MXPA99003888A - Process for preparing starch hydrolyzates with low de by nanofiltration fractionating, products so obtained and use of these products - Google Patents

Abstract

A process for producing a low DE starch hydrolysate, involves fractionating a starch hydrolysate comprising a DE greater than about 18 using a nanofiltration membrane, having a molecular weight cut-off of less than about 4,000 daltons, under nanofiltration conditions effective to result in a low DE starch hydrolysate comprising a DE of less than about 25. A process for producing a low DE starch hydrolysate blend involves combining the product produced by the process of the present invention with At least one other substance in a predetermined blending ratio to result in a low DE starch hydrolysate blend. A process for hydrogenating a low DE starch hydrolysate produced by the process of the present invention to result in an hydrogenated low DE starch hydrolysate. A process for producing a substantially thermal and shelf-life stable emulsion comprising forming a mixture of the low DE starch hydrolysate of the invention with an effective concentration of at least one ingredient to result in an emulsion. A process for producing a substantially dry ingredient encapsulate comprising the steps of:(1) forming an aqueous matrix composition comprising the low DE starch hydrolysate of the invention;(2) mixing at least one ingredient with said matrix composition to form a mixture;and (3) drying said mixture to result in a substantially dry ingredient encapsulate.

Description

PROCESS TO PRODUCE HIDROYSIS OF STARCH WITH LOW ED BY FRACTIONATION OF NANOFILTRATION, PRODUCTS OBTAINED THROUGH THE SAME AND USE OF SUCH PRODUCTS BACKGROUND OF THE INVENTION Field of the Invention The present invention is directed to the production of starch hydrolysates with low ED, which involves fractionating a hydrolyzate thereof having an ED greater than about 18 using a nanofiltration membrane under effective nanofiltration conditions. to result in a starch hydrolyzate with low ED having an ED less than about 24; the resulting starch hydrolyzate products with low ED; mixtures of said starch hydrolysates with low ED with other substances; and emulsions and encapsulates prepared using said starch hydrolysates with low ED. Description of the Related Art. Maltodextrins, a starch hydrolyzate with low ED with dextrose equivalent (ED) not greater than about 20, e.g. , from 4 to 20, have a mild flavor, low sweetener content and low hygroscopicity. Said products are useful as bases for the preparation of food products as well as for body-providing agents and as additives having non-sweet characteristics, which contain non-hygroscopic water.

Other applications include its use as a vehicle for synthetic sweeteners, as spray-drying adjuncts, as bulking agents, bulking agents or dispersants, as moisture-containing agents and as an energy source in sports drinks. The most commercially available maltodextrins in the world market produced by known technology, are in solid form or crystalline form due to deterioration or mist formation or microbial instability in liquid form. However, there is a demand for a maltodextrin in its liquid form that exhibits extreme clarity, low viscosity and will not develop deterioration when stored at room temperature. Liquid maltodextrins with low ED have been produced using conventional processes, such as enzyme conversion, chromatographic fractionation and membrane fractionation. However, the products produced suffered disadvantages including instability in liquid form or high viscosity. The Patents of E.U.A. Nos. 3,974,033 and 3,974,034 describe methods for producing a maltodextrin with low ED and improving the stability by enzymatic hydrolysis of oxidized starch. Maltodextrin is characterized by being free from haze for a long period at a high solids concentration. The maltodextrin is prepared by first liquefying a highly oxidized starch with acid or enzyme to an ED that is substantially not greater than about 7; and, in a subsequent step, converting the oxidized and liquefied starch with a preparation of the bacterial alpha-amylase enzyme to achieve a maltodextrin product having an ED that is substantially not greater than about 20. The U.A. No. 4,298,400, describes another method of enzyme hydrolysis to produce liquid starch hydrolysates with low ED without mist production. The product, prepared by two step hydrolysis using bacterial alpha amylase, has a descriptive ratio higher than 2.0 and therefore, exhibits a property without haze. The Patent of E. U.A. No. 4, 840, 807, discloses a fractionation method for producing branched maltodextrins of low, liquid ED. The process comprises the steps of reacting alpha-amylase with starch to produce a starch hydrolyzate on the ED scale of 10 to 35 and then contacting the resulting saccharified solution with a gel-like filter agent, thus selectively fractionating the branched dextrin and the linear oligosaccharides. The gel type filtration agent is an ion exchange resin and the fractionation system is a simulated moving bed. The resulting branched oligosaccharides have an average molecular weight of about 800 and about 16, 000 with a corresponding ED of about 20 to about 1. Membrane separation is known to fractionate sugar polysaccharides. Waniska et al. (Journal of Food Science, Vol. 45 (1980), 1259) describes the fractionation capacity of three ultrafiltration (UF) membranes compared to gel permeation and chromatography to separate oligosaccharides (DP5 -20) of sugar of low molecular weight. Birch et al. (Die Starke 26. Jahrg. 1974 / Nr. 7, 220) describes the fraction of glucose syrups by reverse osmosis (Ol) which provides a means for the manufacture of several new types of syrup and which allows them to be eliminated. whole groups of sugars under selected conditions. Products in the ED scale of 43-80 or ED of 15-43 can be obtained by using appropriate combinations of different membranes. Kearsley and others (Die Starke 28. Jahrg, 1976 / Nr. 4, 138) describes the reverse osmosis (Ol) of glucose syrups and ultrafiltration (UF) operations to isolate specific groups of sugars, high or low molecular weight or both of the syrup. Sloan et al. (Preparative Biochemistry, 15 (4), 1985, 259-279) describes the molecular filtration of ultrafiltration (UF) membranes to concentrate oligosaccharides with polymerization degrees above 10 from corn starch hydrolyzate . It is not thought that any of these processes can be used to form a non-retrograde maltodextrin having low viscosity.

People associated with starch hydrolysates with low ED recognize the need for an improved low ED starch hydrolyzate, particularly in liquid form and more particularly in mixtures thereof with other substances.

