EP3755163A1

EP3755163A1 - Method for producing resistant pea dextrin

Info

Publication number: EP3755163A1
Application number: EP19712261.7A
Authority: EP
Inventors: Gérald WESOLEK
Original assignee: Roquette Freres SA
Current assignee: Roquette Freres SA
Priority date: 2018-02-22
Filing date: 2019-02-21
Publication date: 2020-12-30
Also published as: JP7411558B2; CA3091315A1; CN111741685B; FR3077959B1; CN111741685A; US20200385494A1; JP2021515067A; WO2019162621A1; FR3077959A1

Abstract

The invention concerns a method for producing a resistant dextrin comprising: a) a step of dehydration and acidification of a pea starch in order to provide a dehydrated and acidified pea starch composition; b) a step of heat treatment of the starch composition provided in step a) in order to form a dextrinised starch; c) one or more steps of treating this dextrinised starch in order to form the resistant dextrin; d) a step of recovering this resistant dextrin. The invention also concerns a resistant pea dextrin having a fibre content according to standard AOAC 2001.03 of more than 60%, that can be obtained, in particular, according to the method of the invention, and the use of same in a food or pharmaceutical composition.

Description

Title: Process for producing resistant pea dextrin

Field of the invention

The invention relates to a method of manufacturing resistant dextrins, a new resistant dextrin and the use of this new resistant dextrin for pharmaceutical and food applications. Technical problem

Anxious to find beneficial solutions for its health and well-being, the modern consumer is looking for food and dietary supplements to fulfill these objectives.

Among the ingredients for providing this type of food, those comprising fibers are of particular interest. In the recent evolution of diets, the consumption of foods comprising these fibers, including soluble dietary fiber, has tended to decrease. This is particularly due to the fact that the agri-food industry has grown strongly in recent decades due to consumer demand for prepared products and that few fiber-based products that can be easily used by this industry have been proposed during this period.

Resistant dextrins are carbohydrate compositions comprising soluble dietary fiber. They have many advantages, such as the nutritional benefits below. In addition to the fact that the resistant dextrins are low in calories, they provide a general well-being and in particular a beneficial effect on the health of the intestine. Moreover, these soluble dietary fiber can reduce the blood sugar level developed during the ingestion of sugary foods; this can be particularly advantageous especially for diabetic consumers. The resistant dextrins also have other functional advantages: their texturing function makes it possible to provide foods of equivalent texture to sweet and / or fatty foods, while having reduced amounts of fat and / or sugar. In addition, the resistant dextrins, which are generally in the form of liquid aqueous solutions or in the form of powders, have, for the food industry, ease of use in food manufacturing processes. In the present Application, a method of manufacturing a resistant dextrin is a process comprising a heat treatment step, called "dextrinification" step, of a starch composition to form a dextrin, the dextrin thus obtained then undergoing different subsequent processing steps. These possible subsequent processing steps include chemical and / or enzymatic treatments, separation and purification.

A dextrinification step of a starch composition can be carried out at high dry matter and in acidic conditions. In the particular case of the resistant dextrins, this dextrinification step is generally carried out by a heat treatment under specific conditions allowing the formation, in large quantities, of so-called "atypical" bonds thus forming at this stage a so-called "starch" starch. dextrinified ". These atypical bonds are bonds other than alpha 1-4 and alpha 1-6 bonds that are naturally and predominantly present in starch.

It has been observed by the Applicant that once this dextrinified starch is formed, the subsequent processing steps mentioned above could be problematic, especially on an industrial scale, these problems leading to production stoppages creating productivity losses and therefore losses. economic. In particular, the process for producing the resistant dextrins generally comprises a step of filtering the dextrinified starch; however, during this filtration step, the passage of this dextrinified starch may cause after a certain time clogging filters. This clogging can cause a loss of filtration flow and thus a loss of productivity. Moreover, it is also necessary, when this flow becomes too low, clean the filter or replace it, this leading to a stop production of the resistant dextrin, which is particularly troublesome in the context of a continuous process of manufacturing of this resistant dextrin. A similar problem also arises when the subsequent treatment step consists of a step of passing dextrinified starch over resins, this step possibly being, for example, a demineralisation step or a fractionation step. In addition to the fact that the clogging of these resins decreases the flow rate, it is also necessary to clean or change these resins so as to recover the initial efficiency of the process.

Commercially resistant dextrins are generally made from corn (for example, Nutriose® FM products sold by Roquette® or Fibersol® marketed by Matsutani®) or wheat-based products (Nutriose F B®).

Methods of manufacturing these resistant dextrins have been described in EP 0538146, EP 0530111, EP 0988323, EP 1006128 and EP 2820050. None of these documents describe the aforementioned problems and no teaching is included to remedy them. . Thus, there is no incentive to change this teaching, in particular to solve the problems that occurred during the subsequent processing steps mentioned above.

DE 10102160 A1 discloses a method of manufacturing high molecular weight resistant starch from leguminous starch. This process comprises enzymatic treatment using a pullulanase in aqueous solution with a low dry matter content (aqueous solution at 20% solids content). This resistant starch is not a resistant dextrin which comprises large amounts of fibers and large amounts of different linkages of alpha 1 -4 bonds. The process also does not include starch dehydration step and heat treatment of this dehydrated starch.

FR 2 955 861 A1 discloses soluble branched glucose polymers having alpha 1 -4 and alpha 1 -6 linkages, with an alpha-6 linkage content of between 7 and 10%, a reducing sugar content between 25 and 35%, as well as a molar mass Mw of between 50,000 and 150,000 daltons. This glucose polymer is not a strong dextrin that includes large amounts of fiber and large amounts of different bonds from the alpha 1-4 bonds.

Document FR 2 764 294 describes the production of acariogenic polysaccharides comprising an extrusion step at a temperature of between 140 and 230 ° C. of a dehydrated and acidified starch.

It would therefore be advantageous to find new resistant dextrines but also methods of manufacture in which the manufacturing process is facilitated.

By carrying out numerous studies with a view to solving the above-mentioned problems, the Applicant has succeeded in providing new resistant dextrins obtained from pea starch. Advantageously, the method of manufacturing these resistant dextrins is easy to implement. In particular, fewer problems are observed during the subsequent processing steps in the dextrinification step compared to the methods of the prior art.

