PROCESS FOR PRODUCING D-ALLULOSE CRYSTALS

专利摘要:
The invention relates to a new process for the manufacture of D-allulose crystals which makes it possible to work continuously and to obtain a high yield. The invention also relates to new D-allulose crystals. Another subject of the invention relates to the use of a nanofiltration unit in a process for producing D-allulose crystals in order to improve the yield and / or the quality of the crystals obtained.
公开号:FR3061413A1
申请号:FR1750103
申请日:2017-01-05
公开日:2018-07-06
发明作者:Baptiste Boit；Geoffrey LACROIX；Laurent Rossi
申请人:Roquette Freres SA；
IPC主号:

专利说明:

® Agent (s): CABINET PLASSERAUD.
® PROCESS FOR THE MANUFACTURE OF D-ALLULOSE CRYSTALS.
The invention relates to a new process for manufacturing D-allulose crystals which makes it possible to work continuously and obtain a high yield. The invention also relates to new D-allulose crystals. Another object of the invention relates to the use of a nanofiltration unit in a process for the production of Dallulose crystals in order to improve the yield and / or the quality of the crystals obtained.
FR 3,061,413 - A1
i
Field of the invention
The invention relates to a new process for manufacturing D-allulose crystals which makes it possible to work continuously and obtain a high yield. The invention also relates to new D-allulose crystals. Another object of the invention relates to the use of a nanofiltration unit in a process for producing D-allulose crystals in order to improve the yield and / or the quality of the crystals obtained.
Prior art
D-allulose (or D-psicose) is a rare sugar with a sweetening power equal to 70% of that of sucrose. Unlike the latter, D-allulose does not cause weight gain because it is not metabolized by humans. It has a very low caloric value (0.2 kcal per gram) and thus prevents fat gain. In addition, studies have shown that D-allulose is non-cariogenic, even anti-cariogenic. These properties have recently generated considerable interest from the food and pharmaceutical industries.
Even if it is possible to obtain D-allulose chemically, for example by reacting an aqueous solution of glucose in an acid medium in the presence of a catalyst of ammonium molybdate type, D-allulose is generally obtained enzymatically, by reacting an aqueous solution of D-fructose with a D-psicose epimerase as described for example in application WO2015 / 032761 A1 in the name of the Applicant. In both cases, the reaction is not complete. For example, the amount of D-fructose transformed into D-allulose after epimerization is generally less than 30%.
Thus, at the end of the epimerization reaction, it is necessary to carry out a step of separation of the D-allulose, in order to increase the richness of the resulting composition of D-allulose. To carry out this separation, a very general chromatography of the composition resulting from the epimerization reaction is carried out, for example by continuous chromatography of the simulated moving bed type.
Document JP2001354690 A describes a process for manufacturing a D-allulose syrup from a mixture of fructose and D-allulose, said process comprising a separation step consisting of a continuous chromatography step using a particular sequence of samples different products of the mixture. A fraction rich in D-allulose (whose richness in D-allulose can reach 98%) and a fraction rich in fructose are recovered. The recovery yield in the fraction rich in D-allulose is 96%.
At the end of the separation steps cited above, liquid compositions rich in Dallulose are obtained. This is how these liquid compositions, generally called syrups, are used for the manufacture of food or pharmaceutical products.
For example, application WO 2015/094342 also in the name of the Applicant describes the manufacture of solid food products comprising a D-allulose syrup, comprising from 50 to 98% D-allulose and a native protein. It is mainly in this form of syrups that various companies have announced the marketing of D-allulose to date.
D-allulose is also sold in the form of powders. However, as explained below, their manufacturing can be quite complex.
It is possible to produce powders using for example atomization techniques. However, atomized powders, the composition of which depends on the atomized raw material, generally include large amounts of impurities. Furthermore, these atomized powders are weakly crystalline; they are very hygroscopic and this causes problems with water resistance. This also creates generally larger caking phenomena.
Because of these difficulties, the atomization of D-allulose has been little described in the literature. By way of example, mention may be made of document EP1860195 which describes the atomization of a mixture comprising D-allulose and D-allose. With regard to the enantiomer of D-allulose, Lallulose, mention may be made of document JP 4761424 which describes the atomization of a cooked mass of Lallulose.
It is also possible to produce powders by granulation techniques, as described for example in application WO2016 / 012853 in the name of the Applicant.
Another form of powders relates to crystals obtained by crystallization from a stock solution of D-allulose.
A process for the manufacture of D-allulose crystals has been described in document CN 104447888 A. This document more particularly describes in the examples a process comprising a step of manufacturing a solution of D-allulose from glucose using a molybdate catalyst then a step of discoloration of this solution using activated carbon then filtration to remove the activated carbon, a step of deionization by electrodialysis, a step of separation by continuous chromatography to form a solution of D-allulose having a purity ranging from 70 to 90%, a step of concentrating said solution to obtain a concentrated solution of D-allulose, followed by a step of crystallization from ethanol to obtain a crystalline product of D-allulose having a limited purity, at most more than 99%. No crystallization yield is indicated in this document.
Another crystallization process has also been described in document WO 2011/119004 in the name of CJ Cheiljedang in which the crystallization yield is of the order of 50%. This method of manufacturing D-allulose crystals comprises a step of providing a D-allulose solution, a step of purifying this solution, a step of concentrating the D-allulose solution to provide a mother solution and a stage of crystallization of this mother solution, in which the stage of crystallization is carried out by maintaining the mother solution in its metastable zone. The purification step described in this document is a separation step by chromatography, which makes it possible to separate the D-allulose from the fructose. This document recognizes, however, that the production of powders in the form of crystals is difficult to carry out:
• First of all, this crystallization is difficult to control as indicated in paragraph [36], in which it is specified that the crystallization must be carried out with care, by continuous observation of the crystals, also measuring the concentration of the supernatant in order to regulate the temperature in the crystallizer. However, this document is silent on the reasons why it is difficult to achieve this crystallization.
• In addition, the crystals obtained have a size less than 200 μm (see paragraph [89]) and are therefore, due to their small size, difficult to separate from the mother liquors of crystallization during centrifugation. The recovered crystals are also difficult to handle during subsequent use.
Document WO 2016/064087, also in the name of CJ Cheiljedang, also describes in Example 3 a process for the manufacture of D-allulose crystals in which a mother solution is introduced into a crystallizer at four distinct times. Between each introduction, four heating and cooling cycles are carried out, which leads to a process which lasts more than 80 hours. Compared with the process described in document WO 2011/119004, the crystallization yield is not improved (it is 52.8%). The crystals obtained have a larger average size (mean aperture equal to 374 μm). However, the crystals obtained have impurities. In addition, the crystals which are marketed by the company CJ Cheiljedang have a shape of needles, which leads to a flow which is not completely satisfactory.
It appears from the above that many problems still remain in the manufacture of D-allulose crystals.
First, the overall yield of D-allulose crystals is excessively low. By “overall yield of D-allulose crystals” is meant the ratio, expressed in dry mass, of the mass of D-allulose crystals obtained on the mass of D-fructose introduced. This low yield, of the order of 15% compared to D-fructose, is essentially linked to the yields of the epimerization stages (less than 30%) and of crystallization (generally of the order of 50%).
In order to improve the efficiency of the processes, it is therefore imperative to carry out "recycling steps". By "recycling step" in a process is meant the reuse in a previous step of the process of a fraction of product obtained during a separation step. By “separation step” in the present Application, is meant any step making it possible to separate a composition comprising a product A and a product B into at least a first fraction richer in product A and a second fraction richer in product B. The fraction can be in any form, for example in solid form, in liquid form, or even in the form of a solid suspension in a liquid. A separation step can be of any type, for example a chromatography step, in which the liquid composition is separated into at least two liquid fractions, or also a crystallization step where a liquid composition is separated into a solid fraction and a fraction liquid.
Steps for recycling fructose-rich fractions have already been described in order to improve the yield of the process for manufacturing D-allulose syrups. In particular, the document JP2001354690 A previously mentioned describes the recycling of the fructose-rich fraction obtained during the chromatography step to subject it to the epimerization step. This improves the yield of D-allulose in the form of a liquid composition.
It is by seeking to apply the teachings of this document in a process for manufacturing D-allulose crystals (such as for example that described in document WO 2011/119004) that the Applicant has been able to note that these do not were not simply transposable.
In fact, when the recycling of the fructose-rich fraction is carried out (see Figure 1), the Applicant has observed that the mother solution obtained becomes increasingly difficult to crystallize. After a certain time, this crystallization even becomes impossible as demonstrated in the Examples section.
Furthermore, still with the aim of improving the overall yield of D-allulose crystals of the process, the Applicant has also attempted to recycle the mother liquors of crystallization (that is to say the solution rich in D-allulose which is obtained after separation of the crystals obtained during the crystallization step) by mixing them with a D-allulose composition to form, after concentration, a new stock solution (see Figure 2). It was able to observe (see the Examples section) that this recycling of the mother liquors caused the same difficulties, and this even faster than in the case of the recycling of the fraction rich in fructose.
In these two cases described above, stops in the production of Dallulose crystals must therefore be made.
Furthermore, the Applicant has been able to observe that, even without carrying out recycling, by transposing the teachings described above into a continuous industrial process for the manufacture of D-allulose crystals, “instabilities” are observed. These instabilities result in mass-cooked crystals inexplicably having a variable appearance during the process. This is particularly troublesome because the massages of crystals can be centrifugable and then non-centrifugable at certain times, and this without any a priori prediction of its behavior can be made. There is then a need to recast the baked masses obtained if one wishes to reuse them in the process and this makes the process impractical and less economical.
However, in order to accelerate the industrial development of D-allulose, which is today mainly marketed in the form of syrup, it is imperative on an industrial scale to be able to carry out a continuous and stable process for the manufacture of D crystals -allulose, in order to be able to supply them at a competitive price.
After much research, the Applicant has succeeded in obtaining a process for the manufacture of D-allulose crystals in which the problems cited above can be resolved.
Due to an improved process stability, the production of the crystals does not require systematic control as for example indicated in the document WO 2011/119004, which makes it possible to carry out a continuous process for manufacturing crystals of D- allulose.
Furthermore, since the process of the invention also allows numerous recycling steps, the yield of the process can be greatly increased.
It is by conducting numerous researches that the Applicant has been able to observe that, in a process for the manufacture of D-allulose crystals, particular impurities are formed during the various stages of the process for preparing the mother solution. These impurities have, to the best knowledge of the Applicant, never been reported in the literature. They could be identified by the Applicant using a particular gas phase chromatography (GC) technique. Without being bound to any theory, the Applicant believes that these impurities are dimers of D-allulose which are formed by condensation throughout the process.
The Applicant has also been able to show that these dimers of D-allulose, unlike other impurities such as glucose or D-fructose, have a very significant anti-crystallizing effect.
Surprisingly, the Applicant has succeeded, by carrying out a process for manufacturing D-allulose crystals in which a particular separation step is carried out, to eliminate this difficult crystallization problem of D-allulose. This separation step consists of a nanofiltration step, which allows the elimination of these anti-crystalline impurities.
This new process presents a major advance for the industrial development of D-allulose crystals since it makes it possible to achieve an overall yield exceeding 25% compared to the D-fructose introduced, advantageously exceeding 50%, or even exceeding 65%. This makes it possible to envisage the production of D-allulose crystals at a competitive price as well as the commercial development of such crystals on a larger scale.
Furthermore, the Applicant has found that the presence of these impurities is a factor which influences the shape of the crystals, in particular when one seeks to produce crystals of large size, in particular when their average size exceeds 200 μm.
During its research, the Applicant also succeeded in manufacturing new D-allulose crystals using a specific crystallization process using, among the manufacturing steps, the nanofiltration step mentioned above. These crystals, which are another aspect of the present invention, have in particular the characteristic of comprising a very low percentage by mass of D-allulose dimer. The crystals obtained can also have a different shape and an improved flow. These shape and flow properties are directly related to the fact that dimers are present in crystals in very small quantities. On the contrary, when it is desired to produce large crystals, the significant presence of D-allulose dimers in the mother solution during crystallization leads to D-allulose crystals comprising significant amounts of these dimers; moreover, the elongation of these crystals is observed to form needles. However, these needle crystals can exhibit less flow than the crystals than the crystals of the invention.
Summary of the invention
The invention thus relates to a process for the manufacture of D-allulose crystals comprising:
• a step of supplying a composition rich in D-allulose, • a step of concentrating said solution to form a mother solution to be crystallized, • a step of crystallizing the mother solution to form Dallulose crystals and waters mothers;
• and at least one nanofiltration step.
As mentioned above, the Applicant has been able to observe that, systematically, in a process for manufacturing D-allulose crystals, particular impurities are formed during the process. To the best of the Applicant's knowledge, these have never been reported in the literature. This is explained by the fact that, by the high performance liquid chromatography (HPLC) technique conventionally used to measure the purity of D-allulose, these impurities are not detected on the chromatograms (see Figures 7 and 8). It is by using a gas chromatography technique that the Applicant has been able to detect their presence (see Figures 9 and 10).
