Classifications

• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
  • A23C9/00—Milk preparations; Milk powder or milk powder preparations
  • A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
  • A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
  • A23C9/1425—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration by ultrafiltration, microfiltration or diafiltration of whey, e.g. treatment of the UF permeate
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
  • A23C9/00—Milk preparations; Milk powder or milk powder preparations
  • A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
  • A23C9/146—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by ion-exchange
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
  • A23C9/00—Milk preparations; Milk powder or milk powder preparations
  • A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
  • A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
  • A23C9/1422—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration by ultrafiltration, microfiltration or diafiltration of milk, e.g. for separating protein and lactose; Treatment of the UF permeate
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
  • A23C9/00—Milk preparations; Milk powder or milk powder preparations
  • A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
  • A23C9/144—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by electrical means, e.g. electrodialysis
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
  • A23J3/00—Working-up of proteins for foodstuffs
  • A23J3/04—Animal proteins
  • A23J3/08—Dairy proteins
• • C—CHEMISTRY; METALLURGY
  • C13—SUGAR INDUSTRY
  • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
  • C13K5/00—Lactose

Definitions

• the present invention relates to the field of upgrading a dairy protein composition, in particular a whey or a milk ultrafiltration permeate, for the manufacture of a liquid composition rich in lactose.
• the agri-food industry generates large quantities of by-products each year, which can have harmful effects on the environment when they cannot be recycled.
• Whey is a by-product of milk processing, in particular the cheese industry, it can be used in animal feed, or if it cannot be recovered it is thrown away.
• Whey (Sérum Lactus), commonly known as “whey” or “whey”, is a dairy co-product which results either from the coagulation of milk during the manufacture of cheese, in particular after the separation of casein and fat during milk coagulation, or a milk membrane filtration process such as milk microfiltration. This is the liquid part.
• the solid part is called curd. It is watery, translucent and is characterized by a greenish-yellow color.
• whey those resulting from the production of caseins or fresh cheeses in an acid medium (acid whey); those from casein manufacturing using rennet and cooked or semi-cooked pressed cheeses (sweet whey); and those resulting from milk microfiltration called ideal or native serum (this is milk microfiltration permeate).
• Whey is mainly made up of water, lactose, proteins, especially serum proteins, and minerals. Whey can be enhanced by isolating lactose on the one hand and proteins on the other. Whey proteins can also be used as an ingredient for the manufacture of numerous food products, for example for the manufacture of nutritional and protein drinks.
• Ultrafiltration permeates are used in animal feed, methanization, or dairy. These permeates, low in protein, rich in lactose but also in minerals, are difficult to recycle. The production costs of these UF permeates are often supported by the high added value of its co-product, non-demineralised WPC.
• the subject of the present invention is a process for treating a dairy protein composition in order to obtain a liquid composition rich in lactose responding to the aforementioned problems, and comprising the steps: (i)- supplying a dairy protein composition;
• the serum proteins are retained in the ultrafiltration retentate, and are therefore concentrated in this retentate whereas the water and the molecules in solution of low weight molecule pass through the ultrafiltration membrane(s).
• Mineral permeation is not equivalent to lactose permeation. Certain minerals are in fact bound to serum proteins and therefore retained in the retentate.
• step (iv) makes it possible to obtain a composition liquid rich in lactose and demineralized from the dairy protein composition of step
• the present invention makes it possible to obtain a liquid composition rich in lactose, in particular with a dry mass fraction of lactose greater than or equal to 90%.
• lactose For dry mass fractions of lactose greater than or equal to 90%, in particular greater than or equal to 95%, it can be considered that it is a liquid lactose.
• Lactose exists in the state of the art in solid form (for example in powder), and is obtained after treatment in a dairy of a liquid composition comprising dry mass fractions of lactose lower than those obtained in the present invention.
• lactose in liquid form is new. This form has many advantages for its implementation, in particular for the formulation of dairy products. In addition, this exempts industrialists using the dairy protein composition (i) from providing expensive dairy products that are complex to implement.
• the lactose obtained via the process according to the invention can be upgraded in liquid form or in solid form (by implementing a water evaporation and drying step).
• the demineralization step (iii) can be any demineralization step known to those skilled in the art making it possible to lower the conductivity (psiemens/cm) and/or the dry mass fraction of minerals and/or ashes: of the composition dairy protein (i) before the ultrafiltration step (ii), and/or ultrafiltration permeate (ii) before the step iv) of treatment on the ion exchange resins.
• the intensity of this demineralization depends on the dry mass fraction of minerals in the milk protein composition in step i).
• This demineralization step (iii) can take place before the UF step (ii) in order to at least partially demineralize the dairy protein composition at the start of the UF step (ii), and/or after the step (ii) UF in order to at least partially demineralize the ultrafiltration permeate at the inlet of step (iv) comprising at least one pass over ion exchange resins.
• the ultrafiltration permeate must be highly demineralized at the input to step (iv) on the ion exchange resins in order to increase the dry mass fraction of lactose in the lactose-rich liquid composition obtained.
• This demineralization step can be carried out in a non-limiting manner as described in the present text or as described in patent EP 1,053,685 B1 or in WO 2020/207894.
• Lactose-rich liquid composition obtained means the composition recovered/collected at the output of step iv), or after a decolorization step described below or a step v) described below in particular to remove the galactose.
• the temperature of the dairy protein composition in step (i) and/or at the inlet of step (ii) and/or of the UF permeate obtained in step (ii) and/or of the retentate of UF obtained in step (ii) and/or of the UF permeate in step iv) and/or of the lactose-rich liquid composition obtained is greater than 0° C., more particularly less than or equal to 40 °C, even more particularly less than or equal to 30°C, especially less than or equal to 20°C.
• the ultrafiltration step (ii) and/or the demineralization step (iii) and/or the step (iv) on the ion exchange resins is/are carried out (i.e in such a way to maintain the treated product) at a temperature greater than 0°C, more particularly less than or equal to 40°C, even more particularly less than or equal to 30°C, in particular less than or equal to 20°C.
• Dairy protein composition The dairy protein composition of step (i) can be chosen from, in particular is chosen from the list consisting of: milk, in particular skimmed milk, a whey, and a mixture of these, optionally partially demineralized ( s).
• the whey according to the invention can be chosen from, in particular is chosen from the list consisting of: a sweet whey; sour whey; an ideal or native whey, in particular a milk microfiltration permeate; and a mixture of these.
• a sweet whey can be obtained by a physico-chemical treatment of the milk (for example precipitation and/or coagulation), in particular using rennet, making it possible to recover on the one hand the caseins and on the other hand the sweet whey .
• An ideal or native whey can be obtained by a physical membrane treatment of the milk, in particular by implementing microfiltration or ultrafiltration, making it possible to recover on the one hand the casein and on the other hand an ideal whey.
• An acid whey is preferably obtained by an acid treatment of the milk, in particular using lactic acid and/or hydrochloric acid, making it possible to recover on the one hand the caseins, and on the other hand the acid whey .
• the CPL of step (i) is milk, or sweet whey, or ideal or native whey, or acid whey.
• the CPL of step (i) is milk
• the method comprises a demineralization step (iii), in particular according to one of the embodiments described in the present text, carried out on the milk ultrafiltration permeate after step (ii).
• dairy protein composition obtained after a demineralization step (iii) carried out after UF step (ii) denotes a CPL ultrafiltration permeate from step (i), said permeate having undergone the demineralization step (iii).