Summary of the invention

The invention thus relates to a process for producing a resistant dextrin comprising: a) a step of dehydrating and acidifying a pea starch to provide a dehydrated and acidified pea starch composition; b) a heat treatment step of the starch composition provided in step a) to form a dextrinified starch;

c) one or more steps of treating this dextrinified starch to form the resistant dextrin;

d) a step of recovery of this resistant dextrin.

The method of manufacturing acariogenic polysaccharides of document FR 2,764,294 described above does not use pea starch as a raw material but a starch of wheat, corn or potato. The examples of this document describe the manufacture of acariogenic polysaccharides using a wheat starch. This document gives no importance to the botanical origin of starch since this origin is presented as indifferent. Thus, this document does not describe that the origin of the starch can have an effect on the properties of the acariogenic polysaccharides obtained or on their manufacturing process. Contrary to what was expected from reading this document, the Applicant has succeeded in obtaining new pea-resistant dextrins, while improving the above-mentioned treatment steps c).

In the process of the invention, the water content in the starch composition during at least a portion of step b) may be less than or equal to 10%, generally less than or equal to 6%, for example less than or equal to equal to 4% by weight relative to the total mass of the composition. The pea starch used in step a) may comprise a total lipid content of less than 0.10%, generally ranging from 0.01 to 0.08%, for example from 0.02 to 0.05%, in particular from 0.02 to 0.04% by dry weight relative to the dry mass of the starch.

The method also has the advantage of being easier to perform than using other types of starch, especially when at least one treatment step c) comprises a filtration and / or demineralisation step and / or subsequent fractionation in step b).

It is pointed out that in the present application, when ranges are indicated, each of the lower terminals can be combined with each of the upper terminals. The pea starch used in step a) advantageously has an amylose / amylopectin mass ratio ranging from 25:75 to 50:50, preferably from 32:68 to 45:55.

The ash content of the pea starch used in step a) is advantageously less than 1%, for example less than 0.2%. The pea starch used in step a) is preferably a yellow pea smooth pea starch.

The pea starch used in step a) is advantageously a native starch.

The heat treatment step b) is generally carried out at least in part at a temperature ranging from 80 to 250 ° C., for example at a temperature ranging from 120 to 220 ° C., preferably at a temperature ranging from 160 to 210 ° C. C.

The heat treatment step b) is advantageously carried out in a reactor chosen from an extruder, a thin-film reactor or a thermostated chamber, preferably an extruder or a thin-film reactor, most preferably a thin-film reactor.

Acidification of the starch in step a) can be carried out with an acid chosen from hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, citric acid or one of their mixtures, preferably hydrochloric acid.

In addition, at least one of the treatment steps c) of the process of the invention advantageously comprises a step of enzymatic hydrolysis of the dextrinified starch. Indeed, the advantages concerning the filtration and demineralisation stages are particularly important according to this variant.

In addition, at least one of the treatment steps c) advantageously comprises a fractionation step. This step makes it possible in particular to reduce the sugar content of the dextrinified starch.

The resistant dextrin recovered at the end of the process advantageously has from 15 to 45%, preferably from 20 to 42%, for example from 28 to 40%, of glucoside bonds 1 6 relative to the total number of glucoside bonds 1 2, 1 3, 1 4 and 1 ® 6.

The resistant dextrin recovered at the end of the process advantageously has a reducing sugar content of less than 30%, for example ranging from 3 to 25%, especially ranging from 4 to 19%, more particularly from 4 to 12%, in glucose equivalent. , in mass relative to the dry mass of the resistant dextrin.

Preferably, the resistant dextrin has:

A polymolecularity index of less than 5, generally ranging from 1.5 to 4, and A number-average molecular mass Mn of less than 4500 g / mol, generally ranging from 500 to 3500 g / mol, for example ranging from 800 to 3000 g / mol, especially from 900 to 1500 g / mol.

The quantity of fibers in this resistant dextrin according to the AOAC 2001.03 standard is generally greater than 60%, preferably ranging from 65 to 99%, generally from 70 to 95%.

Another object of the invention also relates to a resistant pea dextrin having a quantity of fibers according to the AOAC 200103 standard greater than 60%. This pea dextrin may in particular be obtained by the method of the invention. The resistant pea dextrin according to the invention may have properties similar to those described for the resistant pea dextrins recovered at the end of the process according to the invention, in particular with regard to the% of glucoside bonds 1 6 with respect to total number of glucosidic linkages 1 2, 1 3, 1 4 and 1 6, the reducing sugar content, the polymolecularity index and the number average molecular weight Mn.

Yet another object of the invention is the use of the resistant pea dextrin of the invention in a food or pharmaceutical composition.

The invention will now be described in detail below.

Detailed description of the invention

The method of the invention comprises a step of a) dehydrating and acidifying a pea starch to provide a dehydrated and acidified pea starch composition.

Pea starch generally has a high starch content, often greater than 90% by dry weight relative to the dry mass of pea starch. Preferably, the starch content is greater than 95%, more preferably greater than 98%, or even greater than 99% or even greater than 99.5% by dry weight relative to the dry mass of pea starch. .

The pea starch may have a low N protein content of 6.25, for example less than 2%, often less than 1%, preferably less than 0.5%, more preferably between 0.1 and 0.35. % by dry weight relative to the dry mass of pea starch. This content can be determined by the Dumas method. The pea starch advantageously has a total lipid content of less than 0.10%, generally ranging from 0.01 to 0.08%, for example from 0.02 to 0.05%, or even 0.02 to 0, 04% by dry weight relative to the dry mass of pea starch. The Soxhlet method can be used to determine the total lipid content.

The pea starch has an amylose / amylopectin mass ratio advantageously ranging from 25:75 to 50:50, preferably from 32:68 to 45:55. This ratio is that generally observed in pea-type smooth pea starch. yellow starch which gives excellent results in providing the resistant dextrin of the invention. The amylose and amylopectin contents are evaluated by the iodine complexation method.

Amylopectin has alpha 1-6 linkages, at specific points in the starch structure, and this in significant amounts in contrast to amylose. Thus, according to the variants, the pea starch has a particular alpha-6 binding content. Thus, in the same manufacturing process, without being bound to any theory, the resistant dextrin obtained from pea starch may have a structure slightly different from that of the resistant dextrins obtained with other starches. On the other hand, the initial structure of the pea starch can make it possible to explain the results obtained in the Examples section. Indeed, it appears that the resistant pea dextrins have, by identical manufacturing process, a greater amount of fibers, in comparison with the resistant dextrins obtained from other starches such as for example corn or wheat, and this without the need for an additional fractionation step.

