High purity betaine products, polyphenol products, and methods of making the same

Abstract

Provided herein are high purity betaine products and methods of making the same. In some cases, provided herein are methods of recovering betaine from sugar beet molasses by using ion exchange chromatographic method with a salt of a polystyrene sulfonate cation exchange resin cross-coupled with divinyl benzene moiety. Also provided herein are methods of producing free-flowing betaine using specialized drying techniques. Additionally provided herein are betaine-poor products and polyphenol rich products, along with methods of preparing the same.

Description

HIGH PURITY BETAINE PRODUCTS, POLYPHENOL PRODUCTS, AND METHODS OF MAKING THE SAMECROSS REFERENCE TO RELATED APPLICATIONS

[0001] This application claims the benefit of and priority to U.S. Provisional Application No. 63 / 615,934, filed on December 29, 2023, and U.S. Provisional Application No. 63 / 671,350, filed on July 15, 2024, which are hereby incorporated by reference in their entireties.FIELD

[0002] Described herein are high purity betaine products and methods of making the same. In some cases, described herein are methods of recovering betaine from sugar beet molasses by using ion exchange chromatographic method with a salt of a polystyrene sulfonate cation exchange resin cross-coupled with divinyl benzene moiety. Also described herein are methods of producing free-flowing betaine using specialized drying techniques. Additionally described herein are methods of producing and recovering a betaine-poor extract including, for example, amino acids, salts, and polyphenols. Further described herein is a method of producing a polyphenol rich powder extract from the betaine-poor extract.BACKGROUND

[0003] The sugar beet root on harvest contains 15-20% sugars and 2.6% non-sugars, along with 75-76% water and 4-6% leftover pulp. When one ton of freshly harvested sugar beet is processed, 121 kg sugar, 38 kg molasses and 50 kg pulp are yielded. The molasses generally contains 18.2 kg sugar, with impurities accounting for approximately 12.1 kg and water accounting for 7.8 kg. Out of the sugar present in fresh sugar beet roots, nearly 83% is recovered as white sugar, 12.5% is lost in molasses, and 4.4% is lost in some other way. Beet roots also contain 0.3% betaine, an important osmoregulatory agent. Betaine has the following structure:

[0004] Betaine is one of the nitrogenous compounds in beet molasses, and contributes 5% of the dry substances, and has a density of 1250 kg / m3. It is a product that has multiple uses, including use in the pharmaceuticals, cosmetics, and fermentation industries. Recovering betaine from natural materials such as beet molasses and vinasse has been done using chromatographic separation methods for decades. The most commonly used resin type in this application is strong acid cation exchangers, especially sulfonated polystyrene crosscoupled divinyl benzene moiety. This moiety is 3.5 to 8% of the total weight of thecomponent. Water, including warm water at a temperature ranging from 80 °C to 95 °C, has been used as the eluent.

[0005] Recovering betaine from molasses is disclosed in EP 2802665 Bl, which relates to converting the molasses with a fructan-forming enzyme and separating this fructan- molasses to obtain a betaine-rich fraction. With this process, fructo-oligosaccharide has also been separated using a mono- or divalent divinyl benzene cross-coupled strong acid cation exchange resin.

[0006] U.S. Pat. No. 5,384,05 describes a method for processing industrial discharges with respect to using molasses to recover betaine with using ion exclusion chromatography. Vinasse or residual molasses serve as starting materials, in which its components are separated by using ion exclusion chromatography. The chromatography method includes at least a first separation pass through a separating column wherein during the first pass, elution of the substance to be separated takes place with a dilute or back-diluted solution of starting material.

[0007] A separation method for fractionating sulphite cooking liquor to separate xylose from the lignosulfonate contents of sulphite cooking liquor has been described in U.S. Pat. No. 5,637,225. The described method uses a strongly acidic gel type cation exchange resin.

[0008] U.S. Pat. No. 6,093,326 describes a method for the fractionation of molasses by using a simulated moving bed system. In this system, the liquid flows in a single direction in a system containing at least two chromatographic partial packing beds. The sequence includes a feeding phase, an eluting phase, and a recycling phase. During the recycling phase, the liquid in the partial packing material beds with their dry solids profile is recycled in a loop comprising one, two or several partial packing material beds. To obtain pure betaine, a crystallization process, as used in the sugar industry, is applied.

[0009] U.S. Pat. No. 2002 / 0169311 Al relates to a method including a multistep process for recovering betaine, erythritol, inositol, sucrose, mannitol, glycerol and amino acids from beet molasses. In this multistep process, two columns are used with connected to each other. One of the columns is filled with weakly acidic cation exchange acrylic based resin, and the other column is filled with a strongly acidic cation exchange resin.

[0010] U.S. Pat. No. 5,127,957 describes a method wherein betaine is separated from beet molasses using a chromatographic simulated moving bed system having at least three chromatographic columns connected in series. Strong acid cation exchange resins are used where the resin contains sulphonic acid groups. In this method, resin is regenerated into sodium form.

[0011] U.S. Pat. No. 2003 / 0094416 Al relates to a method of recovering betaine in asimulated moving bed chromatographic system as fractionating molasses. Fractions containing solids in different concentrations were separated and betaine was crystallized in a known method from the sugar industry with the same equipment. The crystallization procedure is lengthy, taking approximately 12 hours to achieve pure crystal betaine.

[0012] U.S. Pat. No. 2003 / 0131784 Al describes a process for the crystallization of betaine utilizing the supersaturation zone. Evaporation crystallization of betaine is performed at 98.8 °C with seeding in pure betaine to the crystallization system, and centrifugation is performed as commonly done in the sugar industry.

[0013] Polyphenols, beyond their antioxidant activity, have demonstrated various other functions. They regulate carbohydrate metabolism, inhibit enzymes, and contribute to preventing diseases, such as cardiovascular and neurodegenerative diseases. Spectrophotometric analysis with Folin-Ciocalteu’s phenol reagent is commonly used to quantify polyphenols, providing a quick evaluation of their composition. However, this method's drawback lies in its susceptibility to responding to other reducing compounds present in the sample, potentially leading to an overestimation of measured values.

[0014] While sugarcane molasses presents a rich polyphenol source, its intricate composition poses challenges in characterization due to the multiple processing stages during sugar cane milling, resulting in significant variability. Nevertheless, elucidating its chemical composition is crucial to effectively delve into the reported biological activities linked with sugarcane molasses.

[0015] The total phenolic content (TPC) of the sugar beet peel (Beta vulgaris altissima) has been reported as 4.2 mg / g in some publications. Such publications also indicated that the sugar beet peel had a remarkable antioxidant activity (88% inhibition) compared to the other vegetable sources. Also, the high antifungal activity of sugar beet extract is attributed to the presence of a high amount of ferulic acid and hydroxycinnamic acid-type phenolics. Therefore, due to lack of adequate knowledge about biological activity and phenolic compositions of different parts of sugar beet, a study has been carried out to separate and identify the phenolic compounds of sugar beet flesh and peel (Arjeh et al., Food Science and Nutrition, 2022, 10:4238-4246).

[0016] CA Pat. No. 2,860,448 (also published as W02012 / 106761 Al) describes a method for extracting molasses for obtaining polyphenol rich extracts. After the white sugar processing steps, many kinds of byproducts are discharged. These directly come from sugar beet process byproducts containing amino acids, salts, polyphenols and others. CA Pat. No. 2,860,448 is directed to the extraction of polyphenol rich material from this byproduct byusing adsorbent resin column and freeze dryer equipment.

[0017] W02014 / 032100A1 describes a solvent extraction method, applied to directly sugar cane, to produce different extract compositions.

[0018] A method for recovering of polyphenolic isoflavones from soy molasses, using a separation method, has been described in U.S. Pat. No. 6,680,381. The separation method is based on solvency and centrifugal separation.

[0019] Deseo et al, has determined the polyphenol composition of sugarcane molasses (Food Chemistry, 2020, 314: 126180). The publication states that sugarcane molasses extract contains chlorogenic acid, caffeic acid, syringic acid, vanillin, homoorientin, orientin, sinapic acid, vitexin, swertisin, diosmin, apigenin, tricin and diosmetin.

[0020] As described above, all betaine separation methods for betaine were based on the ion exchange resin column systems. In addition, many of the separation methods are based on the separation of molasses containing 3-8% betaine, as currently used in the sugar industry, followed by crystallization using known equipment and processes. The current methods for obtaining crystallized betaine are costly and lengthy, resulting in a low production capacity of the betaine.SUMMARY

[0021] It is desirable to provide an improved efficient and economical drying process to recover betaine from molasses. The present disclosure relates to a method for recovering betaine from sugar beet molasses by ion exchange chromatography in a single step. In this method, an efficient evaporation and drying process is performed by utilizing falling film plate evaporator (FFPE) and conical ribbon vacuum dryer (CRVD). By using the combination of FFPE and CRVD, the betaine fraction concentration and drying processes are more efficient. Through utilizing the method described herein, a free-flow betaine product is obtained in which process times are shortened and energy consumption is reduced.

