyst. It was found that 13% of this randomised hardstock was required to give hardness data compared with only 8% of the olein hardstock (B) according to the invention, but that randomised hardstock produced substantial loss of "thinness". Table 1 also includes idealised requirements. TABLE 1 Hardness (D) (B) (B) Idealised (4 Days) (13%) (88) (10%) Requirements at OC 5 300 230 435 250 10 200 200 470 200 15 150 195 310 150 20 100 120 250 100 Thinness 150 84 140 100 Table 2 gives the carbon number analysis of the various fats (A), (B), (C), (D) and (E). Fat (E) is a mid-fraction obtained from (D) by successively fractionating tO remove triglycerides with carbon numbers above 48 and below 44. The major triglyceride species permitted in the products (A), (B) and (C) according to the invention as a result of the selective 1,3 activity of the catalyst are as follows: HM2 B2M H3 PStP PStSt LaStLa LaStP StStSt LaStSt No lauric acid or palmitic acid is present in the 2-position. This very limited range of species compares markedly with a much greater number in random rearrangements and substantially improves the case and effect of fractionation of the rearranged fats of the invention. Thus the reaction product (A) was easily fractionated to give the olein (B) with much reduced (HHH) in 738 yield and then a mid-fraction in 60% yield, relatively high in (MHH) and reduced in (MHM). Both yields are based on (A). By contrast the reaction product (D) was much less amenable to fractionation, producing only 30% of the mid-fraction (E) after removing triglycerides with carbon number greater than 48 and less than 44. In Table 3 solid content values over a range of temperatures is given for the fats (B), (C) and (D), measured by NME determinations. From these it is clear that (B) is sharp melting, and (C) even more so, while (D) is markedly inferior. Table 3 includes solid contents measurements of blends of the hard stock fats (B), (C) and (D), in blends with sunflower oil at 8%, 10% and 14% level, and shows that the values for blends with (C) were much higher than (B), which in turn were higher than (D) and that similar solids contents to (D) at 148 were obtained from (B) at 10% and (C) at only 8%. TABLE 2 EMI15.1 <SEP> Example <SEP> Control <tb> Glyceride <SEP> C <SEP> No. <SEP> (A) <SEP> (B) <SEP> (C) <SEP> (D) <SEP> (E) <tb> Species <SEP> Olein <SEP> Mid <SEP> Mid <tb> <SEP> 30-38 <SEP> 2.0 <SEP> 3.5 <SEP> 2.0 <SEP> 14.8 <SEP> 4.7 <tb> <SEP> 40 <SEP> 1.0 <SEP> 1.5 <SEP> 0.5 <SEP> 8.6 <SEP> 5.5 <tb> HM2 <SEP> 42 <SEP> 15.5 <SEP> 21.0 <SEP> 13.5 <SEP> 12.9 <SEP> 12.7 <tb> <SEP> 44 <SEP> 1.5 <SEP> 2.5 <SEP> 2.0 <SEP> 11.9 <SEP> 17.8 <tb> <SEP> 46 <SEP> 9.0 <SEP> 12.0 <SEP> 13.5 <SEP> 15.6 <SEP> 26.6 <tb> H2M <SEP> # <SEP> 45.5# <SEP> 57.5# <SEP> 71.0# <tb> <SEP> 48 <SEP> 36.5 <SEP> 45.5 <SEP> 57.5 <SEP> 14.1 <SEP> 20.6 <tb> <SEP> 50 <SEP> 3.5 <SEP> 4.0 <SEP> 4.0 <SEP> 8.6 <SEP> 7.0 <tb> H3 <SEP> # <SEP> 52 <SEP> 32.5# <SEP> 9.0 <SEP> 15# <SEP> 7.0 <SEP> 8.0 <SEP> 7.8 <SEP> 3.2 <tb> <SEP> 54 <SEP> 20.0 <SEP> 4.0 <SEP> 4.5 <SEP> 4.1 <SEP> 1.3 <tb> <SEP> 56 <SEP> 1.0 <SEP> 0.5 <SEP> 0.5 <tb> TOTAL <SEP> 99.0 <SEP> 101.5 <SEP> 99.0 <SEP> 98.4 <SEP> 99.4 <tb> TABLE 3 N20 N25 N30 N35 N40 N45 N50 N55 N60 (B) 96.3 95.7 95.2 93.6 79.5 40.0 0.4 0.1 0 (C) 97.1 96.8 95.9 95.5 94.4 69.3 2.3 0 0 (D) 88.5 82.3 68.0 51.9 30.3 12.5 0 0 0 TABLE 4 N20 N25 N30 N35 N40 N45 N50 N55 N60 8% (B) 10.7 9.8 9.4 7.3 5.7 4.2 2.3 0 0 (C) 12.0 12.0 11.6 9.9 8.0 5.9 3.6 0.? 