These impurities have been identified by the Applicant as being Dallulose dimers. The Applicant has also been able to show that these dimers, unlike other impurities such as glucose or D-fructose, have a very significant anti-crystallizing effect. However, as these dimers of D-allulose are formed during the process, their presence can limit the yield of a continuous process for the manufacture of D-allulose crystals by outright preventing this crystallization, by forming baked-on not centrigugrable, if the quantities of these dimers are too large. Furthermore, in an industrial and continuous process for the manufacture of D-allulose crystals where numerous successive steps are carried out, the amount of these impurities can vary over time. This makes the process unstable over time, the massages being sometimes centrifugable, sometimes not centrifugable.
It is to the Applicant's credit to have identified these specific impurities and to have succeeded in eliminating them, by carrying out a separation step consisting in at least partially separating these dimers from D-allulose by nanofiltration.
Using the process of the invention which makes the crystallization stage very stable, it is then possible to carry out the process continuously but also to drastically increase the overall yield of D-allulose crystals. This is made possible by being able to provide a mother solution of D-allulose having a very small amount of Dallulose dimers, this thanks to the aforementioned nanofiltration step.
Another merit of the Applicant is that it succeeded in providing new Dallulose crystals using this mother solution, in a particular crystallization process which also limits the in situ formation of said dimers. The result is crystals with a lower mass percentage of D-allulose dimers than those of the prior art. Another subject of the invention thus relates to D-allulose crystals comprising a mass content of D-allulose dimer, determined by gas chromatography (GPC), of less than 0.5%.
Another object of the invention also relates to the use of a nanofiltration unit in a circuit for producing D-allulose crystals to improve the overall yield of D-allulose crystals.
Brief description of the Figures
Figure 1: Figure 1 schematically shows a circuit for the production of Dallulose crystals in which the chromatin raffinate rich in D-fructose is recycled to be mixed with the fructose at the head of the epimerization reaction.
Figure 2: Figure 2 shows schematically a circuit for the production of Dallulose crystals in which the mother liquors of crystallization are recycled to be mixed with the composition of D-fructose / D-allulose resulting from the epimerization reaction.
Figure 3: Figure 3 shows schematically a circuit for the production of Dallulose crystals comprising a nanofiltration unit useful for the process of the invention.
Figure 4: Figure 4 shows an example of an adiabatic crystallizer-evaporator under vacuum useful for a variant of the process of the invention.
Figure 5: Figure 5 shows an example of a vertical crystallizer useful for a variant of the process of the invention.
Figure 6: Figure 6 shows the permeation curve for the nanofiltration step, that is to say the flow rate as a function of the volume concentration factor.
Figure 7: Figure 7 shows an HPLC chromatogram of a composition rich in Dallulose taken in the process of the invention (see Figure 3), that is to say before nanofiltration.
Figure 8: Figure 8 shows an HPLC chromatogram of a permeate taken in the process of the invention (see Figure 3), that is to say after nanofiltration.
Figure 9: Figure 9 shows a CPG chromatogram, in the characteristic region of dimers, of a composition rich in D-allulose taken in the process of the invention (see Figure 3), that is to say before nanofiltration .
Figure 10: Figure 10 shows a GPC chromatogram, in the characteristic region of dimers, of a permeate taken in the process of the invention (see Figure 3), that is to say after nanofiltration.
Figure 11: Figure 11 shows a snapshot obtained by optical microscopy of comparative Dallulose crystals.
Figure 12: Figure 12 shows two photos obtained by optical microscopy of D-allulose crystals according to the invention.
Figure 13: Figure 13 shows a snapshot obtained by optical microscopy of Dallulose crystals manufactured and marketed by the company CJ CheilJedang Food Ingredient.
Figure 14: Figure 14 represents the ratio of the Feret min / Feret max diameters as a function of the particle sizes by volume D4.3 for two types of D-allulose crystals.
Figure 15: Figure 15 shows the Feret min and Feret max diameters of a model particle.
Detailed description of the invention
A process for manufacturing D-allulose crystals conventionally comprises:
• a step of concentrating a composition rich in D-allulose to provide the mother solution to be crystallized;
• a step of crystallization of the mother solution to form Dallulose crystals and mother liquors;
• a step of separation of the mother liquors and the D-allulose crystals.
The process of the invention has the particularity of comprising a nanofiltration step.
This nanofiltration step makes it possible to limit the amount of D-allulose dimers in the mother solution supplied in the process of the invention. This nanofiltration stage takes place in a stage prior to the stage of concentration of the composition rich in D-allulose. This step therefore allows the supply of a stock solution of D-allulose whose dimer content of ίο
D-allulose is weaker than that obtained from the same process not using this nanofiltration step.
In the nanofiltration step, which is essential to the process of the invention, two fractions are formed when a D-allulose composition is subjected to nanofiltration:
• a permeate, which is depleted in D-allulose dimers;
• as well as a retentate, which is enriched in D-allulose dimers.
In Figure 3 which represents a crystal production circuit useful for the process of the invention, Flux 6 represents the permeate and Flux 12 represents the retentate. For illustrative but non-limiting reasons, the flows indicated in the following description refer to the flows in the production circuit of this Figure 3.
The nanofiltration permeate is an intermediate allowing the manufacture of this mother solution.
The terms “depleted in D-allulose dimers” and “enriched in D-allulose dimers” are obviously relative with respect to the content of D-allulose oligomers in the composition to be nanofiltrated. By “D-allulose dimer” is meant a compound comprising a D-allulose condensed with at least one second identical or different monosaccharide. These dimers are, for example, dimers of the D-allulose-D-allulose type.
These dimers could be detected by CPG and could not be detected during the HPLC analysis, as demonstrated in the examples section. It follows that the mass quantities of the various constituents, expressed in dry mass, are in the present application systematically determined by CPG. To determine the quantities of each of the species in the composition, the sample generally undergoes a processing step in order to transform the different species present into methoxime trimethylsilylated derivatives. The mass quantities of each of the species are expressed in this Request, unless otherwise stated, relative to the total dry mass.
The amounts of glucose, fructose and allulose can be determined in a gas chromatograph equipped with an injector heated to 300 ° C, a flame ionization detector (FID) heated to 300 ° C and equipped with '' a 40-meter capillary DB1 column, with an internal diameter of 0.18 mm and a film thickness of 0.4 µm, the temperature of the column being programmed as follows: from 200 ° C to 260 ° C at a rate of 3 ° C / min, then from 260 ° C to 300 ° C at 15 ° C / min, holding at 300 ° C for 5 min.
By quantity of dimers of D-allulose means the difference between the total quantity of dimers in a sample, determined by GPC, and the quantity of known dimers possibly present, which are glucose-glucose dimers such as maltose and isomaltose. However, the quantity of these glucose-glucose dimers is generally very low, or even non-existent. For example, in the stock solution useful for the invention, the mass amount of glucose-glucose dimers is generally less than 0.2%, often less than 0.1%. It is the same with the crystals of the invention.
The possible amount of glucose-glucose dimers can be determined under the same conditions as those described above for glucose, fructose and D-allulose:
• by carrying out a hydrolysis of the glucose-glucose dimers of the sample;
• by determining the amount of total glucose in the same chromatograph and under the same conditions, said total glucose comprising the initial so-called free glucose and the glucose resulting from the hydrolysis of the glucose-glucose dimers;
• by subtracting from this amount of total glucose the amount of initial glucose from the sample.
The total amount of dimers can be determined in a gas chromatograph under the same conditions as described above, with the difference that the column used is a 30-meter capillary DB1 column, having an internal diameter of 0.32 mm and a film thickness of 0.25 μιτι and the temperature of the column is programmed as follows: from 200 ° C to 280 ° C at a rate of 5 ° C / min, holding at 280 ° C for 6 min, then from 280 ° C to 320 ° C at 5 ° C / min, holding at 320 ° C for 5 min.
The method is described in more detail in the Examples section.
To carry out the nanofiltration step useful for the invention, the composition to be nanofiltrated is passed over a nanofiltration membrane. It generally has a dry matter ranging from 5 to 15%.
The temperature of this composition to be nanofiltered can range from 10 to 80 ° C, generally from 15 to 50 ° C, often around 20 ° C.
Those skilled in the art will be able to choose the membrane useful for this separation. This nanofiltration membrane can have a cutoff threshold of less than 300 Da, preferably ranging from 150 to 250 Da. Ideally, the membrane has a MgSO4 rejection rate of at least 98%. It can in particular be a Dairy DK or Duracon NF1 type membrane manufactured by GE®.
The pressure applied to the membrane can also vary widely and can range from 1 to 50 bars, preferably from 5 to 40 bars, most preferably from 15 to 35 bars.
This nanofiltration step can be accompanied by a diafiltration phase.
Preferably, the volume concentration factor (FCV) of the nanofiltration ranges from 2 to 20. This volume concentration factor is easily adjusted by a person skilled in the art.
This nanofiltration step can be carried out continuously.
According to the invention, the step of supplying a composition rich in D-allulose can comprise:
• a step of supplying a composition comprising D-fructose (Flux 1 or Γ);
• an epimerization step to form a composition comprising D-fructose and D-allulose (Flux 2);
• a chromatography step to provide a composition rich in D-allulose (Flux 5) and a raffinate, which is a composition rich in D-fructose (Flux 14).
Preferably, the nanofiltration stage is carried out between the stage of supplying the composition rich in D-allulose (Flux 5) and the stage of concentration to supply the mother solution of Dallulose (Flux 7). The nanofiltration step of said composition rich in D-allulose provides a retentate (Flux 12) and a permeate (Flux 6).
Thus, a variant of the preferred of the invention which comprises:
• a step of supplying a composition rich in D-allulose;
• a nanofiltration step of said composition rich in D-allulose to provide a retentate and a permeate;
• a step of recovery of the nanofiltration permeate;
• a step of concentrating this permeate to provide the mother solution of Dallulose.
In the process of the invention, the nanofiltration step is thus advantageously carried out on the composition rich in D-allulose resulting from the chromatography step, just before the concentration step which provides the mother solution. It is in this configuration that the process makes it possible to most effectively limit the amount of dimers of D-allulose in the mother solution to be crystallized, and therefore to increase most significantly the overall yield of crystals of D- allulose.
The term “composition rich in D-allulose” generally means a composition having, by dry mass, a mass content of D-allulose greater than 80%, advantageously ranging from 80 to 99%, preferably from 82 to 98%.
As regards the permeate obtained, its dry matter can vary, for example in the range from 3 to 15%. The permeate can especially comprise, in addition to D-allulose, D-fructose and glucose, as well as other sugars possibly present. The composition of this filtrate can be very different and depends on the composition to be nanofiltered. At the end of this nanofiltration step, the permeate recovered can comprise, relative to its dry mass, from 0 to 1.2% of D-allulose dimers, for example from 0.1 to 1.0%, in particular from 0.15 to 0.5%. The permeate may be subjected to one or more stages such as a stage of mixing with an additional product, a stage of separation, a stage of purification, a stage of epimerization or a stage of concentration.
As regards the retentate obtained, its dry matter can also vary widely, for example in the range from 15 to 40%. It can mainly include D-fructose, D-allulose, glucose and D-allulose dimers. According to a variant, the retentate is recovered, optionally mixed with an additional composition of D-allulose, to provide, after a possible concentration step, a syrup of D-allulose.
In the preferred variant where the composition rich in D-allulose which comprises dimers of D-allulose is subjected to a nanofiltration step, the permeate obtained (Flux 6), called "preferred permeate", preferably comprises in dry mass:
• from 80 to 99% of D-allulose;
• 0 to 20% D-fructose;
• from 0 to 10% glucose;
• from 0 to 1.2% of D-allulose dimers.
As indicated above, this preferred permeate can be directly subjected to a concentration step to obtain the mother solution to be crystallized (Flux 7).
It is specified that in the present Application, apart from the D-allulose crystals, all of the compositions are generally aqueous compositions. In other words, the solvent for the dry constituents includes water. The solvent for the compositions generally consists of water or a mixture of water and alcohol such as, for example, ethanol. Preferably, the solvent for the compositions is water.
Thus, the mother solution of D-allulose useful for the invention generally consists of an aqueous solution of D-allulose. The mother solution generally has a dry matter of at least 75%, for example from 80 to 95%, preferably from 81 to 92%, most preferably from 83 to 89%.
To reach this dry matter, it is necessary to perform a concentration step. This step can be carried out on a composition rich in D-allulose, the only requirement is that this composition rich in D-allulose has been obtained by a process comprising, in a previous step, the nanofiltration step useful for the invention. This composition rich in D allulose subjected to the concentration step can thus be the preferred permeate described above, but also a composition rich in D-allulose obtained by chromatography, or else a mixture of a permeate with a composition rich in additional Dallulose. . Preferably, the composition rich in D-allulose subjected to the concentration step is the preferred permeate.
As the formation of D-allulose dimers also occurs during the concentration step, it is preferable to select conditions which make it possible to limit the amounts formed in these dimers. The concentration step is thus generally carried out under vacuum, for example at a pressure of 5 to 100 mbar, preferably ranging from 20 to 70 mbar. This vacuum reduces the temperature required for evaporation and reduces the duration of this concentration step. It can be carried out at a temperature ranging from 30 to 80 ° C, advantageously from 34 to 70 ° C, preferably from 37 to 50 ° C. This concentration step can be carried out in a single-stage evaporator, a multi-stage evaporator, for example a double-stage evaporator. At the end of the concentration step, the mother solution of D-allulose useful for the invention is obtained.
This concentration step can be carried out continuously.
The mother solution obtained can comprise, in dry mass:
• from 80 to 99% of D-allulose, preferably from 85 to 98%;
• from 0 to 20% of D-fructose, preferably from 0.5 to 15%;
• from 0 to 10% glucose, preferably from 0 to 5%;
• from 0 to 1.5% of D-allulose dimers, for example from 0.1 to 1.2%, preferably from 0.4 to 1.1%.
The method according to the invention further comprises a step of crystallizing said mother solution of D-allulose to form a suspension of crystals of D-allulose. This suspension comprises crystals and mother liquors of crystallization which are also formed during this stage.
This crystallization step can be of any type. It can in particular be a crystallization stage by cooling or a crystallization stage by evapocrystallization. Those skilled in the art will be able to find the conditions for implementation which are in particular described in document WO 2011/119004. However, it should be noted that the crystallization steps described in these documents are made easier to perform due to the particular preparation of the mother solution useful for the invention.
At the end of the crystallization step, from the suspension of crystals (Flux 9) the crystals (Flux 10) are separated from the mother liquors (Flux 13), in particular by a filtration and / or centrifugation step. This separation step is more preferably done in batch.
The mother liquors (Flux 13) generally have a dry matter ranging from 70 to 80%. They can include in dry mass:
• from 80 to 99% of D-allulose, preferably from 82 to 95%;
• from 0 to 20% of D-fructose, preferably from 0.5 to 15%;
• from 0 to 10% glucose, preferably from 0 to 5%;
• from 0 to 3% of D-allulose dimers, for example from 0.1 to 2.9%, in particular from 1 to 2.5%.
The crystals obtained can be subjected to a clearing step with cold water and / or with alcohol, in particular ethanol. These crystals can then be dried (Flux 11) by a drying step which can be done in any type of suitable dryer. The D-allulose crystals have a water content of less than 5%, preferably less than 1%.
This crystallization step can be carried out continuously, in particular using a vertical crystallizer, an example of which is shown in Figure 5.
According to an entirely preferred mode, the crystallization stage comprises an adiabatic evaporative cooling stage, carried out in an adiabatic crystallizer-evaporator under vacuum to form a mass-cooked (Flux 8), followed by a crystallization stage by cooling said mass-cooked to provide a suspension of crystals (Flux 9). Adiabatic evapo-cooling causes the mother solution to crystallize to cool immediately. Preferably, the crystallizer-evaporator is equipped with a condenser and the water condensed during this stage is reinjected continuously along the walls at the top of the crystallizer to keep the dry matter stable. This preferred crystallization stage comprising two distinct stages, combined with the nanofiltration stage in a particular configuration of the process of the invention, made it possible to continuously obtain the crystals of the invention which are described below in the description . This is linked to the fact that this preferred crystallization stage, in particular the evapo-cooling stage, also makes it possible to very considerably limit the in situ formation of D-allulose dimers. Without being linked to any theory, the Applicant explains it by the fact that the mother solution can be cooled almost instantaneously during its introduction into the crystallizer-evaporator, unlike the crystallization processes already known for D-allulose. which describe the natural cooling of the mother solution, or even by a cooling ramp using a heat exchanger as described in application WO2016 / 064087. The crystals according to the invention have improved purity and properties, although the first stage of the crystallization stage is an instant evapo-cooling stage, which shortens the duration of the crystallization stage. However, this is contrary to what the skilled person would have envisaged, for whom obtaining improved crystals requires an increased crystallization time.
During the evapo-cooling stage, the temperature can range from 30 to 40 ° C, preferably ranging from 33 to 37 ° C, for example around 35 ° C. This temperature is easily reached by a person skilled in the art by determining the appropriate vacuum to be applied. Thus, the pressure in the crystallizer-evaporator can range from 30 to 50 mbar. An adiabatic crystallizer can in particular be a DT tube drafting crystallizer (for Draft Tube) or DTB type drafting (for Draft Tube Baffle), forced circulation or indirect forced circulation (IFC®). Preferably, this evapo-cooling stage is continuous. At this stage, the primers are generated continuously by phenomenon of spontaneous nucleation in the evapo-crystallizer by the supersaturation created by rapid cooling; thus, there is strictly speaking no introduction of primers in this case. By way of non-limiting example, a possibility of carrying out this stage of continuous evapo-cooling is described in the Examples section and in FIG. 4, where a fraction of the crystals formed during the stage of evapo-cooling (Flux 7d) is mixed. in the feed stream 7b of the crystallizer-evaporator, which makes it possible to obtain a stream 7c which comprises, at the time of introduction into the crystallizer-evaporator, crystals which will be able to further magnify during this new passage in the crystallizer-evaporator. According to this example, Flux 7b can be obtained from a mixture of Flux 7 and Flux 7a, which consists of a supersaturated syrup of D-allulose recovered in the crystallizer-evaporator, which comprises "fines", ie i.e. the finest D-allulose crystals from the crystallizer. According to this variant, the Flux 7 can advantageously, before mixing, pass through a heat exchanger, this passage making it possible to heat the Flux 7 almost immediately before mixing it immediately with the Flux 7a. This then makes it possible to recast the fines from Flux 7a and cool the Flux 7 to obtain a Flux 7b free of these fines.
At the end of this stage, a massecuite of D-allulose crystals (Flux 8) is recovered, that is to say a suspension of crystals, generally having a small size. The average residence time of the terracotta during this evaporative cooling stage can be between 5 and 15 hours. The mean size by volume D4.3 of the crystals suspended in the mass-cooked generally ranges from 50 to 200 μm.
The crystallization stage by cooling is carried out in a conventional manner by cooling the massecuite obtained during the evapo-cooling stage (Flux 8). The duration of this crystallization stage can range from 25 to 50 hours. The temperature at the start of crystallization generally depends on the temperature of the mass-cooked introduced and can in particular range from 30 to 40 ° C., preferably ranging from 33 to 37 ° C., for example around 35 ° C. This stage is generally done with mechanical stirring. Preferably, during crystallization by cooling, the temperature is lowered at a rate ranging from 0.3 to 0.5 ° C per hour. FIG. 5 represents an example of a vertical crystallizer with, on the sides, different heat exchangers making it possible to adjust the temperature in the crystallizer. During this operation, it is preferred that the temperature difference between the mass-cooked and the water of the exchanger does not exceed 5 ° C. The crystallization stage by cooling can preferably be carried out continuously, in particular in a vertical crystallizer.
Thus, a preferred variant of the process of the invention comprises:
• a step of supplying a composition rich in D-allulose (Flux 5);
• a nanofiltration step of said composition rich in D-allulose to provide a retentate (Flux 12) and a permeate (Flux 6);
• a step of recovery of the nanofiltration permeate;
• a step of concentrating this permeate to provide the mother solution of Dallulose (Flux 7);
• a crystallization step comprising:
i. an adiabatic evapo-cooling stage, carried out in an adiabatic crystallizer-evaporator under vacuum to form a massecuite (Flux 8), ii. followed by a crystallization stage by cooling said massecuite to form a suspension of crystals (Flux 9).
Apart from the advantages linked to the crystals themselves, an advantage of this preferred variant of the process of the invention is that the crystals obtained can be even more easily separated from the mother liquors of crystallization and more easily dried. This is mainly related to the shape of the crystals obtained.
To start a crystallization step, primers of D-allulose are generally introduced into the selected crystallizer. These D-allulose primers consist of small D-allulose crystals, for example having a size ranging from 10 to 100 μm. The mass quantity of primer can vary widely depending on the type of crystallizer used. It can range from 0.001 to 1%, often from 0.01 to 0.7%, generally from 0.05 to 0.5% relative to the mass of D-allulose in the mother solution. These quantities are particularly suitable when a crystallization stage is carried out by cooling from a stock solution of D-allulose. As mentioned above, it is also possible to create primers in situ when using an evapo-cooling step.
Preferably, the crystallization step is carried out less than an hour after the concentration step, preferably less than 30 minutes after. Most preferably, the crystallization step is carried out immediately after the concentration step. This makes it possible to further limit, during the crystallization step, the amount of dimers in the mother solution to be crystallized.
Once recovered after drying, the crystals can also be subjected to an additional sieving step, which makes it possible to screen these crystals and, depending on the fraction recovered after sieving, to increase or decrease the size of the crystals. For example, this additional step makes it possible, relative to the size of the crystals subjected to the sieving step, to recover a fraction of smaller average size by volume D4.3 of D-allulose crystals passed through the sieve as well as a larger, volume-average fraction D4.3 of D-allulose crystals remaining in the sieve. To modify the crystal population and obtain the desired fraction D 4.3, it is sufficient for a person skilled in the art to select the size of the mesh of the sieve.
It goes without saying that the method according to the invention may include other steps, such as the other steps appearing in the conventional method described above and which will be described in detail later. The process according to the invention can also include additional purification steps and also intermediate dilution or concentration steps with a view to regulating the dry matter and thus carrying out under the best conditions the various steps of the process of the invention. All of these steps can be carried out continuously.
The composition of D-fructose supplied (Flux 1) for carrying out the epimerization step can be a D-fructose syrup, which can be obtained by dissolving D-fructose crystals in water or a glucose syrup / D-fructose. Preferably, this composition comprises a glucose / D-fructose syrup which comprises at least 90% by dry weight of D-fructose, preferably at least 94% of D-fructose. In a preferred mode which will be explained later in the description, the composition of D-fructose supplied for carrying out the subsequent epimerization step is a mixture (Flux 1 ′) of this D-fructose syrup with at least one recycled fraction which may be the raffinate in whole or in part (Flux 14 or 16), this recycled fraction possibly comprising a higher amount of D-allulose.
The composition of D-fructose subjected to the epimerization step can include:
• from 0 to 10% of D-allulose;
• from 70 to 100% D-fructose;
• from 0 to 10% glucose;
• from 0 to 15% of D-allulose dimer.
The epimerization step is carried out using the D-fructose composition provided previously, optionally after adjusting the dry matter. This step is generally carried out with a dry matter ranging from 30 to 60%, often from 45 to 55%. A D-psicose epimerase type enzyme or a composition comprising this enzyme is introduced into this composition. The composition comprising this enzyme can be a lyophilisate of a host microorganism synthesizing D-psicose epimerase, it can be Bacillus subtilis, in particular that described in application WO2015 / 032761 A1. The pH is adjusted according to the enzyme used, for example at a pH ranging from 5.5 to 8.5. The reaction can be carried out by heating at a temperature ranging from 40 to 70 ° C, often from 45 to 60 ° C. The reaction can last from 0.1 to 100 hours, for example from 0.2 to 60 hours. This reaction can for example be carried out on an enzymatic column, which has the advantage of also working continuously on this step. It is also possible to operate continuously to work sequentially with several reactors. To carry out this epimerization step, it is possible in particular to use the teaching of document WO 2015/032761 A1.
At the end of the reaction, a composition is formed comprising D-fructose and D-allulose, generally according to a mass ratio D-fructose / D-allulose ranging from 85/15 to 55/45, often according to a mass ratio D -fructose / D-allulose ranging from 80/20 to 60/40. This ratio depends on the epimerization parameters used and, of course, on the amount of D-allulose and Dfructose in the D-fructose composition supplied in the epimerization step; the amount of D-allulose in this composition can be especially greater in the event of recycling.
At the end of this epimerization step, if necessary, a filtration step can be performed to recover any cellular debris that may be present, especially when a lyophilisate from a host microorganism is used. This step can consist of a microfiltration step. In Figure 3, the microfiltered composition corresponds to Flux 3 and the cellular debris is recovered in Flux 17.
In the process of the invention, additional purification steps can also be carried out. Generally, before the chromatography step, a demineralization step of the composition comprising D-fructose and D-allulose (Flux 3) is carried out which can be carried out by passing over one or more cationic ion exchange resins (by for example a cationic resin of the Dowex 88 type), anionic (for example an anionic resin of the Dowex 66 type) and a cationic-anionic mixture. In Figure 3, this composition corresponds to Flux 4. The composition comprising D-fructose and D-allulose obtained is then demineralized and generally has a resistivity greater than 100 kQ.crri ¹ . It is also possible, before this demineralization step, to carry out a bleaching step of the composition comprising D-fructose and D-allulose, for example by passing over a column comprising active carbon.
The composition comprising D-fructose and D-allulose (Flux 4) can then be subjected to a chromatography step to provide at least one composition rich in D-allulose and one composition rich in D-fructose. In a preferred mode which will be explained in detail later in the description, the composition comprising D-fructose and D-allulose subjected to the chromatography step is a mixture (Flux 4 ′) of the composition resulting from the step epimerization (Flux 4) and at least one recycled fraction, this recycled fraction possibly comprising a greater amount of D-allulose.
The composition subjected to the chromatography step can comprise, relative to its dry mass:
• from 22 to 45% of D-allulose, generally from 25 to 37%;
• from 45 to 75% of D-fructose, generally from 46 to 70%;
• from 0 to 10% glucose;
• from 2 to 10% of D-allulose dimer.
To carry out this chromatography step, any type of continuous chromatography can be used, in particular of the simulated moving bed chromatography type (Simulated Moving Bed SMB), of the Improved Simulated Moving Bed type (ISMB), of the Divide Improved Simulated Moving Bed type (DISMB). ), Sequential Simulated Moving Bed (SSMB) or Nippon Mitsubishi Chromatography Improved (NMCI) type. Water is generally used as the eluent. The chromatography can be equipped with several columns in series, for example from 4 to 8 columns. The columns include ion exchange resin, for example a cationic calcium ion exchange resin. The dry matter of the composition comprising Dfructose and D-allulose can range from 40 to 70%, generally is about 50%. The temperature of the composition during chromatography generally ranges from 40 to 80 ° C, preferably from 55 to 65 ° C. This chromatography lasts the time to obtain a satisfactory separation and can last several hours.