[0022] Additionally, a polyphenol rich powder product is produced using steps of the method as described herein. The polyphenol rich powder product is prepared using a different downstream absorption resin column, as further described herein. Solid materialconcentration and powder form production of the polyphenol rich powder product is achieved with FFPE and / or CRVD.

[0023] Described herein is a purified betaine product, comprising a dry, free flowing particulate mixture comprising at least 70 wt. % of betaine, less than 10 wt. % water, and optionally one or more additional components. Optionally, the one or more additional components comprises an anti-caking agent. The anti-caking agent can be, for example, a stearate salt (e.g., calcium stearate or magnesium stearate) or a silicon-containing compound (e.g., fume silicate or silicon dioxide). In some cases, the one or more additional components comprises sucrose. The sucrose can be present in an amount of less than 0.5 wt. % based on the weight of the dry, free flowing particulate mixture.

[0024] In some cases, the dry, free flowing particulate mixture comprises at least 75 wt. % of betaine (e.g., at least 80 wt. % betaine, at least 85 wt. % betaine, at least 90 wt. % betaine, at least 95 wt. % betaine, at least 97 wt. % betaine or at least 99 wt. % betaine). The betaine in the dry, free flowing particulate mixture can have an average particle size of 100 nm to 1.5 pm.

[0025] Also described herein is a method for obtaining dry powder betaine, comprising purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-containing fraction; concentrating the betaine-containing fraction by performing falling film plate evaporation to form a concentrated betaine fraction; and drying the concentrated betaine fraction by conical ribbon vacuum drying to obtain a dry powder betaine. Other separated fractions comprise a polyphenol-containing fraction, which can be obtained by absorb the polyphenol-containing fraction by performing absorption resin column and washing the absorption column with diluted alcohol in order to obtain the polyphenol rich fraction. Optionally, the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine, 1 - 6 wt. % sucrose, and / or 10 - 30 % colored impurities, polyphenols, salts, and / or amino acids.

[0026] In some cases, the purifying step is accomplished by a single step ion exchange chromatography. The resin used in the ion exchange chromatography can be a strong acidic cation exchange resin. Optionally, the strong acidic cation exchange resin is crosslinked with a crosslinking agent such as, for example, divinyl benzene. In some cases, the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0027] The method can further include a decolorizing step after the purifying step and before the concentrating step. The decolorizing step can comprise performing ion exchange chromatography on the betaine-containing fraction. A strong basic anion exchange resin can be used in the ion exchange chromatography in the decolorizing step.

[0028] The concentrating step in the method can be performed under vacuum and / or with heating. Optionally, the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

[0029] The falling film plate evaporation in the concentrating step can optionally be performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg. The drying step can be performed under vacuum and / or with heating. Optionally, the drying step is performed to achieve a percent humidity of less than 1%. The conical ribbon vacuum drying can be performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45 mmHg.

[0030] Also described herein is a purified betaine liquid product, comprising a liquid solution comprising at least 45 wt. % and not more than 60 wt. % of betaine (to avoid betaine crystallization and oversaturation), less than 50 wt. % water, and optionally one or more additional components. Optionally, the one or more additional components comprises a deicing agent. The de-icing agent can be, for example, a glycol (e.g., propylene glycol or glycerol). In some cases, the one or more additional components comprises sucrose. The sucrose can be present in an amount of less than 0.5 wt. % based on the weight of the liquid solution.

[0031] In some cases, the liquid solution comprises at least 50 wt. % of betaine (e.g., at least 55 wt. % betaine, at least 57 wt. % betaine, or at least 60 wt. % betaine). Optionally, the betaine in the liquid solution can have a light brown to amber color.

[0032] Also described herein is a method for obtaining a betaine liquid product, comprising purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-containing fraction; and concentrating the betaine-containing fraction by performing falling film plate evaporation to form a concentrated betaine fraction until desired solid percentage obtained.

[0033] In some cases, other separated fraction(s) comprises a polyphenol-containing fraction. The method can further include a step of absorbing the polyphenol-containing fraction by performing absorption resin column; washing the absorption column with diluted alcohol in order to obtain a polyphenol rich product. Optionally, the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine, 1 - 6 wt. % sucrose, and / or 10 - 30 % colored impurities, polyphenols, salts, and / or amino acids.

[0034] In some cases, the purifying step is accomplished by a single step ion exchange chromatography. The resin used in the ion exchange chromatography can be a strong acidic cation exchange resin. Optionally, the strong acidic cation exchange resin is crosslinked witha crosslinking agent such as, for example, divinyl benzene. In some cases, the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0035] The method can further include a decolorizing step after the purifying step and before the concentrating step. The decolorizing step can comprise performing ion exchange chromatography on the betaine-containing fraction. A strong basic anion exchange resin can be used in the ion exchange chromatography in the decolorizing step.

[0036] The concentrating step in the method can be performed under vacuum and / or with heating. Optionally, the concentrating step is performed to obtain a solids content of 57 % to 60 % by weight in order to get betaine liquid solution product.

[0037] The falling film plate evaporation in the concentrating step can optionally be performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

[0038] In addition to the betaine rich solution and products, the method described herein can further be used to separate other byproducts, including betaine-poor products. Betaine-poor products as describe herein contain little amounts of betaine, along with amino acids, salts and polyphenols. This betaine-poor separate is also one of the products on this study. Additionally, the betaine-poor fraction as describe herein can be concentrated and obtained in free-flowing powder form with above mentioned equipment.

[0039] Another product described herein includes a polyphenol rich extract obtained by the absorption of polyphenols from betaine-poor fractions to the adsorbent resin. This polymeric adsorbent resin is nonionic, macroporous crosslinked resins that selectively adsorb molecules based on a combination of hydrophobic interactions and molecular size, and a crosslinked adsorbent resin. Optionally, the crosslinked adsorbent resin can be a divinylbenzene (DVB) adsorbent resin with water retention capacity of 60-68%, average surface area of 800 m2 / g, and a mean pore size of -150 A.

[0040] The details of one or more embodiments are forth in the drawings and the description below. Other features, objects, and advantages will be apparent from the description and drawings, and from the claims.BRIEF DESCRIPTION OF THE DRAWINGS

[0041] FIG. 1 shows a detailed equipment flow chart of a pilot plant for producing purified betaine according to the methods described herein.

[0042] FIG. 2 shows a flow chart of a separation process of the pilot plant including a decolorization step according to the methods described herein.

[0043] FIG. 3 shows a flow chart for a drying process according to the methods describedherein.

[0044] FIG. 4 is a picture of a thin layer chromatography plate used to visualize the separation of betaine from other components.

[0045] FIG. 5 shows a TLC plate image for betaine characterization after separation via a resin column.

[0046] FIG. 6 shows a TLC plate image for betaine characterization after separation via a resin column.

[0047] FIG. 7 shows a picture of betaine product prepared according to the method described herein (test tube) as compared to commercial betaine (polyethylene bag).

[0048] FIG. 8 shows a flow chart of an adsorption process including concentration and drying process step of polyphenol rich product from betaine-poor fraction according to the methods described herein.

[0049] FIG. 9 shows a detailed equipment flow chart of a pilot plant for purified betaine, betaine liquid solution product, betaine-poor product and polyphenol rich product according to the methods described herein.DETAILED DESCRIPTION OF THE INVENTION

[0050] Provided herein are novel methods for obtaining free-flowing betaine powder, betaine liquid solution product, betaine-poor extract powder, and polyphenol rich extract powder, along with novel products resulting from the same. In particular, the method described herein is directed to recovering betaine and betaine-poor extract by a chromatographic single step process comprising one or more columns containing one packed bed. In the chromatographic separation step, strong acidic cation exchange cross-coupled divinyl benzene moiety resin metal form can be used. The separation step can be carried out in a single continuous process. The betaine concentration downstream of the column is evaporated to concentrate by using a falling film plate evaporator (FFPE). The betaine fraction, which concentration was brought to around 95%, 90 %, 85%, 80%, or 75% using FFPE, is sent to a conical ribbon vacuum dryer (CRVD), optionally by use of an isolated transfer pump and piping line. By using CRVD, the betaine concentrate is dried to its free- flowing type to result in the purified betaine product. An advantageous feature of the method of the disclosure is that chromatographic separation takes place at ambient temperature without any energy consumption. In addition, a method of increasing solid betaine concentration is provided by an efficient concentrating and drying process in order to increase vaporization surface area that minimizes the energy consumption.