• the dairy protein composition in step (i), or the dairy protein composition before or after a demineralization step (iii) carried out before or after the UF step (ii), can be pre-concentrated to increase its fraction total dry mass, mechanically (eg by reverse osmosis or nanofiltration or a combination thereof) and/or thermally (eg by water evaporation).
• the dairy protein composition in step (i) may or may not be partially demineralised, that is to say raw.
• the demineralization step (iii) can thus be a first demineralization when the dairy protein composition of step (i) has not undergone prior demineralization, or a second or nth demineralization step when the dairy protein composition of the step (i) has already been partially demineralised.
• the dairy protein composition in step (i), preferably obtained after a demineralization step (iii) carried out before or after the UF step (ii), has an ash mass fraction, calculated relative to the total dry mass of said dairy protein composition, greater than 0% and less than or equal to 6%, preferably less than or equal to approximately 2.5%.
• the dairy protein composition in step (i), or obtained after a demineralization step (iii) carried out before or after the UF step (ii), has a dry extract greater than or equal to 5% and less than or equal to 35%, more preferably greater than or equal to 10% and less than or equal to 30%.
• the dairy protein composition in step (i) is liquid during its implementation. It can be obtained by reconstituting a liquid solution from mixed powder(s) and/or liquid(s), for example by dispersing in water a whey powder, optionally partially demineralised, or a milk powder, optionally partially demineralised and skimmed, and mixtures thereof.
• the dairy protein composition in step (i), preferably obtained after a demineralization step (iii) carried out before or after a UF step (ii), has a demineralization rate greater than or equal to to 70%, more preferably greater than or equal to 80%, preferably greater than or equal to 85%, in particular greater than or equal to 90%.
• the dairy protein composition is derived from milk, which milk may be derived from any dairy female.
• the dairy protein composition is derived from a milk chosen from: cow's milk, goat's milk, sheep's milk, donkey's milk, buffalo's milk, mare's milk, camel, and a mixture of the latter, again preferably chosen from: cow's milk, goat's milk and sheep's milk and a mixture of the latter, in particular it is cow's milk.
• the whey comprises serum proteins, and preferably does not comprise any caseins remaining in the solidified (coagulated) part during the processing of the milk and/or in the retentate of the microfiltration of the milk.
• the dairy protein composition in step (i), or obtained after a demineralization step (iii) carried out before or after the UF step (ii), is a whey whose ratio of the dry mass of lactose on the total dry mass of said whey, is greater than or equal to 50%, preferably greater than or equal to 60%, more preferably greater than or equal to 70%, preferably greater than or equal to 80%, in particular greater or equal to 85%.
• the dairy protein composition in step (i), or obtained after a demineralization step (iii) carried out before or after the UF step (ii), is a whey whose ratio of the dry mass of lactose on the total dry mass of said whey is less than or equal to 90%.
• the dairy protein composition in step (i), or obtained after a demineralization step (iii) carried out before or after the UF step (ii), is a whey whose ratio of the dry mass of total nitrogenous matter (MAT), on the total dry mass of said whey, is greater than 0%, preferably greater than or equal to 1%, more preferably greater than or equal to 3%, preferably greater than or equal to 5 %.
• MAT total nitrogenous matter
• the dairy protein composition in step (i), or obtained after a demineralization step (iii) carried out before or after the UF step (ii), is a whey
• the ratio of the dry mass of total nitrogenous matter (MAT) on the total dry mass of said whey is less than or equal to 30%, preferably less than or equal to 25%, preferably less than or equal to 20%.
• the dairy protein composition in step i), or obtained after a demineralization step (iii) carried out before or after step (ii) of UF has a conductivity greater than or equal to 0.10 mS/ cm, preferably greater than or equal to 0.80 mS/cm, more preferably less than or equal to 15 mS/cm.
• the dairy protein composition in step (i), or as an input to step (ii) of UF comprises the following cations: calcium, magnesium, sodium, potassium.
• the dairy protein composition in step (i), or as an input to step (ii) of UF comprises the following anions: chloride, phosphate, sulfate, lactate, and citrate, which are in particular the anions targeted by the demineralization process according to the invention.
• dairy protein composition at the input of the UF step (ii) denotes a dairy protein composition having optionally undergone a demineralization step (Ni).
• the dairy protein composition in step (i) is a sweet whey or a native whey or a mixture of these, optionally at least partially demineralized (for example during a step (iii) before the step (ii) ultrafiltration), or an ultrafiltration permeate of the milk from step (ii), which has one of the following properties, alone or in combination: a pH between 4.7 and 6.9;
• the ratio of the dry mass of lactose to the total dry mass of sweet whey, or native whey, is greater than or equal to 70% or 80%, in particular less than or equal to 90% or 85%;
• the ratio of the dry mass of total nitrogenous matter (MAT) to the total dry mass of sweet whey, or native whey, is greater than or equal to 10%, preferably greater than or equal to 12%, in particular less than or equal at 20%;
• the ratio of the dry mass of the ashes to the total dry mass of the sweet whey, or native whey is greater than or equal to 0.1%, in particular greater than or equal to 0.3%,
• the ratio of the dry mass of the ashes to the total dry mass of the sweet or native whey is less than or equal to 4% or 3%, or
• the ratio of the dry mass of the ashes to the total dry mass of the sweet or native whey is greater than or equal to 5%, in particular greater than or equal to 7%, in particular less than or equal to 13% (when said sweet or native whey is not demineralized).
• the dairy protein composition in step (i) is an acid whey, optionally at least partially demineralized (for example during a step (iii) before step (ii) of ultrafiltration), which exhibits any of the following properties, alone or in combination:
• the ratio of the dry mass of lactose to the total dry mass of acid whey is greater than or equal to 50% or 60% or 70% or 80%, in particular less than or equal to 90%, in particular less than or equal to 85%, for example in the case of a whey resulting from the manufacture in an acid medium of cheeses or in an acid medium of caseins;
• the ratio of the dry mass of the total nitrogenous matter (MAT) to the total dry mass of the acid whey is greater than or equal to 5%, in particular less than or equal to 20%, in particular less than or equal to 15%;
• the ratio of the dry mass of the ashes to the total dry mass of the acid whey is greater than or equal to 1.5%, in particular less than or equal to 5%, or
• the ratio of the dry mass of the ashes to the total dry mass of the acid whey is greater than or equal to 5%, in particular greater than or equal to 7%, in particular less than or equal to 13% (when said acid whey is not demineralised).
• the ultrafiltration of a whey in particular which is partially demineralized, makes it possible to increase the mass fraction of lactose in the permeate.
• the ash mass fraction of the ultrafiltration retentate obtained in step (ii) is close to that of a whey protein isolate (WPI for Whey Protein Isolate).
• the mass fractions of calcium and phosphorus calculated with respect to the total dry mass of the UF retentate of an at least partially demineralized whey are reduced.
• This arrangement makes it possible to limit, or even to eliminate, the precipitation of the calcium phosphate or of the proteins on the membranes during concentration during step (ii).
• the proteins are thermally stabilized in the ultrafiltration retentate by virtue of the prior extraction of the calcium during the demineralization stage (iii) taking place before stage (ii).
• the ratio of the dry mass of lactose to the total dry mass of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), is greater than or equal to 50%, preferably greater than or equal to 60%, more preferably greater than or equal to 70%, preferably greater than or equal to 75% or 80%, more preferably greater than or equal to 85% or 90%.
• the ratio of the dry mass of lactose to the total dry mass of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), is less than or equal to 96%.
• the ratio of the dry mass of lactose to the total dry mass of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii ) on said UF permeate (ii), is greater than or equal to 96%.
