Sugar treatment process and device

Abstract

The invention relates to a sugar treatment process comprising successively: a first frontal filtration of a sugary juice to obtain a first filtrate; a second frontal filtration of the first filtrate to obtain a second filtrate; and contacting the second filtrate with a cation exchange chromatography resin so as to charge the bivalent cationic resin and collect an attenuated sugary juice, the resin being arranged in the form of a bed with a height h of 0.75 to 3 meters. The invention also relates to a sugar treatment device.

Description

1 / 32 SUGAR TREATMENT PROCESS AND DEVICE Field of invention

[001] The present invention relates to a sugar treatment process, including a step for attenuating a sugar syrup over an ion-exchange chromatography resin. The present invention also relates to a sugar treatment device that notably allows the attenuation of a sugar syrup. Technical background

[002] The production of refined sugar from sugar cane comprises a number of treatments carried out in the sugar industry followed by a number of supplementary treatments carried out in the refinery.

[003] In the sugar industry, the main steps are the extraction of sugar by milling, that is, pressing the cane or by diffusion to obtain a raw sugary juice, the clarification of this juice using lime in order to precipitate a certain number of impurities as well as the addition of carbon dioxide (carbonation) or sulfur dioxide (sulfitation) in order to precipitate excess lime, the filtration or decantation of the treated juice, the concentration of the remaining juice and finally the crystallization and centrifugation of the sugar, which lead to obtaining brown sugar, on the one hand, and molasses, on the other.

[004] In a refinery, the main operations to which brown sugar is subjected are refining (washing the crystals with a saturated aqueous sugar solution after centrifugation) to eliminate impurities located on the surface of the crystals, re-soiling the resulting sugar, clarification, decolorization and crystallization.

[005] However, the excess of precipitated lime, notably in the form Petition 870260056618, dated 11 / 06 / 2026, p. 14 / 57 2 / 32 of calcium carbonate (CaCO3) or calcium sulfate (CaSO4) can cause problems by accumulating and precipitating in equipment and piping over time. More precisely, mineral deposits can form in the evaporator used for concentrating sugarcane juice, increasingly reducing heat exchange and thus progressively decreasing its effectiveness. Therefore, maintaining the same evaporation rate over time requires increased steam consumption and / or an increased heating surface area. Furthermore, after a certain level of performance reduction, the evaporator must be deactivated to clean the formed deposits. This cleaning process, which includes a series of chemical and mechanical cleanings (manual operation), requires the systematic opening of the equipment and is considered dangerous, given the high temperatures around the evaporator and the need to use concentrated chemicals.Furthermore, deactivating and restarting an evaporator requires additional consumption of coolant in one case and steam in the other, due to the inertia of the device.

[006] There are some enhanced cleaning solutions, however they require a significant investment as well as high operating costs.

[007] Attenuation of sugarcane juice is a method that allows reducing the amount of cationic counterions that cause mineral deposits. The most common technique for attenuating sugarcane juice is based on the use of a cation exchange chromatography resin (before the evaporation step), for example, in the form of Na+ or K+, to exchange the divalent cations (Ca2+, Mg2+) present in the sugarcane juice for monovalent cations (Na+ or K+) and avoid the problems mentioned above. This technique is frequently combined with membrane filtration (filtration). Petition 870260056618, dated 11 / 06 / 2026, page 15 / 57 3 / 32 tangential) performed before the ion exchange chromatography step, in order to eliminate suspended matter present in the clarified broth, which can very quickly degrade the performance and capacity of the installation used for ion exchange chromatography.

[008] However, the use of filtration membranes makes the implementation of this technique very expensive.

[009] The article by V. Kochergin and JF Alvarez (Ion-exchange softening of clarified juice-results of pilot trials) in the Agribusiness Intelligence JournalInforma in 2017 describes trials carried out for the attenuation of sugarcane juice, in the implementation of filtration in a screen filter, followed by a cation exchange over a shallow resin bed (shallow bed resin).

[010] Document FR 2 838 751 describes a process for manufacturing refined sugar from sugarcane juice, such as raw sugarcane or sugar beet juice, containing sugars and impurities, characterized by comprising (among other things) tangential filtration of the sugarcane juice to obtain a retentate and a filtrate, and attenuation of the filtrate to obtain an attenuated filtrate. Tangential filtration is preferably membrane filtration (ultrafiltration, nanofiltration, microfiltration) and attenuation is carried out using a cation exchange resin.

[011] Document CN 103725802 describes a process for refining sugar. This process comprises (among others) a pretreatment step which may be filtration by screen filter or bag filter, a microfiltration step by membrane, an anion exchange step for decolorizing the juice and a cation exchange step for desalinating the juice.

[012] Document FR 2 732 358 describes a treatment process Petition 870260056618, dated 11 / 06 / 2026, page 16 / 57 4 / 32 of a sugary solution derived from beetroot is filtered using cationic ion exchange resin to attenuate the sugary solution, followed by regeneration of the cationic resin. Filtration may precede the ion exchange step.

[013] US patent 6,479,636 describes a method for extracting and purifying recombinant proteins from transgenic sugarcane. This method comprises several filtration steps in a screen filter and an ion exchange step in an anionic resin.

[014] WO 2005 / 031006 describes a process in which raw sugarcane juice is first refined in several stages, then bioenzymatically converted into inverted syrup or a concentrated solution of refined glucose and fructose. The refining stages preferably comprise a first filtration (particle filtration or microfiltration) followed by a second filtration (microfiltration or ultrafiltration) and then at least one pass through a column comprising an anion exchange resin.

[015] Document CN 102659855 refers to a sugar production process comprising (among others) a filter press filtration step, a pre-treatment step comprising filtration, a membrane filtration step, and an ion exchange step to remove the color from the flavonoids.

[016] There is therefore a need to provide an improved process for sugar treatment, comprising a sugarcane juice attenuation step, which would avoid the risks of plant malfunction, the risks associated with plant cleaning, but also reduce the economic and energy costs related to the various stages of the process. Summary of the invention Petition 870260056618, dated 11 / 06 / 2026, page 17 / 57 5 / 32

[017] The invention relates primarily to a sugar treatment process, comprising successively: - a first frontal filtration of a sugary broth to obtain a first filtrate; - a second front filtration of the first filtrate to obtain a second filtrate; and - bring the second filtrate into contact with a cation exchange chromatography resin in order to load the resin with divalent cations and collect an attenuated sugary broth, the resin being arranged in the form of a bed with a height h of 0.75 to 3 meters.

[018] According to certain embodiments, divalent cations comprise, and preferably consist essentially of Ca2+ cations and / or Mg2+ cations.

[019] According to certain embodiments, the sugared juice has a concentration of solid particles of 20 to 500 mg / kg, and / or a concentration of magnesium ions of 100 to 500 mg / L, and / or a concentration of calcium ions of 100 to 600 mg / L.