At the end of this step, a composition rich in D-allulose (Flux 5) is obtained which can comprise, with respect to its dry matter, at least 80% of D-allulose, advantageously at least 90% of D-allulose. This composition rich in D-allulose can have a dry matter ranging from 5 to 15%. At the end of this stage, a raffinate (Flux 14) is also obtained, which generally comprises, relative to its dry matter, at least 75% of D-fructose, often at least 80% of D-fructose. This raffinate generally has a dry matter ranging from about 15 to 30%.
The composition rich in D-allulose obtained at the end of the chromatography (Flux 5) can thus comprise, relative to its dry mass:
• from 80 to 98% of D-allulose;
• 0 to 20% D-fructose;
• from 0 to 10% glucose;
• 1.5 to 5% of D-allulose dimer.
The raffinate can include, in relation to its dry mass:
• from 1 to 10% of D-allulose;
• from 70 to 99% of D-fructose;
• from 0 to 10% glucose;
• from 5 to 20% of D-allulose dimer.
Unlike a conventional process where, compared to the D-fructose introduced, the overall yield of D-allulose crystals is less than 15%, the yield of the process of the invention can be greater than or equal to 25%. Advantageously, the overall yield of Dallulose crystals is greater than or equal to 50%, for example greater than or equal to 60%, or even greater than or equal to 65%. This particularly improved yield is made possible by the fact that it is possible to carry out recycling steps without disturbing the crystallization step.
Thus the process of the invention can include at least one recycling step.
According to a preferred mode, this recycling step can consist of a recycling step of at least part of the raffinate resulting from the chromatography step (Flux 14). This raffinate may possibly have been concentrated before being mixed. It can advantageously be recycled, in whole or in part, to be mixed with D-fructose (Flux 1), for example in the form of the D-fructose glucose syrup described above, to provide the composition of D-fructose (Flux 1). '). It is then this composition of D-fructose, which is generally richer in Dallulose than the syrup of D-fructose, which is subjected to the epimerization stage.
This recycling step can consist of a step of recycling at least part of the mother liquor (Flux 13). These mother liquors can advantageously be recycled, in whole or in part, to be mixed with the composition comprising D-fructose and D-allulose (Flux 4). It is then this mixture (Flux 4 ’) which is subjected to the chromatography step. These mother liquors may possibly have been diluted before being mixed.
This recycling step can consist of a step of recycling at least part of the retentate (Flux 12). This retentate can advantageously be recycled, in whole or in part, to be mixed with the composition comprising D-fructose and D-allulose (Flux 4) and optionally the recycled mother liquors. It is then this mixture (Flux 4 ’) which is subjected to the chromatography step. This retentate may possibly have been concentrated before being mixed. In the case where the mixture is made with the retentate and mother liquors fractions, it may not be necessary to concentrate or dilute these fractions. It should be noted that the recycling of the retentate and mother liquors fractions, which are two fractions having relatively large amounts of D-allulose, make it possible to increase the richness in D-allulose (and consequently to decrease the amount of D-fructose) of the composition subjected to the chromatography step.
To carry out the possible stages of concentration of the recycled fractions, it is possible to use the same equipment and conditions described for the concentration stage allowing the manufacture of the mother solution.
According to an entirely preferred mode of the invention (FIG. 3 represents a production circuit for this preferred method of the invention), the method comprises:
a) a step of supplying a composition comprising D-fructose (Flux 1 ’);
b) an epimerization step to form a composition comprising D-fructose and D-allulose (Flux 2);
c) a chromatography step to provide a composition rich in D-allulose (Flux 5) and a raffinate consisting of a composition rich in D-fructose (Flux 14);
d) a step of nanofiltration of the composition rich in D-allulose to form a permeate (Flux 6) and a retentate (Flux 12);
e) a step of concentrating the permeate to form the mother solution to crystallize (Flux 7);
f) a step of crystallization of the mother solution (Flux 9) to form crystals (Flux 10) and mother liquors (Flux 13);
and in which is carried out:
• a step of recycling at least part of the raffinate (Flux 14 or 16) to be mixed with D-fructose (Flux 1) and supply the composition (Flux 1 ’) of step a);
• and / or a step of recycling at least part of the retentate (Flux 12) from the nanofiltration step to be mixed with the composition comprising D-fructose and D-allulose (Flux 4) from 'step b) to provide the composition (Flux 4') subjected to the chromatography step c);
• and / or a step of recycling at least part of the mother liquors (Flux 13) from the crystallization step to be mixed with the composition comprising Dfructose and D-allulose from step b) ( Flux 4) to provide the composition (Flux 4 ') subjected to the chromatography step c).
The method comprises a purging step, this purging step possibly being a purging step of at least part of at least one of the recycled fractions chosen from raffinate, retentate and mother liquors of crystallization. Indeed, for the system to remain stable, it is absolutely necessary to remove from the production circuit part of the dimers of D-allulose formed during the process. In general, the more the fractions are recycled, the more the quantity of D-allulose dimers increases in the circuit. Thus, one possibility of decreasing the amount of D-allulose dimers is to increase the quantities purged. However, this is done at the expense of the overall yield of D-allulose crystals. The process of the invention makes it possible to drastically increase the recycling of the different fractions obtained in the process, while maintaining crystallization possible.
By way of example, in the variant of the most preferred method described above where all of the raffinate, retentate and mother liquors of crystallization fractions are recycled, the stage for recycling the raffinate is advantageously partial recycling, for example of 50 to 95% of this raffinate is recycled (Flux 16) and 5 to 50% is purged (Flux 15) to provide a Dfructose composition which includes D-allulose dimers: in other words, the recycling rate the composition rich in D-fructose ranges from 50 to 95%. Preferably, the recycling rate ranges from 70 to 92%. In this case, the other two recycling operations are advantageously total recycling operations.
The purged fractions can then be used to make syrups, optionally after a concentration and / or mixing step with other compositions and / or additives.
Because the crystallization step remains stable over time, the process according to the invention is particularly advantageous because it can be continuous.
As explained above, according to the preferred variant of the invention combining the nanofiltration and crystallization step in an adiabatic crystallizer-evaporator under vacuum, the Applicant has also managed to obtain crystals having improved quality. The crystals according to the invention have, comprising a mass content of Dallulose dimer of less than 0.50%, preferably less than 0.30%. These crystals can advantageously comprise a mass content of D-allulose dimer ranging from 0.01 at 0.48%, preferably ranging from 0.02 to 0.45%, for example ranging from 0.03 to 0.40%, in particular from 0.04 to 0.30%.
An advantage of the crystals of the invention is that these crystals have small amounts of D-allulose dimer. Without being bound by any theory, the Applicant explains it by the fact that the mother solution useful for the manufacture of these crystals comprises a very low content of D-allulose dimers and by the fact that the crystallization step used work limits the formation of these dimers in situ. These crystals could thus have been obtained by the Applicant by this process, by combining the nanofiltration step with the crystallization step comprising an adiabatic evapo-cooling stage and a crystallization by cooling stage.
A disadvantage associated with D-allulose crystals of the prior art, which comprise a higher dimer content than those of the invention, is that an elongation of these crystals is observed to present a shape close to needles, especially when they are large.
Preferably, the D-allulose crystals of the invention have a volume average size D 4.3 greater than 200 μm, advantageously ranging from 210 to 800 μm, preferably from 220 to 350 μm.
The crystals of the invention, which have a lower content of D-allulose dimer, have the advantage of having a more "stocky" shape, as shown in Figures 11, 12 and 13.
This more stocky shape can result in the fact that the D-allulose crystals of the invention can have, for a given particle size by volume D 4.3 and chosen from the range from 200 to 400 μm, a ratio of Feret min / Feret max diameters greater than 0.60, advantageously ranging from 0.62 to 0.90, for example from 0.63 to 0.80. The Feret diameter is a size well known to those skilled in the art. It is deduced from the projected area of a particle, using the caliper principle. The Feret min diameter consists of the smallest of dimensions while the Feret max diameter consists of the largest of dimensions. Figure 15 shows the principle of the min and max Feret diameters on a given particle.
Preferably, the crystals of the invention have this ratio Feret min / Feret max over all of the particle sizes in the range from 200 to 400pm.
The mean volume size D4.3 as well as the min Feret / max Feret diameter ratio of the crystals are determined by a granulometer, in particular the QICPIC RODOS granulometer of the SympaTEC brand such as that used in the Examples section. Since the crystals are observed statistically in all directions in a granulometer, the values obtained by a granulometer for a population of crystals are different from the values obtained by calculation on a simple microscopic photograph of this population of crystals, the values obtained by grain size being generally higher.
Preferably, the crystals are non-agglomerated (or individualized). The fact that the crystals are not agglomerated can be verified by simple observation by optical microscopy. For example, the crystals in Figure 13 are agglomerated, unlike those in Figures 11 and 12.
This different shape results on a macroscopic scale in an improved flow of the crystals of the invention in comparison with crystals of the same average size. Also, these crystals may exhibit better behavior when caking over time.
Thus, because of their properties, the crystals obtained by the preferred process of the invention can flow easily. This is how they made it possible to obtain crystals having a flow never reached to date. They can thus be used for example advantageously as table sugar.
The D-allulose crystals of the invention can be used in known applications of allulose and, in general, of sweeteners. Among the applications which can use the D-allulose crystals of the invention may be mentioned chewings-gums in the form of tablets or dragees, candies and sucking tablets, cookies, cookies, muffins, cakes, gelatin cakes, chews, especially short-textured chews, frostings and powdered drinks.
Another object of the invention also relates to the use of a nanofiltration unit in a circuit for producing D-allulose crystals to improve the stability of the process and / or the overall yield of D-allulose crystals. This use is particularly advantageous when the raw material introduced into the circuit comprises D-fructose.
Another object of the invention also relates to the use of a nanofiltration unit in a circuit for producing D-allulose crystals to improve the quality of the crystals obtained. By improving the quality of the crystals obtained, it is understood in particular to reduce the content of D-allulose dimer and / or increase the ratio of min Feret / max Feret diameters of D-allulose crystals.
By way of illustration, other embodiments of the method according to the invention, comprising a step of recycling the mother liquors and / or a step of recycling the raffinate and / or a step of recycling the retentate are presented below.
According to a first embodiment, the method comprises:
a) a step of supplying a composition rich in D-allulose;
b) a concentration step to form the mother solution to be crystallized;
characterized in that:
• at least one recycling step consists of a recycling step of at least part of the mother liquor;
• the nanofiltration step is carried out on these recycled mother liquors to form a permeate and a retentate;
• the permeate is mixed with the composition rich in D-allulose provided in step a); and • this mixture is subjected to the concentration step b) to provide the mother solution to be crystallized;
• at least part of the mother liquor and / or the retentate is purged.
According to a second embodiment, the method comprises:
a) a step of supplying a composition rich in D-allulose;
b) a concentration step to form the mother solution to be crystallized;
characterized in that:
• at least one recycling step consists of a recycling step of at least part of the mother liquor;
• these recycled mother liquors are mixed with the composition rich in D-allulose provided in step a);
• the nanofiltration step is carried out on this mixture to provide a permeate and a retentate;
• this permeate is subjected to the concentration step b) to provide the mother solution to crystallize; and • at least part of the mother liquor is purged.
According to a third embodiment, the method comprises:
a) a step of supplying a composition comprising D-allulose and D-fructose;
b) a chromatography step to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
c) a step of concentrating the composition rich in D-allulose to form the mother solution to be crystallized;
characterized in that:
• at least one recycling step consists of a recycling step of at least part of the mother liquor;
• the nanofiltration step is carried out on these recycled mother liquors to form a permeate and a retentate;
• the permeate is mixed with the composition provided in step a);
• this mixture is subjected to the chromatography step b); and • at least part of the mother liquor is purged.
According to a fourth embodiment, the method comprises:
a) a step of supplying a composition comprising D-allulose and D-fructose;
b) a chromatography step to provide a composition rich in D-allulose and a composition rich in D-fructose;
c) a concentration step to form the mother solution to be crystallized;
characterized in that:
• at least one recycling step consists of a recycling step of at least part of the mother liquor;
• these recycled mother liquors are mixed with the composition provided in step a);
• the nanofiltration step is carried out on this mixture to provide a permeate and a retentate;
• this permeate is subjected to the chromatography step b); and • at least part of the mother liquor is purged.
According to a fifth embodiment, the method comprises:
a) a step of supplying a composition comprising D-allulose and D-fructose;
b) a chromatography step to provide a composition rich in D-allulose and a composition rich in D-fructose;
c) a concentration step to form the mother solution to be crystallized;
characterized in that:
• at least one recycling step consists of a recycling step of at least part of the mother liquor;
• these recycled mother liquors are mixed with the composition provided in step a);
• the chromatography step b) is carried out on this mixture;
• the nanofiltration step is carried out on the composition rich in D-allulose resulting from this chromatography step b), to provide a permeate and a retentate;
• this permeate is subjected to the concentration step c); and • at least part of the mother liquor is purged.
According to a sixth embodiment, the method comprises:
a) a step of supplying a composition comprising D-fructose;
b) an epimerization step to form a composition comprising D-fructose and D-allulose;
c) a step of chromatography of this composition to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
d) a step of concentrating the composition rich in D-allulose to form the mother solution to be crystallized;
characterized in that:
• at least one recycling step consists of a recycling step of the raffinate;
• the nanofiltration step is carried out on this raffinate to provide a permeate and a retentate;
• the permeate is mixed with the composition comprising D-fructose from step a);