Substantial research has addressed problems of inherent instability of emulsions or multi-phase systems, defined as thermodynamically metastable or unstable systems. Emulsion stability is a complicated phenomenon and a function of many variables, for example, viscosity, temperature, internal phase droplet size distribution, speed and time of agitation type and surfactant concentration, ratio and phase composition, conductivity and dielectric constant (P. Sherman "Emulsion Science", Academic Pres, NY, 2nd Ed. (1988): I. Abou-Nemeh and AP Van-Peteghem "Membrane Aging and Related Phenomena in liquid Surfactant Membranes Process", Sep. Sci. Technol. 29 (6), 727-41, (1994)). Accordingly, the relationships with the emulsion material recognize the need for improved emulsion compositions that exhibit long-term stability comprising, for example, flavors, oils, fragrances, syrups, insecticides, biologically active drugs, etc. In addition it is well known and scientifically documented in the matter of encapsulation of volatiles, oils, fragrances, etc., that the latter is fixed and encapsulated in a glassy substrate, it is recommended to have a certain composition that contains a specific material, ie oligosaccharides of high molecular weight, maltodextrins, starch, etc., which will improve the film forming properties of the mixture and reinforce its encapsulating capacity for spray drying or extrusion purposes. (U.S. Patents 4,689,235; 3,764,346). However, encapsulation with conventional starch hydrolysates suffers from a variety of problems, including: high viscosity of the starch hydrolyzate substrate with low ED, low loading capacity, poor encapsulation stability and formation of colored by-products. Consequently, the elastomers in the encapsulation material recognize the need for improved encapsulation compositions that are stable, exhibit improved loading capacity and retention of, for example, flavors, oils, fragrances, colorants, insecticides, drugs, fine and benign chemicals, etc., and which may be free of antioxidants and can be manufactured using substrates with a relatively low dry solids content with film-forming capability and encapsulating capacity. BRIEF COMPENDIUM OF THE INVENTION The present invention is directed to a process for producing a starch hydrolyzate with low ED which involves fractionating a starch hydrolyzate having an ED greater than about 18 using a nanofiltration membrane, preferably selected from the group consisting of Teflon membranes, stainless steel membranes, ceramic membranes and polymer membranes; and / or that you have a molecular weight cutoff of less than about 4,000 daltons, under effective nanofiltration conditions to result in a starch hydrolyzate with low ED having an ED of less than about 25. In accordance with the present invention, the membranes of nanofiltration preferably comprise a membrane of thin film composite material, wherein the preferred thin film composite material membrane is selected from the group consisting of polyamide membranes and polysulfone polysulfone membranes. In one embodiment of the present invention, the starch hydrolyzate with low ED comprises a liquid, a starch hydrolyzate with low ED having an ED of less than about 25 and a polydispersity index of less than about 5. The starch hydrolyzate with low Liquid ED preferably comprises a dry solids content within a range of about 50% to about 85% and / or a viscosity of 70% dry solids content and at 25 ° C less than about 30,000 centipoises. The starch hydrolyzate with low ED is preferably substantially non-distortible and stable to microbes. The present invention involves hydrogenating and / or deriving and / or drying the starch hydrolyzate with low ED of the present invention to result in a starch hydrolyzate with low hydrogenated ED and / or derivative and / or dry.

Accordingly, it is an object of the present invention to provide a nanofiltration membrane process for producing starch hydrolysates with low ED having an ED less than about 25 and a polydispersity index of less than about 5, particularly in its liquid form which are eventually substantially of free deterioration and have lower viscosity than a high dry solids content compared to conventional products. The liquid form and its low viscosity characteristics are particularly suitable for drying, preferably spray drying or extrusion, the liquid resulting in a solid or a substantially dry product. The present invention is also directed to a process for producing a substantially thermal emulsion with storage life comprising forming a mixture of the starch hydrolyzate with low ED of the present invention, in its non-hydrogenated or hydrogenated form, with an effective concentration of at least one ingredient to result in an emulsion characterized by thermal stability and shelf life. Preferably, the emulsion exhibits a viscosity suitable for spray drying or extrusion. It is still another object of the present invention to provide a process for producing a substantially dry ingredient encapsulation comprising the step of forming an aqueous matrix composition comprising the starch hydrolyzate with low ED of the present invention, in its non-hydrogenated form or hydrogenated or derived; mixing at least one ingredient with the matrix composition to form a mixture; and drying the mixture will result in an encapsulation of substantially dry ingredient. BRIEF DESCRIPTION OF THE DRAWING The Figure shows a flow chart for a nanofiltration process according to the present invention. DETAILED DESCRIPTION OF THE INVENTION The following is a detailed description of the present invention which is intended to be claimed: The starch hydrolysates with low ED of the present invention are produced by a nanomembrane filtration process shown in Figure 1. In general, the process for producing a starch hydrolyzate with low ED according to the present invention involves fractionating a starch hydrolyzate having an ED greater than about 18 and in particular greater than about 21, using a nanofiltration membrane, preferably selected from the group consisting of of Teflon membranes, stainless steel membranes, ceramic membranes and polymer membranes and / or having a molecular weight cutoff of less than about 4,000 daltons, under nanofiltration conditions to result in starch hydrolysates with low ED having an ED less than about 25.