[0051] The betaine-poor extract fraction downstream of the column is evaporated toconcentrate by using a falling film plate evaporator (FFPE). The betaine-poor extract fraction, which concentration was brought to around 85%, 80 %, 75%, 70%, or 65% using FFPE, is sent to a conical ribbon vacuum dryer (CRVD), optionally by use of an isolated transfer pump and piping line. By using CRVD, the betaine-poor extract concentrate is dried to its free- flowing type to result in the betaine-poor extract product. An advantageous feature of the method of the disclosure is that chromatographic separation takes place at ambient temperature without any energy consumption. In addition, a method of increasing solid betaine-poor extract concentration is provided by an efficient concentrating and drying process in order to increase vaporization surface area that minimizes the energy consumption.

[0052] Additionally, the polyphenol rich extract is produced from the betaine-poor extract fraction via adsorbent resin hydrophilic absorption by a single step process comprising one or more columns containing one packed bed. The adsorbed polyphenol rich extract onto resin is washed with a suitable eluent (e.g., diluted monohydric alcohol solution) in order to elute. The polyphenol rich extract concentration downstream of the column is evaporated to concentrate by using a falling film plate evaporator (FFPE). The polyphenol rich extract fraction, which concentration was brought to around 85%, 80 %, 75%, 70%, or 65% using FFPE, is sent to a conical ribbon vacuum dryer (CRVD), optionally by use of an isolated transfer pump and piping line. By using CRVD, the polyphenol rich extract concentrate is dried to its free-flowing type to result in the polyphenol rich extract product. An advantageous feature of the method of the disclosure is that adsorption takes place at ambient temperature without any energy consumption. In addition, a method of increasing solid polyphenol rich extract concentration is provided by an efficient concentrating and drying process in order to increase vaporization surface area that minimizes the energy consumption.Betaine Liquid Product

[0053] Described herein is a purified betaine liquid product, including a liquid solution comprising at least 45 wt. % and not more than 60 wt. % of betaine, less than 50 wt. % water, and optionally one or more additional components. The amount of betaine in the liquid solution is tailored to avoid betaine crystallization and oversaturation. Optionally, the one or more additional components comprises a de-icing agent. The de-icing agent can be, for example, a glycol (e.g., propylene glycol or glycerol). In some cases, the one or more additional components comprises sucrose. The sucrose can be present in an amount of less than 0.5 wt. % based on the weight of the liquid solution. Optionally, the one or more additional components comprises an anti-microbial agent. The anti-microbial agent can be, anti-mold or anti-bacterial agent, for example short chain carboxylic acids and or short chain branchedcarboxylic acids (e.g., propionic acid, formic acid, sorbic acid, etc.).

[0054] As described above, the liquid solution comprises at least 45 wt. % of betaine. In some examples, the liquid solution comprises at least 46 wt. %, at least 47 wt. %, at least 48 wt. %, at least 49 wt. %, at least 50 wt. %, at least 51 wt. %, at least 51 wt. %, at least 53 wt. %, at least 54 wt. %, at least 55 wt. %, at least 56 wt. %, at least 57 wt. %, at least 58 wt. %, at least 59 wt. % or 60 wt. % betaine.

[0055] Optionally, water is present in the mixture in an amount of less than 50 wt. % based on the weight of the particulate mixture. For example, the amount of water in the mixture can be 49 wt. % or less, 48 wt. % or less, 47 wt. % or less, 46 wt. % or less, 45 wt. % or less, 44 wt. % or less, 43 wt. % or less, 42 wt. % or less, 41 wt. % or less, 40.9 wt. % or less, 40.8 wt. % or less, 40.7 wt. % or less, 40.6 wt. % or less, 40.5 wt. % or less, 40.4 wt. % or less, 40.3 wt. % or less, 40.2 wt. % or less, or 40.1 wt. % or less.

[0056] The betaine in the liquid solution can optionally have light brown to amber color.Dry Powder Betaine Product

[0057] Described herein is a purified betaine product, comprising a dry, free flowing particulate mixture comprising at least 70 wt. % of betaine, less than 10 wt. % water, and optionally one or more additional components. Optionally, the one or more additional components comprises an anti-caking agent. The anti-caking agent can be, for example, a stearate salt (e.g., calcium stearate or magnesium stearate) or a silicon-containing compound (e.g., fume silicate or silicon dioxide). In some cases, the one or more additional components comprises sucrose. The sucrose can be present in an amount of less than 0.5 wt. % (e.g., 0.4 wt. %, 0.3 wt. %, 0.2 wt. %, or 0.1 wt. %) based on the weight of the dry, free flowing particulate mixture.

[0058] As described above, the dry, free flowing particulate mixture comprises at least 70 wt. % of betaine. In some examples, the dry, free flowing particulate mixture comprises at least 71 wt. %, at least 72 wt. %, at least 73 wt. %, at least 74 wt. %, at least 75 wt. %, at least 76 wt. %, at least 77 wt. %, at least 78 wt. %, at least 79 wt. %, at least 80 wt. %, at least 81 wt. %, at least 82 wt. %, at least 83 wt. %, at least 84 wt. %, at least 85 wt. %, at least 86 wt. %, at least 87 wt. %, at least 88 wt. %, at least 89 wt. %, at least 90 wt. %, at least 91 wt. %, at least 92 wt. %, at least 93 wt. %, at least 94 wt. %, at least 95 wt. %, at least 96 wt. %, at least 97 wt. %, at least 98 wt. %, at least 99 wt. %, or at least 99.5 wt. % betaine.

[0059] Optionally, water is present in the mixture in an amount of less than 10 wt. % based on the weight of the particulate mixture. For example, the amount of water in the mixture can be 9 wt. % or less, 8 wt. % or less, 7 wt. % or less, 6 wt. % or less, 5 wt. % or less, 4 wt. % orless, 3 wt. % or less, 2 wt. % or less, 1 wt. % or less, 0.9 wt. % or less, 0.8 wt. % or less, 0.7 wt. % or less, 0.6 wt. % or less, 0.5 wt. % or less, 0.4 wt. % or less, 0.3 wt. % or less, 0.2 wt. % or less, or 0.1 wt. % or less.

[0060] The betaine in the dry, free flowing particulate mixture can have an average particle size of 100 nm to 1.5 pm. For example, the average particle size can be 200 nm to 1.3 pm or 500 nm to 1.0 pm.Dry Powder Betaine-poor Extract Product

[0061] Described herein is a betaine-poor extract product, comprising a dry, free-flowing particulate mixture (optionally with a brown to light brown color), comprising at least 750 mgGAE / lOOg total phenolic content and less than 10 wt. % water and optionally one or more additional components. As used herein, mgGAE / g refers to milligrams of gallic acid equivalents per gram, and is used by those of ordinary skill in the art to express total phenolic content. Optionally, the one or more additional components comprises an anti-caking agent. The anti-caking agent can be, for example, a stearate salt (e.g., calcium stearate or magnesium stearate) or a silicon-containing compound (e.g., fume silicate or silicon dioxide). In some cases, the one or more additional components comprises sucrose. The sucrose can be present in an amount of less than 10 wt. % (e.g., 9 wt. %, 8 wt. %, 7 wt. %, or 6 wt. %) based on the weight of the dry, free flowing particulate mixture. As well as, in some cases, the one or more additional components comprises betaine. The betaine can be present in an amount of less than 10 wt. % (e.g., 9 wt. %, 8 wt. %, 7 wt. %, or 6 wt. %) based on the weight of the dry, free flowing particulate mixture.

[0062] As described above, the dry, free flowing particulate mixture comprises at least 750 mgGAE / lOOg total phenolic content. In some examples, the dry, free flowing particulate mixture comprises at least 775 mgGAE / lOOg, at least 800 mgGAE / lOOg, at least 825 mgGAE / lOOg, at least 850 mgGAE / lOOg, at least 875 mgGAE / lOOg, at least 900 mgGAE / lOOg, at least 925 mgGAE / lOOg, at least 950 mgGAE / lOOg, at least 975 mgGAE / lOOg, at least 1000 mgGAE / lOOg or at least 1200 mgGAE / lOOg total phenolic content.

[0063] Optionally, water is present in the mixture in an amount of less than 10 wt. % based on the weight of the particulate mixture. For example, the amount of water in the mixture can be 9 wt. % or less, 8 wt. % or less, 7 wt. % or less, 6 wt. % or less, 5 wt. % or less, 4 wt. % or less, 3 wt. % or less, 2 wt. % or less, 1 wt. % or less, 0.9 wt. % or less, 0.8 wt. % or less, 0.7 wt. % or less, 0.6 wt. % or less, 0.5 wt. % or less, 0.4 wt. % or less, 0.3 wt. % or less, 0.2 wt. % or less, or 0.1 wt. % or less.