[020] According to certain modalities, the sweetened broth has a sugar content of 10 to 20 degrees Brix, and / or a turbidity of 100 to 500 NTU.

[021] According to certain embodiments, the attenuated sugar broth collected after the step of contacting the second filtrate with the resin has a volume of 15 to 80 BV.

[022] According to certain methods, the first filtration allows a retention of 10 to 60% by mass of solid particles in relation to the amount of solid particles present in the sugarcane juice, and / or the first filtration and the second filtration allow a retention of 30 to 70% by mass of solid particles in relation to the amount of solid particles present Petition 870260056618, dated 11 / 06 / 2026, page 18 / 57 6 / 32 in the sugared juice, and / or the first filtration, the second filtration and placing the second filtrate in contact with the resin allow a retention of 50 to 90% by mass of solid particles in relation to the amount of solid particles present in the sugared juice.

[023] Depending on certain modalities, the process is either a discontinuous process or a continuous process.

[024] According to certain embodiments, the process comprises the steps of regenerating the resin loaded with divalent cations, such steps comprising: - bring the resin, loaded with a regeneration solution, into contact with the solution; - to collect a regeneration effluent.

[025] According to certain embodiments, the regeneration solution is derived from molasses formed during a sugar crystallization step, or the regeneration solution is derived wholly or partly from attenuated sugar juice, with or without added sodium hydroxide or potassium hydroxide, or the regeneration solution is a regeneration brine solution comprising a chloride, potassium or sodium salt, or the regeneration solution is derived from a distillation vinasse of molasses; or the regeneration solution is derived from a raffinate resulting from a chromatography treatment of molasses.

[026] According to certain embodiments, contacting the resin loaded with a regeneration solution involves using different regeneration solutions alternately between two production cycles.

[027] According to certain modalities, the regeneration effluent is used to carry out a clarification step of the sugarcane juice, in particular a liming step, the clarification step being carried out before Petition 870260056618, dated 11 / 06 / 2026, page 19 / 57 7 / 32 of the first filtration; or the regeneration effluent is used to perform one or more crystallization steps, with the crystallization step(s) being performed after the second filtrate is placed in contact with the resin.

[028] According to certain embodiments, the process also comprises a washing step of the resin loaded with divalent cations, or of the regenerated resin, with a washing solution, the washing solution having a direction in the resin bed opposite to a direction of the second filtrate in the resin bed during the step of bringing the second filtrate into contact with the resin.

[029] According to certain embodiments, the washing solution is derived from attenuated sugar broth or from sugar broth, or the washing solution is water.

[030] According to certain models, at the end of the washing stage a washing effluent is collected, the washing effluent being returned to a clarification stage of the sugary juice, the clarification stage being carried out before the first filtration.

[031] According to certain embodiments, the step of bringing the second filtrate into contact with the resin is carried out at a temperature equal to or greater than 75°C.

[032] The invention also relates to a sugar treatment device, comprising: - a supply line for a sugary broth; - a first front filtration unit fed by the sugarcane juice supply line; - a collection line for the first filtrate exiting the first front filtration unit; - a second front filtration unit fed by the collection line Petition 870260056618, dated 11 / 06 / 2026, page 20 / 57 8 / 32 of first filtered; - a collection line for the second filtrate exiting the second front filtration unit; - an ion-exchange chromatography unit comprising a cationic resin fed through the second filtrate collection line, the resin having the form of a bed with a height h of 0.75 to 3 meters; and - a collection line for attenuated sugar broth exiting the ion-exchange chromatography unit.

[033] According to certain embodiments, the first filtration unit comprises one or more screen filters, each filter with pores having a diameter of 50 to 200 μm, and preferably 80 to 120 μm.

[034] According to certain embodiments, the first filtration unit comprises a cleaning unit for at least one of the screen filters.

[035] According to certain embodiments, the second filtration unit comprises at least one filter basket having pores with a diameter of 20 to 100 µm, and preferably 40 to 60 µm.

[036] According to certain embodiments, the ion-exchange chromatography unit comprises at least one column, preferably at least 5 columns, preferably even at least 10 columns, and even at least 15 columns.

[037] According to certain embodiments, the resin bed has a diameter of 0.25 to 6 m, and preferably 0.25 to 5 m.

[038] The present invention makes it possible to respond to the need expressed above. It provides more particularly an improved sugar treatment process, comprising a sugar syrup attenuation step, making it possible to avoid the risks of plant malfunction, the risks related to plant cleaning, but also to reduce the Petition 870260056618, dated 11 / 06 / 2026, page 21 / 57 9 / 32 economic and energy costs related to the different stages of the process.

[039] This is achieved by means of a sugar treatment process comprising the successive steps of a first front filtration, a second front filtration and an ion exchange chromatography step in a cationic resin. The two successive front filtration steps protect the ion exchange chromatography resin and the ion exchange chromatography unit from performance and capacity degradation problems by separating solid particles that are suspended in the sugar juice and that risk accumulating in the ion exchange chromatography unit. This allows for improved efficiency of the attenuation step without damaging the ion exchange chromatography unit. The two filtration steps then smooth out variations in the solid particles present in the product and limit the number of fibrous solid particles accumulated in the ion exchange chromatography unit.Thus, advantageously, at the end of the second filtration, 30 to 70% by mass of particles present in the sugarcane juice are retained by the filters, and at the end of the ion-exchange chromatography stage, 50 to 90% by mass of particles present in the sugarcane juice are retained by the filters and the resin. Therefore, this process not only protects the ion-exchange chromatography resin and the ion-exchange chromatography unit, but also prevents the formation of deposits in the installations, particularly in the evaporator during juice concentration, and limits all the inconveniences related to the cleaning and recurrent deactivation of these installations.

[040] Furthermore, the first front filtration and the second front filtration are preferably carried out in filtration units without ceramic or other mineral-type membranes (stainless steel, for example), which Petition 870260056618, dated 11 / 06 / 2026, page 22 / 57 10 / 32 allows you to reduce the cost of these steps in the process.

[041] Advantageously, washing the resin loaded with divalent cations (Ca2+ and Mg2+) with a washing solution, the washing solution with a direction in the resin bed opposite to the direction of the second filtrate in the resin bed (during the production of the attenuated sugar broth), this washing is also called backwashing, makes it possible to expel the solid particles retained in the ion-exchange chromatography unit. More precisely, these retained particles preferentially accumulate near the inlet (e.g., at the top) of the ion-exchange chromatography unit. During the washing step, and thanks to the direction of the washing solution (e.g., from the bottom to the top of the unit) and the flow of the washing solution, an expansion of the resin bed in the ion-exchange chromatography unit can be obtained.The solid particles present in the unit generally have a lower density than the resin, and can be expelled from the unit without causing the resin particles to be released. Thus, the resin, now essentially devoid of solid particles, can be regenerated and reused. Brief description of the figures

[042] [Fig. 1] schematically represents a Cartesian grid comprising a first series of wires (A), a second series of wires (B), and a third series of wires (C).