The starch hydrolyzate having an ED greater than about 18, which is suitable for purposes of the present invention, are starch hydrolysates having an ED greater than about 18 and in particular greater than about 21 and which may be in a form non-hydrogenated, hydrogenated, oxidized or derivatized, which are effective to give a starch hydrolyzate with low ED having an ED of less than about 25 up to fractionation according to the present invention. In accordance with the present invention, the polymeric nanofiltration membranes are preferably selected from the group consisting of polyamide membranes and polysulfone polysulfone membranes. For purposes of the present invention, the nanofiltration membranes are preferably selected from the group consisting of polyamide membranes and polysulfone polysulfone membranes having a molecular weight cut within a range of about 400 to about 4,000 daltons, more preferably within from a scale of about 800 daltons to about 2,500 and even more preferably of about 1,000 daltons. Said nanofiltration membranes preferably comprise a membrane of thin film composite material, wherein a preferred thin film composite material membrane is selected from the group consisting of polyamide membranes and polysulfone polysulfone membranes. Specific examples of nanofiltration membranes include membranes selected from the group consisting of ASP40 and ASP50 (manufactured by Advanced Membrane Technology) and GH and GE, (manufactured by Osmonics / Desal). The membranes of thin film composite materials may comprise polysulfone as support and polyester as reinforcement. The membrane configuration can be selected from the group consisting of flat sheets, tubes and spirally wound membranes. The permeate flow, defined as 0.587 lt / cm2 per day, in nanofiltration processes according to the present invention, varies with pressure. The greater the pressure, the higher the flow. According to the process of the present invention, the nanofiltration step of the present invention is operated at a pressure preferably less than about 42.18 kg / cm2 and even more preferably within a range of about 7.03 kg / cm2 and about 35.15 kg / cm2. In contrast, conventional reverse osmosis processes usually require an operating pressure of 35.1 kg / cm2 to 175.7 kg / cm2 in order to obtain significant flow. According to the present invention, for a permeate flow of a feed of the corn syrup starting material having an ED of 36 and 30% dry solids at 50 ° C and a pressure of about 33.74 kg / cm2 is not less than 7.04 lt / cm2 per day (LCD) The permeate flow in nanofiltration processes also varies with different temperatures. An increase in operating temperature of about 10 ° C can increase the flow by as much as 100%. However, as the operating temperature increases, there is an increase in the tendency of certain membranes (e.g., polymeric) to rupture. As a result, the nanofiltration step of the processes of the present invention is operated at as high a temperature as possible in order to obtain maximum permeate flow without damaging the membrane and structure materials or degrading the product. Accordingly, the operating temperature of the nanofiltration processes of the present invention is preferably less than about 95 ° C, more preferably within the range of about 40 ° C to about 80 ° C and even more preferably about 45 ° C. at around 65 ° C. Accordingly, a starch hydrolyzate with low ED is fractionated using said nanofiltration membrane under nanofiltration conditions comprising a pressure less than about 352.2 lt / cm2 per day, preferably wherein the pressure is less than about 35.15 kg / cm2.; and a temperature of less than about 95 ° C, preferably where the temperature is less than about 80 ° C. The nanofiltration step of the present invention can be operated as a batch operation or continuous operation. A batch operation can be performed using a single closed nanofiltration membrane element or a plurality of nanofiltration membrane elements in parallel or in series, wherein a starch hydrolyzate fed as a starting material is fractionated through a membrane of adequate nanofiltration at a pressure and a temperature within the depression scales previously described and temperature scales, respectively, the retentate being recycled back to the feed tank to coat the ED of the material in the feed tank and thus obtain a hydrolyzate of starch with low ED having the desired ED value. In continuous operation, the starch hydrolyzate as a feed of starting material can be pumped through a series of membrane elements in a serial or series-parallel fashion for the fraction of reducing the ED of the starch hydrolyzate and obtaining a hydrolyzate of starch with low ED having the desired ED value. In one embodiment, the process of the present invention comprises refining the starch hydrolyzate having an ED greater than about 18. Then, said starch hydrolyzate is refined before fractionation using nanofiltration membrane. The refining step takes place before the separation of the membrane. In another embodiment, the process of the present invention comprises refining the starch hydrolyzate with low ED. The step of refinement takes place after the separation of the membrane. Obviously, it is possible to have the refinement steps both before and after the separation step of the membrane. For purposes of the present invention, refining more preferably comprises a conventional charcoal treatment and a conventional ion exchange treatment of the material to be refined in order to discolor and remove the ash from the material. Referring to Figure 1, at the beginning of the process, the starting material, ie the corn syrup at about 30% dry substance, is transferred into the feed tank (1). The corn syrup starting material preferably has an ED greater than about an ED of 18. The starting material as a feed is pumped through the feed pump (2) to a membrane element. A recirculation pump (3) is used to increase the speed of the transverse flow of the liquid. The feedstock is subjected to membrane fractionation by the permeation of small molecular weight materials such as oligosaccharides below DP5 through a nanofiltration membrane which retains large molecular weight materials. The permeate (6) of the membrane (5) is taken from the system. The retentate (7) of the membranes (5) is recycled (8) back to the feed tank (1) until the ED of the retentate (7) reaches the target, preferably less than 20 ED. Said retentate (7) is recycled (8) to the feed tank (1) during batch processing, the dry substance is increased. Therefore, water dilution (9) needs to be added in order to maintain high membrane fractionation flow. In continuous processing, the valve (10) always closes, and the recycle fluid is not returned to the tank.

In one embodiment of the present invention, the starch hydrolyzate with low ED that is produced comprises a liquid, the starch hydrolyzate with low ED having an ED of less than about 25. The starch hydrolyzate with low liquid ED preferably comprises a content of dry solids within a range of approximately 50% to around 85%. The starch hydrolyzate with low liquid ED preferably has a viscosity at 70% dry solids content and at 25 ° C less than about 30,000 centipoises (cp), measured using a Brookfield viscometer. For the purposes of the present invention, at viscosity at 70% dry solids by weight and at 25 ° C more preferably it is between about 4,000 cp and 20,000 cp. The starch hydrolysates with low ED produced in accordance with the present invention have a lower viscosity than the converted material of acid or enzyme conventionally having substantially the same ED. For the same ED product the viscosity increases with a higher concentration of long chain molecules (e.g., DP21 + oligosaccharides). While not wishing to be bound by any particular theory, the lower viscosity property of the products produced according to the present invention is attributed to its lower weight concentration of DP21 + which was only about 11% at about 14 ED. This is in contrast to conventionally converted ED 14 maltodextrin having at least about 40% DP21 +. In general, a nanofiltration membrane produced ED 18 maltodextrin and 70% dry substance at 25 ° C has a viscosity of less than about 8,000 centipoise. While maltodextrin conventionally converted by enzyme to the same ED, the same dry substance and the same temperature has a viscosity of about 20,000 centipoise (cp). The low viscosity of the starch hydrolysates with low ED and the maltodextrins produced according to the present invention allows said products to be concentrated or evaporated to approximately 80% dry solids content, or higher without any handling difficulty. A high content of dry substance, e.g., equal to or above about 75%, results in an additional advantage of the starch hydrolysates with low ED of the present invention which is stably microbial. The water activity of starch hydrolysates with low ED and the maltodextrins produced according to the present invention with a dry solids content is about 75% by weight, is less than about 0.86 at room temperature, which is sufficient stable to embark in liquid form. The starch hydrolysate product with low ED of the present invention preferably has an ED of less than about 25, a polydispersity index of less than about 5, less than about 10% by weight of the concentration of mono- and di-saccharides and less than about 40% by weight of the concentration of oligosaccharides with higher degree of polymerization around 21. Preferably, the starch hydrolyzate product with low ED comprises starch hydrolyzate with low liquid ED having a moisture content within a scale from about 50% to about 85% and / or a viscosity at 70% dry solids content and at 25 ° C less than about 30,000 cp, preferably where the viscosity is within the range of about 2,000 cp to about 25,000 cp and more preferably from about 4,000 cp to about 20,000 cp. In accordance with the present invention, the preferred low ED starch hydrolyzate products have an ED within a range of about 4 to about 20; the concentration of mono- and di-saccharides is less than about 10% by weight; and the concentration of oligosaccharides having a degree of polymerization greater than about 21 is less than about 35% and preferably less than about 30% by weight. Starch hydrolysates with low ED produced according to the present invention exhibit stability of liquid solution, low viscosity and can remain substantially in free deterioration during extended periods, even with dry solids content, in refrigeration and ambient temperatures. The starch hydrolysates with low ED and the maltodextrins of the present invention usually have an ED that is substantially not above 25 for starch hydrolysates with low ED and are not substantially above 20 for maltodextrins. The starch hydrolysates with low ED and the maltodextrins of the present invention preferably have an ED within the range of 4 to 20. A normal maltodextrin produced according to the present invention generally has an ED within the range of about 8 to As used herein, the starch hydrolyzate with low ED means a starch hydrolyzate having an ED not greater than about 25. Maltodextrin is a starch hydrolyzate having an ED not greater than about 20. The dextrose equivalent term (ED), referred to herein, as defined as the reduction value of the maltodextrin hydrolyzate or starch, the material compared to the reduction value of an equal dextrose weight, expressed as a percentage of the base in dry measured by the School method described in Encyclopedia of Industrial Chemical Analysis, Vol. 11, p. 41-42. The term "polydispersity index", also referred to as "polymolecularity index", is defined as the ratio of Mp / Mn, where Mp is the weight average molecular weight and Mn is the number average molecular weight. This relationship allows the global dispersibility of the molecular weights of a polymer mixture to be characterized. In practice, the values of Mp and Mn can be determined by gel permeation chromatography, which is a technique well known to those skilled in the art.