0.4 (D) 9.2 8.8 7.4 5.2 3.8 2.7 1.5 1.0 0 10% (B) 13.7 13.5 2.1 9.7 8.3 6.6 3.9 0.6 0.1 (C) 13.6 13.6 13.0 10.7 9.3 7.4 5.5 2.0 0.5 (D) 10.5 9.2 8.3 6.4 5.2 3.3 1.9 0.4 0 14% (B) 17.5 17.2 15.5 13.7 11.7 9.1 6.4 2.1 0.4 (C) 18.5 17.6 16.6 15.2 12.4 10.3 7.6 4.0 0.7 (D) 15.7 14.9 13.1 10.4 8.8 6.7 3.8 2.1 0.8 Example II A mixture of 0.1 parts butyric acid with 1 part of a mid-fraction of palm oil (PMF) was dissolved in 2 parts of petroleum ether (BPt 100-1200C), all by weight, and percolated at an average feed-rate of 10 mls per hour and 400C, up a column. The column was packed with 8 gms of catalyst comprising Rhizopus lipase (Nagase 2A) enzyme deposited on Celite as described in our British patent No. 1,577,933 and pre-activated with 10% water. The catalyst hydrolytic activity was 2.5 units per mg. Below the catalyst bed was a bed of 4 gms of Celite pre-activated with 3.6 mls water to hydrate the feedstock. After distilling off solvent the collected reaction mixture was extracted with methanol to remove free fatty acid and glyceride isomers containing two butyric acid residues, which were preferentially dissolved in the methanol, and saturated at 100C for two hours with hydrogen in the presence of 0.2% fresh nickel catalyst. The saturated product was dissolved in six times its weight of acetone containing 0.5% water and after maintaining at 3O0C with stirring for one hour, the solution was cooled at a cooling rate of 300C per hour 200C which was then held for one hour. A crystalline fraction was removed, washed twice with 0.6 times its weight each time, with acetone at 200C and the olein recovered before being analysed and tested for its effect in margarine. Carbon number analyses are given in table 5 showing the introduction of substantial amounts of butyric acid which as shown is absent from palm mid-fraction, and comparison is made with butter oil. TABLE 5 Wt % Carbon No. Triglyceride * PMF Fraction Butter Oil 24-34 5 9.3 36 PPB 14 10.5 38 POB/PStB 63 12.6 40 OOB/StPB/StStB 14 10.7 42-46 20.5 48 PPP 5 2 8.8 50 POP/PStP 74 1 11.3 52 POO/PoSt/PSt2 19 1 10.3 54 O3/StOSt/St3 2 5.8 B = Butyric O = Unsaturated P = Palmitic St = Stearic * Found in PMF and rearranged fraction. Table 6 shows a comparison of the effect of introducing the fraction recovered into a margarine hardstock, estimated by a trained panel who expressed a marked preference for the margarine containing the recovered product. This preference was substantially maintained even after the margarine was subjected to cyclic temperature changes. TABLE 6 Product Panel Score Churned butter 9.5 Votator - made butter 7.5 Margarine 3.3 Temperature: Cycled margarine 3.0 Margarine + 15% fraction 7.2 Margarine + 15% fraction, 6.5 temperature - cycled The solid content data in Table 7 shows that the margarine remained acceptable in its melting properties after addition of the fraction. TABLE 7 N Value Fraction Margarine Margarine + at OC 15% fraction 10 93.1 35.4 38.28 20 90.7 16.4 10.20 30 49.1 3.5 2.6 35 7.3 0.8 0 40 2.7 0 0 Example III Blends of palm and palm kernel oil in the weight ratios 40:60, 60:40 and 80:20, were compared by carbon number analysis and melting profile, measured by pulse NMR, before and after interesterification under the influence as catalyst of Mucor miehei 1, 3 selective enzyme, and compared with corresponding randomised compositions using sodium methoxide randomisation catalyst in a conventional interesterification. The oils were refined, neutralised and bleached before blending. The enzyme rearrangement reaction was carried out on a 25% dispersion by volume in the petroleum ether of the blend, which was passed at 25ml per hour, successively through a pre-saturation column containing 4 grammes of acid-washed Celite pre-dehydrated with 80% by weight of water, and a reaction column containing 6 grammes of the enzyme supported on Celite catalyst which was prehydrated before being packed in the column, with 10% by weight of the catalyst of water. The reaction column was maintained at 400C. The crude product was neutralised before recovering the rearranged fat. In