the mixture of diglycerides ( a ) that can be used can contain diglycerides of the ss - and su - type . this means , that they can contain simultaneously one or two saturated fatty acid residues s with 12 - 24 c - atoms and one or two unsaturated fatty acid residues with at least 16 c - atoms . the exact position of the residues s and u is not very important . still we have a preference for the use of 1 . 3 - diglycerides as they have slightly better structuring properties . so , e . g . 1s - 2u - diglycerides are as suitable as 1s - 3u diglycerides or as 1u - 2s - diglycerides . however , we prefer to apply a mixture with a very high content of diglycerides of the type su , in particular diglycerides with one oleic and with one palmitic acid residue and diglycerides with one oleic and one stearic acid residue . these diglycerides can be present in weight ratios of 5 : 95 - 95 : 5 , preferably 20 : 80 - 80 : 20 . our compositions can be made by blending of mixtures of diglycerides , rich in the required diglycerides with triglycerides , in particular liquid triglycerides , such as sunflower oil , olive oil , maize oil , soybean oil , rapeseed oil etc . the diglycerides can be obtained according to many methods , such as : 1 . hydrolysis of triglycerides , this hydrolysis can be performed along a chemical route ( using a base ) or along an enzymic route . 2 . interesterification of glycerol with a triglyceride or an acid . again a chemical or an enzymic route can be applied . the starting fatty material for the interesterification with glycerol preferably has a high s 2 u - content (& gt ; 40 %, in particular & gt ; 50 %). a convenient enzymic route using glycerol and an acid is disclosed in e . g . ep 307 , 154 . in general , the crude products obtained by those routes need to be purified , e . g . removal of monoglycerides by distillation , followed by fractionation . the above blends can be free of trans acids and free of chemically interesterified fats . however , blends that contain chemically interesterified fat - component can also be applied ( either per se or in combination with non - chemically interesterified fats ). although the triglyceride - component of our blends can be selected from a broad range of triglycerides , provided that the total composition meet our safa - requirement (& lt ; 40 %), we prefer to use fats with an n 5 & lt ; 40 as our triglyceride - source . components of those fats are suitably selected from the group consisting of sunflower oil ; soybean oil ; safflower oil , olive oil , high oleic sunflower oil , maize oil , high oleic safflower oil and olein fractions of vegetable oils , such as palm oil . it is , however , also possible to use fats obtained by enzymic conversion , or olein - fractions obtainable by fractionation ( wet - or dry ) of enzymically made oils . the enzymic conversions can be performed using the technology disclosed in our gb 1 , 577 , 953 . the starting materials should be selected such , that the desired fats or oils are obtained . it is , of course , also possible to use fats that are made according to chemical interesterification - processes ( with or without a fractionation step ). food products that can be made comprise filling fats , enrobed filling fats , confectionery products , wrapper spreads , wrapper margarines , wrapper shortenings , tub spreads , tub margarines , cream alternatives , bakery products , doughs , cheese , mayonnaise and dressings . each of these food products comprise a fat phase and this fat phase then consists at least partly of the novel fats according to the invention . it should be understood that for each application the fat blends require a specific n - line . briefly , it can be said that the following n - requirements must be fulfilled for the application indicated : 1 . 