• the epimerization stage b) is carried out on this mixture and;
• at least part of the raffinate is purged.
According to a seventh embodiment, the method comprises:
a) a step of supplying a composition comprising D-fructose;
b) an epimerization step to form a composition comprising D-fructose and D-allulose;
c) a step of chromatography of this composition to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
d) a concentration step to form the mother solution to be crystallized;
characterized in that:
• a recycling step consists of a step of recycling the raffinate obtained in the step
vs) ;
• a first nanofiltration step is carried out on this raffinate to provide a first permeate and a first retentate;
• the first permeate is mixed with the composition comprising D-fructose from step
at) ;
• the epimerization step b) is carried out on this mixture;
• a recycling step consists of a step of recycling at least part of the mother liquor;
• a second nanofiltration step is carried out on these recycled mother liquors to form a second permeate and a second retentate;
• the second permeate is mixed with the composition rich in D-allulose provided in the step
vs) ;
• this mixture is subjected to the concentration step d) to provide the mother solution to be crystallized and;
• at least part of the raffinate and / or mother liquor is purged.
According to an eighth embodiment, the method comprises:
a) a step of supplying a composition comprising D-fructose;
b) an epimerization step to form a composition comprising D-fructose and D-allulose;
c) a step of chromatography of this composition to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
d) a concentration step to form the mother solution to be crystallized;
characterized in that:
• a recycling step consists of a step of recycling the raffinate obtained in step c);
• a first nanofiltration step is carried out on this raffinate to provide a first permeate and a first retentate;
• the first permeate is mixed with the composition comprising D-fructose from step
at) ;
• the epimerization step b) is carried out on this mixture;
• a recycling step consists of a step of recycling at least part of the mother liquor;
• these recycled mother liquors are mixed with the composition rich in D-allulose provided in step c);
• a second nanofiltration step is performed on this mixture to provide a second permeate and a second retentate;
• this second permeate is subjected to the concentration step d) to provide the mother solution to be crystallized and;
• at least part of the raffinate and / or mother liquor is purged.
According to a ninth embodiment, the method comprises:
a) a step of supplying a composition comprising D-fructose;
b) an epimerization step to form a composition comprising D-fructose and D-allulose;
c) a chromatography step to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
d) a step of concentrating the composition rich in D-allulose to form the mother solution to be crystallized;
characterized in that:
• a recycling step consists of a step of recycling the raffinate obtained in step c);
• a first nanofiltration step is carried out on this raffinate to provide a first permeate and a first retentate;
• the first permeate is mixed with the composition comprising D-fructose from step a);
• the epimerization step b) is carried out on this mixture;
• a recycling step consists of a step of recycling at least part of the mother liquor;
• a second nanofiltration step is carried out on these recycled mother liquors to form a second permeate and a second retentate;
• the second permeate is mixed with the composition formed in step b);
• this mixture is subjected to step c) of chromatography; and • at least part of the raffinate and / or mother liquors is purged.
According to a tenth embodiment, the method comprises:
a) a step of supplying a composition comprising D-fructose;
b) an epimerization step to form a composition comprising D-fructose and D-allulose;
c) a chromatography step to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
d) a step of concentrating the composition rich in D-allulose to form the mother solution to be crystallized;
characterized in that:
• a recycling step consists of a step of recycling the raffinate obtained in step c);
• a first nanofiltration step is carried out on this raffinate to provide a first permeate and a first retentate;
• the first permeate is mixed with the composition comprising D-fructose from step a);
• the epimerization step b) is carried out on this mixture;
• a recycling step consists of a step of recycling at least part of the mother liquor;
• these recycled mother liquors are mixed with the composition formed in step b);
• a second nanofiltration step is performed on this mixture to provide a second permeate and a second retentate;
• this second permeate is subjected to the chromatography step c); and • at least part of the raffinate and / or mother liquors is purged.
According to an eleventh embodiment, the method comprises:
a) a step of supplying a composition comprising D-fructose;
b) an epimerization step to form a composition comprising D-fructose and D-allulose;
c) a chromatography step to provide a composition rich in D-allulose and a raffinate consisting of a composition rich in D-fructose;
d) a step of concentrating the composition rich in D-allulose to form the mother solution to be crystallized;
characterized in that:
• a recycling step consists of a step of recycling the raffinate obtained in step c);
• a first nanofiltration step is carried out on this raffinate to provide a first permeate and a first retentate;
• the first permeate is mixed with the composition comprising D-fructose from step a);
• the epimerization step b) is carried out on this mixture;
• a recycling step consists of a step of recycling at least part of the mother liquor;
• these recycled mother liquors are mixed with the composition formed in step b);
• the chromatography step c) is carried out on this mixture;
• a second nanofiltration step is performed on the composition rich in D-allulose resulting from this chromatography step b), to provide a second permeate and a second retentate;
• this second permeate is subjected to the concentration step c); and • at least part of the raffinate and / or mother liquors is purged.
In a nonlimiting manner, the invention will now be detailed in order to illustrate its advantage in the examples below.
Examples
Analytical methods
Gas chromatography
The gas chromatograph used is of the Varian 3800 type and is equipped with:
A split-splitless injector (with or without dividers);
A flame ionization detector (FID);
A computer system for processing the detector signal;
An automatic sampler (type 8400).
The different quantities are determined by gas chromatography in the form of trimethylsilylated methoxime derivatives, then quantified by the method of internal calibration.
Determination of D-allulose, D-fructose and glucose contents
The response coefficients applied are 1.25 for D-allulose and D-fructose and 1.23 for glucose. The other monosaccharides were not detected.
Sample preparation
In a tare box, weigh 100 to 300 mg of the test sample + 10 ml internal standard solution consisting of methyl α-D-glucopyranoside 0.3 mg / ml in pyridine. In a 2 ml cup, take 0.5 ml from the tare box and evaporate to dryness under a stream of nitrogen. Add 20 mg of methoxylamine hydrochloride and 1 ml of pyridine. Stopper and leave in the Reacti-therm ® type incubation system at 70 ° C for 40 min. Add 0.5 ml of N, O Bis (trimethylsilyl) trifluoroacetamide (BSTFA). Heat 30 min at 70 ° C.
Chromatographic conditions
Column: capillary DB1 40 meters, internal diameter 0.18 mm, film thickness 0.4 pm, made of 100% dimethylpolysiloxane, apolar (J&W Scientific ref.: 121-1043)
Column temperature: 100 ° C programming up to 260 ° C at a rate of 3 ° C / min, then up to 300 ° C at 15 ° C / min, maintain 5 min at 300 ° C.
Injector temperature: 300 ° C
Detector temperature: 300 ° C (Range 10 ¹² )
Pressure: 40 psi (constant flow)
Carrier gas: Helium
Injection mode: Split (Split flow rate: 100 ml / min)
Volume injected: 1, ΟμΙ
D-allulose, D-fructose and glucose were detected in this order. D-allulose, which was unknown, has a retention time under these conditions of between 39.5 and 40 minutes.
Determination of the contents of D-allulose dimers and of glucose-glucose dimers
The response coefficients applied are 1.15 for the dimers of D-allulose and maltose, and 1.08 for isomaltose. The other glucose dimers were not detected.
Sample preparation:
In a tare box, weigh 100 to 300 mg of the sample to be tested + 10 ml internal standard solution consisting of Phenyl beta-D-glucopyranoside 0.3 mg / ml in pyridine.
In a 2 ml cup, take 0.5 ml from the tare box and evaporate to dryness under a stream of nitrogen. Take up with 0.5 ml of the hydroxylamine hydrochloride solution at 40 g / l in pyridine, stopper, stir and leave for 40 min at 70 ° C.
Add 0.4 ml of BSTFA and 0.1 ml of N-Trimethylsilylimidazole (TSIM). Heat 30 min at 70 ° C.
Chromatographic conditions
Column: capillary DB1 30 meters, internal diameter 0.32 mm, film thickness 0.25 pm (J&W Scientific ref.: 123-1032)
Column temperature: 200 ° C programming up to 280 ° C at a rate of 5 ° C / min (maintain 6 min), then up to 320 ° C at 5 ° C / min, maintain 5 min at 320 ° C.
Injector temperature: 300 ° C
Detector temperature: 300 ° C (Range 10 ¹² )
Pressure: 14 psi (constant flow)
Carrier gas: Helium
Injection mode: Split (Split flow rate: 80 ml / min)
Injected volume: 1.2μΙ
Expression of results:
The content of the various constituents is expressed in g per 100 g of crude product and is
given by the following equation: Yes Pe 100 % constituent i = ---- x ---- x ---- Se P Ki
With:
Si = area of constituent peak (s) i
Se = area of the internal standard peak
Pe = Weight of internal standard introduced into the beaker (in mg)
P = weight of sample weighed (in mg)
Ki = response coefficient of component i
If the percentage obtained (expressed here in gross) exceeds 20% for one of the constituents, the sample is diluted and the CPG analysis recommenced in order to obtain a mass quantity of less than 20%.
The mass quantities expressed in crude are then expressed in dry, dividing for the dry matter of the test sample.
The mass amounts of D-allulose, D-fructose and glucose are easily determined, none of the characteristic peaks being co-eluted.
The maltose peak and D-allulose dimers can be co-eluted. It should be noted, however, that in the crystals of the invention and described in the examples below, maltose is never present.
If the characteristic maltose peaks are not detected, the surface area of Dallulose dimers is determined by integration of the unknown peaks, between 10 and 17 minutes. If the characteristic peaks of maltose are detected (which may be the case in the syrups of the invention), the amounts of maltose are determined and this amount is subtracted from the total amount of dimers.
To determine the total amount of glucose-glucose dimers, the following protocol is carried out on a sample:
• Hydrochloric hydrolysis
In a 15 ml hydrolysis tube with a Teflon screw cap, weigh approximately 50 to 500 mg of sample approximately (adjust the weighing according to the expected sugar content), add 2 ml with a two-pipette pipette of the solution d internal standard (galactitol 5 mg / ml in RO water), add 3 ml of water and 5 ml of the 4N HCl solution.
Seal tightly, shake for 1 min with the Vortex shaker. Place the tube in a thermostatically controlled dry bath regulated at 100 ° C for 1 hour, shaking from time to time.
• Demineralisation and concentration
After cooling, place the entire hydrolysis in a 50 ml beaker. Add 6 to 8 g of a 50/50 mixture of anionic resin AG4 X 4 and AG50 W 8. Leave under magnetic stirring for 5 minutes. Filter on paper. Recover the juice and repeat the demineralization stage until a pH close to water is obtained.
• Sample preparation
In a tare box, weigh 100 to 300 mg of the test sample + 10 ml internal standard solution consisting of methyl α-D-glucopyranoside 0.3 mg / ml in pyridine. In a 2 ml cup, take 0.5 ml from the tare box and evaporate to dryness under a stream of nitrogen. Add 20 mg of methoxylamine hydrochloride and 1 ml of pyridine. Stopper and leave in Reacti-therm® at 70 ° C for 40 min. Add 0.5 ml of BSTFA. Heat 30 min at 70 ° C.
The amount of total glucose in the solution (which includes the initial so-called "free" glucose and the glucose resulting from hydrolysis and in particular linked to the presence of maltose and isomaltose) is determined by GPC analysis of the glucose. The amount of maltose is easily deduced therefrom and, by difference with the total amount of dimers attributed to the peaks between 10 and 17 minutes, the amount of D-allulose dimers.
Granulometer
The values of mean size in volume D 4.3 and of Feret min / Feret max diameter ratio of the crystals are determined on a QICPIC RODOS granulometer of the SympaTEC brand, equipped with its powder dispersion module (dry process), following the manufacturer's technical manual and specifications.
Carrying out of continuous industrial processes for manufacturing D-allulose crystals
Example 1
Example 1 is a method of continuously producing D-allulose crystals. The steps of the process used are detailed in Figure 3. The composition and the flow rate after stabilization in the process are described in Tables 1a and 1b.
Step 1 :
13.1 tonnes of a mixture made up of 26% of a D-fructose syrup Fructamyl (Tereos) comprising 95% of D-fructose with 50% of dry matter (13%) is added to a stirred batch reactor of 12 m ³ MS) (Fluxl), and 74% of Flux 16 reduced to 50% MS. The whole (Flux T) is maintained at 55 ° C. Is introduced into the tank a lyophilisate of the strain Bacillus subtilis host of the enzyme D-Psicose 3 Epimerase detailed in patent WO2015032761 in an amount sufficient to have 2.5 * 10 ⁷ units of activity in the reactor. Five reactors are used sequentially so as to supply a syrup essentially composed of fructose and allulose (Flux 2) continuously at a flow rate of 1.3 t / h. The reaction conditions are as follows:
• Temperature: 55 ° C • pH = 7 • Reaction time 48h
At the end of the reaction, Flux 2 is obtained comprising a richness in D-allulose approximately equal to 25% and a richness in D-fructose approximately equal to 75%.
2nd step :
Flux 2 passes through a microfiltration membrane during a batch operation. A Flux 3 free of cellular debris is obtained and a microfiltration retentate (Flux 17) comprising the debris from the lyophilisate of Bacillus subtilis which is purged from the circuit. The microfiltration parameters are as follows:
• Transmembrane pressure: 0-3 bar • Pore size: 0.1 pm • Temperature: 50 ° C • Average flow: 15 l / h / m ² • Membrane: Sepro PS35 • Volume Concentration Factor: 33
Table 1a: Flows and composition of the flows of steps 1 to 5 of Example 1
Stage / Flow Characteristics Flux Step 1 Flow 1 Flow 16 Flux T Mass flow (kg / h) 360 1005 1365 Dry matter (%) 50 50 50 Wealth Fructose (%) 94.5 75.5 80.5 Wealth Dextrose (%) 2 6.6 5.4 Wealth Allulose (%) 1 2.1 1.7 Di-Allulose wealth (%) 1 10.9 8.3 Wealth Other (%) 1.5 4.9 4.1Step 2 / Step 3 Flux2 / 3/4 Flow 17 - Mass flow (kg / h) 1324 41 - Dry matter (%) 50 50 -Step 4 Flux 4 ’ Flow 14 Flow 5 Mass flow (kg / h) 1673 2061 2993 Dry matter (%) 50.2 26.2 10 Wealth Fructose (%) 49.6 75.5 2.8 Wealth Dextrose (%) 4.5 6.6 0.6 Wealth Allulose (%) 33.4 2.1 90.1 Di-Allulose wealth (%) 8.3 10.9 3.5 Wealth Other (%) 4.2 4.9 3Step 5 Flow 5 Flow 6 Flux12 Mass flow (kg / h) 2993 2797 196 Dry matter (%) 10 8.7 29 Wealth Fructose (%) 2.8 2.7 3 Wealth Dextrose (%) 0.6 0.6 0.7 Wealth Allulose (%) 90.1 94.4 71.7 Di-Allulose wealth (%) 3.5 0.4 16.6 Wealth Other (%) 3 1.9 8
Table 1b: Flow rates and flow composition of steps 6 to 9 of Example 1
Stage / Characteristic Flux Step 6 Flow 6 Flow 7 - Mass flow (kg / h) 2797 279 - Dry matter (%) 8.7 87 - Wealth Fructose (%) 2.7 2.7 - Wealth Dextrose (%) 0.6 0.6 - Wealth Allulose (%) 94.4 93.7 - Di-Allulose wealth (%) 0.4 1.1 - Wealth Other (%) 1.9 1.9 -Step 7a / 7b Flux7 / 8/9- Mass flow (kg / h) 279 - - Dry matter (%) 87 - -Step 8 Flow 9 Flux10 Flow 13 Mass flow (kg / h) 279 126 152 Dry matter (%) 87 97 76.5 Wealth Fructose (%) 2.7 0.1 5.4 Wealth Dextrose (%) 0.6 0 1.2 Wealth Allulose (%) 93.7 99.7 87.5 Di-Allulose wealth (%) 1.1 0.2 2.2 Wealth Other (%) 1.9 0 3.7Step 9 Flow 10 Fluxl 1 - Mass flow (kg / h) 126 122 - Dry matter (%) 97 99.8 -
Step 3:
Flux 3 is demineralized by passing over a strong Dowex 88 cationic resin and then a weak Dowex 66 anionic resin at an average flow rate of 2BV / h. The cylinders are maintained at a temperature of 45 ° C and the resistivity of Flux 4 at the end of demineralization remains greater than 100kQ.cm ' ¹ at output (Flux 4). Otherwise, the resins are regenerated.
Step 4:
Flux 4 is mixed with Flux 12 (nanofiltration retentate) and Flux 13 (crystallization mother liquors) to form a Flux 4 'which feeds continuous simulated moving bed chromatography (SMB) (SCC ARI® equipped with 8 columns) of the circuit. The average feed rate is 1673kg / h at 50% DM.
The chromatography parameters are defined as follows:
• Volume / column: 2m ³ • Resin: Dowex Monosphere 99Ca / 320 • Temperature: 60 ° C • Water flow / Flow 4 '(vol./vol.): 2.4 • Load (Supply flow / resin volume): 0 , 09 h ^-1
Two fractions are extracted: the SCC raffinate (Flux 14), the fraction rich in D-allulose (Flux 5) which leaves in the direction of step 5. 7% of Flux 14 is purged (Flux 15) in order to evacuate the allulose dimers while the rest (Flux 16) starts again in step 1 after having been brought to a dry matter of 50% by means of an evaporator.
Step 5:
Flux 5 is treated on a nanofiltration installation in batch mode. The parameters are as follows:
• Transmembrane pressure: 30 bars • Temperature: 20 ° C • Membrane: GE Duracon NF1 8040C35 • Volume Concentration Factor (FCV): 16
The allulose dimers are concentrated in the retentate (Flux 12) and this retentate is recycled and mixed with Flux 4, while the permeate (Flux 6) is recovered. FIG. 6 gives the detail of the permeation of the syrups according to the FCV.
Step 6:
Flux 6 passes through a two-stage evaporator, the pressure inside is 50 mbar. At the exit of the first stage, the Flux is at a temperature of 38 ° C and has a dry matter of 35%. Leaving the second stage, the Flux reaches a temperature of 48 ° C and has 87% dry matter. The mother solution of D-allulose (Flux 7) is obtained at the end of this step. Step 7a:
The mother solution thus formed (Flux 7) is introduced immediately after being heated to 68 ° C. by an exchanger, in an adiabatic crystallizer-evaporator under vacuum of ³ m ³ useful, inside which the pressure is maintained at 35mbars.
The operating principle of the vacuum adiabatic crystallizer-evaporator used here is detailed in Figure 4:
• Flux 7a is composed of D-allulose syrup supersaturated at 35 ° C and the finest D-allulose particles. It is mixed with Flux 7 in a ratio such that the mixture is found just below the solubility limit of the mixture (84% dry matter and 46 ° C) (Flux 7 b). The fine particles are thus remelted.
• The mass-cooked is withdrawn from the adiabatic crystallizer-evaporator at a temperature of 35 ° C, at the same speed as the mixture, so as to maintain the constant level in the adiabatic crystallizer-evaporator. This recovered mass-cooked is separated into two flows: Flux 7d and Flux 8. Flux 7d is entrained with Flux 7b to form a Flux 7c comprising the stock solution of D-allulose as well as primers for crystallization. The mixing ratio is made so as to be found again beyond the solubility (85.5% of dry matter and 42.7 ° C) so that the crystals can continue their magnifications.
• Flux 7c is thus introduced into the vacuum adiabatic crystallizer-evaporator to prolong crystallization and form the mass-cooked. The water condensed at this stage is continuously reinjected along the walls at the top of the crystallizer.
The different flows during the evapo-cooling stage in the adiabatic crystallizer-evaporator under vacuum is reported in Table 2.
Table 2: Characteristics of the different flows in the adiabatic evaporator crystallizer-evaporator
Setting Flow 7 Flow 7a) Flow 7b) Flow 7c) Flow 7d) Flow 8 Mass flow (kg / h) 279 519 798 1203 405 279 Dry matter (%) 87 83 84.1 85.1 87 87 Temperature (° C) 68.3 35 46 42.4 35 35
Step 7b:
The racked mass-cooked is injected at the top of a vertical crystallizer with a useful volume of 8m ³ and equipped with an agitator and five cooling layers. The massecuite is brought from 35 to 20 ° C in 40 hours, i.e. a cooling ramp of approximately 0.4 ° C / h. The diagram of the crystallizer is presented in Figure 5. The temperature of the cooling water in the sheets is as follows:
1. 34 ° C at input, 32 ° C at output
2. 31 ° C at inlet, 29 ° C at outlet
3. 28 ° C in inlet, 26 ° C in outlet
4. 25 ° C in inlet, 22 ° C in outlet
5. 21 ° C at inlet, 20 ° C at outlet
Step 8:
At the bottom of the crystallizer, the suspension of crystals (Flux 9) is recovered and then centrifuged on a Rousselet Robatel SC 100KSA wringer. The suspension of crystals is systematically centrifugable, which means that the process is very stable over time. The mother liquors (Flux 13) are recycled and mixed with Flux 4 and 12. The wet Dallulose crystals are recovered (Flux 10). A first clearing with water and then a final clearing with ethanol of the order of 0.5% m / m is carried out to improve the separation. The clear crystals include 3% water. Step 9:
The wet crystals are passed through a rotary dryer and dried crystals are obtained which include 0.4% water. Final cooling in a fluidized bed lowers the temperature of the crystals from 60 to 25 ° C. The final crystals are collected (Flux 11) and then conditioned. The overall yield of D-allulose crystals, which is the ratio expressed in dry mass of the mass of D-allulose crystals obtained over the mass of D-fructose introduced, is 72%.
Example 2
Example 2 is identical to Example 1 except that no recycling is carried out. Flux 7 comprises 0.7% of D-allulose dimers. The suspension of Flux 9 crystals is always centrifugable over time. Although the overall yield of crystals is only 12%, the method has the advantage of being stable, unlike the methods of the comparative examples, not using the nanofiltration step, which will be presented below.
Comparative example 1
Comparative Example 1 is identical to Example 1 except:
• that no nanofiltration step is carried out, • that no mother liquor recycling step is carried out, • that the recycling of the raffinate (Flux 14) is recycled in full to be mixed with Flux 1 of the syrup of D-fructose, • the crystallization step is carried out as follows: the mother solution formed (Flux 7) is introduced sequentially into three vertical crystallizers of useful volume of 8m ³ identical to that used for step 7b of crystallization of Example 1. The cooling ramp is 0.33 ° C / h up to 20 ° C. A primer of D-allulose of D4.3 approximately equal to 60 μm in mass quantities of 0.1% is introduced into each crystallizer, this quantity being expressed relative to the dry weight of D-allulose introduced into the crystallizer.
The production circuit used (i.e. the different stages of the process used) is that corresponding to Figure 1.
Flux 7 comprises 1.9% of D-allulose dimers. We recover a Flux 9 which is carried out in step 8. This Flux 9 is a mass-cooked material which is not always centrifugable. After a week, Flux 7 comprises 2.2% of D-allulose dimers and the mass-cooked material of Flux 9 even becomes systematically non-centrifugable (crystals of too small size).
Comparative example 2
Comparative Example 2 is identical to Comparative Example 1 with the difference that the mother liquors are completely recycled (Flux 13) to be mixed with the composition rich in Dallulose resulting from the chromatography step (Flux 5) and that the raffinate (Flux 14) is not recycled and is purged from the circuit.
The production circuit used is that corresponding to Figure 2.
Flux 7 comprises 1.9% of D-allulose dimers. We recover a Flux 9 which is carried out in step 8. This Flux 9 is a mass-cooked material which is not always centrifugable. As soon as the mother liquors are recycled, Flux 7 comprises 2.4% of D-allulose dimers and the mass-cooked material of Flux 9 even becomes systematically non-centrifugable (crystals of too small size).
Comparative example 3
Comparative Example 3 is identical to Comparative Example 1 except that the raffinate is not recycled.
The production circuit used is that corresponding to Figure 1.
Flux 7 comprises 1.9% of D-allulose dimers. We recover a Flux 9 which is carried out in step 8. This Flux 9 is a mass-cooked material which is not always centrifugable. When it is centrifugable, the mother liquors separate from the allulose crystals which can be recovered. But sometimes Flux 9 consists of a mass of small inseparable crystals, synonymous with spontaneous nucleation in the crystallizer. In this case, it is necessary to drain the Flow from the circuit. This makes the process unusable industrially.
The summary of the results obtained for these processes are reported in Table 3. The overall reported yield is an average over one week of use.
The characteristics of the crystals obtained for Examples 1, 2 and Comparative Example 3, as well as the D-allulose crystals sold by the company CJ Cheiljedang Food Ingredient are given in Table 4.
Table 3: Comparison of the different circuits tested
Example Circuit Recyclingfrom Flux 14(%) Recyclingfrom Flux 13(%) Recycling ofFlow 12 (%) Overall yield of D-allulose crystals from the continuous process Comparative example 1 Figure 1 100 0 0 (no nanofiltration) Unstable then installation stop, do notnot running continuously Comparative example 2 Figure 2 0 100 0 (No nanofiltration) Unstable then installation stop, do notnot running continuously Comparative example 3 Figure 1 0 0 0 (no nanofiltration) Unstable, does not run continuously Example 1 Figure 3 93 100 100 Stable, 72% Example 2 Figure 3 0 0 0 Stable, 12%
The process of the invention makes it possible to obtain a stable crystallization over time, which is demonstrated in the industrial process exemplified above (Examples 1 and 2). It also makes it possible to carry out very significant recycling and thus to increase the overall yield of D-allulose crystals (see Example 2). By carrying out recycling without making sure to separate the dimers of D-allulose by the nanofiltration step, the illustrative comparative examples 1 and 2 above have demonstrated that the industrial crystallization process had to be stopped because the mass-baked becomes systematically non-centrifugable (too small crystals).
Table 4: Characteristic of the crystals obtained
Crystals Residual humidity D4.3(pm) % dimers of D-allulose (CPG) Feret min / Feret max at 200 pm Feret min / Feret max at 400 pm Example 1 0.3% 302 0.2% 0.63 0.68 Example 2 0.3% 285 <0.1% 0.68 0.76 Comparative example 3 0.3% 297 0.7% 0.55 0.53 Crystals marketed by CJ Cheiljedang Food Ingredient 0.5% 346 0.7% 0.53 0.50
FIG. 14 which represents, for the crystals of Example 2 and the crystals marketed by
CJ of D-allulose, the ratio of the min Feret / max Feret diameters as a function of the particle sizes in volume D 4.3, demonstrates that it is for populations of large size, greater than or equal to 200 μm (for example in the range from 200 to 400 μm), only marked differences in appearance are observed between the crystals according to the invention and the comparative crystals. Thus, in this range from 200 to 400 μm, the Feret min / Feret max 10 ratios are, for the comparative crystals, always less than 0.55 while the crystals according to the invention have a ratio of at least 0, 63. This difference is in complete agreement with the light microscopy images of Figures 11 and 12, which visually demonstrate that the crystals according to the invention have a much chunkier appearance than the comparative crystals. With regard to the CJ crystals of FIG. 13 (light microscopy images), it is noted that these are crystals in the form of needles, not individualized.
Use of the crystals of the invention in various applications
The crystals of Example 2 were used in the manufacture of the following products.
Meal replacement drinks
The goal is to create a powdered meal replacement drink with few calories. This powdered drink should be able to flow well and form few lumps when formulated.
Formula :
Ingredients Percentages Allulose Sucrose Sugar 28.29 28.29 Milk protein concentrate 26.62 26.62 GLUCIDEX® 19 maltodextrin 22.63 22.63 NUTRIOSE® FM 06 Soluble fiber 10.82 10.82 Pea protein 9.98 9.98 Sodium caseinate 0.67 0.67 Vanilla cream flavor 0.50 0.50 Vanilla flavor 0.33 0.33 Cekol 10,000 0.17 0.17 Total 100.00 100.00
After being weighed, the ingredients are vigorously mixed in a dry blender. The drink is then easily reconstituted by adding 210 g of water to 30 g of the formula, without forming lumps.
The formula using the crystals of the invention exhibits a flow behavior quite similar to the formula comprising sucrose, while comprising far fewer calories.
Yellow cake making
The objective is to provide a yellow cake with a satisfactory texture and appearance with a caloric content reduced by 25%.
Formula :
Ingredients Reference Invention Sucrose 24.10 0.00 Cake flour 27.09 25.24 Nutriose® FB06 0.0 1.75 Egg yolk 10.00 10.00 Butter 15.45 15.45 Milk 21.81 21.81 Salt 0.25 0.25 Baking powder 0.80 0.90 Vanilla 0.50 0.50 Allulose 0.00 24.10 Total 100.00 100.00
Method:
1. Mix the flour, salt, Nutriose® and yeast;
2. Cream the butter with sucrose or allulose;
3. Add the egg yolk and vanilla to the cream then add the milk to form a creamy mixture;
4. Add the mixture comprising the flour to the creamy mixture and mix in a blender in the slow position (1 minute) then more vigorously until the formula is well mixed;
5. Pour 600 g of the dough into a 9-inch greased circular pan;
6. Bake at 180 ° C for 20 minutes.
The objective is achieved: the cake using the crystals of the invention has a very pleasant texture in the mouth (we speak of "crumb texture") and the shape of the cake is maintained after baking.
Making chocolate cookies
The following formulas have been implemented:
Ingredients Reference Allulose Allulose + Nutriose® Wheat flour 25 25 23 Baking soda 0.14 0.14 0.14 Salt 0.17 0.17 0.17 Melted butter 14.16 14.16 14.16 Nutriose® FB06 0 0 2 Allulose 0 29.17 29.17 Brown sugar 20.35 0 0 Granulated sugar 8.82 0 0 Vanilla 1.14 1.14 1.14 Eggs 7 7 7 Chocolate chips 23.22 23.22 23.22 Total 100 100 100
Method:
1. Mix the dry ingredients together;
2. Cream the butter with the sugars or allulose;
3. Add the eggs and vanilla to the creamy mixture;
4. Add the mixture comprising the flour to the creamy mixture and mix in a blender in the slow position (1 minute) then more vigorously until the formula is well mixed;
5. Add the chocolate chips and mix;
6. Weigh 30 g portions and cook at 160 ° C for 8 minutes.
Allulose cookie dough (column 2) spreads less than sugar dough (column 1). However, the dough in column 3 spreads out in the same way as the dough in column 1.
During baking, allulose cookies brown more quickly.
Note that cookies have a domed shape. The height of the cookie according to the invention is less inflated and it does not collapse after baking, unlike the sugar-based cookie, which allows it to keep a better appearance.
Allulose cookies have a good taste, although not as sweet. The texture of the cookies according to the invention is tender and wetter than sugar-based cookies.
The water activity (w a) and the humidity (M) of cookies are measured over time:
Dated Reference Allulose Allulose + Nutriose®w a Humidity (%) w a Humidity (%) w a Humidity (%) Day 1 0.6429 7.62 0.5482 8.91 0.5027 8.69 Day 7 0.7531 9.42 0.5859 9.59 0.5472 8.82 Day 30 0.7633 8.33 0.5888 9.47 0.5563 9.11
Allulose-based cookies have better moisture stability.
Making oatmeal cookies
Formulas:
Ingredients Reference Invention Wheat flour 16.84 15.09 Nutriose® FB06 0.00 1.75 Baking soda 0.42 0.42 Yeast 0.27 0.27 Salt 0.44 0.44 Butter 14.53 14.53 Sucrose 14.08 11.30 Brown sugar 13.89 0.00 Allulose 0.00 16.67 Eggs 6.43 6.43 Vanilla 0.60 0.60 Oatmeal 19.35 19.35 Inclusions * 13.15 13.15 Total 100.00 100.00
* The inclusions include 50.0 grams of pecans, 20.0 grams of cranberries and 18.6 grams of blueberries.
Method:
1. Mix the flour, Nutriose®, baking soda, yeast and salt;
2. Cream the butter with the sugars or allulose;
3. Add the eggs and vanilla to the creamy mixture;
4. Add the mixture comprising the flour to the creamy mixture and mix in a blender in the slow position (1 minute) then more vigorously until the formula is well mixed;
5. Add the oats and mix;
6. Add the inclusions and mix;
7. Weigh 30 g portions and bake at 160 ° C for 10 minutes.
Cookies obtained using allulose instead of sucrose are slightly browner and have a crunchy texture after baking.
Bubble qum manufacturing
A bubble gum was made with the recipe below:
Ingredients Parts Flama T base eraser 24 Allulose 50 Lycasin® 85/55 10 Nutriose® FB06 13.4 Liquid flavor 0.9 Powder flavor 1.2 Acidifier 0.5 Total 100
Bubble gum has a completely satisfactory appearance, similar to commercial bubble gums.