[043] [Fig. 2] schematically represents the different stages of the process according to the invention, in certain embodiments. Detailed description

[044] The invention is now described in more detail and not limitingly in the following description.

[045] The invention relates to a device as well as a process Petition 870260056618, dated 11 / 06 / 2026, page 23 / 57 11 / 32 for sugar treatment, which allows the elimination of solid particles found in suspension in a sugar syrup as well as divalent cations such as calcium ions Ca2+ and / or magnesium ions Mg2+ present in the sugar syrup. More specifically, this process aims to purify and notably attenuate a sugar syrup. Sugary broth

[046] By sugarcane juice, it is understood a liquid stream containing sugars and impurities, notably suspended solid particles and Ca2+ and / or Mg2+ cations. Preferably, the suspended solid particles comprise bagasse and fine bagasse fractions called bagasse chips. By bagasse, it is understood the suspended fibrous solid particles resulting from the extraction of the sugarcane juice, and by bagasse chips, it is understood the suspended fine fibrous solid particles resulting from the extraction of the sugarcane juice.

[047] Sugary juice is advantageously derived from sugar cane. It may have undergone one or more pre-treatment steps called clarification, such as centrifugation, filtration, carbonation, flocculation, decantation, sulfitation and / or liming.

[048] Attenuation refers to the reduction in the hardness of the sugarcane juice due to the presence of divalent ions, notably Ca2+ and / or Mg2+. Thus, during the attenuation of the sugarcane juice, the Ca2+ and / or Mg2+ ions are eliminated and replaced by monovalent cations such as sodium (Na+) or potassium (K+) ions.

[049] Ca2+ and / or Mg2+ ions may be naturally present in the sugarcane juice and / or originate from one or more pretreatment steps such as those mentioned above.

[050] Advantageously, the sugary broth to which the invention process is applied comprises Ca2+ ions at a concentration of 100 to 800 Petition 870260056618, dated 11 / 06 / 2026, page 24 / 57 12 / 32 mg / L, and preferably 100 to 600 mg / L. For example, this concentration of Ca2+ ions can be 100 to 150 mg / L; or 150 to 200 mg / L; or 200 to 250 mg / L; or 250 to 300 mg / L; or 300 to 350 mg / L; or 350 to 400 mg / L; or 400 to 450 mg / L; or 450 to 500 mg / L; or 500 to 550 mg / L; or 550 to 600 mg / L; or 600 to 650 mg / L; or 650 to 700 mg / L; or 700 to 750 mg / L; or 750 to 800 mg / L. The concentration of Ca2+ ions can be measured using the ICUMSA GS7-19 standard.

[051] Advantageously, the sugary broth to which the invention process is applied comprises Mg2+ ions at a concentration of 100 to 800 mg / L, and preferably 100 to 500 mg / L. For example, this concentration of Mg2+ ions may be 100 to 150 mg / L; or 150 to 200 mg / L; or 200 to 250 mg / L; or 250 to 300 mg / L; or 300 to 350 mg / L; or 350 to 400 mg / L; or 400 to 450 mg / L; or 450 to 500 mg / L; or 500 to 550 mg / L; or 550 to 600 mg / L; or 600 to 650 mg / L; or 650 to 700 mg / L; or 700 to 750 mg / L; or 750 to 800 mg / L. The concentration of Mg2+ ions can be measured using the ICUMSA GS7-19 standard.

[052] According to certain embodiments, the sugary broth comprises divalent Ca2+ cations.

[053] According to other forms, the sugary broth comprises divalent Mg2+ cations.

[054] Alternatively and advantageously, the sugary broth comprises divalent cations Ca2+ and Mg2+.

[055] Advantageously, the sugary broth to which the invention process is applied comprises solid particles at a concentration of 10 to 800 mg / kg, and preferably 20 to 500 mg / kg. For example, this concentration of solid particles can be 10 to 50 mg / kg; or 50 to 100 mg / kg; or 100 to 150 mg / kg; or 150 to 200 mg / kg; or 200 to 250 mg / kg; Petition 870260056618, dated 11 / 06 / 2026, page 25 / 57 13 / 32 or 250 to 300 mg / kg; or 300 to 350 mg / kg; or 350 to 400 mg / kg; or 400 to 450 mg / kg; or 450 to 500 mg / kg; or 500 to 550 mg / kg; or 550 to 600 mg / kg; or 600 to 650 mg / kg; or 650 to 700 mg / kg; or 700 to 750 mg / kg; or 750 to 800 mg / kg. The concentration of solid particles can be measured using the NF T90-105 standard and replacing the 0.45 μm filter as recommended in the standard with an 8 μm filter.

[056] The sugar syrup to which the invention process is applied may also have a sugar content of 10 to 30 degrees Brix, and preferably 10 to 20 degrees Brix. Thus, the sugar syrup to which the invention process is applied may have a sugar content of 10 to 12; or 12 to 14; or 14 to 16; or 16 to 18; or 18 to 20; or 20 to 22; or 22 to 24; or 24 to 26; or 26 to 28; or 28 to 30 degrees Brix. The degrees Brix may be measured using the ICUMSA GS7-31 standard.

[057] Furthermore, the sugarcane juice to which the invention process is applied may have a turbidity of 100 to 800 NTU, and preferably 100 to 500 NTU (NTU = Nephelometric Turbidity Unit). Turbidity means the content of light suspended materials in a liquid. It is a quantity that measures the more or less turbid nature of the liquid. The turbidity of the sugarcane juice can be measured using the ICUMSA GS7-21 standard. Thus, the turbidity of the sugarcane juice to which the invention process is applied may be 100 to 150 NTU; or 150 to 200 NTU; or 200 to 250 NTU; or 250 to 300 NTU; or 300 to 350 NTU; or 350 to 400 NTU; or from 400 to 450 NTU; or from 450 to 500 NTU; or from 500 to 550 NTU; or from 550 to 600 NTU; or from 600 to 650 NTU; or from 650 to 700 NTU; or from 700 to 750 NTU; or from 750 to 800 NTU. Sugar processing device

[058] The device according to the invention comprises, firstly, a supply line for a sugary broth which is connected by a Petition 870260056618, dated 11 / 06 / 2026, page 26 / 57 14 / 32 side to a first front filtration unit. On the other hand, this feed line may be connected to (derived from) a clarification unit, or a carbonation unit, or a decantation unit, or a flocculation unit, or a centrifugation unit, or a filtration unit, or a reservoir comprising the sugary juice to be purified. Thus, the feed line allows the transfer (and thus feeding) of the sugary juice to be purified into the first front filtration unit.