1 a mixture of palm oil - midfraction , glycerol and lipolase 100 l - enzyme ® ( ex novo - nordisk ) was converted in a weight - ratio of 100 : 20 : 1 . the ph was kept at 7 , 0 , using a phosphate buffer . the conversion was performed at 35 ° c . for 24 hours under stirring . excess glycerol was decanted off . monoglycerides and free fatty acids were removed from the crude reaction product ( containing 38 , 6 wt % of diglycerides and 33 , 7 wt % of monoglyceride ) in a falling film evaporator at 260 ° c . and 0 , 3 mm hg : the product contained 47 , 8 wt % of diglycerides and 2 , 1 wt % of monoglycerides . the product was bleached and deodorised and fractionated from hexane ( 1 , 5 : 1 hexane to oil ratio at 30 ° c .). the olein was collected ( yield 78 %) and contained 45 , 6 wt % of diglycerides . in a second hexane fractionation , above olein - fraction was fractionated , ( 3 , 22 : 1 hexane to oil ratio at - 10 ° c . ); a stearin fraction was obtained . this stearin fraction contained 60 wt % of diglycerides of which 56 , 7 wt % were of the su - type . the overall yield from fractionations was 29 %. a third fractionation was performed on the stearin fraction obtained ( 5 : 1 hexane to oil at 24 , 5 ° c .). the olein - fraction was collected , it contained 62 wt % of diglycerides of which 72 , 5 wt % were su - diglycerides . the overall yield was 23 %. excess monoglycerides was removed from the final olein - fraction via a silica - treatment with hexane / acetone ( 88 : 12 ) as solvent ( 5 : 1 : 0 , 78 = solvent : oil : silica ). the product was washed with solvent . the resulting product was rich in po ( p = c 16 : 0 o = c 18 : 1 ) and contained 61 , 4 % diglycerides and 0 , 0 % monoglycerides . the diglycerides consisted of 25 % ss ; 70 , 7 % su and 4 , 2 % uu . its fatty acid composition was : f . f . a .- residue 14 : 0 16 : 0 16 : 1 18 : 0 18 : 1 18 : 2 18 : 3 20 0 , 4 50 0 , 0 7 , 3 39 , 3 2 , 1 0 , 0 0 , 6 1 . 2 shea - stearin , glycerol , lipolase 100 l ®) ( ex novo - nordisk ) were mixed in a weight - ratio of 100 : 20 : 1 . the ph was adjusted at 7 . 0 using a phosphate buffer . the conversion was performed at 40 ° c . during 8 hours under stirring . excess glycerol was decanted off . monoglycerides and free fatty acids were removed ( falling film evaporator 260 ° c ., 0 , 3 mm hg ). the resulting product was fractionated from hexane ( 3 : 1 hexane : oil ; 21 ° c .). an olein fraction was collected ( yield 96 % : diglyceride content 22 , 5 wt %). in a second hexane - fractionation above olein fraction was fractionated ( 6 , 65 : 1 hexane : oil at - 7 ° c . ), the stearin - fraction was collected ( 18 % diglyceride of which 72 , 6 % su - type ). overall yield 60 %. the product was refined by a two - stage silica - treatment . diglycerides and monoglycerides were adsorbed onto silica ( hexane as solvent ; ratio hexane : oil : silica = 2 : 1 : 1 , 22 ). the silica - complex was washed with hexane and the wash was discarded . the silica - complex was washed with hexane / acetone ( 88 / 12 ) in ratio 3 , 5 wash : 1 oil . the resulting oil contained 46 , 8 wt % diglyceride and 0 , 0 % monoglyceride . it &# 39 ; s composition was 22 % ss , 73 , 6 % su and 4 , 4 % uu . the fatty acid composition of the diglycerides was : f . f . a .- residue 14 : 0 16 : 0 16 : 1 18 : 0 18 : 1 18 : 2 18 : 3 20 0 , 4 2 , 3 0 , 0 57 , 4 35 , 9 2 , 1 0 , 0 1 , 9 1 . 3 a blend was made from sunflower oil , the po - rich products from example 1 . 1 and the sto - rich product from example 1 . 2 ( ratio : 71 : 14 , 5 : 14 , 5 ). the blend contained 19 , 6 % diglycerides . the diglyceride - composition was : 21 , 2 % ss , 70 , 3 % su and 8 , 4 % uu . f . f . a .- residue 14 : 0 16 : 0 16 : 1 18 : 0 18 : 1 18 : 2 18 : 3 20 0 , 2 12 , 6 0 , 1 12 , 5 26 , 6 46 , 5 0 , 0 0 , 6 ______________________________________ ° c . n______________________________________ 10 18 . 3 30 3 . 4 35 3 . 0______________________________________ ______________________________________fat phasefat blend of example 1 . 3 40 % hymono 7804 ( monoglyceride : iv = 80 ) 0 . 3 % colour ( β - carotene ) 0 . 01 % flavour 0 . 1 % total 40 . 41 % aqueous phase ( to ph 5 . 1 ) water 56 . 5 % skimmed milk powder 1 . 5 % gelatin ( 270 bloom ) 1 . 5 % potassium sorbate 0 . 15 % citric acid powder 0 . 07 % ______________________________________ all percentages on product basis . the processing was performed on a microvotator , comprising an acac - set up . 3 kg of material was prepared and processed . ______________________________________premix condition stirrer speed 100 rpm temperature 50 ° c . pump proportioning pump set at 80 % ( 40 . 3 g / min ). a . sub . 