权利要求:
Claims (19)
[1" id="c-fr-0001]
1. Process for the manufacture of D-allulose crystals comprising:
• a step of supplying a composition rich in D-allulose, • a step of concentrating said solution to form a mother solution to be crystallized, • a step of crystallizing the mother solution to form Dallulose crystals and waters mothers;
• and at least one nanofiltration step.
[2" id="c-fr-0002]
2. Method according to claim 1 characterized in that the membrane used for nanofiltration has a cutoff threshold less than 300 Da, preferably ranging from 150 to 250 Da.
[3" id="c-fr-0003]
3. Method according to one of the preceding claims, characterized in that the volume concentration factor of the nanofiltration ranges from 5 to 20.
[4" id="c-fr-0004]
4. Method according to one of the preceding claims, characterized in that the crystallization step comprises:
i. an adiabatic evapo-cooling stage, carried out in an adiabatic crystallizer-evaporator under vacuum to form a massecuite, ii. followed by a crystallization stage by cooling said massecuite to form crystals.
[5" id="c-fr-0005]
5. Method according to claim 4 characterized in that the temperature during the adiabatic evapo-cooling stage ranges from 30 to 40 ° C, preferably ranging from 33 to 37 ° C, for example around 35 ° C.
[6" id="c-fr-0006]
6. Method according to one of the preceding claims characterized in that it is continuous.
[7" id="c-fr-0007]
7. Method according to one of the preceding claims characterized in that it comprises at least one recycling step.
[8" id="c-fr-0008]
8. Method according to one of the preceding claims characterized in that it comprises a step of recycling at least part of the mother liquors.
[9" id="c-fr-0009]
9. Method according to one of the preceding claims, characterized in that the step of supplying the mother solution of D-allulose comprises:
• a step of supplying a composition rich in D-allulose;
• a nanofiltration step of said composition rich in D-allulose to provide a retentate and a permeate;
• a step of recovery of the nanofiltration permeate;
• a step of concentrating this permeate to provide the mother solution of Dallulose.
[10" id="c-fr-0010]
10. Method according to claim 9 characterized in that it comprises a step of recycling at least part of the retentate.
[11" id="c-fr-0011]
11. Method according to one of claims 9 or 10 characterized in that the step of supplying the composition rich in D-allulose comprises:
• a step of supplying a composition comprising D-fructose;
• an epimerization step to form a composition comprising D-fructose and D-allulose;
• a chromatography step to provide a composition rich in D-allulose and a composition rich in D-fructose.
[12" id="c-fr-0012]
12. Method according to claim 11 characterized in that it comprises a step of recycling at least a part of the composition rich in D-fructose.
[13" id="c-fr-0013]
13. Method according to claim 12 characterized in that the recycling rate of the composition rich in D-fructose ranges from 50 to 95%.
[14" id="c-fr-0014]
14. D-allulose crystals comprising a mass content of D-allulose dimer, determined by gas chromatography (GPC), of less than 0.50%.
[15" id="c-fr-0015]
15. D-allulose crystals according to claim 14, characterized in that they comprise a mass content of D-allulose dimer ranging from 0.01 to 0.48%, preferably ranging from 0.02 to 0.45%, for example ranging from 0.03 to 0.40%, in particular from 0.04 to 0.30%.
[16" id="c-fr-0016]
16. D-allulose crystals according to one of claims 14 and 15 characterized in that they
5 have an average size by volume D 4.3 greater than 200 μm, advantageously ranging from 210 to 800 μm, preferably from 220 to 350 μm.
[17" id="c-fr-0017]
17. D-allulose crystals according to one of claims 14 and 15 characterized in that they have, for a particle size by volume D4.3 given and chosen in the
10 range from 200 to 400pm, a Feret min / Feret max ratio greater than 0.60, advantageously ranging from 0.62 to 0.90, for example from 0.63 to 0.80.
[18" id="c-fr-0018]
18. D-allulose crystals according to claim 17 characterized in that they have this ratio Feret min / Feret max over all the particle sizes by volume D4.3
15 in the range from 200 to 400pm.
[19" id="c-fr-0019]
19. Use of a nanofiltration unit in a circuit for the production of Dallulose crystals to improve the overall yield of D-allulose crystals.
1/11
Flow 14
D-Fructose
Fluxl
Fluxl '
-------->
V
Step 1: Epimerization
Flow 2
Ψ
Step 2: Microfiltration
Flow 3> Flow 17
V
Step 3: Demineralization
Flux 4 ψ
Step 4: Chromatography
Flow 5
Ψ
Step 6: Evaporation
Flow 7
Ψ
Step 8: Crystallization
Flow 9
Ψ
Step 9: Centrifugation
Flow 10> Flow 13
Ψ
Step 10: Drying
Stream it ψ
Final crystals