More specifically, the pea starch advantageously has a dry weight relative to the dry mass of the pea starch:

A starch content greater than 90%, preferably greater than 95%, more preferably greater than 98%, even greater than 99% or even greater than 99.5%;

A protein content of less than 2%, advantageously less than 1%, preferably less than 0.5%, more preferably between 0.1 and 0.35%,

A total lipid content of less than 0.10%, generally ranging from 0.01 to 0.08%, for example from 0.02 to 0.05%, or even from 0.02 to 0.04%.

An advantage of this pea starch useful in step a) is that it can have, by its intrinsic botanical nature, exceptional properties allowing it to be used in the process of the invention with the above-mentioned advantages . Another advantage is that it can be obtained using an extraction process using virtually exclusively or exclusively water as a solvent, without using complex preparation steps. Advantageously, the method for extracting pea starch useful in the invention does not use an organic solvent. The pea starch can be extracted from pea using known methods such as that described in EP1400537.

Such starches are marketed by the Applicant.

To provide the dehydrated and acidified composition of step a), an acidification step and a stage of dehydration of the pea starch must be carried out. Preferably, the dehydration stage is carried out after the acidification stage. The water content in the starch composition can be measured by Karl-Fisher titration.

During the acidification stage, the amount of acid used in the process according to the invention is generally between 2 and 100 meq H + / kg dry pea starch, advantageously between 5 and 50 meq H + / kg. dry, and preferably between 10 and 30 meq H + / kg dry.

It is preferable that the distribution of the acid in the starch is as homogeneous as possible. Various techniques can be used for the acidification of starch, such as acidification, in the dry or liquid phase. Generally, this acidification is carried out by introducing an aqueous acid solution into the pea starch.

This acidification stage may be carried out batchwise or continuously. Nevertheless, the acidified starch may be intended to be used in a continuous modification process, it is preferred in the present invention to use a means of continuous acidification to achieve the most continuous process possible, and thus limit the operations unproductive (loading, unloading, emptying).

During the dehydration stage, which takes place preferably after the acidification stage, the starch is dehydrated so as to promote, during the next step b), the formation of the atypical bonds. Indeed, at steady state and under normal conditions, the pea starch generally has a moisture of about 12%, this moisture may be greater if an aqueous solution is added in the d phase. acidification mentioned above.

During the dehydration stage, it is better to be careful not to favor the hydrolysis reactions because the various parameters conducive to this hydrolysis (high humidity, temperature, acidity) are collected. The Applicant has been able to demonstrate that it was better to give priority, at this stage, to continuous drying techniques making it possible to achieve the desired humidity in a residence time of the order of the minute or even a few seconds and thus minimize the hydrolysis reactions of the starch.

This drying stage can be carried out in any type of adapted dryer and in particular in a fluidized bed dryer, a dryer under air flow or a drum dryer.

It is also possible to carry out different stages of drying in step a), for example firstly to carry out a first stage of drying the pea starch, followed by a stage of starch acification followed by a second stage of drying the acidified pea starch to complete step a).

Preferably, at the end of step a), the water content in the starch composition is less than or equal to 10%, generally less than or equal to 6%, for example less than or equal to 4%.

The method according to the invention comprises a step b) of heat treatment of the composition provided in step a) to form a dextrinified starch. This step b) can be carried out in such a way as to allow the formation, and this in large quantities, of non-digestible bonds, called "atypical bonds", other than the alpha 1 -4 bonds mainly present in the native starch. The treatment may comprise a heating, generally at least in part at a temperature ranging from 80 to 250'O, for example at a temperature ranging from 120 to 220'O, preferably at a temperature ranging from 160 to 210 ^q C. Advantageously at least 50% of the time of the heat treatment step, preferably at least 80%, most preferably during the whole of this step, is carried out at these temperatures. During this step, it is also possible to concomitantly perform a continuous drying; thus in this case, it is possible to carry out simultaneously the dehydration stage of step a) and the heat treatment of step b). Depending on the configuration of the reactor chosen, the possible drying concomitant heating can be achieved by passing an air stream or a vacuum pump to extract moisture.

At least during part of step b), the water content in the starch composition may be in the water content ranges for at least 50% of the time of the heat treatment step, preferably at least 80 %, preferably during the whole of this step.

The heat treatment step can be carried out in a reactor chosen from an extruder, a thin-film reactor or a thermostated chamber, preferably an extruder or a thin-film reactor, most preferably a thin-film reactor. The use of an extruder to form a dextrinified starch, which can then be converted into a strong dextrin, has already been described in the documents EP0538146, EP0530111 and EP0988323.

An extruder makes it possible to conduct heat treatments under pressure. It can be a single-screw or twin-screw extruder, co-rotating or counter-rotating. Particularly advantageously, the extruder is a twin screw extruder, in particular co-rotating.

The extrusion step may further comprise a concomitant drying step of dehydrated and acidified pea starch. This drying is preferably carried out by a depression, for example using a vacuum pump.

The screw or screws of the extruder may have a length / diameter ratio of 5: 1 to 50: 1. The screw length can range from 0.5m to 5m. The screw speed of the extruder is adapted to the selected screw and the introduced pea starch; it can go from 100 to 500 revolutions per minute. The residence time is adapted by the various parameters to obtain a dextrinified starch at the end of this step.

With regard to the thin-film reactor, a method of manufacturing resistant dextrin using this type of reactor has been the subject of the application EP 1006128. Thin-film reactor is any type of reactor that can be applied to the reactor. produces a high temperature for a short time, in order to obtain a major transformation of the structure of the product, mainly at the level of glucosidic bonds, simultaneously generating the least possible degradation products. An example of a thin-film reactor that can be used is a turboshaker (for example of the VOMM® brand) or a continuous-type mixer, in particular a continuous-type screw mixer. As an example of a continuous screw type kneader, there may be mentioned a BÜSS type kneader marketed by BÜSS AG. With respect to the continuous type screw mixer, the mixer screw can have a length / diameter ratio of from 5: 1 to 50: 1. The screw length can range from 0.5m to 5m. The screw speed of the kneader is adapted to the selected screw and pea starch introduced. The temperature is preferably that mentioned above and the residence time is adapted by the various parameters to obtain a dextrinified starch at the end of this step. It can be particularly short, for example going from 3 to 15 seconds. The kneading step in the continuous type kneader may further comprise a concomitant drying step of dehydrated and acidified pea starch. This drying is preferably carried out by a depression, for example using a vacuum pump.