[0064] The betaine-poor extract powder in the dry, free flowing particulate mixture can have an average particle size of 100 nm to 1.5 pm. For example, the average particle size can be 200 nm to 1.3 pm or 500 nm to 1.0 pm. In some examples, the average particle size can be 100 nm, 200 nm, 300 nm, 400 nm, 500 nm, 600 nm, 700 nm, 800 nm, 900 nm, 1 pm, 1.1 pm, 1.2 pm, 1.3 pm, 1.4 pm, or 1.5 pm.

[0065] Additionally, concentrated betaine-poor extract without anti-caking agent comprises at least 1500 mgGAE / lOOg total phenolic content. In some examples, concentrated extract comprises atleast 1525 mgGAE / lOOg, at least 1550 mgGAE / lOOg, atleast 1575 mgGAE / lOOg, at least 1600 mgGAE / lOOg, at least 1625 mgGAE / lOOg, at least 1650 mgGAE / lOOg, at least 1675 mgGAE / lOOg, at least 1700 mgGAE / lOOg, at least 1725 mgGAE / lOOg, at least 1750 mgGAE / lOOg or at least 2000 mgGAE / lOOg total phenolic content.Dry Powder Polyphenolic Extract Product

[0066] Described herein is a polyphenolic extract product, comprising a dry, free-flowing particulate mixture, optionally with a dark brown to brown color and vanillic odor, comprising at least 6000 mgGAE / lOOg total phenolic content and less than 10 wt. % water and optionally one or more additional components. Optionally, the one or more additional components comprises an anti -caking agent. The anti-caking agent can be, for example, a stearate salt (e.g., calcium stearate or magnesium stearate) or a silicon-containing compound (e.g., fume silicate or silicon dioxide). In some cases, the one or more additional components comprises sucrose. The sucrose can be present in an amount of less than 0.5 wt. % (e.g., 0.4 wt. %, 0.3 wt. %, 0.2 wt. %, or 0.1 wt. %) based on the weight of the dry, free flowing particulate mixture.

[0067] As described above, the dry, free flowing particulate mixture comprises at least 6000 mgGAE / lOOg total phenolic content. In some examples, the dry, free flowing particulate mixture comprises at least 6250 mgGAE / lOOg, at least 6500 mgGAE / lOOg, at least 6750 mgGAE / lOOg, at least 7000 mgGAE / lOOg, at least 7250 mgGAE / lOOg, at least 7500 mgGAE / lOOg, at least 7750 mgGAE / lOOg, at least 8000 mgGAE / lOOg, at least 8250 mgGAE / lOOg, at least 8500 mgGAE / lOOg or at least 10000 mgGAE / lOOg total phenolic content.

[0068] Optionally, water is present in the mixture in an amount of less than 10 wt. % based on the weight of the particulate mixture. For example, the amount of water in the mixture can be 9 wt. % or less, 8 wt. % or less, 7 wt. % or less, 6 wt. % or less, 5 wt. % or less, 4 wt. % or less, 3 wt. % or less, 2 wt. % or less, 1 wt. % or less, 0.9 wt. % or less, 0.8 wt. % or less, 0.7 wt. % or less, 0.6 wt. % or less, 0.5 wt. % or less, 0.4 wt. % or less, 0.3 wt. % or less, 0.2 wt. % or less, or 0.1 wt. % or less.

[0069] The polyphenolic extract powder in the dry, free flowing particulate mixture can have an average particle size of 100 nm to 1.5 pm. For example, the average particle size can be 200 nm to 1.3 pm or 500 nm to 1.0 pm. In some examples, the average particle size can be 100 nm, 200 nm, 300 nm, 400 nm, 500 nm, 600 nm, 700 nm, 800 nm, 900 nm, 1 pm, 1.1 pm, 1.2 pm, 1.3 pm, 1.4 pm, or 1.5 pm.

[0070] Additionally, concentrated polyphenolic extract without anti-caking agent comprises at least 15000 mgGAE / lOOg total phenolic content. In some examples, concentrated extract comprises at least 15250 mgGAE / lOOg, at least 15500 mgGAE / lOOg, at least 15750 mgGAE / lOOg, at least 16000 mgGAE / lOOg, at least 16250 mgGAE / lOOg, at least 16500 mgGAE / lOOg, at least 16750 mgGAE / lOOg, at least 17000 mgGAE / lOOg, at least 17250 mgGAE / lOOg, at least 17500 mgGAE / lOOg or at least 20000 mgGAE / lOOg total phenolic content.Methods for Obtaining Betaine Liquid Product

[0071] Also described herein is a method for obtaining betaine liquid product, comprising purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a containing fraction; concentrating the betaine-containing fraction by performing falling film plate evaporation to form a concentrated betaine fraction to obtain a solids content of 45 % to 60 % by weight in order to get betaine liquid solution product. The steps are described in detail below.Separation Step

[0072] Molasses (e.g., sugar beet molasses) or vinasse can be used as the starting material for the methods described herein. The molasses can have a 50-70% dry substance profile. This dry substance profile consists of 50-70% betaine, 3-8.5% sucrose and 21.5-47% colored impurities, polyphenols, salts and amino acids. In the present method, there is no need to predilute the molasses on the feeding operation. In some cases, prediluting the molasses on the feeding operation is not performed, and non-prediluted molasses is used in the separation process.

[0073] In other examples, the molasses can have a betaine concentration of 25-50 wt. % based on the total concentration of the starting material. This starting material can also contain around 14-64 wt. % water, 1-6 wt. % sucrose, and around 10-30 wt. % other colored materials such as a mixture of polyphenols, amino acids, salts, and the like.

[0074] To start the separation process, non-prediluted molasses can be fed on the strongly acidic cation exchange resin loaded columns. The feeding operation can be controlled manually or can be operated with a fully automated technological apparatus. Eluting withwater can be controlled manually or fully automated technological apparatus. Molasses separation can be performed by passing the material through the cation exchange resin with eluting water. The separating step can be performed at room temperature. In some cases, water used for the fractionation of molasses can be around 20 °C to 30 °C, such as at 25 °C.

[0075] In some cases, the separation step is accomplished by a single step ion exchange chromatography. The resin used in the ion exchange chromatography can be a strong acidic cation exchange resin. Optionally, the strong acidic cation exchange resin is crosslinked with a crosslinking agent such as, for example, divinyl benzene. In some cases, the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0076] According to the present disclosure, betaine and betaine-poor extract recovery is performed by using strong acidic ion exchange resin which comprises gel type sulphonated polystyrene divinylbenzene in metal form, from beet molasses. In some examples, the strong acidic cation exchange resin is cross-coupled divinylbenzene moiety (6%), has a uniformity coefficient of 1.1, and a mean bead diameter around 0.30 mm. Preferably, the strongly acidic cation exchange resin can be in monovalent or divalent form. The monovalent form can include, e.g., sodium, potassium, or mixtures thereof. The divalent form can include, e.g., calcium, magnesium or mixtures thereof. Strongly acid gel-type cation exchange resin (e.g., “Purolite”, “Seplite CM” or “Lewatit”), preferably in sodium or potassium form, can be used as a packing for the columns for the separation of beet molasses. With respect to the chromatographic column design, column resin loading capacity height can be 2-11 meters and the column diameter can be 0.3-2.5 meters. The flow rate of the molasses from fractionation column can be 0.1 to 0.5 m3 / h / m2, more preferably 0.2 to 0.3 m3 / h / m2.

[0077] Three separation profiles can be attained from downstream elution in the chromatographic separation step based on the solid content characteristics. The first fraction can contain colored impurities that can include a mixture of salts, sucrose, polyphenols, amino acids, and some other impurities. The second fraction can include some sucrose, typically in minimal amounts, as most sucrose fractionates with the first waste mixture. The last, third fraction contains purified betaine.

[0078] FIG. 1 illustrates the separation process. The first fraction, which contains colored impurities, salts, polyphenols and amino acids, along with negligible amount of sucrose, is collected to the T4 as illustrated in FIG. 1. The second fraction, which contains betaine, is collected to T5 as illustrated in FIG. 1. These separations can be controlled manually or fully automated technological apparatus and valves. New feeding of the molasses can be performed by using automated feeding pumps after second fraction (which contains betaine) is fullyrecovered from the downstream of the separation column. Feeding of molasses with an automated technological apparatus utilizes continuous fractionation with using other automated apparatus connected to each other via an automation software.Optional Decolorization Step

[0079] The method can further include a decolorizing step after the purifying step and before the concentrating step. The decolorizing step can comprise performing ion exchange chromatography (a decolorization resin column) on the betaine-containing fraction. A strong basic anion exchange resin can be used in the ion exchange chromatography in the decolorizing step. Optionally, the fraction can be passed through a food grade, chloride form strongly basic anion exchange resin with beads of uniform size (monodisperse) based on a styrene- divinylbenzene copolymer.