• the ratio of the dry mass of the total nitrogenous matter (MAT), to the total dry mass of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), is greater than 0%, preferably greater than or equal to 1%, more preferably greater than or equal to 3%.
• the ratio of the dry mass of the total nitrogenous matter (MAT), to the total dry mass of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), is less than or equal to 20%, preferably less than or equal to 15%, more preferably less than or equal to 10%, preferably less than or equal to 5 %.
• the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), has a rate of demineralization greater than or equal to 70%, in particular greater than or equal to 75%, particularly greater than or equal to 80%, more particularly greater than or equal to 85%.
• the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), has a rate of demineralization greater than or equal to 90%, in particular greater than or equal to 95%.
• the ratio of the dry mass of the ashes to the total dry mass of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), is greater than or equal to 0.1%, in particular greater than or equal to 0.3%.
• step (iii) carried out after step (ii) on said UF permeate (ii), in particular at the input to step
• UF permeate (ii) at the inlet of stage (iv) of passage over the ion exchange resins denotes a UF permeate having optionally undergone a demineralization stage (iii).
• the conductivity of the ultrafiltration permeate obtained in step (ii), or after a demineralization step (iii) carried out after step (ii) on said UF permeate (ii), in particular at the input of step (iv), is less than or equal to 3 mS/cm.
• the UF permeate from step (ii) can be preconcentrated mechanically (eg by reverse osmosis or nanofiltration or a combination thereof) and/or thermally (eg by water evaporation).
• This concentration step makes it possible to increase the mass content of dry matter and can be carried out before or after a demineralization step (iii) carried out after step (ii).
• stage iv) comprising at least one pass over ion exchange resins makes it possible to demineralize, and optionally to deacidify the ultrafiltration permeate from stage ii).
• This step iv) also makes it possible to remove the residual nitrogenous material.
• Stage iv) also makes it possible to increase the dry mass fraction of lactose in the UF permeate resulting from stage ii) of ultrafiltration. If this UF permeate is not demineralized or is but insufficiently so, it is necessary to carry out a demineralization step (iii) before step iv).
• Percolation on a cationic resin also makes it possible to acidify the UF permeate (ii), preferably before it passes over an anionic resin which makes it possible to raise the pH of the permeate.
• the percolation on a cationic resin is advantageously a step of cationic substitution, in particular of the divalent and/or monovalent cations by hydrogen ions FT.
• this step is an acidification step (that is to say that the pH of the UF permeate (ii) is lowered following its passage over the cationic resin).
• the percolation on an anionic resin is advantageously a step of anionic substitution, in particular of divalent and/or monovalent anions by hydroxyl ions, in particular this step is a neutralization step (that is to say that the pH of the permeate of 'UF (ii) is reassembled following its passage on the anionic resin).
• the cationic resin in step (iv) can be strong or weak.
• the anion resin in step (iv) can be strong or weak.
• the percolation on a cationic resin is carried out without the latter being mixed with an anionic resin.
• the percolation on an anionic resin is carried out without the latter being mixed with a cationic resin.
• percolation on a cationic or anionic resin is understood to mean the percolation on at least one column comprising a cationic or anionic resin, preferably the treatment, in particular the circulation, of the product to be treated on a bed of particles (in particular beads) comprising a cationic or anionic resin.
• step (iv) of treatment on ion exchange resins of the at least partially demineralized ultrafiltration permeate comprises at least one pass comprising percolation on a strong cationic resin followed by percolation on a weak anionic resin.
• the weak or strong anionic resin makes it possible to raise the pH of the ultrafiltration permeate when the latter is acidic before it passes over said weak or strong anionic resin.
• said strong cationic resin comprises sulfonate groups S0 3 .
• Said strong cationic resin in the H + form makes it possible to fix the cations bound to strong or weak anions.
• a weak cationic resin in the H + form can only bind cations bound to weak acids.
• the cationic resin in particular strong, has an exchange capacity greater than or equal to 1.8 eq/litre.
• the bed of cationic resin in particular strong, preferably comprises balls whose size is greater than or equal to 0.45 mm, in particular of strong cationic styrene resin.
• the bed of anionic resin, in particular weak preferably comprises balls whose size is greater than or equal to 0.40 mm, in particular of styrene weak anionic resin.
• the anionic resin in particular weak, has an exchange capacity greater than or equal to 1.6 eq/liter.
• the water content by mass of at least one column of anionic resin, in particular weak, or of at least one column of cationic resin, in particular strong is less than or equal to 65%, in particular less than or equal to 60 %.
• the strong cationic resin during the first pass, and optionally during the second pass and/or the subsequent pass(es), is a strong cationic resin with high porosity.
• said weak anionic resin comprises tertiary amine groups, in particular making it possible to fix anions in solution at acidic pH.
• a strong anionic resin makes it possible to fix anions in solution whatever the pH of said solution.
• the weak anionic resin during the first pass, and optionally during the second pass and/or the subsequent pass(es), is a weak anionic resin with high porosity.
• Lactose-rich liquid composition obtained according to the process of the invention
• the ratio of the total mass of sugar(s) to the total dry mass of the lactose-rich liquid composition obtained is greater than or equal to 90%, preferably greater than or equal to 95%, more preferably greater than or equal to 98%, in particular greater than or equal to 99%.
• said sugar is lactose.
• sugar(s) in the present text means the monosaccharides of milk and the polysaccharides of milk, in particular lactose, and galactose.
• Polysaccharides herein include disaccharides and oligosaccharides.
• the sugar(s) is/are one or more non-ionically charged monosaccharide(s) and/or polysaccharide(s).
• the ratio of the dry mass of total nitrogenous matter to the total dry mass of the lactose-rich liquid composition obtained is less than or equal to 5%, preferably less than or equal to 3%, even more preferably less or equal to 1%, in particular less than or equal to 0.5%.
• the ratio of the dry mass of glycomacropeptide(s) to the total dry mass of the lactose-rich liquid composition obtained is less than or equal to 2%, preferably less than or equal to 0.5%, even preferably less than or equal to 0.1%, in particular not detectable or in the state of insignificant traces.
• the lactose-rich liquid composition obtained has a demineralization rate greater than or equal to 90%, preferably greater than or equal to 95%, in particular greater than or equal to 96%, or 97%, or 98% , or 99%.
• the ratio of the total dry mass of the lactose-rich liquid composition obtained to the total mass of said lactose-rich liquid composition is greater than 0%, preferably greater than or equal to 5%, even preferably greater than or equal to 10%.
• the ratio of the total dry mass of the lactose-rich liquid composition obtained to the total mass of said lactose-rich liquid composition is less than or equal to 30%, preferably less than or equal to 25%, still preferably less than or equal to 20%.
• the lactose-rich liquid composition preferably comprises water, in particular the mass fraction of which relative to its total mass is between 70% and 95%.
• the ash mass content (or dry ash mass fraction), in particular of the dairy protein composition in step (i), optionally after a demineralization step (iii), of the UF retentate (ii), or of the UF permeate (ii), optionally after a demineralization step (iii), or of the lactose-rich liquid composition obtained can be determined with the standardized method NF V04-208 October 1989, entitled "Milk - Determination of ashes - Reference method”, in particular implementing an incineration method at 525°C.
• dry extract by mass or total dry mass means the dry mass, for example of the dairy protein composition, of the UF retentate (ii), or of the UF permeate, or the dry mass of the composition liquid rich in lactose, obtained after evaporation of the water until a stable total dry mass is obtained, based on the total mass of the dairy protein composition, of the UF retentate (ii), or of the UF permeate or of the lactose-rich liquid composition, in particular at atmospheric pressure.