The terms "without deterioration", "free of deterioration" and the like are intended to be synonymous with "non-nebulous" which is defined as having less than about 0.3 absorbance and preferably an absorbance less than about 0.1, measured spectrophotometrically at about 600 nm, after storage at room temperature, that is, approximately 23 ° C, for about three months. As used herein, the terms "stable", "stability" and the like refer to microbial stability and / or physical stability. Although the present invention is described using corn starch hydrolysates, also referred to as "corn syrup", corn derivative with normal amylose content can be used as starting materials, glucose syrups and other starch hydrolysates of various cereals. (e.g., wheat), tubers (e.g., potato) or other sources of starch (e.g., chicory) and other types (e.g., waxy). The starch hydrolysates with low ED of the present invention have a narrow saccharide distribution. In general, the polydispersity index is less than about 5 and the amount of monosaccharides and disaccharides is less than about 10% by weight and the amount of polymerization oligosaccharides greater than about 21 is less than about 40% by weight, preferably less that about 35% by weight and more preferably less than about 30% by weight.

The starch hydrolyzate with low ED can be used to produce a mixture comprising starch hydrolyzate with low ED which is substantially non-retrograde, with at least one other substance in a predetermined mixing ratio to result in a hydrolyzate mixture of starch with low ED. The other substance is preferably a carbohydrate selected from the group consisting of sugar alcohols such as sorbitol, mannitol, xylitol, maltitol, erythritol, isomalt and hydrogenated starch hydrolysates (e.g., maltitol syrups), propylene glycol, glycerin and saccharides such as inolina, glucose syrup, maltose syrup and fructose syrup, lactose, eritosa, xylose and isomaitosa. Preferably the mixture of starch hydrolyzate with low ED produced according to this embodiment of the present invention is substantially non-retrograde. The starch hydrolysates with low ED and maltodextrins produced by the nanofiltration membrane fractionation process of the present invention, can be mixed or in some way combined with said substances to obtain a mixed product having a lower viscosity and water activity than a mixed product using conventional maltodextrins of substantially the same ED. The process of the present invention also involves drying the starch hydrolyzate with low liquid ED to result in a substantially dry product. Preferably the resulting low ED starch hydrolyzate has a moisture content of less than about 10% by weight. The drying media that can be used for the purpose of dehydrating the starch hydrolyzate with low liquid ED in accordance with the present invention includes conventional dehydration apparatuses and methods suitable for dehydrating liquids having characteristics, such as viscosities, similar to those of starch hydrolysates with low ED. Preferably the drying comprises drying by spraying or extrusion. The process of the present invention also involves hydrogenating the starch hydrolyzate with low ED having an ED of less than about 25 to result in a starch hydrolyzate with low hydrogenated ED, preferably wherein the starch hydrolyzate with low hydrogenated ED comprises starch hydrolyzate with low liquid hydrogenated ED or wherein the hydrolyzed starch with low hydrogenated ED substantially comprises starch hydrolyzate with low substantially hydrogenated ED. A co-hydrogenation of a mixture of starch hydrolyzate with low ED can also be directed. Preferably, this co-hydrogenation comprises mixing a starch hydrolyzate with low ED produced by the nanofiltration according to at least one other substance, preferably a carbohydrate as defined above, to form a mixture of starch hydrolyzate with low ED; and hydrogenating the starch hydrolyzate mixture with low ED to result in a mixture of starch hydrolyzate with low hydrogenated ED. To obtain the corresponding hydrogenated products, ie starch hydrolysates with low hydrogenated ED and mixtures described above, they can be subjected to conventional hydrogenation.

For example the starch hydrolyzate with low ED that results from the fractionation of nanofiltration can be subjected to the nickel method Raney hydrogenation under suitable conditions for the same.