[059] Frontal filtration refers to filtration that is carried out essentially perpendicular to the filter surface. Thus, all material retained by the filter accumulates on its surface. In contrast, tangential filtration consists of making the fluid pass tangentially across the filter surface.

[060] The first front filtration unit may comprise one or more screen filters, that is, filters comprising a mesh grid for ordering and retaining solid particles. The mesh grid may be made of wires which are preferably welded together.

[061] According to certain embodiments, the mesh grid may comprise a first series of wires that are parallel to each other.

[062] According to other embodiments, the mesh grid may comprise the first series of wires and a second series of wires that are parallel to each other and perpendicular to the wires of the first series.

[063] According to other modalities, and referring to figure 1, the mesh grid may comprise the first series of wires (A), the second series of wires (B), and a third series of wires (C) that are parallel to each other and have an angle greater than 0° and less than 90° in relation to the wires of the first series (A). This angle may, for example, be from 0 to 10°; or from 10 to 20°; or from 20 to 30°; or from 30 to 40°; or from 40 to 50°; or from 50 to 60°; or from Petition 870260056618, dated 11 / 06 / 2026, p. 27 / 57 15 / 32 to 70°; or 70 to 80°; or 80 to 90°. Preferably, this angle is 30 to 60°, and even more preferably this angle is around 45°.

[064] This preferred and particular mesh makes it possible to prevent fibrous solid particles (bagasse) from getting caught in the mesh grid in a way that is difficult to clean.

[065] Preferably, the first front filtration unit comprises at least 5 screen filters, preferably at least 10 screen filters, preferably at least 15 screen filters, and even more preferably at least 20 screen filters. Thus, the first front filtration unit may, for example, comprise from 1 to 5 filters; or from 5 to 10 filters; or from 10 to 15 filters; or from 15 to 20 filters; or from 20 to 25 filters; or from 25 to 30 filters; or more than 30 filters. Preferably, these filters are arranged in parallel. Even more preferably, these filters are arranged according to a general cylindrical surface in the first filtration unit.

[066] Each filter can have a filtration surface of 1 to 5 m2, and preferably 1.5 to 3 m2. Thus, the total filtration surface of the first front filtration unit can be 1 to 150 m2, and preferably 15 to 50 m2.

[067] Furthermore, each filter (or more particularly the filtration surface of each filter) has pores (openings in the mesh grid) allowing the retention of solid particles on one side and the passage of the sugary juice on the other side (first filtered). When the pores do not have a circular opening, the diameter of the pores is understood to be the maximum distance between two points that lie in a plane parallel to the opening. For example, for pores with a rectangular or square opening, the diameter designates the diagonal of each opening. The same applies to the pores of a grid comprising a perpendicular mesh combined with a diagonal mesh, Petition 870260056618, dated 11 / 06 / 2026, p. 28 / 57 16 / 32 as described above.

[068] The pores of the filters in the first filtration unit have advantageously a larger diameter than the pores of the filters in the second filtration unit.

[069] Thus, the pores of each filter in the first filtration unit may have a diameter of 50 to 80 μm; or 80 to 100 μm; or 100 to 120 μm; or 120 to 140 μm; or 140 to 160 μm; or 160 to 180 μm; or 180 to 200 μm. A pore diameter of about 100 μm is particularly suitable.

[070] According to certain embodiments, the filters included in the first filtration unit all have pores of the same diameter.

[071] According to other embodiments, the filters included in the first filtration unit have pores with a different diameter from each other.

[072] Preferably, the first filtration unit is devoid of membrane filters (membrane filters are generally used to perform tangential filtration).

[073] The first filtration unit may comprise a cleaning unit for at least one of the filters. This cleaning unit thus allows the cleaning of at least one filter while the remaining filters continue in operation. More particularly, the pressure is measured for each of the filters throughout the filtration. When the pressure of a filter reaches a limit (clogged filter), a rotary valve allows the flow of the sugary juice to be directed from the clogged filter to a clean filter. The clogged filter can be cleaned while the filtration continues. The filter cleaning can, for example, be carried out with a cleaning solution that has a direction opposite to the direction of the flow of the sugary juice to be purified. This cleaning solution can be hot water and / or an aqueous solution comprising Petition 870260056618, dated 11 / 06 / 2026, page 29 / 57 17 / 32 sodium hydroxide (3-5% by mass).

[074] According to certain embodiments, the first filtration unit allows the simultaneous use of at least two filters for filtering the sugary juice.

[075] In certain embodiments, the first filtration unit allows the simultaneous cleaning of at least two filters.

[076] According to certain embodiments, the first sugarcane juice filtration unit allows the simultaneous use of at least two filters for filtration and, at the same time, the simultaneous cleaning of at least two filters and then allows switching in order to use the previously cleaned filters for filtering the sugarcane juice and, at the same time, cleaning the filters previously used for filtration.

[077] According to certain models, the flow of sugared juice through the filter can be from 50 to 150 m3 / h, and preferably from 70 to 110 m3 / h.

[078] The invention device also comprises a collection line that allows the collection of the first filtrate obtained at the outlet of the first filtration unit. The first filtrate collection line feeds a second front filtration unit with the first filtrate.

[079] The second front filtration unit may comprise at least one filter (compartment) consisting of filter baskets or screens. According to certain embodiments, the second front filtration unit may comprise at least two filters, and preferably at least four filters.

[080] Each filter basket included in the filter (compartment) may have pores (mesh grid opening) allowing the retention of solid particles on one side and the passage of the sugary juice on the other side (second filtrate).

[081] Thus, the pores of each filter basket of the second unit of Petition 870260056618, dated 11 / 06 / 2026, page 30 / 57 18 / 32 filtration filters can have a diameter of 20 to 30 μm; or 30 to 40 μm; or 40 to 50 μm; or 50 to 60 μm; or 60 to 80 μm; or 80 to 100 μm. A pore diameter of about 50 μm is particularly suitable.

[082] According to certain embodiments, the filter baskets included in the second filtration unit all have pores of the same diameter.

[083] According to other embodiments, the filter baskets included in the second filtration unit have pores with different diameters from each other.

[084] Preferably, the second filtration unit is devoid of membrane filters (membrane filters are commonly used to perform tangential filtration).

[085] The device of the invention also comprises a collection line that allows the collection of the second filtrate obtained at the outlet of the second filtration unit. The second filtrate collection line feeds an ion-exchange chromatography unit with the second filtrate.

[086] The ion-exchange chromatography unit comprises a cation-exchange chromatography resin. Preferably, it consists of a strong cation-exchange resin, in the form of Na+ and / or K+. The resin is in the form of a compact bed in the ion-exchange chromatography unit with a bed height greater than that defined by the name shallow bed. In fact, the bed heights are on the order of 0.5 m in the shallow bed and the distribution of the product through the resin is carried out by means of a very complex distributor called a fractal. The columns of the invention preferably do not include a fluid distributor at the top of the column; at best, the principle of distribution of the sugary broth of the invention is found in a simple weir positioned at the top of the column. By weir is meant a structure comprising a Petition 870260056618, dated 11 / 06 / 2026, page 31 / 57 19 / 32 single inlet and outlet for the fluid (here the second filtrate) to bring the fluid to the chromatographic column. Thus, the columns of the invention preferably do not comprise a fluid distributor comprising a plurality of holes (or outlets) for distributing the fluid in the column.