[0080] The decolorization process can be performed using gel-type monodisperse, strongly basic anion exchange resin based on a styrene-divinylbenzene copolymer. The decolorization resin functional group can be a quaternary amine and have a chlorine ionic form; uniformity coefficient is 1.1 and mean bead size is 0.62 mm.

[0081] The decolorization process is depicted in FIG. 2. The decolorization process is provided by passing through of betaine fraction which is stored in T5 illustrated in FIG. 2 from the column that is fully packed with strongly basic styrene- divinylbenzene copolymer type decolorization resin matrix. Preferably, a single pass is sufficient to obtain a decolorized betaine fraction. After the decolorization process, the decolorized betaine fraction is transferred to the intermediate storage tank which is spotted as T7 illustrated in FIG. 2. The flow rate of the betaine fraction from T5 in the decolorization column can be 0.5 to 3 m3 / h / m2, more preferably 0.8 to 1.2 m3 / h / m2.Concentrating Step

[0082] Concentration of betaine fraction to get betaine liquid product, can be performed by using high temperature and vacuum applicable equipment, e.g., thin film evaporator, falling film evaporator, or vacuumed rotary evaporator. However, this type of equipment has limited vaporization capacity caused by small vaporization surface in their systems. To increase vaporization capacity with this equipment, the process temperature can be increased or the system quantity increased by connecting these systems parallel in each other. These methods are unattractive, however, due to increased capital expenses.

[0083] In the present disclosure, however, the concentration of the decolorized betaine fraction is performed with using “Falling Film Plate Evaporator” (FFPE). This method utilizes the high vaporization surface capacity. Its vaporization surface area can be 10-20 times and even 40 times higher from the thin film vaporization surface area. FFPE vaporization surface area can be increased with additional plates to the system. In this type of evaporator, the fact that the film uses its own attraction to fall provides an additional advantage in terms of energy savings. Providing an equal amount of product to the plates is done by the distribution chamber mounted on the plate bundle. Through the circulation system and pump, consecutive evaporation processes can be carried out in the same body, that is, in a single effect. This method allows the vapor and liquid phases to be separated very quickly and works much more efficiently compared to tubular type models.

[0084] Decolorized betaine fraction concentration process takes place with pumping decolorized betaine fraction from T7 illustrated in FIG. 3 to the FFPE bottomed circulation side. From there, decolorized betaine fraction is circulated on the plates with a desired flow rate in order to vaporize water inside the fraction. Continuous concentration change can be monitored with manually by a hand refractometer or automated in-process refractometer equipment known in the art.

[0085] The concentrating step for betaine liquid product in the method can be performed under vacuum and / or with heating. The falling film plate evaporation in the concentration step can optionally be performed at a vacuum pressure of 35 mmHg to 70 mmHg, such as from 40 mmHg to 60 mmHg or from 50 mmHg to 55 mmHg. The falling film plate evaporation in the concentrating step can optionally be performed at a temperature of 50 °C or greater. Optionally, vaporization can be performed at 60 °C to 80 °C, such as at 65 °C, to avoid any coloration of betaine caused by heating.

[0086] Optionally, the concentrating step is performed to obtain a solids content of 45 % to 60 % by weight (e.g., 47 %, 50 %, 53 %, 57 %, or 60 %).Methods for Obtaining Dry Powder Betaine and Betaine-Poor Extract

[0087] Also described herein is a method for obtaining dry powder betaine and betaine-poor extract, comprising purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a containing fraction; concentrating the betaine-containing fraction by performing falling film plate evaporation to form a concentrated betaine fraction; and drying the concentrated betaine fraction by conical ribbon vacuum drying to obtain a dry powder betaine and concentrating betaine-poor fraction by performing falling film plate evaporation to form a concentrated betaine-poor fraction; and drying the concentrated betaine-poor fraction by conical ribbon vacuum drying to obtain a dry powder betaine-poor extract. The steps are described in detail below.Separation Step

[0088] Molasses (e.g., sugar beet molasses) or vinasse can be used as the starting material for the methods described herein. The molasses can have a 50-70% dry substance profile. This dry substance profile consists of 50-70% betaine, 3-8.5% sucrose and 21.5-47% colored impurities, polyphenols, salts and amino acids. In the present method, there is no need to predilute the molasses on the feeding operation.

[0089] In other examples, the molasses can have a betaine concentration of 25-50 wt. % based on the total concentration of the starting material. This starting material can also contain around 14-64 wt. % water, 1-6 wt. % sucrose, and around 10-30 wt. % other colored materials such as a mixture of polyphenols, amino acids, salts, and the like.

[0090] To start the separation process, non-prediluted molasses can be fed on the strongly acidic cation exchange resin loaded columns. The feeding operation can be controlled manually or can be operated with a fully automated technological apparatus. Eluting with water can be controlled manually or fully automated technological apparatus. Molasses separation can be performed by passing the material through the cation exchange resin with eluting water. The separating step can be performed at room temperature. In some cases, water used for the fractionation of molasses can be around 20 °C to 30 °C, such as at 25 °C.

[0091] In some cases, the separation step is accomplished by a single step ion exchange chromatography. The resin used in the ion exchange chromatography can be a strong acidic cation exchange resin. Optionally, the strong acidic cation exchange resin is crosslinked with a crosslinking agent such as, for example, divinyl benzene. In some cases, the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0092] According to the present disclosure, betaine and betaine-poor extract recovery is performed by using strong acidic ion exchange resin which comprises gel type sulphonated polystyrene divinylbenzene in metal form, from beet molasses. In some examples, the strong acidic cation exchange resin is cross-coupled divinylbenzene moiety is 6%, has a uniformity coefficient of 1.1, and a mean bead diameter around 0.30 mm. Preferably, the strongly acidic cation exchange resin can be in monovalent or divalent form. The monovalent form can include, e.g., sodium, potassium, or mixtures thereof. The divalent form can include, e.g., calcium, magnesium or mixtures thereof. Strongly acid gel-type cation exchange resin (e.g., “Purolite”, “Seplite CM” or “Lewatit”), preferably in sodium or potassium form, can be used as a packing for the columns for the separation of beet molasses. With respect to the chromatographic column design, column resin loading capacity height can be 2-11 meters and the column diameter can be 0.3-2.5 meters. The flow rate of the molasses from fractionationcolumn can be 0.1 to 0.5 m3 / h / m2, more preferably 0.2 to 0.3 m3 / h / m2.

[0093] Three separation profiles can be attained from downstream elution in the chromatographic separation step based on the solid content characteristics. The first fraction can contain colored impurities that can include a mixture of salts, sucrose, polyphenols, amino acids, and some other impurities. The second fraction can include some sucrose, typically in minimal amounts, as most sucrose fractionates with the first waste mixture. The last, third fraction contains purified betaine.

[0094] FIG. 1 illustrates the separation process. The first fraction, which contains colored impurities, salts, polyphenols and amino acids, along with negligible amount of sucrose, is collected to the T4 as illustrated in FIG. 1. The second fraction, which contains betaine, is collected to T5 as illustrated in FIG. 1. These separations can be controlled manually or fully automated technological apparatus and valves. New feeding of the molasses can be performed by using automated feeding pumps after second fraction (which contains betaine) is fully recovered from the downstream of the separation column. Feeding of molasses with an automated technological apparatus utilizes continuous fractionation with using other automated apparatus connected to each other via an automation software.Optional Decolorization Step

[0095] The method can further include a decolorizing step after the purifying step and before the concentrating step. The decolorizing step can comprise performing ion exchange chromatography (a decolorization resin column) on the betaine-containing fraction. A strong basic anion exchange resin can be used in the ion exchange chromatography in the decolorizing step. Optionally, the fraction can be passed through a food grade, chloride form strongly basic anion exchange resin with beads of uniform size (monodisperse) based on a styrene- divinylbenzene copolymer.

[0096] The decolorization process takes place with using gel-type monodisperse, strongly basic anion exchange resin based on a styrene-divinylbenzene copolymer. The decolorization resin functional group can be a quaternary amine and have a chlorine ionic form; uniformity coefficient is 1.1 and mean bead size is 0.62 mm.