Therefore, according to the present invention, the starch hydrolyzate with low ED and the maltodextrin products can be liquid or substantially dry, hydrogenated or unhydrogenated, substantially undamaged or deteriorated, and mixed with a carbohydrate or other substances or do not. The hydrogenated form of the starch hydrolysate with low ED and maltodextrin can be obtained by conventional hydrogenation of the starch hydrolyzate with low ED, by hydrogenation of starch hydrolyzate starting material or by the co-hydrogenation of a mixture comprising hydrolyzate of starch with low ED and other substances, which can be carbohydrates. Referring now to Figure 1, according to the process of the present invention, a conventionally converted corn starch hydrolyzate, also referred to herein as "syrup" and "corn syrup", with an ED greater than about ED of 18 and preferably greater than about ED of 21 and in particular within a scale of about ED of 28 to ED of 50, is fed into a nanofiltration membrane as shown in Figure 1, for fractionation. The permeate of the membrane is taken from the system and the retentate is recycled to the feed tank for additional concentration. Once the value of the retentate ED reaches a white level, which is less than about ED of 25, preferably an ED within a scale of 8 to about 20, the valve (11) in Figure 1 opens and the valve (10) closes. The retentate is sent forward in a storage tank as a product. Operating pressures and temperatures are important parameters of the process. For the purposes of the present invention, the operating pressure of the system is controlled at less than about 42.18 kg / cm2 and preferably below about 35.15 kg / cm2. For the purposes of the present invention, the operating temperature of the system is controlled at less than about 95 ° C and more preferably below 80 ° C. For the purposes of the present invention, a pH between about 2 to about 10 is preferred; and a pH between about 3 to about 8 is more preferred. More specifically, in the process of the present invention, a starting material converted from acid, such as corn starch hydrolysates (syrup) with an ED within a scale of about ED from 25 to about ED of 63, but preferably Within a preferred range of about 25 ED to about ED of 42, it is pumped through a nanofiltration membrane for the fractionation at a trans-membrane pressure of less than 35.15 kg / cm2, the permeate is removed from the system and the Retentate is recycled to the feed until the ED of the syrup has been reduced to a desired level which is less than about ED of 25 and preferably within a range of about 8 to about 20. For the purposes of the present invention, the ED of the starch hydrolyzate starting material is not less than about ED of 18, preferably not less than about ED of 21, more preferably an ED within a scale of about 25 to about 63 and even more preferably an ED within a range of about 25 to about 42. For purposes of the present invention, the preferred starch hydrolyzate comprises a member selected from the group consisting of starch hydrolyzate corn, wheat starch hydrolyzate, starch hydrolyzate of roots and waxy corn starch hydrolyzate and the like most preferably wherein the starch hydrolyzate comprises corn syrup. The raw material used can be its corresponding modified or unmodified form, although starches from any source of starch can be used. For the purposes of the present invention, the starch hydrolyzate comprising an ED not less than about an ED of 18 is made by a conversion process selected from the group consisting of a one step conversion and multi step conversion, preferably wherein the conversion process is selected from the group consisting of acid conversion, enzyme conversion and mixed conversion of acid and enzyme and more preferably comprises conversion of acid and conversion of enzyme-enzyme. The starch hydrolysates with low ED and maltodextrins of the present invention, where either in the form of syrups or dry powder, are particularly suitable for use in food and beverage products, maltodextrins are especially useful in syrups with low ED stable The characteristics of the starch hydrolysates with low ED and maltodextrins produced in accordance with the present invention form the products of the invention particularly suitable for applications as vehicles for coloring agents, flavors, fragrances and essences and synthetic sweeteners; spray-drying adjuncts for coffee extracts and tea extracts; agents for the provision of volume, body and dispersants in synthetic creams or coffee bleaches, ingredients that promote moisture retention in bread, pasta and meats; components of dry soup mixes, bakery mixes, mixtures and combinations of spaces and cover powders, mixtures for dressings, mixes for frozen sauces and dairy foods and fats imitations. Furthermore, they are useful for the formulation of tabulation compounds that can be used in food products or pharmaceuticals, anti-caking agents, whipped products, protective coatings, agglomeration aids, low-calorie foods and beverages. In addition, the starch hydrolysates with low ED and maltodextrins of the present invention are particularly suitable for use with beverage ingredients, food ingredients, animal feed ingredients, pharmaceutical ingredients, nutritional ingredients, cosmetic ingredients and industrial ingredients. The present invention is also directed to a process for producing a substantially thermal and stable emulsion in the storage life. In a preferred embodiment of the present invention, the starch hydrolyzate with low ED used to produce the emulsion comprises starch hydrolyzate with low liquid ED. According to this embodiment, the process comprises combining the starch hydrolyzate product with low ED of the present invention, in its hydrogenated or non-hydrogenated form, as described herein with an effective concentration of at least one other ingredient to give as a result a stable emulsion. For the purposes of the present invention, the ingredient preferably comprises at least one member selected from the group consisting of organoleptic (e.g., flavors or fragrances), agricultural chemicals (e.g., insecticides, fertilizers), enhancers of flavor (e.g., acetaldehyde, citral), high intensity sweeteners (e.g., aspartame, acesulfame potassium) and active pharmaceutical substances (e.g., growth hormones, maturation inhibitors). The ingredient can be in pure form, in combination with other substances, with or without vehicles. The proportion of ingredient and in particular of flavoring agent, which will be incorporated in the emulsion can be varied depending on the desired strength in the final product.

Generally, the effective concentration of the ingredient is within the range of about 0.1% to about 50% by weight.

According to the present invention, the mixing of starch hydrolyzate with low ED of the present invention the ingredient can be achieved by suitable means such as mixing, v. gr. , starch hydrolyzate with low ED evaporated to a dry substance content on a scale of about 1% to about 70%, with an ingredient in a mixing tank. Other ingredients may be present in the emulsion of the present invention. These include emulsifiers, viscosity control agents, e.g. , C2-C4 alkylene glycols such as ethylene glycol, propylene glycol, butylene glycol, etc. , in effective amounts, generally below 15%. In another embodiment of the present invention, the emulsion further comprises an emulsifying amount of an emulsifier. For the purposes of the present invention, the emulsifier, for example, is selected from the group consisting of nonionic surfactants (eg, sorbitan esters), lecithin, ionic surface active agents (eg, sodium dodecyl sulfate). ) and amphoteric agents (e.g., n-alkylbetaines).

According to the invention, the substantially thermal and storage-stable emulsion comprises the starch hydrolyzate with low ED of the invention as an aqueous matrix and at least one other ingredient. In a preferred embodiment. The content of the ingredient is preferably less than about 65% by weight. The emulsion of the present invention may be an oil-in-water emulsion or a water-in-oil emulsion, the emulsion comprising an emulsifier in the aqueous matrix. In particular, the emulsion may be an oil-in-water emulsion comprising the ingredient as an internal oil phase and the starch hydrolyzate with low ED of the invention as an external aqueous matrix. The emulsions produced in accordance with the present invention exhibit improved emulsion stability purchased with the emulsions produced using the conventional low ED starch hydrolysates or maltodextrins. In addition, the present invention is also directed to a process for producing a substantially dry ingredient encapsulate comprising mixing the starch hydrolyzate with low hydrogenated or unhydrogenated ED of the present invention with an effective concentration of at least one ingredient to form a mix and dry said mixture. More especially, the process according to the present invention involves a first step comprising forming an aqueous matrix composition comprising starch hydrolyzate with low ED of the present invention, in its hydrogenated or non-hydrogenated form. Said composition is useful as a matrix for encapsulating and entrapping the previously defined ingredient in a glassy amorphous structure and is superior in performance compared to powdered maltodextrins or analogous formulation used in the encapsulation industry. In a preferred embodiment, the starch hydrolyzate with low ED comprises a dry solids content within a range of about 25% to about 55% by weight. The second step of the process according to the present invention comprises mixing at least one other ingredient with the matrix composition to form a mixture. In a preferred embodiment, the ingredient is within a range of about 0.1% to about 50% by weight. The mixture may comprise an emulsion and may contain an emulsifier that depends on the nature of the ingredient. The mixing can be achieved by any suitable means as are conventionally used for that purpose. The process of the present invention also involves drying the mixture to result in an encapsulation of substantially dry ingredient. Said drying preferably comprises drying by spraying or extrusion. Therefore, the resulting substantially dry ingredient capsulate comprises at least one ingredient treated in an amorphous matrix of the starch hydrolyzate with low ED of the present invention.