• Solids content by mass can be determined with the standardized method ISO 6731: January 2011, "Milk, cream, and unsweetened condensed milk - Determination of dry matter (Reference method)".
• Lactose is understood in this text to mean lactose as defined in the Codex Alimentarius, Codex Stan 212-1999: a natural constituent of milk normally obtained from whey, in particular with an anhydrous lactose content greater than or equal to 99 % mass/mass on a dry basis.
• the determination of the mass content of lactose or sugar (or dry mass fraction) can be carried out by high performance liquid chromatography, in particular using the NF ISO 22662 standard, dating from November 2007.
• the methods that can be used to quantify milk cations and anions can be chosen from the following methods: molecular absorption spectrometry, titrimetric/complexometric method, electrochemical, atomic spectrometry, capillary electrophoresis, ion chromatography/conductometric detection, nuclear magnetic resonance for 31 P, enzymatic method/UV detection.
• the dry mass fraction in total nitrogenous matter can be determined using standard NF EN ISO 8968-1 dating from May 2014 (Kjeldhal method).
• the following standards can be used to determine the mass content: for example chlorides: potentiometric titration method (NF ISO 21422, February 2019); by example in total phosphorus: method by molecular absorption spectrometry (NF ISO 9874, April 2008); for example in calcium: titrimetric method (ISO 12081:2010 standard); for example in calcium, sodium potassium and magnesium: atomic absorption spectrometric method (ISO 8070:2007 standard) or ion chromatography; for example in lactic acid/lactate via the ISO 8069 standard dating from 2005.
• CPL denotes the dairy protein composition according to the invention.
• UF is meant in the present, an ultrafiltration.
• demineralization rate means the mass reduction rate in minerals (including cations and anions) measured from the formula: ((dry mass fraction in ash or in minerals of the non-demineralized CPL - the mass content in ash or in minerals of the target CPL at least partially demineralized)/content of ashes of the non-demineralized CPL)*100).
• the demineralization rate can also be evaluated by replacing the dry mass fraction of minerals or ashes by a measurement of the conductivity (mS/cm).
• a dry mass fraction in one or more given component(s) is calculated with respect to the total dry mass of the liquid composition comprising the said component(s).
• step iv) comprises at least two passes.
• This arrangement is optimal for increasing the dry mass fraction of lactose, lowering the ash and/or mineral content and removing the remaining nitrogenous matter.
• the ultrafiltration step (ii) comprises the use of one or more ultrafiltration membrane(s) each having a minimum cut-off threshold greater than or equal to approximately 1000 Daltons, preferably greater than or equal to approximately 3000 Daltons, more preferably greater than or equal to 4000 Daltons.
• the ultrafiltration step (ii) comprises the use of one or more ultrafiltration membrane(s) each having a minimum cut-off threshold less than or equal to approximately 10,000 Daltons, preferably less than or equal to approximately 8000 Daltons, more preferably less than or equal to 7000 Daltons, preferably less than or equal to 6000 Daltons.
• the dairy protein composition at the inlet of the ultrafiltration stage ii) has a demineralization rate greater than or equal to 70%, preferably greater than or equal to 75%, more preferably greater than or equal to 80%, preferably greater than or equal to 85% or 90%.
• the dairy protein composition (i) is a whey and the method comprises at least one demineralization step (iii) taking place before the UF step (ii) in order to at least partially demineralize the protein composition dairy (i) until the target demineralization rate is reached.
• the method does not include a demineralization step (iii) taking place after the UF step (ii) and before step (iv).
• the demineralization upstream of the ultrafiltration is sufficiently advanced so that the stages (ii) of UF and of percolation on the resins in stage (iv) combined make it possible to reach a dry mass fraction of lactose between 90% and 100 %, in particular between 95% and 100%.
• the ultrafiltration permeate at the inlet of the resin treatment step (iv) has a demineralization rate greater than or equal to 80%, preferably greater than or equal to 85%, more preferably greater than or equal to 90%.
• the demineralization must be sufficient before passing over the resins so that the latter do not saturate too quickly and that the said resins make it possible to complete the demineralization already initiated and increase the dry mass fraction of lactose.
• the dairy protein composition of step (i) is milk or a whey, optionally not demineralized
• the method comprises a demineralization step (iii) carried out after step (ii) of ultrafiltration to demineralize the UF permeate until the target demineralization rate is reached.
• the demineralization step (iii), at least partially, comprises a step of substitution of the cations (iiia) by hydrogen ions FT.
• This arrangement lowers the pH of the dairy protein composition or of the UF permeate of step (ii), in particular to a pH of between 2 and 4, more particularly at a pH of between 2 and 3 (upper and lower limits included).
• the lowering of the pH and the demineralization facilitate any step(s) of nanofiltration and/or electrodialysis downstream by improving their yield and by stabilizing the composition to be treated.
• the substituted cations can be divalent cations and/or monovalent cations.
• the step of exchanging the cations (iiia) with hydrogen ions H + comprises at least one percolation of the dairy protein composition of step (i) or of the UF permeate from step (ii) on at least one column comprising (consisting of) a cationic, in particular weak or carboxylic, resin.
• the cationic resin can be strong or weak, in particular it is a weak cationic resin.
• the demineralization stage (iii) comprises, in particular downstream of stage (iiia), a stage of substitution of the anions (iiib) by hydroxyl or chloride ions.
• the substituted anions can be divalent anions and/or monovalent anions.
• the anion exchange step (iiib) with chloride ions comprises, in particular downstream of step (iiia) involving a cationic, in particular weak or carboxylic, resin, at least one step percolation of the dairy protein composition from step (i) or of the UF permeate from step (ii) over at least one column comprising (consisting of 7 ) an anionic resin, in particular strong, optionally mixed with a cationic resin, especially strong (i.e. mixed-bed).
• the step of substitution of the cations (iiia) is a step of substitution electrodialysis, in particular exclusively, cationic, carried out on an electrodialyzer comprising cells each comprising (consisting of) three compartments.
• the dairy protein composition (i) or the UF permeate (ii) circulates in a compartment, in particular the central compartment, delimited between two cationic membranes.
• the demineralization step (iii) comprises a step of substitution, in particular exclusively, of the anions (iiib), by hydroxyl ions, and the said step (iiib) is carried out on an electrodialyser comprising cells comprising
• step (iiib) is preferably carried out after step (iiia).
• the dairy protein composition (i) or the UF permeate (ii) circulates in a compartment, in particular the central compartment, delimited between two anionic membranes.
• the demineralization step (iii) comprises:
• an electrodialysis step in particular to extract anions and cations, carried out on an electrodialyzer whose cells comprise (are made up of) two compartments; then
• step (iiib) is carried out on an electrodialyser comprising cells comprising (constituted of) each three compartments.
• the demineralization step (iii) at least partially, comprises an electrodialysis step and/or a nanofiltration step, in particular carried out after step (iiia) and/or after the step (iiib).
• This electrodialysis step advantageously allows the extraction of anions and cations.
• the choice between the electrodialysis and/or nanofiltration step is made according to the dry mass extract of the dairy protein composition in step (i) or of the UF permeate in step (ii) .
• the demineralization step comprises a nanofiltration step when the dry mass extract of the dairy protein composition or of the UF permeate is less than or equal to 15%.
• the demineralization step (iii) comprises, preferably only, an electrodialysis step, in particular carried out on an electrodialyzer whose cells comprise (consist of) two compartments, still preferably carried out after the ultrafiltration step (ii).