[0097] The decolorization process is depicted in FIG. 2. The decolorization process is provided by passing through of betaine fraction which is stored in T5 illustrated in FIG. 2 from the column that is fully packed with strongly basic styrene- divinylbenzene copolymer type decolorization resin matrix. Preferably, a single pass is sufficient to obtain a decolorized betaine fraction. After the decolorization process, the decolorized betaine fraction is transferred to the intermediate storage tank which is spotted as T7 illustrated inFIG. 2. The flow rate of the betaine fraction from T5 in the decolorization column can be 0.5 to 3 m3 / h / m2, more preferably 0.8 to 1.2 m3 / h / m2.Concentrating Step

[0098] Concentration of betaine and / or betaine-poor extract has been performed can be performed by using high temperature and vacuum applicable equipment, e.g., thin film evaporator, falling film evaporator, or vacuumed rotary evaporator. However, this type of equipment has limited vaporization capacity caused by small vaporization surface in their systems. To increase vaporization capacity with this equipment, the process temperature can be increased or the system quantity increased by connecting these systems parallel in each other. These methods are unattractive, however, due to increased capital expenses.

[0099] In the present disclosure, however, the concentration of the decolorized betaine fraction is performed with using “Falling Film Plate Evaporator” (FFPE). This method utilizes the high vaporization surface capacity. Its vaporization surface area can be 10- 20 times and even 40 times higher from the thin film vaporization surface area. FFPE vaporization surface area can be increased with additional plates to the system. In this type of evaporator, the fact that the film uses its own attraction to fall provides an additional advantage in terms of energy savings. Providing an equal amount of product to the plates is done by the distribution chamber mounted on the plate bundle. Through the circulation system and pump, consecutive evaporation processes can be carried out in the same body, that is, in a single effect. This method allows the vapor and liquid phases to be separated very quickly and works much more efficiently compared to tubular type models.

[0100] Decolorized betaine fraction concentration process takes place with pumping decolorized betaine fraction from T7 illustrated in FIG. 3 to the FFPE bottomed circulation side. From there, decolorized betaine fraction is circulated on the plates with a desired flow rate in order to vaporize water inside the fraction. Continuous concentration change can be monitored with manually by a hand refractometer or automated in-process refractometer equipment known in the art.

[0101] Betaine-poor fraction concentration process takes place with pumping decolorized betaine fraction from T8 illustrated in FIG. 8 to the FFPE bottomed circulation side. From there, betaine-poor fraction is circulated on the plates with a desired flow rate in order to vaporize water inside the fraction. Continuous concentration change can be monitored with manually by a hand refractometer or automated in-process refractometer equipment known in the art.

[0102] The concentrating step for both betaine and betaine-poor fractions in the method canbe performed under vacuum and / or with heating. The falling film plate evaporation in the concentration step can optionally be performed at a vacuum pressure of 35 mmHg to 70 mmHg, such as from 40 mmHg to 60 mmHg or from 50 mmHg to 55 mmHg. The falling film plate evaporation in the concentrating step can optionally be performed at a temperature of 50 °C or greater. Optionally, vaporization can be performed at 60 °C to 80 °C, such as at 65 °C, to avoid any coloration of betaine caused by heating.

[0103] Optionally, the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight (e.g., 65 %, 70 %, 75 %, 80 %, or 85 %).Drying Step

[0104] Concentrated decolorized betaine fraction or betaine-poor fraction can be transferred, for example, by an isolated pipeline utilizing a circulation pump, to the conical ribbon vacuum dryer (CRVD).

[0105] A spiral mixing ribbon inside the vertical dryer initiates a three-dimensional flow of the mixing betaine. The conical designed dryer vessel enables powers to be discharged at a maximum level. The equipment consists of a vertical cone-shaped vessel with an exclusive combination of top placed vortex breakers and a helical ribbon agitator with minimal clearance to the side walls enabling the feed raw materials to be dried uniformly and efficiently, resulting in a quality final product. The CRVD can be heatable by steam, thermal oil, or water. The vertical spiral mixing ribbon can be set up using different rotary speeds according to the mixing material specifications. The CRVD system can also contain a powder trap, a heat exchanger for vacuumed steam condensation, and a vacuum pump.

[0106] The drying step can be performed under vacuum and / or with heating. The conical ribbon vacuum drying can be performed at a temperature of 80 °C to 125 °C (e.g., from 90 °C to 120 °C, such as at 110 °C). The vacuum pressure can be from 10 mmHg to 50 mmHg (e.g., from 30 mmHg to 45 mmHg or from 35 mmHg to 40 mmHg).

[0107] Optionally, the drying step is performed to achieve a percent humidity of less than 1%. Dry, free-flow powder betaine and / or free-flow powder betaine-poor can be obtained based on this process. After the drying process takes place, dry free-flow powder betaine and / or free-flow powder betaine-poor can be treated with anticaking agents such as metal salts of stearic acid, e.g., calcium stearate or magnesium stearate, or silicate compounds, e.g., fume silicate, silicon dioxide, or the like.Absorption Step for Polyphenol Rich Extract

[0108] Polyphenol rich fraction absorption process takes place with pumping betaine-poor fraction from T8 illustrated in FIG. 8 and FIG. 9 to the adsorption column. According to thepresent disclosure, absorption performed by using polymeric, nonionic, macroporous crosslinked adsorbent resins that selectively adsorb molecules based on a combination of hydrophobic interactions and molecular size, and a crosslinked divinylbenzene (DVB) adsorbent resin with water retention capacity of 60-68%, average surface area of 800 m2 / g, and a mean pore size of -150 A. Polymeric, nonionic adsorbent resin (e.g., “Amberlite”, “Seplite” or “Lewatit”) can be used as a packing for the columns for the absorption of polyphenols. Absorption process takes place by passing betaine-poor fraction directly through the adsorbent resin column and elution with a single step or more cycle. When passing betaine-poor fraction directly through the adsorbent resin column, hydrophilic polyphenolic molecules are absorbed by the help of resin surface activated functional groups. Betaine-poor fraction flow is continued until all the adsorbent resin fully loaded. After loading accomplished to the adsorbent resin, adsorption column is rinsed with deionized water. Absorbed polyphenols are desorbed with an appropriate solvent (e.g., diluted monohydric alcohol especially ethanol-water mixture).

[0109] Concentrating and drying steps are performed according to the methods described herein.

[0110] Throughout this application, various publications are referenced. The disclosures of these publications in their entireties are hereby incorporated by reference into this application.[OHl] The following examples are set forth below to illustrate the methods and results according to the disclosed subject matter. These examples are not intended to be inclusive of all aspects of the subject matter disclosed herein, but rather to illustrate representative methods and results. These examples are not intended to exclude equivalents and variations of the subject matter described herein which are apparent to one skilled in the art.EXAMPLESExample 1: Thin Layer Chromatography (TLC) For Betaine Determination

[0112] Glycine-betaine molecule has a very low log P value due to the high polarity of the molecule. Betaine molecule has a cationic trimethylammonium moiety and an anionic carbonyl moiety. This rich ionic character gives the molecule high polarity and very specific ionic selectivity. These characteristics make it difficult to stain this molecule on a thin layer chromatography (TLC) silica surface. To achieve detection of betaine via thin layer chromatography, a specific mobile phase was first designed for these studies.

[0113] A butanol / acetic acid / water mobile phase was used first, but the components were not separated via chromatography. A more polar, ethanol / water mixture mobile phase was used; however, the separated spots were not spherical and were distorted. Because of that, anethanol / water / chloroform mixture was used as the eluent to achieve spherical shaped spots.

[0114] Stain procedure: A standard pure betaine solution and a stock solution containing betaine were loaded onto a TLC plate. The mobile phase used was a mixture of 43 mL ethanol / 43 mL water / 4 mL chloroform. After 80% of the plate was wetted with the mobile phase, the TLC procedure was stopped. The plate was dried, then 0.1 N sodium hydroxide solution was applied onto the plate. Then it was dried by oven at 105 °C for 2 minutes. Then, the dried plate was wetted with a phenolphthalein solution. Then, the plate was dried completely by oven at 105 °C for 5 minutes. Then the plate became pink in color but the betaine molecule spot was not, as illustrated in FIG. 4.Example 2: Chromatographic Separation of Betaine and Betaine-Poor Extract from a Known Betaine- Concentration Molasses

[0115] Column preparation'. 250 g of Purolite PCR642K resin was suspended in 250 mL of deionized water with good stirring in order to release air bubbles in resin beads. The suspension was poured into the column that was prepared with a cotton piece on the bottom of it to obstruct the leakage of resin slurry from the tap. Loading was completed after all resin beads were settled down. Deionized water (500 mL) was passed through the column for washing resin. A betaine stock solution (38% betaine concentration; 25 mL) was added via a cannula hose. Addition was performed on top of the resin beads upper side of the column with a constant addition of water. When the addition was complete, the downstream process was started and tap of the column was opened. Effluent flow was adjusted to 6-8 mL / min.