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同族专利:

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公开号 | 公开日

---

EP3565656A1|2019-11-13|

---

MX2019008062A|2019-09-11|

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WO2018127668A1|2018-07-12|

---

FR3061413B1|2021-08-27|

---

US20190330253A1|2019-10-31|

---

JP2020514294A|2020-05-21|

---

KR20190098991A|2019-08-23|

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法律状态:
2018-01-31| PLFP| Fee payment|Year of fee payment: 2 |

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2018-07-06| PLSC| Publication of the preliminary search report|Effective date: 20180706 |

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2019-01-30| PLFP| Fee payment|Year of fee payment: 3 |

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2020-01-30| PLFP| Fee payment|Year of fee payment: 4 |

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2021-01-28| PLFP| Fee payment|Year of fee payment: 5 |

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2022-01-31| PLFP| Fee payment|Year of fee payment: 6 |

优先权:

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申请号 | 申请日 | 专利标题

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FR1750103A|FR3061413B1|2017-01-05|2017-01-05|PROCESS FOR MANUFACTURING D-ALLULOSE CRYSTALS|

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FR1750103|2017-01-05|FR1750103A| FR3061413B1|2017-01-05|2017-01-05|PROCESS FOR MANUFACTURING D-ALLULOSE CRYSTALS|

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JP2019536587A| JP2020514294A|2017-01-05|2018-01-05|Method for producing D-allulose crystals|

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KR1020197019099A| KR20190098991A|2017-01-05|2018-01-05|Process for preparing D-allulose crystal|

---

US16/471,753| US20190330253A1|2017-01-05|2018-01-05|Method for producing d-allulose crystals|

---

MX2019008062A| MX2019008062A|2017-01-05|2018-01-05|Method for producing d-allulose crystals.|

---

EP18700791.9A| EP3565656A1|2017-01-05|2018-01-05|Method for producing d-allulose crystals|

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PCT/FR2018/050026| WO2018127668A1|2017-01-05|2018-01-05|Method for producing d-allulose crystals|