1 conditions shaft speed 1000 rpm temperature set at 10 ° c . c . sub . 1 conditions shaft speed 1000 rpm temperature set to 13 ° c . a . sub . 2 conditions shaft speed 1000 rpm temperature set to 12 ° c . c . sub . 2 conditions shaft speed 1000 rpm temperature set to 15 ° c . ______________________________________ the aqueous phase was prepared by heating the required amount of water to approximately 80 ° c . and then , using a silverson mixer , slowly mixing in the ingredients . the ph of the system was adjusted to 5 . 1 by adding 20 % lactic acid solution as required . a premix was prepared by stirring the fat phase in the premix tank and then slowly adding in the aqueous phase . when addition was complete , the mix was stirred for a further 5 minutes before pumping through the line . when the process had stabilised ( around 20 minutes ), product was collected for storage and evaluation . ______________________________________ a1 15 . 0 ° c . c1 17 . 1 ° c . a2 16 . 5 ° c . c2 16 . 6 ° c . ______________________________________ products were collected from both of the c - units . very good oil continuous low fat spreads were produced using this system . hardness c and conductivity of the products were measured . ______________________________________ c - value c - value conductivity conductivityproduct @ 5 ° c . @ 20 ° c . @ 5 ° c . @ 20 ° c . ( 40 % fat ) ( gcm . sup .- 2 ) ( gcm . sup .- 2 ) ( μscm . sup .- 1 ) ( μscm . sup .- 1 ) ______________________________________ex c . sub . 1 1180 190 10 . sup .- 4 10 . sup .- 4ex c . sub . 2 1400 210 10 . sup .- 4 10 . sup .- 4______________________________________ all products had a good oral melt down and were fat - continuous . ______________________________________fat phasefat blend of example 1 . 3 80 % hymono 7804 0 . 3 % flavour 0 . 1 % colour ( β - carotene ) 0 . 01 % aqueous phase ( to ph 5 . 1 ) water 18 . 3 % gelatin ( 270 bloom ) 0 . 5 % skimmed milk powder 0 . 5 % potassium sorbate 0 . 05 % citric acid powder 0 . 025 % ______________________________________ all percentages on product basis . identical conditions were used for the preparation and processing as for the 40 % fat spread . ______________________________________ a1 15 . 3 ° c . c1 15 . 9 ° c . a2 15 . 7 ° c . c2 15 . 6 ° c . ______________________________________ as before , oil continuous product could successfully be obtained at any point after c - unit 1 . ______________________________________ c - value c - value conductivity conductivityproduct @ 5 ° c . @ 20 ° c . @ 5 ° c . @ 20 ° c . ( 80 % fat ) ( gcm . sup .- 2 ) ( gcm . sup .- 2 ) ( μscm . sup .- 1 ) ( μscm . sup .- 1 ) ______________________________________ex c . sub . 1 1820 200 10 . sup .- 5 10 . sup .- 5ex c . sub . 2 2100 180 10 . sup .- 5 10 . sup .- 5______________________________________ ______________________________________ % ______________________________________sugar 45cocoa powder n - 11 - n 7skimmed milk powder 10fat 38lecithin 0 . 5______________________________________ 1 . blend of an interestified fat and palm oil olein in ratio 5 : 95 , known as biscuitine sf ® . the fillings were made using a hobart mixer , buhler refiner and pascal conche . filling 1 was cooled to 22 . 5 ° c . and filling 2 was cooled to 19 . 5 ° c ., before they were piped into aluminum cups . the aluminum cups were stored at 20 ° c . and 25 ° c . the fillings were evaluated on : the sta - hardness of the fillings was determined after one day storage at 20 ° c . and 25 ° c . the results were : the fillings were evaluated by the taste panel after storage at 20 ° c . filling 2 was much harder than filling 1 . filling 2 had a slightly slower and lower flavour release probably because it was harder . although the safa content of the diglyceride based filling was lower , the product was much harder and had better body .
fat - blends suitable for food applications are disclosed . these blends contain 10 - 60 % diglycerides , 90 - 40 % triglycerides wherein contains ≧ 70 % su - diglycerides , including high melting diglycerides and simultaneously a fatty compound so that the melting point of is & gt ; 5 ° c ., lower than the melting point of wherein has an n 5 ≦ 40 while the total blend has a safa - content & lt ; 40 %.