[087] The resin bed has a height of 0.75 to 3 m, preferably 1 to 3 m and even more preferably 1 to 2 m. For example, the resin bed may have a height of 0.75 to 1 m; or 1 to 1.5 m; or 1.5 to 2 m; or 2 to 2.5 m; or 2.5 to 3 m.

[088] The resin bed may also have a diameter of 0.25 to 6 m, preferably 0.25 to 5 m and even more preferably 0.25 to 4.5 m. For example, the resin bed may have a diameter of 0.25 to 0.5 m; or 0.5 to 1 m; or 1 to 1.5 m; or 1.5 to 2 m; or 2 to 2.5 m; or 2.5 to 3 m; or 3 to 3.5 m; or 3.5 to 4 m; or 4 to 4.5 m; or 4.5 to 5 m; or 5 to 5.5 m; or 5.5 to 6 m. In the case where the resin bed does not have a cylindrical shape with a circular cross-section, the diameter refers to the maximum dimension of the resin bed in a section perpendicular to its main axis (flow axis). For example, for a rectangular or square section, the diameter designates the diagonal. Alternatively, the resin bed may have a truncated cone shape. By truncated cone, we mean a resin bed in the shape of a truncated cone whose upper part has been truncated by a plane. In this case, the diameter refers to the diameter of the larger base of the resin bed.

[089] The ion-exchange chromatography unit may comprise at least one column, preferably at least 5 columns, preferably at least 10 columns, and even more preferably at least 15 columns. Thus, in the case where several columns are used, each column comprises a resin bed. Petition 870260056618, dated 11 / 06 / 2026, page 32 / 57 20 / 32

[090] The resin bed volume per column can be from 15 to 40 m3, and preferably from 20 to 35 m3.

[091] The total resin bed volume (i.e., the resin bed volume included in all columns of the ion-exchange chromatography unit) can be from 15 to 500 m3, and preferably from 15 to 450 m3.

[092] Each column can have a height of 2 to 10 m, preferably 3 to 4 m. The height of the column here refers to the height of the inner rim of the column.

[093] Furthermore, each column may have a diameter of 0.25 to 6 m, preferably 0.25 to 5 m and even more preferably 0.25 to 4.5 m.

[094] By column diameter, the external diameter of the column is meant here. In the case of a column that is not cylindrical in circular section, the diameter refers to the maximum dimension of the column in a section perpendicular to its main axis. For example, for a rectangular or square section, the diameter designates the diagonal. In the case of a truncated cone column, the diameter is understood to be the diameter of the large base of the column.

[095] According to certain embodiments, the column height (ferrule height) may be greater than the resin bed height by at least 2 m, and preferably at least 1.5 m. This feature is important for implementing a resin backwashing step that will allow the resin to expand in the ion-exchange chromatography column(s), as described below.

[096] Thus, as mentioned above, the ion exchange chromatography unit may comprise a single-column ion exchange chromatography system, or a multi-column ion exchange chromatography system.

[097] When the ion-exchange chromatography unit comprises Petition 870260056618, dated 11 / 06 / 2026, page 33 / 57 21 / 32 multiple columns, these columns can be arranged in series with each other.

[098] Alternatively and advantageously, when the ion-exchange chromatography unit comprises several columns, they can be arranged in parallel with each other. In this case, at least two columns can be used simultaneously for the production of attenuated sugar broth. According to certain embodiments, a portion of these columns can be used for the production of attenuated sugar broth, while another portion of these columns can simultaneously undergo washing and / or regeneration steps.

[099] The invention device further comprises a collection line for attenuated sugar broth at the outlet of the ion-exchange chromatography unit. The attenuated sugar broth collection line can, for example, transfer the attenuated sugar broth to an evaporation unit or a reservoir that allows the attenuated sugar broth to be stored or recovered. Sugar treatment process

[0100] As mentioned above, the invention also relates to a sugar treatment process. Preferably, this process is implemented in the device described above. This process is described with reference to Figure 2.

[0101] The invention process comprises successively: - a first stage of frontal filtration 1a (or first frontal filtration 1a) of the sugary juice to obtain a first filtrate; - a second frontal filtration stage 1b (or second frontal filtration 1b) of the first filtrate to obtain a second filtrate; and - a step involving contacting the second filtrate with a cation exchange chromatography resin 2 in order to load the resin with divalent cations and collect an attenuated sugary broth. Petition 870260056618, dated 11 / 06 / 2026, page 34 / 57 22 / 32

[0102] As described above, sugary juice can be derived from grinding (or diffusion) 3 of sugar cane.

[0103] Upstream of the steps mentioned above, the process may also comprise one or more steps, such as sulfitation 4, carbonation 5, clarification 6, flocculation 7 and / or decantation 8.

[0104] Downstream of the steps mentioned above, the process may comprise one or more steps such as evaporation 9 and / or crystallization 10.

[0105] Thus, the sugary juice is subjected to a first frontal filtration 1a, in order to obtain a first filtrate. The solid particles, notably the fibrous solid particles, are retained in the filter. Thus, these particles are separated from the sugary juice and are retained in the filter or filters used for the first filtration 1a.

[0106] The first frontal filtration 1a can be carried out at a temperature of 75 to 98°C.

[0107] According to certain methods, this first frontal filtration 1a allows the retention of 10 to 60% by mass of the solid particles initially found in the sugary juice.

[0108] The first filtrate comprises, in turn, the sugary broth comprising solid particles that passed through the filter(s) used for the first filtration 1a, as well as Ca2+ and / or Mg2+ ions.

[0109] The first filtrate is then subjected to a second filtration 1b, in order to provide a second filtrate. The solid particles, notably the fibrous solid particles, are retained in the filter. Thus, these particles are separated from the sugary juice and are retained in the filter or filters used for the second filtration 1b.

[0110] The second frontal filtration 1b can be carried out at a Petition 870260056618, dated 11 / 06 / 2026, page 35 / 57 23 / 32 temperature of 75 to 98°C.

[0111] According to certain methods, the combination of the first and second frontal filtrations 1a, 1b allows the retention of 30 to 70% by mass of the particles initially found in the sugary juice.

[0112] The second filtrate comprises the sugary broth comprising solid particles that passed through the filter used for the second filtration 1b, as well as Ca2+ and / or Mg2+ ions.

[0113] According to certain embodiments, the solid particles included in the second filtrate include fine bagasse particles.