[0116] After the added betaine solution was buried in resin beads, around 500 mL deionized water was poured on the resin column and the separation procedure was continued with the same conditions. The fractions were collected into the 20 mL test tubes. All test tubes were analyzed using TLC to determine whether betaine was present. FIG. 5 shows a TLC plate image for betaine characterization after separation via the resin column.

[0117] The first spot from the left side is the standard pure betaine. The remaining samples, from left to the right, represent the fraction tube numbers. At fraction 6, almost all betaine had eluted from the column and the process was finalized.

[0118] All betaine containing tubes were poured into an evaporator bottle for rotary evaporation. After all the water was evaporated, crystallized material remained in the rotary balloon and it was around 10.5 g. The material was very hygroscopic material and was mixed with an appropriate anti-caking agent, such as stearic acid calcium, magnesium or other related metal salts.

[0119] All colored fractions as first fraction were poured into an evaporator bottle for rotaryevaporation. After half of the water was evaporated, a calculated amount of fumed silicate (around 3.36 g, 40% of total betaine-poor fraction solid percentage) was added to the evaporator bottle and the evaporation / drying process was continued. After all the water was evaporated, brown powder was obtained as 11.7 g betaine-poor powder product.Table 1 - Process detailsExample 3: Chromatographic Separation of Betaine from a Known Betaine- Concentration Molasses at Lower Input Weight

[0120] The general procedure was the same with the procedure according to Example 2, with the following modifications as shown in Table 2.Table 2 - Example 3 Process Details

[0121] FIG. 6 shows a TLC plate image for betaine characterization after separation via the resin column. The product that was obtained from Example 3 was more colorless and purer than the Example 2. This shows that the column loading capacity impacts the separation and purification of betaine.Example 4 - Decolorization Process by Using Ion Exchange Resin

[0122] Column preparation: 220 g of Lewatit S 6268 resin was suspended in 250 mL of deionized water with good stirring to release air bubbles in resin beads. The suspension was then poured into the column that was prepared with a cotton piece on the bottom of it to obstruct the leakage of resin slurry from the tap. Loading was completed after all resin beads were settled down. Deionized water (500 mL) was passed through the column for washing resin.

[0123] Using a graduated dropping funnel, fractionated betaine solution was dropped onto the resin and at the same time PTFE plug of the resin column was set up to the desired flow rate. After all the betaine fractions passed through to the decolorization resin column, the resin had been washed with demineralized water to run off the residual betaine in the column.Table 3 - Decolorization Process DetailsExample 5: Industrial Scale Betaine and Betaine-Poor Fractionation and Production of Free-Flow Betaine and Betaine-Poor Products with Using Specialized Equipment

[0124] Molasses feeding ( 130 kg) was performed with automated valves to a column packed with strong acidic polystyrene cation exchange resin cross-coupled with 6% divinyl benzene moiety at ambient temperature. The molasses were eluted with demineralized water which was at ambient temperature in order to separate the betaine fraction. The first fraction was collected in a storage tank dedicated to store betaine-poor fractions utilizing an in- process conductivity sensor and in-line refractometer which commands the valves automatically via a Scada Automation System. The second betaine fraction was automatedlypumped to the decolorization column at ambient temperature until its elution was finished. That cycle was performed in approximately 30 minutes. After elution completed, command was taken from the in-process sensors, and a new 130 kg batch of molasses feeding was initiated for a new sequence. The process was completed in approximately 24 hours.

[0125] From the decolorization column, around 750 liters of decolorized betaine fraction was transferred to its dedicated intermediate storage tank every 30 minutes. Decolorized betaine fraction (1250 L) was transferred to the falling film plate evaporator (FFPE) bottomed circulation tank and at 65 °C and under 50 mmHg vacuum, decolorized betaine fraction was concentrated to 85% in solid dry substance with controlled in-process refractometer. The process took approximately 1 hour. Around 120 kg concentrated betaine slurry was pumped with a thermally isolated pipeline to the conical ribbon vacuum dryer (CRVD). Drying temperature and vacuum were set at 95 °C and 35 mmHg. Ribbon mixing was performed at 100 rpm. Betaine (101 kg) was obtained after 1 hour drying process with 0.8 % (w / w) humidity, 98.9% purity (HPLC). The resulting betaine product is shown in the test tube in FIG. 7, as compared to commercial betaine (in the polyethylene bag in the figure).

[0126] After powder betaine was obtained, 1250 L of betaine-poor fraction was transferred to the FFPE bottomed circulation tank and at 65 °C and under 50 mmHg vacuum, the betaine- poor fraction was concentrated to 60% in solid dry substance with controlled in-process refractometer. The process took approximately 45 minutes. Approximately 125 kg of concentrated betaine-poor slurry was pumped with a thermally isolated pipeline to the conical ribbon vacuum dryer (CRVD). Before the drying procedure, 50 kg of fumed silica was added to the CRVD. Drying temperature and vacuum were set at 95 °C and 35 mmHg. Ribbon mixing was performed at 100 rpm. Betaine-poor powder (125 kg) was obtained after 1 hour of the drying process with 1.5 % (w / w) humidity.Table 4 - Industrial Betaine Production Process Details

[0127] Betaine purification can be increased with optimization of the process with different feeding amount. It has been determined by the studies shown herein that there is an inverse proportion between the feeding amount and purity.Example 6: Absorption of Polyphenolic Compounds to the Absorbent Resin from a Known Concentration Betaine-poor Stock Solution

[0128] Column preparation'. 250 g of Seplite LXA 816 adsorbent resin was suspended in 250 mL of deionized water with good stirring to release air bubbles in the resin beads. The suspension was poured into a column that was prepared with a cotton piece on the bottom of it to obstruct the leakage of resin slurry from the tap. Loading was completed after all resin beads were settled down. Deionized water (500 mL) was passed through the column to wash the resin. A betaine-poor stock solution (6% solid concentration) was added directly without avoiding any mess of resin. Addition was performed until all column storage balloon was filled up. When the addition was complete, the downstream process was started and tap of the column was opened. Effluent flow was adjusted to 10-12 mL / min.

[0129] Around 3000 mL of the betaine-poor stock solution was passed through the adsorbent resin column with a constant flow rate. After the adsorption process finished, the column was rinsed with 500 mL of deionized water. Desorption was performed with a 40% ethanolic water mixture. The adsorbent resin column was washed with 40% ethanolic water solution, and polyphenolic dark colored effluent was collected (250 mL solution). Solution solid concentration was measured with moisture analyzer as 7.2% w / w.

[0130] All polyphenol containing solution was poured into an evaporator bottle for rotary evaporation. A calculated amount of fumed silicate (around 27 g, 60% of total polyphenolic fraction solid percentage) was added to the bottle and evaporation / drying process continued. After all the water was evaporated, a dark brown powder was obtained as 45g polyphenolic powder product (6345 mgGAE / 100 g total phenolic content, 1950 mgTE / 100 g total antioxidant capacity).EXEMPLARY EMBODIMENTS

[0131] As used below, any reference to a series of embodiments (e.g., “Embodiments 1-4”)or non-enumerated group of embodiments (e.g., “any previous or subsequent embodiment”) is to be understood as a reference to each of those embodiments disjunctively (e.g., “Embodiments 1-4” is to be understood as “Embodiments 1, 2, 3, or 4”). Non-limiting embodiments are provided below.

[0132] Embodiment l is a purified betaine product, comprising a dry, free flowing particulate mixture comprising: at least 70 wt. % betaine; less than 10 wt. % water; and optionally one or more additional components.

[0133] Embodiment 2 is the purified betaine product of any previous or subsequent embodiment, wherein the one or more additional components comprises an anti-caking agent.

[0134] Embodiment 3 is the purified betaine product of any previous or subsequent embodiment, wherein the anti-caking agent comprises a stearate salt.

[0135] Embodiment 4 is the purified betaine product of any previous or subsequent embodiment, wherein the stearate salt comprises calcium stearate or magnesium stearate.

[0136] Embodiment 5 is the purified betaine product of any previous or subsequent embodiment, wherein the anti-caking agent comprises a silicon-containing compound.

[0137] Embodiment 6 is the purified betaine product of any previous or subsequent embodiment, wherein the silicon-containing compound comprises fume silicate or silicon dioxide.

[0138] Embodiment 7 is the purified betaine product of any previous or subsequent embodiment, wherein the one or more additional components comprises sucrose.

[0139] Embodiment 8 is the purified betaine product of any previous or subsequent embodiment, wherein the sucrose is present in an amount of less than 0.5 wt. % based on the weight of the dry, free flowing particulate mixture.

[0140] Embodiment 9 is the purified betaine product of any previous or subsequent embodiment, wherein the dry, free flowing particulate mixture comprises at least 75 wt. % of betaine.