Regarding the thermostatically controlled enclosure, it can be any type of oven. At the end of step b), the dextrinified starch is recovered.

The dextrinified starch obtained at the end of step b) may have a number-average molecular weight Mn of at most 4500 g / mol, generally ranging from 500 to 3500 g / mol, for example ranging from 800 to 3000. g / mol, in particular from 900 to 1500 g / mol. The dextrinified starch obtained at the end of step b) may comprise a quantity of sugars (that is to say a quantity of saccharides of degree of polymerization equal to 1 or 2) generally less than 15%, by example less than 10%, especially less than 5%, expressed as dry mass relative to the dry mass of the dextrinified starch. The sugars are usually mainly glucose, maltose and isomaltose.

The process according to the invention comprises one or more treatment steps c) dextrinified starch to form the resistant dextrin. These steps have different functions that will be explained below.

All of these processing steps can be successively combined with each other. Therefore, and for the sake of simplicity in the understanding of the description of the steps of treatment c) which follows, it is specified that the terms "dextrinified starch" will be used, even if this dextrinified starch has previously undergone a step of other treatment. By way of example, in the following part, the terms "dextrinified starch" include a dextrinified starch as recovered in step b) having subsequently undergone a first enzymatic hydrolysis step.

These treatment steps c) are generally carried out on the dextrinified starch which is in the form of an aqueous solution. For each of these treatment steps, the concentration and the pH of the dextrinified starch solution can be adjusted in advance so as to allow each of these steps to proceed under good conditions.

One of the treatment steps c) advantageously comprises a step of reducing the molecular weight of the dextrinified starch. This step may be an enzymatic hydrolysis step or a chemical hydrolysis step of the dextrinified starch. Preferably, this molecular weight reduction step is an enzymatic hydrolysis step.

To carry out this enzymatic hydrolysis step, the dextrinified starch is preferably placed in a medium having a dextrinified starch mass concentration, a pH and a temperature close to the optimum operating conditions of the selected enzyme. The amounts of enzymes are adapted by those skilled in the art to allow the hydrolysis reaction under the selected conditions. The middle is advantageously maintained in a known reactor under these optimum operating conditions the time to allow the reaction to occur. The enzymatic hydrolysis step can be carried out with an enzyme or a mixture of enzymes. The enzyme may be an amylase, in particular an amylase chosen from alpha-amylases, beta-amylases, pullulanases and glucoamylases or amyloglucosidases, advantageously an alpha-amylase. By way of example, a medium in which the dextrinified starch has a temperature of from 50 to 100% can be used. The pH can range from 3 to 5. The dry mass of the medium can range from 25 to 45%. This step can last from 30 minutes to 5 hours. The molecular weight reduction step can also be carried out by acid hydrolysis using the same acids as used in step b) and by adapting the conditions to hydrolyze the dextrinified starch, using a lower dry matter.

Since the step of reducing the molecular weight, and in particular the enzymatic hydrolysis step that can generate sugars, the dextrinified starch obtained at the end of the enzymatic hydrolysis step can comprise a quantity of sugars (that is, that is to say a quantity of saccharides with a degree of polymerization equal to 1 or 2) greater than that of the dextrinified starch before this step, this amount being generally less than 20% of sugars, especially less than 15%, for example less than 10%, in dry weight relative to the dry mass of the dextrinified starch obtained at the end of this treatment. One of the treatment steps c) may also comprise an enzymatic branching step using a branching enzyme such as transglucosidase.

The method may also comprise a treatment step c) treatment of the dextrinified starch using lipases such as lysophospholipase and / or phospholipase. The process may also comprise a processing step c) dextrinified starch using hemicellulases.

These enzymatic processing steps of dextrinified starch (enzymatic hydrolysis, enzymatic branching, treatment with lipases and / or treatment with hemicellulases) are well known. They can take place separately or even concomitantly. Such steps are described in particular in documents US5620873 and US201 1020496.

At least one of the treatment steps c) is advantageously a filtration step. This filtration step known per se can in particular be carried out using known techniques of press filter, passage over diatomaceous earth or filtration by passage through rotational vacuum filter RVF (Rotary Vacuum Filter). At least one of the treatment steps c) may also consist of a demineralization step. This demineralization step can be carried out in a known manner by passage over anionic and / or cationic resin.

At least one of the treatment steps c) may comprise one or more fading steps. A bleaching means may for example be carried out by adsorption by contacting the dextrinified starch with pulverulent or granular active carbon. In the case of a bleaching step using pulverulent activated carbon, the Applicant has determined that high percentages of discoloration can be obtained by using porous volumes of large mesopores (pore rays between 1, 5 and 25 nm and in particular between 4 and 20 nm). Successive discolorations can be implemented to optimize the discoloration. However, to avoid the loss of activated carbon, it is preferred in the context of the invention to use recyclable supports such as granular black columns. The same process advantage is observed for the filtration and demineralization stage: the dextrinified starch useful in the invention causes less fouling of the granular black columns.

One of the processing steps c) may also comprise at least one fractionation step. This fractionation step can in particular make it possible to reduce the sugar content of the dextrinified starch. In the context of the present invention, the fractionation step is intended to eliminate the smallest molecules of the dextrinified starch, and in particular to reduce the sugar content. This fractionation step makes it possible to collect a fraction of polysaccharides having higher molecular weight characteristics and a lower polymolecularity index. This fractionation step may consist, for example, in a chromatographic separation step or in a membrane separation step.

This fractionation step may be carried out continuously or discontinuously.

In general, the fractionation is carried out on the dextrinified starch, possibly after having undergone a preliminary treatment step which may in particular be a molecular weight reduction step. The dextrinified starch may also have been subjected to a molecular weight reduction step, such as an enzymatic hydrolysis step.

The dextrinified starch subjected to the fractionation step is generally in the form of an aqueous solution. For example, in the case of the chromatographic separation step, the solution may have a solids content of between 20 and 60%, preferably between 25 and 55%. In the case of the membrane separation step, the solution may generally have a lower solids content. The solution may have, for example, from 2 to 50%, or even 5 to 30%.