Table 8 the measured carbon number for the enzyme-rearranged blend shows good agreement with the theoretical values calculated on the basis of complete reaction. Values for the corresponding randomised blends also appear for comparison. Table 9 shows the melting profile results for the blends, both before and after silica treatment carried out on a dispersion of the blends in petroleum ether to remove partial glycerides. The various blends were made up into a margarine fat composition consisting of 65 parts of the blend with 35 parts of low-erucic rape seed oil and melting profiles were determined as before and are given in Table 10. Margarine was prepared by conventional methods from these latter fat compositions and evaluated. Low fat water-in-oil emulsion spreads were similarly prepared from these compositions and evaluated. The melting profiles show that the enzymatically interestified reaction products are softer than their chemically interesterified counterparts and that this difference persists after silica treatment, suggesting that the difference is not entirely due to the presence of diglycerides. All the margarine fat compositions are however acceptable for margarine and low fats spread production and the products taken were found to be acceptable to consumers. The melting profile of the blend with the highest palm oil content in particular shows a substantially lower N35 value after the enzymic interesterification, demonstrating the extended flexibility of blends that can be used in this process. Margarine and low fats spread containing less than 20% of the interesterified blend with other fat components, showed no significant difference in solids content values. Satisfactory margarine and low fats spreads was obtained in each case. Table 8 Carbon Number Distribution of PO/PK Biends and interesterified Products Carbon number 30 32 34 36 38 40 42 44 46 48 50 52 54 56 40PO/60PK 1.0 4.0 6.0 15.0 11.0 6.0 5.0 3.5 3.0 6.5 16.0 16.0 6.0 0.5 enzymic 2.0 3.0 3.0 7.0 7.5 10.0 14.0 11.00 13.5 11.0 8.0 7.0 2.5 0 Chemica@s 0 2.5 2.5 6.0 7.0 10.0 14.0 12.0 14.0 12.5 7.5 6.5 4.0 0.5 60PO/40PK 0.5 2.5 4.5 11.5 8.0 4.0 3.5 2.5 2.5 7.5 22.5 22.5 7.5 0.5 enzymic 1.5 2.5 2.5 5.0 4.5 6.5 9.5 9.0 13.5 12.5 14.0 13.5 5.0 0.5 chemical 1.0 2.0 2.0 4.0 4.0 6.5 9.5 11.0 15.5 15.0 12.5 12.0 5.0 0.5 80PO/20PK 0.5 1.5 3.0 7.5 5.0 2.0 1.5 1.5 1.5 7.5 29.0 29.0 9.5 1.0 enzymic 1.0 1.5 2.0 4.5 3.0 3.0 4.0 5.0 9.5 11.5 22.5 23.0 8.0 1.0 chemical 1.0 1.0 1.5 3.0 2.5 2.5 4.5 7.5 13.0 15.5 19.5 20.0 8.5 1.0 Table. 9 Solids Contents of PO/PK blends and Interesterified Products N0 N5 N10 N15 N20 N25 N30 N35 N40 40P0/60PK 72.0 69.5 60.5 42.0 23.5 6.5 2.0 1.0 1.0 enzymic - 69.0 66,5 54.0 36.5 21.0 8.0 1.0- 0.5 0 chemical - 73.5 71.0 64; ;0 48.0 30.5 17.0 4.0 0.5 0 60P0/40PK 66.5 64.0 53.0 36.5 19.0 9.5 6.0 3.0 2.0 enzymic 60.0 58.5 46.5 30.5 17.0 9.0 4.0 1.0 1.5 chemical 67.0 66.0 58.0 44.0 29.5 17.5 8.0 2.0 1.0 80P0/20PK 60.5 58.5 46.5 31.5 19.5 11.0 7.0 4.5 2.0 enzymic 53.0 52.5 45.0 31.5 19.0 11.5 6.5 3.0 1.0 chemical 65.0 64.0 56.0 43.5 32.0 21.0 13.0 6.5 2.0 After silica treatment 40P0/60PK 74.0 72.0 62.0 46.0 27.0 8.5 4.0 1.0 0 enzymic 72.5 69.5 56.0 40.0 24.5 10.0 1.5 1.0 1.0 commercial 75.5 72.1 66.1 53.1 36.8 21.8 8.0 0.9 0.3 Table 10 Solids Contents of Blends containing 35% rapeseed oil N0 N5 N10 N15 N20 N25 N30 N35 40PO/60Pk 42.5 38.5 28.5 18.0 6.0 2.5 1.5 1.0 ez,ym1c 41.0 37.0 26.0 17.0 7.0 2.0 0.5 0.0 Chemical 45.0 41.5 33.5 23.0 13.5 7.0 1.0 1.0 60P0/40PK 38.5 35.0 25.0 @ 14.0 6.0 4.0 2.5 1.5 enzymic 35.5 33.0 23.0 14.5 7.5 4.0 1.5 <RTI ID=25.2> 1.0 chemical 42.5 40.0 31.5 22.5 14.5 8*0 3.5 1.0 80P0/20PK 35.0 33.0 25.0 15.5 9.5 7.0 4.0 2.5 enzymic c 31.0 30.5 23.0 15.0 9.0 6.0 3.5 1.0 chemical 41.0 39.5 32.5 23.5 15.5 11.0 7.0 2.5