EXAMPLES The present invention will now be described in greater detail by means of the following representative examples. EXAMPLE 1 An acid-converted corn syrup having ED of about 42 and a dry solids content of about 24.7% by weight was pumped through a fractionation membrane using a one-step nanofiltration process. The retentate was recycled to the feed tank until the ED was reduced to ED 14.5. A nanofiltration membrane of mixed thin-film material, ASP-40, made by Advanced Membrane Technology, Inc., San Diego, California, was used for the test operations. The ASP 40 membrane has the following characteristics: Membrane material: polysulfone sulphide or polysulfone thin film mixed material with a nonwoven polyester reinforcement Configuration: Spiral winding Surface area: approximately 5.3 m2 (a diameter of 10.16 cm and a length of 101.6 cm) Operating pressure: up to approximately 42.18 kg / cm ' Operating temperature: up to approximately 60 ° C Operating pH scale: approximately 2-11 Maximum Chloride: approximately 200 ppm Rejection Specification: NaCl = 30-40%, Lactose = 45-65% The preparation of starch hydrolyzate starting material with ED of 42 was achieved by conventional acid conversion methods. The conversion process was terminated when the ED value of the converted corn starch material reached approximately 42. The corn starch material converted with a resulting ED of 42 was rinsed using a centrifuge to remove residual oil and protein. After this, a carbon treatment and an ion exchange refining process were carried out to decolorize and remove the ash from the material. Finally, the material was evaporated to a dry substance content of about 70% by weight. 55.5 liters of corn syrup converted with acid having an ED of 42 was fed into the feed tank, e.g., as shown in Figure 1 and diluted to a dry substance content of about 23.7% by weight . The processing line was a single-stage system having a nanofiltration membrane element having a diameter of 10.16 cm. The fractionation process was carried out as a batch operation. The permeate was removed from the system and the retentate was recycled back to the feed tank. The ED value was periodically monitored. The dilution water was added periodically in the feed tank to keep the dry substance content of the material below about 50% by weight. The recycled retentate was terminated when the ED value of the retentate reached approximately an ED of 15. The retentate was then sent forward and recovered in a storage container as a product. The product had a collection volume of 48.1 liters and a dry substance content of about 50.5% by weight. The processing line was operated at a pressure of approximately 33.3 kg / cm2 and a temperature of around 50 ° C. The permeate flow was 1 1 .6 (LCD) at the beginning and 0.87 LCD at the end of the fractionation. The resulting maltodextrin is substantially free of deterioration, had an ED of 14.5 and the following carbohydrate profile: The maltodextrin described above was further evaporated using a rotary laboratory vacuum evaporator to obtain a starch hydrolyzate with low ED having different solids content. The starch hydrolyzate products with low ED were evaluated in a designed experiment where the variables and their scales were: dry solids content within the range of approximately 65% to 75% by weight; storage temperature within the range of about 7 ° C to about 49 ° C; sorbic acid content within the range from about 0% to about 0.15% by weight; pH within the range of about 2.8 to about 3.5. The color, direct content of nebulosity (represented by absorbance at 600 nm) of bacteria, yeast and mold were tested at the beginning and after each month of storage. After 4 months of storage, the 28 samples tested are still transparent and free from deterioration. The polydispersity index of the resulting maltodextrin is 1.59. the viscosity of the resulting maltodextrin according to the present invention is 65,000 cp at 75.3% dry solids and 7450 cp at 70% dry solids, which is lower than conventionally converted maltodextrin as listed in Table 1 in the example 6 EXAMPLE 2 In this example, an acid-converted corn syrup with ED of 36 was used as the starting material. This starting material was produced by the same process as in Example 1 except that the conversion ended when the ED value of the corn syrup material converted with acid reached approximately ED 36 and the converted material was not completely refined by ion exchange. . The same processing system and the nanofiltration membrane were used as in Example 1 to produce the sample of this example. 111 liters of corn syrup with ED of 36 at a dry substance content is about 80% by weight were fed into the feed tank, e.g., as shown in Figure 1 and diluted to a content of dry substance of approximately 32.6% by weight. The fractionation process was carried out as a batch operation. The permeate was taken from the processing system and the retentate was recycled back to the feed tank. The ED value was periodically monitored.

The dilution water was added periodically in the feed tank to keep the dry substance content of the material below about 50% by weight. The recycled retentate was terminated when the ED value of the retentate reached approximately an ED of 18. The retentate was then sent forward and recovered in a storage container as a product. The recovered product had a total recovered volume of about 85.1 liters and a dry substance content of about 51.3% by weight. Operating conditions included a pressure of approximately 33.75 kg / cm2 and a temperature of around 50 ° C. The permeate flow was 4.7 liters LCD at the beginning and 0.87 LCD at the end of the fractionation. The resulting maltodextrin has an ED of 17.2 and the following carbohydrate profile.

The recovered maltodextrin product was further evaporated using a rotary laboratory vacuum evaporator at a dry solids content of 70.2% and 75.5% by weight. Samples of the maltodextrin product for each of this dry solid content were stored at room temperature for 2 months and analyzed. Both remained transparent and free from deterioration. The polydispersity index of the resulting maltodextrin is 2.45. The viscosity of the maltodextrin according to the present invention is from 6930 cp to 70% dry solids by weight and at 25 ° C. EXAMPLE 3 A corn syrup converted with acid has an E.D. of approximately 42 and 43.5% dry solids content is pumped through a nanofiltration membrane for fractionation using a one-step nanofiltration pilot plant as shown in the figure. The retentate was recycled to the feed tank until the ED is reduced to 14.9. The pilot plant used to produce sample products was formed by Niro, Inc., Hudson, Wisconsin. A polyamide membrane of mixed thin-film material, GH, was used for the test operations and was made by Desalination System, Inc., Vista, California. The GH membrane has the following characteristics.

Membrane material: Polyamide of mixed film material. thin Configuration: Spiral winding Surface area: approximately 5.3 m2 (a diameter of 10.16 cm and a length of 101.6 cm) Operating pressure: up to 42.18 kg / cm2 Operating temperature: up to 50 ° C Operation pH scale: 2 -11 Maximum Chloride: 20-50 ppm day Rejection Specification: 50% MgSO4 at 10.54 kg / cm2 and 25 ° C The corn syrup food material with ED of 42 converted with acid in this example was corn starch. Corn starch having a dry substance within the range of about 34 to 40% by weight was hydrolyzed using hydrochloric acid at a pH of 1.8 and at a temperature of about 128 ° C. The conversion process was terminated when the ED value of converted corn syrup material reached approximately 42. The corn material converted from corn syrup converted with ED acid of 42 resulting was rinsed using a centrifuge to remove the oil and protein residual. After that, a process of carbon treatment and ion exchange was carried out to discolor and remove the ashes from the material. Finally, the material was evaporated to a dry substance content of about 80% by weight. 37 liters of corn syrup converted with acid having an ED of 42 was fed into the feed tank, e.g., as shown in Figure 1 and diluted to a dry substance content of about 43.5% by weight . The process was a one-stage system with a nanofiltration membrane element having a diameter of 10.16 cm. The fractionation process was carried out as a batch operation. The permeate was removed from the system and the retentate was recycled back to the feed tank. The dilution water was added periodically in the feed tank to keep the dry substance content of material below about 50% by weight. Retentate recycling was terminated when the ED value of the retentate reached approximately 15. The recovered product had a volume of 29 liters and a dry substance content of approximately 52.55% by weight. The process was operated at a pressure of approximately 34 kg / cm2 and at a temperature of approximately 50 ° C. The permeate flow was 4.8 LCD at the beginning and 0.96 LCD at the end of the fractionation. The resulting maltodextrin has an ED of 14.9 and the following carbohydrate profile.