• the demineralization step (iii) comprises an electrodialysis step, in particular carried out on an electrodialyzer whose cells comprise (consist of) two compartments, after the cation substitution step (iiia) by hydrogen ions FT, preferably the step of substitution, in particular exclusively, of the cations (iiia) is a step of cationic substitution electrodialysis carried out on an electrodialyzer comprising cells comprising (constituted of) each three compartments.
• the dairy protein composition (i) or the UF permeate (ii) circulates in a compartment, in particular the central compartment, delimited between two cationic membranes.
• the demineralization step (iii) comprises an electrodialysis step, in particular carried out on an electrodialyzer whose cells comprise (consist of) two compartments, after the cation substitution step (iiia) with hydrogen ions H + , and after the substitution step, in particular exclusively, with anions iiib).
• steps iiia) and iiib) are percolation steps on ion exchange resins, as described above.
• Said step of substitution, in particular exclusively, of the anions (iiib) can be carried out as described above on ion exchange resins or on an electrodialyzer whose cells each comprise (consist of) three compartments.
• Said step of substitution, in particular exclusively, of the cations (iiia) can be carried out as described above on ion exchange resins or on an electrodialyzer whose cells each comprise (consist of) three compartments.
• the demineralization step (iii) comprises at least one pass comprising the percolation of the CPL of step (i), or of the UF permeate (ii) of the CPL of step ( i), on a weak cationic resin, followed by a nanofiltration step, and an electrodialysis step applied to said nanofiltration retentate, in particular carried out on an electrodialyzer comprising cells each of which comprises (in particular consists essentially of) two compartments.
• the CPL in step (i) is in this case a sweet whey having a dry extract greater than or equal to 5.5%, more preferably step (iii) is carried out before the UF step (ii) on the CPL (i).
• this step (iii) makes it possible to achieve a demineralization rate greater than or equal to 70%.
• the demineralization step (iii) comprises a step of nanofiltration of the CPL of step (i), or of the UF permeate (ii) of the CPL of step (i), then an electrodialysis step carried out on said nanofiltration retentate, in particular the electrodialysis is carried out on an electrodialyzer comprising cells each of which comprises (in particular consists essentially of) two compartments.
• the CPL in step (i) is in this case an acid whey having a dry extract greater than or equal to 5.5%, more preferably step (iii) is carried out before the UF step (ii) on the CPL (i).
• this step (iii) makes it possible to achieve a demineralization rate greater than or equal to 70%.
• the demineralization step (iii) comprises at least one pass comprising the percolation of the CPL of step (i), or of the UF permeate (ii) of the CPL of step ( i), on a weak cationic resin, followed by percolation on a mixed bed of a strong cationic resin and a strong anionic resin, followed by a nanofiltration step, and finally by an electrodialysis step on said nanofiltration retentate, in particular said electrodialysis step being carried out on an electrodialyzer comprising cells each of which comprises (in particular essentially consists of) two compartments, and finally said step (iii) comprises percolation on an anionic resin, in particular weak.
• the CPL in step (i) is in this case a whey having a dry extract greater than or equal to 5.5%, more preferably step (iii) is carried out before the UF step ( ii) on the CPL O) ⁇
• this step (iii) makes it possible to achieve a demineralization rate greater than or equal to 90%.
• An electrodialysis unit may comprise cationic (cation-permeable) MEC membranes and/or anionic (anion-permeable) MEA membranes arranged in parallel and in an alternating manner.
• MECs block anions and allow cations to pass, while MEAs block cations and allow anions to pass.
• Concentration compartments (concentrates) and desalination compartments are then created.
• This most common type of electrodialysis is an electrodialysis whose basic cell unit comprises two compartments.
• the cellular unit corresponds, at the smallest repetition pattern, to concentration and desalination operations (a compartment corresponding to a concentration or a desalination).
• concentration and desalination operations a compartment corresponding to a concentration or a desalination.
• the solutions are renewed in the compartments by a circulation parallel to the plane of the membranes.
• the application of a current is ensured by two electrodes parallel to the plane of the membranes and placed at the ends of the electrodialyzer.
• the method comprises a step, taking place after step iv), comprising at least one pass comprising percolation on an adsorbent resin.
• the pass is performed on at least one column of adsorbent resin.
• this arrangement makes it possible to remove the color of the treated UF permeate, in particular riboflavin (vitamin B2).
• the adsorbent resin can be functionalized.
• the adsorbent resin is a resin with a porosity of between 10 ⁇ to 1000 ⁇ (angstrom), in particular making it possible to adsorb small organic molecules.
• the method comprises a nanofiltration step (v) carried out after the treatment step on ion exchange resins (iv).
• the nanofiltration step (v) can be carried out after or before the treatment on an adsorbent resin, preferably after the treatment on an adsorbent resin.
• This nanofiltration step (v) is carried out to remove saccharides other than lactose, in particular monosaccharides such as galactose.
• This nanofiltration step (v) can be implemented when the dry mass fraction of galactose relative to the total dry mass of the lactose-rich liquid composition obtained at the end of step (iv) is greater than or equal to 1%, in particular less than or equal to 15%. This dry mass fraction in galactose can be encountered in the processing of certain acid wheys.
• the nanofiltration membrane or membranes have a cut-off threshold greater than or equal to 150 Daltons and less than or equal to 350 Daltons.
• the lactose-rich liquid composition obtained after step v) of nanofiltration comprises a dry mass fraction of lactose relative to its total dry mass greater than or equal to 98% or 99%.
• the ratio of the dry mass of sugar(s), in particular lactose, to the total dry mass of the liquid composition rich in lactose obtained is greater than or equal to approximately 90%, preferably greater than or equal to equal to 95%.
• This ratio may be greater than or equal to 96%, 97%, 98% or even 99%.
• the lactose-rich liquid composition can be used as edible lactose, or refined lactose.
• the method comprises a step of concentration by evaporation (in particular of the water contained in the lactose-rich liquid composition) and of drying carried out after the step of treatment on the ion exchange resins iv ) for obtaining sugar(s), in particular lactose, in solid form.
• This stage of transformation of the lactose-rich liquid composition into a solid can be carried out directly after stage iv), or after the treatment on an adsorbent resin and/or after stage v).
• the lactose-rich liquid composition is subjected to a step of concentration by evaporation, then a step of drying and atomization, in particular on an atomization tower, for the manufacture of powdered lactose.
• the liquid composition obtained being very rich in lactose, it allows the manufacture of lactose without going through a dairy. This provision allows the whey producer to valorize the latter without going through the investment of a dairy which generates large volumes of crystallization mother liquors which are very difficult to valorize.
• the method comprises a demineralization step iii) carried out before the ultrafiltration step (ii), and the ultrafiltration retentate obtained at the end of step (ii) ultrafiltration, at least partially demineralized, is stable at a temperature greater than or equal to 100°C.
• the proteins of the ultrafiltration retentate are preferably stable at a temperature greater than or equal to 100°C, greater than or equal to 110°C, in particular greater than or equal to 120°C or 130°C, for at least 1 minute, preferably for at least 5 minutes, more preferably for at least 10 minutes, especially for at least 20 minutes.
• the ultrafiltration retentate (ii) has a pH adjusted to a pH greater than or equal to 6.5, in particular greater than or equal to 7.0.
• the ratio of the dry mass of Total Nitrogenous Matter (MAT) to the total dry mass of the ultrafiltration retentate obtained in step (ii) is greater than or equal to approximately 50%, preferably greater than or equal to 60% or 70% or 80% or 90%.