[0114] Subsequently, the second filtrate is placed in contact with the cation exchange resin 2 as described above. Placing the second filtrate in contact with resin 2 allows the adsorption of the divalent cations Ca2+ and / or Mg2+ onto said resin. Thus, the divalent cations Ca2+ and / or Mg2+ present in the second filtrate are exchanged and replaced by the monovalent ions Na+ and / or K+ initially present in the resin. Preferably, the flow rate of the sugar broth in the ion exchange chromatography unit is 5 to 20 BV / h, and preferably 5 to 15 BV / h (BV corresponds to the volume equivalents of the resin bed of a column).

[0115] According to certain embodiments, this step can be carried out by circulating the second filtrate in the ion-exchange chromatography unit in a bottom-to-top direction in the ion-exchange chromatography column(s).

[0116] According to preferred embodiments, this step can be performed by circulating the second filtrate in the ion-exchange chromatography unit in a top-to-bottom direction in the ion-exchange chromatography column(s).

[0117] This step can be carried out at a temperature of 75 to 98°C. Petition 870260056618, dated 11 / 06 / 2026, page 36 / 57 24 / 32

[0118] At the end of the step of bringing the resin into contact with the second filtrate 2, an attenuated sugary broth is obtained while the resin is henceforth loaded with divalent cations.

[0119] The attenuated sugary broth obtained at the end of the step of contacting the resin with the second filtrate 2 can have a volume of 15 to 80 BV, and preferably 20 to 50 BV.

[0120] According to certain embodiments, the combination of the first frontal filtration 1a, the second frontal filtration 1b and the contact of the second filtrate with the resin 2 allows the retention of 50 to 90% by mass of the particles initially found in the sugary juice.

[0121] Advantageously, attenuated sugar broth can have a Ca2+ ion concentration of 5 to 150 mg / L, and preferably 20 to 120 mg / L. Thus, this concentration can be 5 to 10 mg / L; or 10 to 15 mg / L; or 15 to 20 mg / L; or 20 to 25 mg / L; or 25 to 30 mg / L; or 30 to 35 mg / L; or 35 to 40 mg / L; or 40 to 45 mg / L; or 45 to 50 mg / L; or 50 to 55 mg / L; or 60 to 60 mg / L; or 60 to 65 mg / L; or 65 to 70 mg / L; or 70 to 75 mg / L; or 75 to 80 mg / L; or 80 to 85 mg / L; or 85 to 90 mg / L; or 90 to 95 mg / L; or 95 to 100 mg / L; or 100 to 105 mg / L; or 105 to 110 mg / L; or from 110 to 115 mg / L; or 115 to 120 mg / L; or 120 to 125 mg / L; or 125 to 130 mg / L; or 130 to 135 mg / L; or 135 to 140 mg / L; or 140 to 145 mg / L; or 145 to 150 mg / L.

[0122] Advantageously, the attenuated sugar broth can have a Mg2+ ion concentration of 5 to 150 mg / L, and preferably 20 to 120 mg / L. Thus, this concentration can be 5 to 10 mg / L; or 10 to 15 mg / L; or 15 to 20 mg / L; or 20 to 25 mg / L; or 25 to 30 mg / L; or 30 to 35 mg / L; or 35 to 40 mg / L; or 40 to 45 mg / L; or 45 to 50 mg / L; or 50 to 55 mg / L; or 55 to 60 mg / L; or 60 to 65 mg / L; or 65 to 70 mg / L; or 70 Petition 870260056618, dated 11 / 06 / 2026, page 37 / 57 25 / 32 at 75 mg / L; or 75 to 80 mg / L; or 80 to 85 mg / L; or 85 to 90 mg / L; or 90 to 95 mg / L; or 95 to 100 mg / L; or 100 to 105 mg / L; or 105 to 110 mg / L; or 110 to 115 mg / L; or 115 to 120 mg / L; or 120 to 125 mg / L; or 125 to 130 mg / L; or 130 to 135 mg / L; or 135 to 140 mg / L; or 140 to 145 mg / L; or 145 to 150 mg / L.

[0123] Advantageously, the attenuated sugar broth can have a solid particle concentration of 1 to 100 mg / kg, and preferably 1 to 50 mg / kg. Thus, this concentration can be 1 to 5 mg / kg; or 5 to 10 mg / kg; or 10 to 15 mg / kg; or 15 to 20 mg / kg; or 20 to 25 mg / kg; or 30 mg / kg; or 30 to 35 mg / kg; or 35 to 40 mg / kg; or 40 to 45 mg / kg; or 45 to 50 mg / kg; or 50 to 55 mg / kg; or 55 to 60 mg / kg; or 60 to 65 mg / kg; or 65 to 70 mg / kg; or 70 to 75 mg / kg; or 75 to 80 mg / kg; or 85 mg / kg; or 85 to 90 mg / kg; or 90 to 95 mg / kg; or 95 to 100 mg / kg.

[0124] The sugared broth can then be evaporated 9 to reduce the amount of water contained in the attenuated sugared broth. Thus, the evaporation step 9 makes it possible to obtain an attenuated sugared broth called syrup.

[0125] Next, the syrup can undergo one or more crystallizations 10 to provide crystallized sugar. Thus, at least one crystallization 10 can be carried out during which the syrup is evaporated so that it is saturated with sugars and so that crystals begin to form. At the end of the first crystallization 10, the crystals can be recovered and what remains of the syrup can undergo further sequential crystallizations 10, so as to provide different degrees of sugar crystals. At the end of the sequential crystallizations 10, what remains of the syrup is called molasses and can be used by the agri-food industry, perfumery and galenic pharmacy, in the production of biofuels or even for resin regeneration, as described Petition 870260056618, dated 11 / 06 / 2026, page 38 / 57 26 / 32 below (arrow 12).

[0126] The loaded resin comprises, in this state, a quantity of sugary broth remaining in the ion-exchange chromatography unit (e.g., in the ion-exchange chromatography column(s)). Furthermore, the ion-exchange chromatography unit may comprise solid particles (e.g., particles with a diameter less than 50 μm), notably fine bagasse particles, accumulated on top of the resin bed.

[0127] The process according to the invention can also provide steps for regenerating the loaded resin.

[0128] However, before proceeding with resin regeneration, at least one washing step may be carried out in order to remove any remaining solid particles in the ion exchange chromatography unit.

[0129] Advantageously, this washing can be carried out by injecting the washing solution from bottom to top into the ion-exchange chromatography column(s) (thus during the washing step, the washing solution in the ion-exchange chromatography unit has a direction opposite to that of the second filtrate during the production of the sugar juice). The washing solution can have a flow rate of 10 to 20 BV / h.