The above maltodextrin was further evaporated using a rotary vacuum evaporator at 70% by weight dry solids content for storage stability tests. Two samples, one without pH adjustment (approximately pH = 4.5) and one with pH adjusted to 3.0 using 7% HCl, were prepared for storage tests. After 4 months of storage at ambient temperature conditions, both samples were still as clear as the original and free from deterioration. There was not so little microbial growth.

The polydispersity index of the resulting maltodextrin is 1.54. The maltodextrin viscosity of this example is 7116 cp at 70% dry solids by weight and at room temperature. EXAMPLE 4 The starting material for the nanofiltration membrane fractionation in this example was corn syrup converted with enzyme-enzyme with an ED of 23 made by, in a first step, liquefying with starch at an ED of 14 using bacterial alpha amylase enzyme (Thermamyl T-120, obtained from Novo Nordisk) and in the second step, saccharifying the resulting liquefied material at a solids content of approximately 30% by weight and at a temperature of approximately 65 ° C using bacterial alpha amylase ( enzyme of Termamayl T-120, Novo Nordisk). The conversion process was terminated when the ED value of the converted material reached approximately 23. The corn starch hydrolyzate converted with enzyme-enzyme was rinsed using an ultrafiltration membrane to remove oil and protein. The same processing system and nanofiltration membrane were used as in Example 1 to produce the maltodextrin of this example. 74 liters of corn syrup with ED of 23 was fed to a dry solids content of about 305 by weight in the feed tank, e.g., as shown in Figure 1. The fractionation process was carried out. in a batch operation. The permeate was taken from the processing system and the retentate was recycled back to the feed tank. The ED value was periodically monitored. The dilution water was added periodically to maintain the dry solids content of the feed tank material at less than about 40% by weight. The recycling of the retentate was terminated when the ED value of the retentate reached approximately 17. The retentate was then sent forward. After this, a carbon treatment and an ion exchange refining process were carried out to decolorize and remove the ashes from the retentate. The retentate was then recovered in a storage container as a product. The recovered product had collected volume of 25.9 liters and a dry substance content of approximately 47% by weight. The operating conditions included a pressure of approximately 35.15 kg / cm2 and a temperature of approximately 45C. The permeate flow was 5.19 LCD at the start and 2.6 LCD at the end of the fractionation. The resulting maltodextrin has an ED of 16.7 and the following carbohydrate profile.

The recovered maltodextrin product was further evaporated using a rotary laboratory vacuum evaporator and a dry solids content of 67% by weight. The maltodextra product was stored at room temperature for 2.5 months and analyzed. The maltodextrin product remained clear and free of retrogradation. The polydispersity index of the resulting maltodextrin is 4.3. the viscosity of the resulting maltodextrin according to the present invention is 8330 cp at 25 ° C and 70% by weight dry solids, which is lower than the conventionally converted maltodextrin listed in Table 3 in Example 6. EXAMPLE 5 were fed 111 liters of corn syrup with ED of 42 converted with acid into a single-stage nanofiltration membrane processing system, e.g., as shown in Figure 1 (NIRO Hudson, Wl), with a spiral nanomembrane . 16 cm (ASP40 of Advanced Membrane Technology, CA). 48.1 liters of clear liquid retentate that has an ED of 13.5 were obtained. The process was carried out at 35.15 kg / cm2 and 45 ° C. The membrane used was made of a polysulfone polysulfone with a molecular weight cutoff of about 1000 Daltons. During the process, the permeate flow was removed from the system and the retentate flow was recycled to the feed tank. The continuous test until ED of the retentate reached approximately an ED of 14. The dry solids content of the resulting product was approximately 50% by weight and furthermore it was evaporated to a dry solids content of approximately 70% by weight using an evaporator of rotating vacuum at laboratory scale. The resulting product was analyzed using a Brookfield viscometer and CLAR. The viscosity of the product analyzed is only less than about half the viscosity of the conventionally produced material having a similar ED and the carbohydrate profile was unique in that it had only 2.2% of mono and di-saccharides and 11.6% by weight of oligosaccharides with DP > 21. The product analyzed at 71% by weight of dry substance was stored at ambient temperature conditions and remained transparent for more than four months. EXAMPLE 6 The advantage of the viscosity of the present invention over conventionally converted maltodextrins with enzyme is shown in Table 1. In this example, the samples produced in Examples 1, 2, 3, and 4 were analyzed and compared with Glucidex ® 19, a conventional maltodextrin commercially available from ROQUETTE FRERES and Maltrin® M180, a conventional maltodextrin commercially available from Grain Processing Co., in terms of viscosity. Table 1. Viscosity (cp) at 25 ° C of maltodextrins While not wishing to be bound by any particular theory, it is thought that the advantage of the viscosity of the present invention over conventional maltodextrins was due to the narrow carbohydrate profile distribution. EXAMPLE 7 With reference to Example 6, the carbohydrate profile of the present invention, exemplified in Examples 1, 2, 3 and 4 has lower DP1 and DP2 as well as lower DP21 +, compared to commercial maltodextrins having a similar ED, as shown in table 2. Again in this example, the samples produced in Examples 1, 3, 3, and 4 were analyzed and compared with Giucidex® 19 and Maltrin? M180, as in Example 6, to determine their respective carbohydrate profiles and polydispersity (Mp / Mn) as shown in Table 2. Table 2. Carbohydrate profile by HPLC and Polydispersity (Mp / Mn) by CFG EXAMPLE 8 Three oil-in-water emulsions comprising orange oil flavor, lecithin and starch hydrolyzate with low ED representative of: (1) a conventional low ED starch hydrolyzate (DRI-SWEET15 manufactured by Roquette America, Keokuk, Iowa) ) having an ED of about 18, or (2) an unhydrogenated low ED starch hydrolyzate of the present invention having an ED of about 18 (LDESH), or (3) a hydrogenated form of the starch hydrolyzate with low ED of the present invention having an ED of about 18 (HLDESH, for its acronym in English), were prepared and evaluated for stability. The preparation of the emulsion was carried out at a temperature of about 22 ° C to about 30 ° C. In a first step to prepare the emulsions, 3g of lecithin (emulsifier) was mixed with 97g of the starch hydrolyzate product with respective low ED having a dry solids content of about 45% by weight in a ultra high speed homogenizer at 20,000. rpm for 3 minutes. In a second step, while continuing to mix at 20,000 rpm, 5 g of orange oil flavor was drip added to the mixture for 5 minutes. After completing the addition, mixing was continued for another 2 minutes. The resulting emulsions were determined to comprise, in weight percent: 4.8% orange oil flavor, 2.8% lecithin, 50.8% water and 41.6 dry solids bases of DRI-SWEET® or LDESH or HLDESH. The 20 mL samples of each resulting emulsion were transferred into individual flasks of the type used for chromatographic top space analysis and were crowned and sealed with a silicone-teflon septum. Samples of each of the three emulsion compositions were then stored in the bottles under three different temperature conditions, i.e. about 22 ° C, 50 ° C and 60 ° C. Samples of the three emulsion compositions were stored under each of the three temperature conditions and evaluated for stability. The results of the periodic evaluation were presented in Table 3. Table 3. Emulsions comprising Flavoring of Orange Oil, Lecithin and DRI-SWEET ~ or LDESH or HLDESH 2) that is, appearance of a cream-like layer on the surface of the emulsion (3) ie a colored by-product that is observed to form on the top of the emulsion.