• the ratio of the dry mass of the ashes to the total dry mass of the ultrafiltration retentate obtained in step (ii) is less than approximately 6%, in particular less than or equal to approximately 5%.
• This ratio is preferably less than or equal to 4%, more preferably less than or equal to 3%.
• the dairy protein composition of step (i) is chosen from: milk, in particular skimmed milk, wheys, and a mixture of the latter.
• the dairy protein composition of step (i) is chosen from: an acid whey, a sweet whey, a native whey, and a mixture of these.
• the variant embodiments 1 to 16, and aforementioned embodiments can be combined independently with each other, unless otherwise specified.
• a subject of the present invention is, according to a second aspect, a liquid composition rich in lactose which can be obtained by the process with reference to the first aspect of the invention according to any one of the variant embodiments one to sixteen.
• the ratio of the dry mass of sugar(s), in particular lactose, to the total dry mass of said liquid composition rich in lactose is greater than or equal to 90%, preferably greater than or equal to 95%, still preferably greater than or equal to 96% or 97% or 98% or 99%.
• the subject of the present invention is, according to a third aspect, an installation for the implementation of a process for the treatment of a dairy protein composition to obtain a liquid composition rich in lactose, in particular according to one any of the variant embodiments with reference to the first aspect of the invention, comprising, in particular in series: a- an ultrafiltration unit comprising a first inlet intended to receive a dairy protein composition, a first outlet of an ultrafiltration permeate, and a second outlet of an ultrafiltration retentate; b- a demineralization unit for the at least partial demineralization of the dairy protein composition upstream of the ultrafiltration unit, and/or a demineralization unit for the at least partial demineralization of the ultrafiltration permeate downstream of the ultrafiltration unit; c- a treatment unit comprising ion exchange resins, downstream of the ultrafiltration unit for the demineralization of the ultrafiltration permeate previously at least partially demineralized, said unit comprising:
• At least one column A comprising a cationic resin and comprising a first inlet intended to receive said previously at least partially demineralized ultrafiltration permeate, and a first outlet for the at least partially demineralized ultrafiltration permeate PI,
• At least one column B comprising an anionic resin and comprising a first inlet intended to receive said ultrafiltration permeate PI, and a first outlet for the at least partially demineralized ultrafiltration permeate P2.
• the ultrafiltration unit comprises a concentration subunit for increasing the dry mass fraction of the dairy protein composition (as defined herein) and a diafiltration subunit downstream of the concentrating subunit.
• the ultrafiltration unit in particular the diafiltration unit, comprises one or more ultrafiltration membrane(s) each having a minimum cut-off threshold greater than or equal to approximately 1000 Daltons, preferably greater than or equal to approximately 3000 Daltons, more preferably greater than or equal to 4000 Daltons.
• the ultrafiltration unit in particular the diafiltration unit, comprises one or more ultrafiltration membrane(s) each having a minimum cut-off threshold less than or equal to approximately 10,000 Daltons, preferably less than or equal to approximately 8000 Daltons, more preferably less than or equal to 7000 Daltons, preferably less than or equal to 6000 Daltons.
• the ultrafiltration unit allows step (ii) to be carried out.
• the treatment unit comprising ion exchange resins comprising at least one chain comprising, in particular in series, at least one column comprising (made up of) a cationic resin (strong or weak), preferably strong, followed by at least one column comprising (consisting of) an anionic resin (strong or weak), preferably weak.
• the processing unit comprises ion-exchange resins allowing step (iv) to be carried out.
• the demineralization unit comprises (consists of an electrodialyser comprising cells comprising (consists of) two compartments.
• the demineralization unit comprises, in particular in series:
• an electrodialyzer comprising cells comprising (consisting of) three compartments, each cell preferably comprising a central compartment in which the product to be treated circulates (dairy protein composition/ultrafiltration permeate), said central compartment is delimited between exchange membranes of cations (mono and/or divalent), in particular it is a substitution, in particular exclusively, cationic as described above;
• an electrodialyzer comprising cells comprising (consisting of) two compartments
• an electrodialyzer comprising cells comprising (consisting of) three compartments, preferably each cell comprises a central compartment in which circulates the product to be treated (dairy protein composition/ultrafiltration permeate), said central compartment is delimited between exchange membranes of anions (mono and/or divalent), in particular it is a substitution, in particular exclusively, anionic as described above.
• the demineralization unit comprises, in particular in series:
• At least one column comprising an anionic resin, in particular strong, optionally mixed with a cationic resin, in particular strong (that is to say with mixed beds);
• nanofiltration unit or an electrodialyzer comprising cells comprising (consisting of) two compartments.
• the demineralization unit allows step (iii) to be carried out.
• the installation comprises a treatment unit comprising an adsorbent resin, in particular downstream of the treatment unit comprising ion exchange resins c).
• the installation comprises a nanofiltration unit, in particular downstream of the treatment unit comprising ion exchange resins c), in particular also downstream or upstream of the treatment unit comprising a adsorbent resin.
• Figure 1 illustrates the process for treating a dairy protein composition according to the invention
• FIG. 2 Figure 2 illustrates the treatment of the ultrafiltration permeate of Figure 1 on ion exchange resins, step (iv).
• the dairy protein composition 10 is fed to an ultrafiltration unit 20, in particular comprising a concentration subunit and a diafiltration subunit, to form a retentate of UF 30 rich in serum proteins. and a lactose-rich UF 40 permeate.
• the UF membranes have in this specific example a cut-off rate comprised between 1000 Daltons and 10000 Daltons, preferably between 4000 and 6000 Daltons.
• the milk protein composition (CPL) can be at least partially demineralized during a demineralization step (iii) before the ultrafiltration step (ii).
• the UF 40 permeate obtained in step (ii) can be demineralized, alternatively to the demineralization step taking place before the UF step (ii), or additionally to the latter during a step demineralization (iii) taking place after the UF step (ii) and before step (iv) on the ion exchange resins in order to achieve a satisfactory demineralization rate allowing the recovery of a rich liquid composition lactose after step iv), in particular the dry mass fraction of sugar(s), in particular lactose, relative to its total dry mass is greater than or equal to 90%.
• the process according to the invention can also comprise a reverse osmosis step in order to increase the dry mass fraction of the UF permeate (ii), preferably carried out before a demineralization step (iii).
• the UF 40 permeate is percolated as illustrated in FIG. 2 on columns comprising ion exchange resins, in particular in two passes 80 and 90.
• the UF 40 permeate partially demineralised is percolated on a column comprising a 50, preferably strong, cationic resin, then is percolated on a column comprising an anionic, preferably weak, 60 resin.
• the partially demineralized UF 40 permeate at the outlet of the first pass 80 is again percolated over a column comprising a cationic resin 55, preferably strong, then on a column comprising an anionic resin 65, preferably weak.
• the UF 40 permeate leaving the two passes 80 and 90 can also undergo percolation on a column comprising an adsorbent resin 70 in order to remove the coloring of the UF 40 permeate, in particular to remove the riboflavin responsible for the coloring. This step does not significantly modify the lactose mass fraction.
• the adsorbent resin may for example be an adsorbent resin with a styrene divinyl benzene matrix with sulphonic groups, highly porous, whose pore size is greater than or equal to 350 ⁇ , and having an exchange capacity of the order of 1.
• a liquid composition rich in lactose is recovered at the end of step iv) and in this specific example after the treatment on an adsorbent resin.
• This liquid composition rich in lactose, and generally in sugar(s) comprises a mass fraction of lactose relative to its very high total dry mass.