[0130] Thus, during this step, due to the direction of the washing solution (preferably from bottom to top) and the flow rate of the washing solution, the resin bed may undergo expansion in the ion-exchange chromatography unit. For example, during this step, the expansion of the resin bed may be at least 50% relative to the initial bed height. The resin may, for example, assume the form of a fluidized bed. As explained above, since the remaining solid particles in the unit have a lower density than the density of the resin, they can be expelled without causing the resin particles to be ejected. Petition 870260056618, dated 11 / 06 / 2026, page 39 / 57 27 / 32

[0131] The washing solution can be an aqueous solution.

[0132] In certain forms, the washing solution is water.

[0133] According to other preferred embodiments, the washing solution is derived from the attenuated sugary broth as described above.

[0134] According to other preferred embodiments, the washing solution is derived from the sugary juice as described above.

[0135] Different washing solutions can be used sequentially.

[0136] The washing stage can be carried out notably at a temperature of 75 to 98°C.

[0137] Alternatively, this washing step can be performed after the regeneration step described below or after a final rinsing step.

[0138] At the end of the washing stage, a washing effluent can be recovered. This effluent is a sugary aqueous solution and can, for example, be returned to the clarification stage 6 (arrow 11).

[0139] As mentioned above, the sugar treatment process according to the invention also provides for steps involving the regeneration of the resin loaded with divalent cations. The regeneration comprises, firstly, bringing the loaded resin into contact with a regeneration solution. At the end of the regeneration, the ion exchange resin is regenerated and a stream of aqueous solution is obtained, collected at the end of the regeneration, called the regeneration effluent.

[0140] According to certain embodiments, the regeneration solution may be derived, in whole or in part, from the molasses formed after a crystallization step 10 or after several sequential crystallization steps 10 as described above (arrow 12). More particularly, the molasses formed during the crystallization 10 of the sugar (since it comes from the sugar syrup) Petition 870260056618, dated 11 / 06 / 2026, pp. 40 / 57 28 / 32 attenuated) comprise monovalent Na+ and / or K+ ions, in higher concentrations than in attenuated sugar juice. Thus, during its passage through the ion-exchange chromatography unit and its contact with the loaded resin, the monovalent Na+ and / or K+ ions are exchanged with the divalent Ca2+ and / or Mg2+ ions of the loaded resin. The resin is thus regenerated, while the regeneration effluent comprises molasses loaded with divalent Ca2+ and / or Mg2+ ions that can be used and integrated into the crystallization steps of a sugar production process (arrow 13). Alternatively, these molasses loaded with Ca2+ and / or Mg2+ can be used for ethanol production. These methods allow resin regeneration without the use of chemicals such as sodium chloride.

[0141] According to other embodiments, the regeneration solution may be derived, in whole or in part, from the attenuated sugar broth produced (arrow 14). Thus, sodium hydroxide (NaOH) or potassium hydroxide (KOH) may be added to at least part of the attenuated sugar broth to form the regeneration solution. This solution may then pass through the ion-exchange chromatography unit and then through the loaded resin in order to exchange the monovalent Na+ and / or K+ ions of the regeneration solution with the divalent Ca2+ and / or Mg2+ ions of the loaded resin. In this case, the regeneration effluent may comprise a water-soluble compound called calcium saccharate formed due to the complexation of Ca2+ ions with sucrose. This regeneration effluent can be used later in clarification stage 6 (arrow 15), in particular in the liming stage, which allows for the use of fewer chemicals such as lime for the clarification of the sugary juice.Thus, instead of using just a milk of lime solution, a mixture of milk of lime and sugar of... Petition 870260056618, dated 11 / 06 / 2026, pp. 41 / 57 29 / 32 calcium can be mixed with the sugary broth to precipitate impurities and then separate them in a decanter. The calcium ratio presented respectively by the milk of lime and the calcium saccharate thus formed in the mixture is 100:0 to 50:50. Preferably, this ratio is 100:0 to 80:20.

[0142] According to other embodiments, the regeneration solution may be an aqueous solution of sodium chloride, here referred to as regeneration brine.

[0143] According to other embodiments, the regeneration solution may be an aqueous solution comprising sodium hydroxide or potassium hydroxide.

[0144] According to other embodiments, the regeneration solution may be derived from a distillation vinasse resulting from the molasses mentioned above. In fact, the monovalent Na+ and / or K+ ions present in molasses are also present in the distillation vinasse and in similar quantities. This vinasse must first be clarified, for example, using a rapid separation centrifuge.

[0145] According to other embodiments, the regeneration solution may be derived from a raffinate resulting from a chromatographic treatment of molasses, and more particularly from a raffinate obtained after a molasses sugar removal step mentioned above by chromatography. In fact, the monovalent Na+ and / or K+ ions present in molasses are also present in the raffinate and in similar quantities.

[0146] According to certain embodiments, resin regeneration is carried out using the same regeneration solution throughout the regeneration period.

[0147] According to other methods, resin regeneration is carried out using more than one regeneration solution during the Petition 870260056618, dated 11 / 06 / 2026, pp. 42 / 57 30 / 32 regeneration, that is, the regeneration solution is modified during the regeneration process. For example, in the same regeneration process, a regeneration solution comprising molasses may alternate with a regeneration solution comprising attenuated sugar broth and NaOH or with a regeneration solution comprising regeneration brine.

[0148] Advantageously, resin regeneration can be carried out by injecting the regeneration solution from bottom to top into the ion-exchange chromatography column(s) (thus, during the regeneration step, the regeneration solution in the ion-exchange unit has a direction opposite to that of the second filtrate during the production of the attenuated sugar broth). The regeneration solution can have a flow rate of 1 to 10 BV / h, and preferably 2 to 5 BV / h.

[0149] Alternatively, resin regeneration can be carried out by injecting the regeneration solution from top to bottom into the ion-exchange chromatography column(s) (thus, during the regeneration step, the regeneration solution in the ion-exchange chromatography unit has the same direction as the second filtrate during the production of the attenuated sugar broth). The regeneration solution can have a flow rate of 1 to 10 BV / h, and preferably 2 to 5 BV / h.

[0150] According to certain embodiments, when the process of the invention is implemented in the device described above, and more particularly when the step of bringing the second filtrate into contact with resin 2 is implemented in several ion-exchange chromatography columns, a portion of these columns can be used for the production of attenuated sugar broth while another portion of these columns can be used for the regeneration of the loaded resin. In other words, a first portion of the columns is initially used for the production of attenuated sugar broth. Petition 870260056618, dated 11 / 06 / 2026, pp. 43 / 57 31 / 32 After a certain period of time, a second section of the columns resumes the production of attenuated sugar syrup, while the first section of the columns is henceforth used for the regeneration of the loaded resin.

[0151] For example, if the ion exchange chromatography unit comprises 15 to 20 ion exchange chromatography columns, 5 to 10 columns can be used for the production of attenuated sugar broth, while 10 to 15 columns can be used for resin regeneration.