EXAMPLE 9 Three encapsulated compositions comprising orange oil flavor, lecithin and starch hydrolyzate with low ED representative of: (1) a conventional low ED starch hydrolyzate (DRI SWEET®, manufactured by Roquette America, Keokuk, Iowa) has an ED of about 18, or (29) an unhydrogenated low ED starch hydrolyzate of the present invention having an ED of about 18 (LDESH), or (3) a hydrogenated form of starch hydrolyzate with low ED of the present invention having an ED of about 18 (HLDESH), were prepared and evaluated in this example. In a first step, a composition comprising an emulsion was prepared by mixing 6 g of lecithin with 594 g of the starch hydrolyzate product with respective garlic ED having a dry solids content of about 45% by weight in a ultra high speed homogenizer. 20,000 rpm for 3 minutes. While mixing was continued, 30 g of orange oil flavor was added dropwise to the mixture for 5 minutes. After the addition was complete, mixing was continued for another 2 minutes. The resulting emulsion was determined to comprise, weight percent, 4.8% orange oil flavor, 0.95% lecithin, 51.8% water, and 42.4% dry solids bases of DRI-SWEET 'or LDESH or HLDESH. In a second step, the resulting emulsion was fed to the feed nozzle of a spray dryer, e.g., Büchi, CH, via a peristaltic pump. Compressed hot air provided atomization of the feed and drying of the drops in the dryer. The operating conditions of the spray dryer are summarized in Table 4. Table 4. Spray dryer operating conditions.

The fate of the flavor oil was determined by gas chromatography analysis and verified by mass balance. The following resultant spray dried flavor encapsulates prepared using non-hydrogenated hydrogenated forms of starch hydrolyzate with low ED of the present invention (LDESH and HLDESH, respectively) are powders generally comprised of non-crystalline spherical particles of amorphous material having a morphology. of continuous glassy film. The results obtained by examining various properties of the resultant spray-dried flavor encapsulation are summarized in Table 5.

Table 5. Encapsulates comprising Orange Oil Flavor and DRI-SWEET® or LDESH or HLDESH.

The resulting spray-dried flavor encapsulates comprising LDESH and HLDESH were found to have the following properties: spherical shape, powdery and amorphous material of continuous glassy film morphology with an average diameter size of about 10 to about 13 μm; structure without crystallinity with a glass transition temperature of about 8 ° C; High flavor oil retention, exceeding 70%; low surface oil content, which was below 0.05%; moisture content of approximately 3%; low water activity of about 0.157 to about 0.177; high oil stability and slow oxidation regime, measured by the formation of limoen oxide, in relation to those encapsulated with the same oil concentration and comprised of conventional starch hydrolyzate. Although only one illustrative embodiment of the invention has been described in detail, those skilled in the art will readily appreciate that many modifications are possible without departing materially from the teachings and novel advantages of this invention. Accordingly, all of these modifications are intended to be included within the scope of this invention as defined in the following claims. In the claims, the media clauses plus functions are intended to comply with the structures described herein by carrying out the recited function and not only the structural equivalents but also the equivalent structures.

Claims (16)

1. CLAIMS 1. A process for producing a starch hydrolyzate with low ED, the process comprising fractionating a hydrolyzate having an ED greater than about 18 using a nanofiltration membrane selected from the group consisting of Teflon membranes, stainless steel membranes, membranes of ceramic and polymeric membranes having molecular weight cut less than 4,000 daltons under effective nanofiltration conditions to result in a starch hydrolyzate with low ED having an ED less than about 25. The process of claim 1, in wherein the nanofiitration membrane is selected from the group consisting of polyamide membranes and polysulfone polysulfone membranes having a molecular weight cut within a scale of about 400 daitons to about 4,000 daltons, preferably within a scale of about 800 daltons to around 2,500 daltons. The process of claim 1, wherein the starch hydroiisate with low ED comprises a starch hydrolyzate with low substantially liquid non-retrograde ED, having an ED of less than about 25. 4. The process of claim 1, which it comprises the starch hydrolyzate with low ED to result in a starch hydrolyzate with low hydrogenated ED. 5. A starch hydrolyzate product with low ED comprising a starch hydrolyzate with low ED having an ED less than about 25 and having a polydispersed index of less than about 5. 6. A process to produce a substantially thermal and stable emulsion in the storage life comprising forming a mixture of the starch hydrolyzate with low ED of claim 5 with an effective concentration of at least one ingredient to result in an emulsion. The process of claim 6, wherein the effective concentration of the ingredient is within a range of from about 0.1% to about 50% by weight. The process of claim 6, wherein the starch hydrolyzate with low ED comprises a dry solids content within a range of about 1% to about 75% by weight. 9. The process of claim 6, wherein the emulsion further comprises an emulsifying amount of an emulsifier. 10. The process of claim 6, wherein the starch hydrolyzate with low ED is hydrogenated. 11. A substantially thermal and storage-stable emulsion comprising the starch hydrolyzate with low ED of claim 5 as an aqueous matrix and at least one other ingredient 12. The emulsion of claim 11, wherein the starch hydrolyzate with low ED is hydrogenated. 13. A process for producing a substantially dry ingredient encapsulation comprising the steps of: (1) forming an aqueous matrix composition comprising a starch hydrolyzate with low ED of Claim 5; (2) mixing at least one ingredient with the matrix composition to form a mixture; and (3) drying the mixture to result in an encapsulation of substantially dry ingredient. The process of claim 13, wherein the mixture comprises an emulsion. 15. The process of claim 13, wherein the starch hydrolyzate with low ED is hydrogenated. 16. An encapsulate of substantially dry ingredient comprising at least one ingredient trapped in an amorphous matrix of the product of claim 5.