• This composition may in certain cases also comprise galactose depending on the starting dairy protein composition.
• the lactose-rich liquid composition then undergoes a step v) of nanofiltration in order to remove or reduce the mass fraction of galactose, and thus increase the mass fraction of lactose.
• This nanofiltration step v) can take place after the treatment on the adsorbent resin.
• the strong cationic resins 50 and 55 can for example be strong cationic resins, styrenic, porous, the size of the balls of which is 0.45 mm mini, the water content of which is less than or equal to 58% and the capacity of exchange of 1.8 eq/l. It may be a resin supplied by the companies Mitsubishi, Dao, or Purolite.
• the weak anionic resins 60 and 65 can for example be weak anionic, styrenic, porous resins, the size of the balls of which is at least 0.40 mm, the water content of which is less than or equal to 58% and the capacity of exchange 1.6 eq/L min.
• the dairy protein composition can be a sweet whey, an acid whey, or a native whey.
• the dairy protein composition can be milk, in particular skimmed milk.
• the ultrafiltration retentate 40 in step (ii) is rich in serum proteins and caseins.
• a strong cationic resin in particular suitable for the implementation of step (iv), can be a resin marketed by the company Mitsubishi or Dow or Purolite, in particular of the Relite RPS type, or FPC22 or PPC150S.
• a weak anionic resin in particular suitable for the implementation of step (iv), can be a resin marketed by the company Mitsubishi or Dow or Purolite, in particular of the RAM1S type, or FPA54 or A133S.
• an adsorbent resin suitable for implementing the invention may be a resin marketed by the company Mitsubishi or Dow or Purolite, in particular of the Relite RAD/F or MN500 type.
• Example 1 for treating an acid whey with partial demineralization (iii) before the UF PP step a-
• the acid whey from step i) underwent a demineralization step (iii) before the ultrafiltration step (ii).
• the partially demineralized acid whey at the inlet of the ultrafiltration stage (ii) has a pH of approximately 6; a conductivity less than or equal to 5 mS/cm, a demineralization rate of 74%, a mass dry extract of approximately 18%, a dry mass fraction of MAT of approximately 13%, an ash mass fraction of approximately 2%, a dry mass fraction of lactose of the order of 86%, a mass fraction of cations (Na + , K + , NH 4 + , Mg 2+ , Ca 2+ ) less than or equal to 1.5%, a mass fraction of anions (Cl, N0 3 ⁇ , PO4 3 , SO4 2 ) less than or equal to 0.5%.
• This partially demineralized acid whey undergoes a UF stage ii), then the UF permeate obtained is percolated on ion exchange resins in stage iv).
• the whey supply pressure during the UF in stage ii) is of the order of 4 bars.
• the temperature of the partially demineralized whey entering the UF stage (ii) is around 10°C, this temperature is maintained during the UF stage ii) and during stage iv) on ion exchange resins.
• the preceding mass fractions are calculated relative to the total dry mass of the partially demineralized acid whey at the inlet of step (ii) of UF.
• the UF permeate of the partially demineralized acid whey obtained at the outlet from UF step (ii) has a pH of approximately 6; a mass dry extract of approximately 13%, a conductivity of less than or equal to 2 mS/cm, a dry mass fraction of MAT of approximately 4%, a mass fraction of ash of less than 2%, a mass fraction of cations (Na + , K + ,NH 4 + ,Mg 2+ ,Ca 2+ ) less than or equal to 0.9%, a mass fraction of anions (CI , N0 3 ⁇ , PO 4 3 , SO 4 2 ) less than or equal to 0, 2%, a lactose mass fraction of the order of 93%.
• the preceding mass fractions are calculated relative to the total dry mass of the UF permeate of the whey at the outlet of stage (ii) of UF.
• the UF retentate of the partially demineralized acid whey obtained as a result of UF step (ii) has a pH of between 5.5 and 5.9; a mass dry extract of approximately 15%, a dry mass fraction of MAT of approximately 50%, a mass fraction of ash less than approximately 2.8%, a mass fraction of cations (Na + , K + , NH, 4 + , Mg 2+ ,Ca 2+ ) less than or equal to 1.5%, a mass fraction of anions (Cl , N0 3 ⁇ , PCV , SO 4 2 ) less than or equal to 0.3%, a mass fraction of lactose of around 50%.
• the lactose-rich liquid composition that is recovered after step iv ), and optionally passage over at least one column of adsorbent resin has a pH of the order of 6.8, a dry mass extract of approximately 10%, a conductivity less than or equal to 10 pS/cm, a dry mass fraction in MAT less than approximately 0.3%, an ash mass fraction less than or equal to 0.1%, a cation mass fraction (Na + , K + , NFi 4 + , Mg 2+ , Ca 2+ ) less than or equal to 0.001%, and a mass fraction of anions (Cl, N0 3 , P0 4 3 , SO4 2 ) less than or equal to 0.001%,
• Example 2 according to the invention of treatment of a sweet whey with partial demineralization (iii) before the UF step (ii) a-
• the sweet whey of step i) underwent a demineralization step (iii) before the ultrafiltration step (ii).
• the partially demineralised sweet whey at the inlet of the ultrafiltration stage (ii) and used below has a pH of 6.8; a demineralization rate of 90%, a mass dry extract of approximately 20%, a dry mass fraction of MAT of approximately 13%, a mass fraction of non-protein nitrogenous matter of less than 2%, an ash mass fraction of approximately 1% , a lactose mass fraction of 80%.
• the preceding mass fractions are calculated relative to the total dry mass of the partially demineralized sweet whey at the inlet of step (ii) of UF.
• This partially demineralized sweet whey undergoes a UF stage ii), then the UF permeate obtained is percolated on ion exchange resins in stage iv).
• the whey supply pressure during the UF in stage ii) is of the order of 4 bars.
• the temperature of the partially demineralized whey entering the UF stage (ii) is around 10°C, this temperature is maintained during the UF stage ii) and during stage iv) on ion exchange resins.
• the UF permeate of the partially demineralised sweet whey obtained at the output of UF step (ii) has a pH of 6.5; a mass dry extract of approximately 13%, a conductivity of the order of 600 pS/cm, a dry mass fraction of MAT of approximately 1%, a mass fraction of non-protein nitrogenous matter of less than 1%, a mass fraction of ash less than or equal to 0.6%, a mass fraction of cations (Na + , K + , NH 4 + , Mg 2+ , Ca 2+ ) less than or equal to 0.3%, a mass fraction of anions (CI , N0 3 ⁇ , PO 4 3 , SO 4 2 ) less than or equal to 0.1%, a lactose mass fraction of 91%.
• the demineralization rate of the UF permeate is around 99%.
• the preceding mass fractions are calculated relative to the total dry mass of the UF permeate of the whey at the outlet of stage (ii) of UF.
• the UF retentate of the partially demineralized sweet whey obtained at the output of UF step (ii) has a pH of less than or equal to 7; a mass dry extract of approximately 20%, a dry mass fraction of MAT of approximately 50%, a mass fraction of non-protein nitrogenous matter less than or equal to 5%, a mass fraction of ash less than or equal to approximately 0.5% .
• the lactose-rich liquid composition obtained after step iv), and optionally passing over at least one column of adsorbent resin has a pH between 5 and 6, a dry mass extract of approximately 13%, a conductivity less than or equal to 5 pS/cm, a dry mass fraction of MAT less than or equal to approximately 0.4%, a mass fraction of non-protein nitrogenous matter less than or equal to 0.1%, mass fraction of ash less than or equal to 0.1%, mass fraction of cations (Na + , K + , NH 4 + , Mg 2+ , Ca 2+ ) less than or equal to 0.012%, and a mass fraction of anions (Cl, N0 3 , P0 4 3 , S0
• the lactose mass fraction is around 99%, which is lower than the value of 99.8% obtained with a double pass.