[0152] The process according to the invention may also comprise a final rinsing step after regeneration of the loaded resin, using a rinsing solution. Preferably, the rinsing solution is attenuated sugar broth. According to other embodiments, the rinsing solution is water. Thus, rinsing can be carried out by injecting the rinsing solution from top to bottom of the ion-exchange chromatography column(s) (thus, during the rinsing step, the rinsing solution injected into the ion-exchange chromatography unit has the same direction as that of the second filtrate during the production of attenuated sugar broth).

[0153] The process according to the invention can be a continuous process.

[0154] Alternatively, the process according to the invention may be a discontinuous (batch) process.

[0155] A multi-column system, as described in document WO 2007 / 144522, may also be mentioned.

[0156] The process according to the invention allows obtaining attenuated sugarcane juice with a degree of attenuation greater than 80%. By degree of attenuation is meant the ratio between the hardness of the attenuated sugarcane juice (at the outlet of the ion exchange unit) and the hardness of the sugarcane juice at the inlet of the ion exchange chromatography unit, the hardness corresponding to Petition 870260056618, dated 11 / 06 / 2026, pp. 44 / 57 32 / 32 total concentration of Ca2+ and Mg2+ cations.

[0157] The concentration values ​​and concentration ratios described in this application correspond to average values ​​over a production period. Petition 870260056618, dated 11 / 06 / 2026, pp. 45 / 57

Claims

1 / 5 CLAIMS 1. Sugar treatment process, characterized in that it successively comprises: - a first frontal filtration (1a) of a sugary juice to obtain a first filtrate; - a second frontal filtration (1b) of the first filtrate to obtain a second filtrate; and - contacting the second filtrate with a cation exchange chromatography resin (2) so as to charge the resin with divalent cations and collect an attenuated sugary juice, the resin being arranged in the form of a bed of height h from 0.75 to 3 meters.

2. Process according to claim 1, characterized in that the divalent cations comprise, and preferably consist essentially of, Ca2+ cations and / or Mg2+ cations.

3. Process according to claim 1 or 2, characterized in that the sugary broth has a concentration of solid particles of 20 to 500 mg / kg, and / or a concentration of magnesium ions of 100 to 500 mg / L, and / or a concentration of calcium ions of 100 to 600 mg / L.

4. Process according to any one of claims 1 to 3, characterized in that the sugary broth has a sugar content of 10 to 20 degrees Brix, and / or a turbidity of 100 to 500 NTU.

5. Process according to any one of claims 1 to 4, characterized in that the attenuated sugary broth collected after the step of contacting the second filtrate with the resin (2) has a volume of 15 to 80 BV.

6. Process according to any one of claims 1 to 5, characterized in that the first filtration (1a) allows a retention of 10 to 60% by mass of solid particles in relation to the amount of solid particles present in the sugared juice; and / or the first filtration (1a) and the second filtration (1b) allow a retention of 30 to 70% by mass of solid particles in relation to the amount of solid particles present in the sugared juice; and / or the first filtration (1a), the second filtration (1b) and the contact of the second filtrate with the resin (2) allow a retention of 50 to 90% by mass of solid particles in relation to the amount of solid particles present in the sugared juice.

7. A process according to any one of claims 1 to 6, characterized in that it is either a batch process or a continuous process.

8. A process according to any one of claims 1 to 7, characterized in that it comprises the steps of regenerating resin loaded with divalent cations, these steps comprising: contacting the loaded resin with a regeneration solution; collecting a regeneration effluent.

9. Process according to claim 8, characterized in that the regeneration solution is derived from the molasses formed during a crystallization step (10) of the sugar, or the regeneration solution is derived wholly or in part from the attenuated sugar juice, with or without the addition of sodium hydroxide or potassium hydroxide, or the regeneration solution is a regeneration brine solution comprising a chloride, potassium or sodium salt, or the regeneration solution is derived from a distillation vinasse of the molasses; or the regeneration solution is derived from a raffinate resulting from a treatment of the molasses by chromatography.

10. Process according to claim 8 or 9, characterized in that the contact of the resin loaded with a regeneration solution comprises the use of different regeneration solutions alternating between two production cycles.

11. Process according to any one of claims 8 to 10, characterized in that the regeneration effluent is used to carry out a clarification step (6) of the sugared juice, in particular a liming step, the clarification step (6) being carried out before the first filtration (1a); or in which the regeneration effluent is used to carry out one or more crystallization steps (10), the crystallization step(s) (10) being carried out after the second filtrate is placed in contact with the resin (2).

12. Process according to any one of claims 1 to 11, characterized in that it also comprises a washing step of the resin loaded with divalent cations, or of the regenerated resin, with a washing solution, the washing solution having a direction in the resin bed opposite to a direction of the second filtrate in the resin bed during the step of contacting the second filtrate with the resin (2).

13. Process according to claim 12, characterized in that the washing solution is derived from attenuated sugarcane juice or sugarcane juice, or the washing solution is water.

14. Process according to claim 12 or 13, characterized in that at the end of the washing stage a washing effluent is collected, the washing effluent being returned to a clarification stage (6) of the sugary juice, the clarification stage (6) being carried out before the first filtration (1a).

15. Process according to any one of claims 1 to 14, characterized in that the step of contacting the second filtrate with the resin (2) is carried out at a temperature equal to or greater than 75°C.

16. Sugar treatment device, characterized in that Petition 870260056618, dated 11 / 06 / 2026, page 48 / 57 4 / 5 comprises: - a sugarcane juice feed line; - a first front filtration unit fed by the sugarcane juice feed line; - a first filtrate collection line at the outlet of the first front filtration unit; - a second front filtration unit fed by the first filtrate collection line; - a second filtrate collection line at the outlet of the second front filtration unit; - an ion exchange chromatography unit comprising a cationic resin (2) fed by the second filtrate collection line, the resin having the form of a bed with a height h of 0.75 to 3 meters; and - an attenuated sugarcane juice collection line at the outlet of the ion exchange chromatography unit.

17. Device according to claim 16, characterized in that the first filtration unit comprises one or more screen filters, each filter having pores with a diameter of 50 to 200 μm, and preferably 80 to 120 μm.

18. Device according to claim 17, characterized in that the first filtration unit comprises a cleaning unit for at least one of the screen filters.

19. Device according to any one of claims 16 to 18, characterized in that the second filtration unit comprises at least one filter basket with pores having a diameter of 20 to 100 µm, and preferably 40 to 60 µm.

20. Device according to any one of claims 16 to 19, Petition 870260056618, dated 11 / 06 / 2026, page 49 / 57 5 / 5 characterized in that the ion-exchange chromatography unit comprises at least one column, preferably at least 5 columns, preferably even at least 10 columns, and even more preferably at least 15 columns.

21. Device according to any one of claims 16 to 20, characterized in that the resin bed has a diameter of 0.25 to 6 m, and preferably 0.25 to 5 m. Petition 870260056618, dated 11 / 06 / 2026, pp. 50 / 57

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