The chromatographic separation fractionation step is carried out in a manner known per se, discontinuously or continuously (simulated moving bed), on strong cationic resins of macroporous type, preferably loaded with alkaline or alkaline earth ions such as calcium and magnesium but more preferably using sodium or potassium ions. Examples of such fractionations are described in particular in patents US 3,044,904, US 3,416,961, US 3,692,582, FR 2,391,754, FR 2,099,336, US 2,985,589, US 4,024,331 and US 4,226,977. , US 4,293,346, US 4,157,267, US 4,182,623, US 4,322,623, US 4,405,455, US 4,412,866, US 4,422,881 and WO 92/12179. Preferably, as regards the adsorbent, a strong cationic resin used in sodium or potassium form of macroporous type is used. The resins are advantageously of homogeneous particle size and between 100 and 800 micrometers. It may be of polystyrenic type, comprising divinyl benzene (DVB). The macroporous strong cationic resin in potassium form can be selected from the group consisting of Purolite® C 141 with 5% DVB, Purolite® C 145 with 8% DVB or Purolite® C 150 at 12%. % of DVB. The same process advantage is observed for the demineralization resins: the dextrinified starch useful in the invention does not cause fouling of the adsorbent resin.

As regards the fractionation fraction by separation on membranes, it can be done by nanofiltration, possibly with diafiltration. This separation step can be carried out using nanofiltration cartridges, for example of the Desal® DK or DL type. The temperature conditions of the nanofiltered stream and the pressure applied to the membrane are adapted by those skilled in the art. Membrane filtration produces a permeate that mainly comprises low molecular weight species whereas the retentate mainly comprises polysaccharides of higher molecular weight. The conditions of the membrane filtration and in particular the choice of the membrane makes it possible to modify the cut-off threshold and thus to eliminate more or less importantly in the permeate glucose, maltose, etc. By way of example, a membrane of the Desa® DL type makes it possible to decrease more significantly the amount of maltose in the polysaccharides of higher molecular weight (retentate) than a Desal® DK type membrane. The same advantage It is observed that for the above-mentioned filtration tools: the dextrinified starch useful in the invention causes less fouling of the membranes.

At the end of the fractionation step, the dextrin generally comprises less than 10% of sugars, for example less than 5%, especially less than 1%, by dry weight relative to the dry mass of the composition. By carrying out this step and concomitantly with the reduction in sugars in the resistant dextrin, its reducing sugar content obtained after fractionation decreases.

In a nonlimiting manner, various preferred variants of the method of the invention are described below which comprise different sequences of processing steps c), themselves combinable in their preferred variants presented above.

According to a first preferred variant of the process of the invention, the treatment steps c) comprise:

C1) a step of reducing molecular weight;

C2) a filtration step and / or a demineralization step. According to a second preferred variant of the process of the invention, the treatment steps c) comprise:

C1) a filtration step and / or a demineralization step;

C2) a fractionation step.

According to a third preferred variant of the process of the invention, the treatment steps c) comprise:

C1) a step of reducing molecular weight;

C2) a filtration step and / or a demineralization step;

C3) a fractionation step.

The method according to the invention also comprises a step d) of recovery of the resistant pea dextrin obtained at the end of or steps c). Without being bound by any theory, the resistant pea dextrin has properties which are specific to it, in particular because of the starch-specific starch structure used in the process of the invention but also as a whole. characteristics of the composition of pea starch (impurities, etc.). The resistant dextrin obtained may have from 15% to 45% of glucoside bonds 1 6, preferably from 20 to 42%, for example from 28 to 40% relative to the total number of glycoside bonds 1 2, 1 3, 1 4 and 6. The amounts in glucosidic linkages 1 2, 1 3, 1 4 and 1 6 can be determined by the conventional method known as the "Hakomori method", this technique being described in the publication HAKOMORI, S., 1964, J. Biochem, 55, 205.

The resistant dextrin obtained may also have a reducing sugar content of less than 30%, for example ranging from 3 to 25%, especially ranging from 4 to 19%. The reducing sugar content is expressed in glucose equivalent, in dry weight relative to the dry mass of product analyzed, and is measured by the BERTRAND method.

The resistant dextrin obtained may also have a polymolecularity index of less than 5, generally ranging from 1.5 to 4. The resistant dextrin obtained may have, for example, a number-average molecular mass Mn of at most 4500 g / mol, generally ranging from from 500 to 3500 g / mol, for example ranging from 800 to 3000 g / mol, especially from 900 to 1500 g / mol.

This resistant dextrin obtained may have a quantity of fibers according to the AOAC 200103 standard greater than 60%, preferably ranging from 65 to 99%, generally from 70 to 95%. This method makes it possible to completely determine the quantity of fibers of the resistant dextrins of the invention. The amount of these total fibers may be especially adjusted by the skilled person by modifying the heat treatment, enzymatic hydrolysis, branching and / or fractionation steps.

The above-mentioned treatment steps, which are well known to those skilled in the art, are described in the reference works of his field such as, for example, Separation and Purification Techniques in Biotechnology, Dechow (Noyes publication, 1st Edition, 1989). ), Filtration Technology, Meriguet G. (Engineering Techniques, Sept. 10, 1997, Ref: J3510 v1) and Membrane Filtration (01, NF, UF) - Various Applications, Bourdon et al. (Engineering Techniques, Sept. 10, 2006, Ref: J2796 v1).

The method according to the invention may also comprise a step of chemical modification of the resistant dextrin, for example by a step of hydrogenation or ozonolysis of resistant dextrin, these steps being already known elsewhere.

The method according to the invention may also comprise an additional step of shaping this resistant dextrin. The resistant dextrin of the invention may be in the form of a concentrated aqueous solution, called "syrup", or in solid form. The resistant dextrin, generally still in liquid form after the above-mentioned treatment steps c), or even of possible chemical modification, can be put into the form of a syrup by using a concentration step, known per se, making it possible to regulate the content dry matter of the dextrin syrup resistant to the desired mass concentration. This concentration step can be performed using any device for evaporation. This syrup may have a solids content ranging from 60 to 90%, for example from 65 to 85%.