• the extraction rate of Glycomacropeptides and riboflavin is close to 100%.
• the preceding mass fractions are calculated relative to the total dry mass of the lactose-rich liquid composition obtained.
• Example 3 according to the invention of treatment of a native whey with demineralization (iii) after the UF step (ii) a- A native whey (step i) undergoes an ultrafiltration step (ii) then reverse osmosis to preconcentrate it.
• the preconcentrated native whey ultrafiltration permeate has a pH of 6.0; a conductivity less than or equal to 10.5 mS/cm, a dry mass fraction of approximately 15%, a dry mass fraction of MAT of approximately 3%, an ash mass fraction of approximately 9%, a dry mass fraction of lactose of around 84%, a mass fraction of cations (Na + , K + , Mg 2+ , Ca 2+ ) calculated with respect to the total dry mass less than or equal to 3.6%, a mass fraction of anions ( CI, P-P0 4 3 , S-S0 4 2 ) less than or equal to 2.3%.
• This ultrafiltration permeate (40) undergoes a demineralization step (iii) by electrodialysis iii) (whose cells comprise two compartments), then is percolated over ion exchange resins in step iv).
• the temperature of the ultrafiltration permeate during the electrodialysis step (iii) is of the order of 30° C., this temperature is lowered to 10° C. during step iv) on the ion exchange resins.
• the preceding mass fractions are calculated relative to the total dry mass of ultrafiltration permeate at the inlet of step (iii) of demineralization.
• a dry mass fraction of MAT of approximately 2%, a mass fraction of ash less than 1%, a mass fraction of cations (Na + , K + , Mg 2+ , Ca 2+ ) less than or equal to 0.13%, a mass fraction of anions (Cl, P-P0 4 3 , S-SO 4 2 ) less than or equal to 0.27%, a dry mass fraction of lactose of the order of 97%.
• the rate of demineralization of the UF permeate after stage (iii) is of the order of 96%.
• the preceding mass fractions are calculated relative to the total dry mass of the UF permeate at the outlet from step (iii) of demineralization.
• (iv) such as the 80.90 double pass, the lactose-rich liquid composition obtained after step iv), and optionally the passage over at least one column of adsorbent resin, has a pH of the order of 5, a mass dry extract of approximately 13%, a conductivity less than or equal to 5 pmS/cm, a dry mass fraction of MAT less than approximately 0.8%, an ash mass fraction less than or equal to 0.1%, a fraction mass fraction in cations (Na + , K + , Mg 2+ , Ca 2+ ) less than or equal to 0.001%, and a mass fraction in anions (CI , P0 4 3 , SO 4 2 ) less than or equal to 0.001%, and a dry mass fraction of lactose of the order of 99.5%.
• the preceding mass fractions are calculated relative to the total dry mass of the lactose-rich liquid composition obtained.
• Example 4 according to the invention of treatment of a native whey with demineralization (iii) after the UF step (ii) a-
• the native whey (i) undergoes an ultrafiltration step (ii) and osmosis reverse to pre-concentrate it.
• the preconcentrated native whey ultrafiltration permeate has a pH of approximately 6; a conductivity less than or equal to 10.5 mS/cm, a dry mass fraction of approximately 17%, a dry mass fraction of MAT of approximately 3%, an ash mass fraction of approximately 9%, a dry mass fraction of lactose of around 84%, a mass fraction of cations (Na + , K + , Mg 2+ , Ca 2+ ) calculated with respect to the total dry mass less than or equal to 3.6%, a mass fraction of anions ( CL, P-PO 4 3 ,, S-SO 4 2 ) less than or equal to 2.3%.
• the demineralization stage iii) comprises a sequence of three electrodialyses: an electrodialysis of substitution of cations by hydrogen ions H + (iiia) (ESC) in three compartments, followed by electrodialysis two compartments of demineralization, and followed by anion substitution electrodialysis by hdroxyl ions (iiib) (ESA) in three compartments.
• the temperature of the ultrafiltration permeate during the electrodialysis stage (iii) is of the order of 30° C., this temperature is lowered to 10° C. during stage iv) on the exchange resins of ions.
• the preceding mass fractions are calculated with respect to the total dry mass of ultrafiltration permeate at the inlet of the demineralization stage (iii), b-
• the UF permeate from the whey undergoes a first ESC electrodialysis (iiia) which makes it possible to to substitute the cations by protons and thus to work in acid way.
• the whey leaving the ESC (iiia) has a pH of approximately 1.5; a mass dry extract of approximately 16%, a conductivity of approximately 12 mS/cm, a dry mass fraction in MAT of approximately 2%, a mass fraction in cations (Na + , K+, Mg 2+ , Ca 2+ ) lower or equal to 0.8%, a mass fraction of anions (Cl, P-P0 4 3 , S0 4 2 ) less than or equal to 1.9%, a mass fraction of lactose of the order of 95%.
• the acidified whey then undergoes approximately 90% demineralization by conventional two-compartment ED electrodialysis.
• the whey leaving the ED has a pH of approximately 2.6; a mass dry extract of approximately 16%, a conductivity of approximately 1 mS/cm, a dry mass fraction in MAT of approximately 2%, a mass fraction in cations (Na + , K + , Mg 2+ , Ca 2+ ) lower or equal to 0.13%, a mass fraction of anions (CI, P-P0 4 3 , S0 4 2 ) less than or equal to 0.19%, a dry mass fraction of lactose of the order of 97%.
• the partially demineralized whey then undergoes approximately 96% demineralization by anionic substitution electrodialysis ESA (iiib).
• the whey leaving ESA (iiib) has a pH of approximately 8; a mass dry extract of approximately 16%, a conductivity of approximately 0.4 mS/cm, a dry mass fraction of MAT of approximately 2%, a mass fraction of cations (Na + , K + , Mg 2+ , Ca 2+ ) less than or equal to 0.13%, a mass fraction of anions (Cl, P-P0 4 3 , S0 4 2 ) less than or equal to 0.15%, a dry mass fraction of lactose of around 98% .
• the lactose-rich liquid composition obtained after step iv), and optionally passage over at least adsorbent resin has a pH of the order of 5, a dry mass extract of approximately 13%, a conductivity less than or equal to 5 ⁇ S/cm, a dry mass fraction of MAT less than 0 8%, a mass fraction of ash less than or equal to 0.1%, a mass fraction of cations (Na + , K + , Mg 2+ , Ca 2+ ) less than or equal to 0.001%, and a mass fraction in anions (Cl, PC, SO 4 2 ) less than or equal to 0.001%, and a dry mass fraction in lactose of the order of 99.5%.
• the preceding mass fractions are calculated relative to the total dry mass of the lactose-rich liquid composition obtained.
• the demineralization step (iii) carried out in Examples 1 and 2 can be any demineralization step known to those skilled in the art making it possible to demineralize the dairy protein composition at the start of the UF step (ii) and/or after step (ii) of UF in order to lower the dry mass fraction of minerals of the UF permeate at the inlet of step (iv) comprising at least one pass over ion exchange resins.
• This demineralization step can be carried out in a non-limiting manner as described in the present text or as described in patent EP 1,053,685 B1 or WO 2020/207894 or as described in examples 3 and 4.

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