Claims: CLAIMS 1. Process for the preparation of interestified fats or glycerides oil, in which a mixture of fatty reactants is interesterified in the presence, as interesterification catalyst, of a lipase enzyme and a small amount of water to activate the catalyst and recovering a hardstock fat, the process including, if necessary, a hardening and/or fractionation step and the mixture comprising reactants distinguished from one another by fatty acid residues of different chain length. 2. Process according to claim 1 wherein the fatty mixture includes a vegetable oil or fat. 3. Process according to claim 1 or 2 wherein the fatty mixture comprises a mixture of a palmitic fat containing at least 20% palmitic acid and a lauric fat containing at least 40% lauric acid or fats derived therefrom. 4. Process according to claim 3 wherein the fatty mixture comprises palm oil and palm kernel or coconut oil. 5. Process according to claim 1, 2 or 3 wherein the fatty mixture comprises a mixture of a palmitic fat or fat derived therefrom and a saturated fatty acid containing up to 12 carbon atoms. 6. Process according to claim 5 wherein the fatty acid contains from 4 to 8 carbon atoms. 7. Process according to any of the preceding claims wherein the interesterification is carried out at a temperature from 50 to 800C. 8. Process according to any of the preceding claims wherein the water activity of the interesterification feedstock is maintained at 0.4 to 0.85. 9. Process according to any of the preceding claims wherein the amount of catalyst present is from 0.5 to 10% by weight of the fatty mixture. 10. Process according to any of the preceding claims wheein the catalyst is selectively active. 11. Process according to any of the preceding claims wherein the catalyst comprises Candida cylindracae, A. niger, Mucor, Rhizopus and Thermomyces lipases. 12. Process according to any of the preceding claims wherein the interesterification is carried out in a water-immiscible solvent. 13. Process according to claim 12 wherein the solvent comprises an aliphatic liquid having a boiling point not more than about 100"C. 14. Process according to claim 13 wherein the solvent comprises hexane. 15. Process according to any of the preceding claims 12 to 14 wherein pre-selected glycerides comprising interesterified fat having a solids content at 200C of at least 20 are recovered by fractionation from the solvent. 16. Process according to any of the preceding claims wherein the interesterification is carried out at a temperature at which pre-determined glycerides comprising the interesterified product are crystallised out to direct the interesterification. 17. Process for the preparation of a margarine hardstock fat according to any of the preceding claims comprising saturation hydrogenating and interesterifying steps carried out in either order, wherein the fatty mixture comprises a mixture of a fat or glyceride oil with the fatty acid reactant and in which as interesterification catalyst a 1, 3 selective enzyme is used, and fractionating the glyceride mixture in the product to recover a saturated hardstock fat. 18. Margarine hardstock fat comprising a fraction of a blend of palm and lauric fats selectively rearranged as claimed in any of the preceding claims, and a liquid vegetable base stock, wherein the said fraction comprises from 40 to 75% glycerides of carbon number 46 to 48 and is present in an amount from 5 to 20% of the blend. 19. Margarine harstpck fat as prepared in any of the preceding claims 1 to 17 and comprising glycerides MHH in which M = C8 and H = C16/C18 fatty acid residues.

Inventors: CROOK, STEPHEN, MACRAE, ALASDAIR ROBIN, MOORE, HARRY
Applicants: UNILEVER NV, UNILEVER PLC
Application year: 1985
Main classification: C11C3
IPC codes: A23D7, C11C3, C11D3