The resistant dextrin of the invention can also be solidified. Advantageously, the composition is in the form of a powder which is preferably an atomized powder. The process may thus comprise a concentration step followed by a drying step. The concentration step can be done using any type evaporator and the drying step can be in particular an atomization step or a granulation step. These methods are well known to those skilled in the art. The resistant dextrin of the invention is particularly useful in all applications already known resistant dextrins. They can be used as an ingredient in pharmaceutical and food compositions, human or animal.

The subject of the present invention is therefore the use of the resistance dextrin obtained by the process according to the invention in a food or pharmaceutical composition.

Indeed, because of its high fiber content and its low calorific value, such a strong dextrin is of interest in many industrial applications, particularly in the food industry or pharmaceutical, and animal nutrition.

By food composition is meant a composition intended for human or animal food. The term food composition includes food products and dietary supplements. By pharmaceutical composition is meant a composition intended for therapeutic use.

Examples of food compositions comprising said resistant dextrin are dairy products, yogurts, milk-based specialties, ice creams, milkshakes, smoothies, pastries, pies, puddings, cookies, cookies, donuts, brownies, confectioneries, chocolates, spreads, cheeses, sweets, sweets, boiled sweets, soft or non-carbonated beverages, alcoholic or non-alcoholic beverages, fruit juices, concentrated mixtures of fruit juices, flavored waters, beverages powder for example powdered chocolate drinks, soups, sauces, special nutrition compositions, especially compositions for maternal and infant nutrition, for weight management, for sports nutrition, for the elderly and for nutrition clinic, fruit preparations, jams, biscuits, cakes, snacks, pastries, bars and agglomerates of cereals coated or not, breads and buns.

Examples of pharmaceutical compositions include drugs such as elixirs, cough syrups, tablets or tablets, lozenges, veterinary products, dietary products or sanitary products such as, for example, oral hygiene solutions. , pasta and toothpaste gels.

Examples of such compositions using similar products, called branched maltodextrins, are already described in EP1201 133,

EP1245578, EP1245582, EP1245580, EP1245581, EP1245579, EP1245161,

EP1388294, FR2846518, EP1713340, EP1871394, EP2306846, EP2515910,

EP2632428 and EP2919592. The resistant dextrins of the invention can be used in place of these branched maltodextrins, according to the teaching of these documents which are incorporated by reference.

The invention will now be exemplified below in particular non-limiting embodiments.

Examples

Example 1: Preparation of a resistant dextrin with the process according to the invention

Pea starch: ROQUETTE® native pea starch. Native yellow smooth pea starch comprising, in dry weight relative to the dry mass of pea starch, a protein content (N6, 25) of 0.20%, a total lipid content of 0.03%, an ash content of 0.09% and a starch content of about 99.7%. The amylose: amylopectin ratio is 38:62. The equilibrium moisture of the pea starch is 12%.

The composition is acidified with hydrochloric acid at a rate of 17.6 meq H + / kg dry, then dried at a residual moisture of 1.5% by introducing it into a drier on fluidized air. This raw material is then introduced into a PRES type BÜSS® kneader maintained at a temperature of 200 ° C. and at a flow rate of 20 kg / h. The residence time is about 5 seconds.

The dextrinified starch is recovered at the outlet and has the molecular weight Mn shown in Table 1.

This dextrinified starch then undergoes an enzymatic hydrolysis step and is then placed in solution at 35% dry matter, this solution being adjusted to a pH of 4. An alpha-amylase is introduced into the medium (Termamyl® 120L, Novozymes® ) and the medium is heated at 75 ° C for two hours. At the end of this enzymatic hydrolysis step, the dextrinified starch is passed through a RVF vacuum rotary filter. This dextrinified starch is then contacted with granular charcoal and then filtered again. The dextrinified starch is then passed through ionic resins to demineralize it. In Table 1 are reported the level of ease of conduct of these steps (flow losses, need to clean the filters or resins ...). The dextrinified starch is then recovered as a liquid solution.

Part of the dextrinified starch in the form of a liquid solution is put to a solids content of about 40% and then the product is subjected to a fractionation step consisting of a SMB (simulated moving bed) chromatography step. After fractionation, the resistant dextrin recovered in the form of a solution having 20% dry matter comprises, in dry mass, a% DP1 -2 equal to 4.3% relative to the dry mass of the resistant dextrin. The properties of the resistant dextrin are shown in Table 2.

The resistant dextrin is also evaporated to 70% dry matter and is then solid form by atomization. Example 2: Preparation of a resistant dextrin with the process according to the invention

Example 2 differs from Example 1 in that the fractionation step is carried out by adjusting the chromatography so as to reduce more significantly the amount of sugars, so that, in dry mass, the% DP1 -2 is equal to 0.5% relative to the dry mass of the resistant dextrin. The properties of the resistant dextrin are shown in Table 2. Counterexample 1: Preparation of a resistant dextrin with a process which is not according to the invention

This example is identical to Example 2 and differs only in that corn starch (ROQUETTE®) is used instead of pea starch. The same observations as for Example 1 are presented in Table 1.

Counterexample 2: Preparation of a resistant dextrin with a process which is not according to the invention

This example is identical to Example 2 and differs only in that wheat starch (ROQUETTE®) is used instead of pea starch. The same observations as for Example 1 are presented in Table 1. Moreover, the properties of the wheat resistant dextrin obtained before and after chromatography are also reported in Table 2.

Table 1: properties observed for the different dextrinified starches

+++: no decrease in observed flow

++: slight decrease in throughput

+: significant reduction in flow

0: decrease in flow rate requiring the cleaning of the filter or resin

The Applicant has noted that the filtration step on the rotary vacuum filter was done much more easily than when corn starch or wheat starch was used in place of the pea starch useful to the invention. The filtration rate is improved compared to the other dextrinified starches and no clogging of the filter was observed during the test.

As for the demineralization step, it also takes place more easily, without clogging the demineralization resins. This is all the more surprising since the molecular mass of the dextrinified starch is similar, whatever the base used.

Table 2 demonstrates that the strong pea dextrin of the invention has very attractive properties, making it quite suitable for use in food and pharmaceutical products.

Table 2: Properties of the resistant dextrins

It is interesting to note that the amount of fiber from the ECx dextrin. 2 before chromatography has a lower fiber content than that of Example 1. Thus, it appears that the particular structure of the pea starch makes it possible to obtain, with an equivalent process, a higher fiber content as well as a lower sugar content. Without being bound by any theory, an explanation of this phenomenon could be that the structure of the pea resistant dextrin of the invention, although not able to be distinguished from the wheat resistant dextrin by the methods used, would have a distinct structure in its links. The resistant dextrins of the invention can thus be used in the recipes described below.

Example 3: Yogurt

Yogurt can be made with the resistant dextrin of Example 2 as an ingredient.

Ferments:

The ferments are supplied by CHR HANSEN® in freeze-dried form. - a "traditional" ferment, a balanced blend of the usual yoghurt strains (Streptococcus thermophilus, Lactobacillus delbruekii sp.bulgaricus), reference YC-380.

- a "modern" ferment consisting of the same strains after adaptation to current consumer expectations (lower acidity, increased lubricity), reference YC-X1 1. a bifidogenic ferment consisting of Bifidobacterium lactis, reference BB-12.

Formulation:

3 yogurts can be made using each of the ferments.

The ferments comprise about 4.8g of traditional or modern ferments per 100 liters of milk as well as 2g per 100 liters of milk with the bifid ferment. Protocol:

- Moisturize the skimmed milk powder in water for 15 minutes with agitation (800 rpm (revolutions per minute)).

- Add the resistant dextrin, and shake for 7 minutes at 500 rpm.

- Pasteurize the solution in a coil immersed in a boiling water bath, residence time of the milk in the coil: 7 minutes.

- Let the milk cool down to 44 ° C. Then add the sweeteners previously diluted to 10% in sterile water and the ferments diluted in pasteurized milk.

- Place the milk in an oven at 44 ° C and follow the pH to a value of 4.4.

- Stop the fermentation brew yoghurt 1 minute at 500 rpm and poured into glass jars, stored at 4 C. ^q

Example 4: Non-alcoholic soft drink

An alcohol-free soft drink (soda) containing the resistant dextrin of Example 2 can be made according to the recipe and protocol below. Quantities in grams for 1 liter of drink:

0.5 liters of carbonated water are prepared. The sweeteners or sugar substitute are then added. The rest of the ingredients are then incorporated and water is added to a volume of 1 liter. Example 5: Soups

With the aid of the resistant dextrin of Example 2, it is possible to prepare, according to the following protocol, a concentrated tomato soup.

Recipe in g for 100g:

Protocol:

Mix the oil, water at 90 ° C, the CLEARGUM®CO01 emulsifier, and the whey in the bowl of a KENWOOD® blender for 10 minutes at maximum speed.

Mix sucrose, CLEARAM®CH20 modified starch, tomato concentrate, citric acid and water separately: Bake in a water bath up to 80 ° C.

Mix the tomato sauce thus obtained with the previous emulsion for 30 seconds. Put the canned soup, and sterilize at II O'C for 50 minutes. The pH of the soup is 4.2.

Before consumption, the soup is diluted to 50% by weight in water.

Example 6: Chewable paste with gelatin The resistant dextrin of the invention (Example 2) can be used to make a chewable paste with gelatin.

A - FORMULA

B - PREPARATORY MODE

Bake the mixture (A) at 110 ° C. (Brix = 85.2) under atmospheric pressure,

- Cool while mixing and add the mixture B (previously melted at 60 ° C), the gelatin solution C maintained at 60 ° C, then D when the temperature of the mixture reaches 60 'O,

- Cool the dough,

- stretch the dough (1 min or 50 revolutions of the arm of the stretching machine),

Form,

- Cut and pack.

Example 7: Chewable Paste without Gelatin

The resistant dextrin of the invention (Example 2) can be used to make a chewable paste without gelatin. A - FORMULA

B - PREPARATORY MODE

Bake the mixture (A) at 108 ° (Brix = 83.5) under atmospheric pressure,

- Cool by mixing and adding the mixture B (previously melted at 60 ° C), then C when the temperature of the mixture reaches 60 'O,

- Cool the dough,

- To train,

- Cut and pack. Example 8: Caramel

The resistant dextrin of the invention (Example 2) can be used to make a caramel.

A - FORMULA

B - PREPARATORY MODE

- Cook the mixture (A) + the mixture (B) (previously melted at 60 ° C) at 108 ° C (Brix = 84.5) at atmospheric pressure,

- During cooking, add the mixture C,

- Cool,

- To train,

- Cut and pack.

Example 9: Fodder jam

The resistant dextrin of the invention (Example 2) can be used to prepare a fodder jam.

The ingredients are mixed (see table below), then the mixture is boiled over for a period of time necessary to obtain a brix of 90. The cooking parameters are described in FIG. table below.

Example 10: Fruit preparation for yogurts The resistant dextrin of the invention (Example 2) can be used to make a yogurt fruit preparation.

^** frozen fruit puree concentrated at 50 brix

^*** % citric acid to be adjusted to obtain a pH of 3.8 (pH of a fruit preparation intended to be mixed with a yoghurt). Operating mode:

The fruits are mixed with half of the sucrose or intense sweeteners, glucose syrup, modified starch and citric acid.

The resistant pectin-dextrin solution and any sucrose residue are heated in water at 85 ° for 5 minutes and added to the above mixture.

The mixture is baked at 95 ° C. for 5 minutes and potassium sorbate is added.

Example 11: Stackable Rolled Snacks

Can be prepared according to the following formula laminated low fat laminated snacks with the resistant dextrin of Example 2.

Laminated low-fat and fiber-enriched rolled snacks are prepared according to the formula. The various ingredients are mixed and water is incorporated in order to obtain a paste hydration of 40%. The mixture obtained is passed through a cold extruder in order to obtain a paste, which is then rolled and cut into chips. The chips are then fried in oil at 195 ° C for 15 seconds. Example 12: Cooked Sugars

Cooked sugars comprising the resistant dextrin of Example 2 can be prepared from the following syrups:

Trial 1

90% Isomalt + 10% dry strength dextrin / cooking temperature = 180 ° C - Test 2

80% Isomalt + 20% dry resistant dextrin / cooking temperature = 180 ° O Test 3

70% Isomalt + 30% resistant dextrin on dry / t ° of cooking = 180 'O Test 4

60% Isomalt + 40% dry resistant dextrin / cooking temperature = 180 ° O All blends are made at 75% DM, and are cooked in a cooker at the indicated temperatures, so as to obtain water contents of less than 3%. The cooked masses are placed on a cold table and shaped.

EXAMPLE 13 Brioches Buns can be made using the resistant dextrin of Example 2.

Weighing and beating 500g brioches and 60g brioches.

The brioches are shaped manually.

190 ° O rotary oven, brioche 23 minutes, brioche 15 minutes.

Egg and water gilding. Example 14: Fiber-enriched breads

Breads can be prepared using the resistant dextrin of Example 2.

The paste formulas used are detailed in the table below (the percentages indicate the proportion in the finished product).

Oven cooking at 200 ° C for 25 minutes.

Example 15: Breads

The loaves can be made using the resistant dextrins of Examples 1 and 2 according to a French bread formula from bread wheat flour (moisture 15.4%, protein 10.9%, alveogram W280 and P / L 0.75).

Knead the dough in a spiral mixer VMI for 2 minutes at speed 1, followed by 9 minutes of kneading at speed 2. Dough left to rest for 10 minutes at 20 ^q C before being cut into dough pieces of 500g and shaped.

Fermentation dough made at 24 ° C and 75% relative humidity for about 2:30 and baking done at 240'O for 24 minutes in a fixed hearth oven. The table below shows the detailed formulas for pasta composition.

Example 16: Biscuits

Sugar-free biscuits can be made with the resistant dextrin of Example 2, the pasta composition of which is shown in the table below.

The water and the leavening powder are weighed and then mixed for 5 minutes in a Hobart mixer at speed 1.

The fat and soy lecithin are added and the mixture is stirred for 1 minute at speed 1, then 4 minutes at speed 2. Then the eggs, if any, are added before further homogenization.

The rest of the powders: flour, salt, flavorings, cocoa powder defatted if necessary, maltitol, pea fiber, resistant dextrin, resistant starch and pea protein if necessary, are added and mixed in the kneader. The compositions and products are tuned according to the compositions shown in the table above. The whole is kept stirring for 10 minutes at speed 1, with an interruption to scrape the edges of the kneader and the stirring blade.

The biscuits are formed at the rotary molding machine, and arranged on a baking tray.

Pasta mounds are rotated at 200 ° C for 10 minutes and allowed to cool to 25 ° C.

Claims

A process for producing a resistant dextrin comprising:

a) a step of dehydrating and acidifying a pea starch to provide a dehydrated and acidified pea starch composition;

b) a heat treatment step of the starch composition provided in step a) to form a dextrinified starch;

d) a step of recovery of this resistant dextrin.

2. The manufacturing method according to claim 1 characterized in that at least one treatment step comprises a filtration step and / or demineralization.

3. The manufacturing method according to claim 1 or 2 characterized in that the water content in the starch composition during at least a portion of step b) is less than or equal to 10%, generally less than or equal to 6 %, for example less than or equal to 4% by weight relative to the total mass of the composition.

4. The method of manufacture according to any one of claims 1 to 3 characterized in that the pea starch used in step a) comprises a total lipid content less than 0.10%, generally ranging from 0.01 at 0.08%, for example from 0.02 to 0.05%, especially from 0.02 to 0.04% by dry weight relative to the dry mass of the starch.

5. Manufacturing process according to any one of claims 1 to 4 characterized in that at least one treatment step comprises a fractionation step.

6. Manufacturing process according to any one of claims 1 to 5 characterized in that the pea starch used in step a) has an amylose / amylopectin mass ratio ranging from 32: 68 to 45: 55.

7. Manufacturing process according to any one of claims 1 to 6 characterized in that the ash content of the pea starch used in step a) is less than 1%, for example less than 0.2%. .

8. Manufacturing process according to any one of claims 1 to 7 characterized in that the pea starch used in step a) is a yellow pea-type smooth pea starch.

9. The method of manufacture according to any one of claims 1 to 8 characterized in that the pea starch used in step a) is a native starch.

10. The manufacturing method according to any one of claims 1 to 9 characterized in that the heat treatment step b) is carried out at least in part at a temperature ranging from 60 to 250'O, for example at a temperature ranging from from 120 to 220 ° C, preferably at a temperature ranging from 160 to 210 C. ^q

1 1. Manufacturing process according to any one of claims 1 to 10 characterized in that the heat treatment is carried out in a reactor selected from an extruder, a thin-layer reactor or a thermostatically controlled chamber, preferably an extruder or a reactor to thin layer, most preferably a thin-film reactor.

12. The manufacturing method according to any one of claims 1 to 1 1 characterized in that the starch composition is acidified in step a) with an acid selected from hydrochloric acid, sulfuric acid nitric acid, phosphoric acid, citric acid or a mixture thereof, preferably hydrochloric acid.

13. The manufacturing method according to any one of claims 1 to 12 characterized in that at least one of the treatment steps c) comprises a step of enzymatic treatment of the dextrinified starch.

14. The manufacturing method according to any one of claims 1 to 13 characterized in that at least one of the treatment steps c) comprises a fractionation step for reducing the sugar content of the dextrinified starch.

15. Manufacturing process according to any one of claims 1 to 14 characterized in that the recovered resistant dextrin has: From 15% to 45%, preferably from 20% to 42%, for example from 28% to 40%, of glucosidic linkages with respect to the total number of glucosidic linkages 1 2, 1 3, 1 4 and 1 6,

A reducing sugar content of less than 30%, for example ranging from 3 to 25%, especially ranging from 4 to 19%, more particularly from 4 to

12%, in glucose equivalent, in mass relative to the dry mass of the resistant dextrin.

16. The manufacturing method according to any one of claims 1 to 15 characterized in that the recovered resistant dextrin has:

A polymolecularity index of less than 5, generally ranging from 1.5 to 4,

And a number-average molecular mass Mn of less than 4500 g / mol, generally ranging from 500 to 3500 g / mol, for example ranging from 800 to 3000 g / mol, especially from 900 to 1500 g / mol.

17. The method of manufacture according to any one of claims 1 to 16 characterized in that the amount of fibers in the resistant dextrin according to the AOAC 2001 .03 greater than 60%, preferably ranging from 65 to 99%, generally 70 at 95%.

18. Resistant pea dextrin with a fiber content in accordance with AOAC 2001 .03 above 60%.

19. Heavy pea dextrin according to claim 18, characterized in that it is obtainable by the process of one of claims 1 to 17.

20. Use of the resistant pea dextrin according to claim 18 or 19, in a food or pharmaceutical composition.