[0141] Embodiment 10 is the purified betaine product of any previous or subsequent embodiment, wherein the dry, free flowing particulate mixture comprises at least 85 wt. % betaine.

[0142] Embodiment 11 is the purified betaine product of any previous or subsequent embodiment, wherein the dry, free flowing particulate mixture comprises at least 95 wt. % betaine.

[0143] Embodiment 12 is the purified betaine product of any previous or subsequent embodiment, wherein the betaine has an average particle size of 100 nm to 1.5 pm.

[0144] Embodiment 13 is a method for obtaining dry powder betaine, comprising purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-containing fraction; concentrating the betaine-containing fraction by performing falling film plate evaporation to form a concentrated betaine fraction; and drying the concentrated betaine fraction by conical ribbon vacuum drying to obtain a dry powder betaine.

[0145] Embodiment 14 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

[0146] Embodiment 15 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

[0147] Embodiment 16 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

[0148] Embodiment 17 is the method of any previous or subsequent embodiment, wherein the purifying step is accomplished by a single step ion exchange chromatography.

[0149] Embodiment 18 is the method of any previous or subsequent embodiment, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography.

[0150] Embodiment 19 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with a crosslinking agent.

[0151] Embodiment 20 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0152] Embodiment 21 is the method of any previous or subsequent embodiment, wherein the crosslinking agent is divinyl benzene.

[0153] Embodiment 22 is the method of any previous or subsequent embodiment, further comprising a decolorizing step after the purifying step and before the concentrating step.

[0154] Embodiment 23 is the method of any previous or subsequent embodiment, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine- containing fraction.

[0155] Embodiment 24 is the method of any previous or subsequent embodiment, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

[0156] Embodiment 25 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed under vacuum and / or with heating.

[0157] Embodiment 26 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

[0158] Embodiment 27 is the method of any previous or subsequent embodiment, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

[0159] Embodiment 28 is the method of any previous or subsequent embodiment, wherein the drying step is performed under vacuum and / or with heating.

[0160] Embodiment 29 is the method of any previous or subsequent embodiment, wherein the drying step is performed to achieve a percent humidity of less than 1%.

[0161] Embodiment 30 is the method of any previous or subsequent embodiment, wherein the conical ribbon vacuum drying is performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45 mmHg.

[0162] Embodiment 31 is a method for recovering betaine from molasses, said molasses as a starting material containing between 38 and 40% betaine, between 2.5 and 4% sucrose and between 23.5 and 26% colored impurities, salts and amino acids, wherein the starting material comprises a sugar beet molasses by-product formed in a process for preparation of sucrose; said method comprising the steps of a separation step, in which the molasses from sucrose production is subjected to a chromatographic separation, thereby obtaining a betaine fraction and other dry-matter constituents of the molasses wherein the separation step is accomplished by ion-exchange chromatography in a single step process and a strong acidic cation exchange resin is used in the ion-exchange chromatographic separation; a decolorization step, in which the betaine fraction obtained from the strong acidic cation exchange resin is subjected to decolorization by using ion-exchange chromatography in a single pass through from the column and a strong basic anion exchange resin is used in the ion-exchange decolorization process; a concentration step, in which the decolorized betaine fraction is subjected to a concentration process by using a falling film plate evaporator under vacuum and heating; and a drying step, in which the concentrated decolorized betaine fraction is subjected to a drying process by using conical ribbon vacuum dryer under vacuum and heating.

[0163] Embodiment 32 is the method according to any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is cross-coupled with 6% divinyl benzene moiety.

[0164] Embodiment 33 is the method according to any previous or subsequent embodiment, wherein the strong acidic cation exchange cross-coupled with 6% divinyl benzene moiety resin is in sodium form.

[0165] Embodiment 34 is the method according to any previous or subsequent embodiment, wherein the separation of the betaine fraction is performed at ambient temperature.

[0166] Embodiment 35 is the method according to any previous or subsequent embodiment, wherein the decolorization of betaine fraction is performed at ambient temperature.

[0167] Embodiment 36 is the method according to any previous or subsequent embodiment, wherein the decolorized betaine fraction is concentrated by evaporation to a solids content within the range of about 60 to 85% by weight utilizing the falling film plate evaporator.

[0168] Embodiment 37 is the method according to any previous or subsequent embodiment, wherein the decolorized betaine fraction is subjected to evaporation by using the falling film plate evaporator at 65 °C with the application of vacuum around 50-55 mmHg.

[0169] Embodiment 38 is the method according to any previous or subsequent embodiment, wherein the concentrated decolorized betaine fraction is subjected to the drying process by using the conical ribbon vacuum dryer to achieve a humidity at around 0.8% by weight.

[0170] Embodiment 39 is the method according to any previous or subsequent embodiment, wherein the concentrated decolorized betaine fraction is subjected to the drying process by using the conical ribbon vacuum dryer at 110 °C with the application of vacuum around 35-40 mmHg.

[0171] Embodiment 40 is the method according to any previous or subsequent embodiment, wherein the dried decolorized betaine is obtained as a free-flow powder from the conical ribbon vacuum dryer.

[0172] Embodiment 41 is a purified betaine liquid product, comprising a liquid solution comprising at least 45 wt. % betaine; less than 50 wt. % water; and optionally one or more additional components.

[0173] Embodiment 42 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the one or more additional components comprises a de-icing agent.

[0174] Embodiment 43 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the de-icing agent comprises a glycol.

[0175] Embodiment 44 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the glycol comprises propylene glycol or glycerol.

[0176] Embodiment 45 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the one or more additional components comprises sucrose.

[0177] Embodiment 46 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the sucrose is present in an amount of less than 0.5 wt. % based on the weight of the liquid solution.

[0178] Embodiment 47 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the liquid solution comprises at least 55 wt. % of betaine.

[0179] Embodiment 48 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the liquid solution comprises at least 57 wt. % of betaine.

[0180] Embodiment 49 is the purified betaine liquid product of any previous or subsequent embodiment, wherein the liquid solution comprises at least 60 wt. % of betaine.

[0181] Embodiment 50 is a method for obtaining a betaine liquid product, comprising purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-containing fraction; and concentrating the betaine-containing fraction by performing falling film plate evaporation to obtain a betaine liquid product.

[0182] Embodiment 51 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

[0183] Embodiment 52 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

[0184] Embodiment 53 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

[0185] Embodiment 54 is the method of any previous or subsequent embodiment, wherein the purifying step is accomplished by a single step ion exchange chromatography.

[0186] Embodiment 55 is the method of any previous or subsequent embodiment, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography.

[0187] Embodiment 56 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with a crosslinking agent.

[0188] Embodiment 57 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0189] Embodiment 58 is the method of any previous or subsequent embodiment, wherein the crosslinking agent is divinyl benzene.

[0190] Embodiment 59 is the method of any previous or subsequent embodiment, further comprising a decolorizing step after the purifying step and before the concentrating step.

[0191] Embodiment 60 is the method of any previous or subsequent embodiment, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine- containing fraction.

[0192] Embodiment 61 is the method of any previous or subsequent embodiment, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

[0193] Embodiment 62 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed under vacuum and / or with heating.

[0194] Embodiment 63 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

[0195] Embodiment 64 is the method of any previous or subsequent embodiment, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

[0196] Embodiment 65 is a betaine-poor product, comprising a dry, free flowing particulate mixture comprising 750 mgGAE / 100 g total phenolic content; less than 10 wt. % betaine; less than 10 wt. % water; and optionally one or more additional components.

[0197] Embodiment 66 is the betaine-poor product of any previous or subsequent embodiment, wherein the one or more additional components comprises an anti-caking agent.

[0198] Embodiment 67 is the betaine-poor product of any previous or subsequent embodiment, wherein the anti-caking agent comprises a silicon-containing compound.

[0199] Embodiment 68 is the betaine-poor product of any previous or subsequent embodiment, wherein the silicon-containing compound comprises fume silicate or silicon dioxide.

[0200] Embodiment 69 is the betaine-poor product of any previous or subsequent embodiment, wherein the one or more additional components comprises sucrose.

[0201] Embodiment 70 is the betaine-poor product of any previous or subsequent embodiment, wherein the sucrose is present in an amount of less than 10 wt. % based on the weight of the dry, free flowing particulate mixture.

[0202] Embodiment 71 is the betaine-poor product of any previous or subsequent embodiment, wherein the dry, free flowing particulate mixture comprises less than 9 wt. % of betaine.

[0203] Embodiment 72 is the betaine-poor product of any previous or subsequent embodiment, wherein the dry, free flowing particulate mixture comprises less than 5 wt. % of betaine.

[0204] Embodiment 73 is the betaine-poor product of any previous or subsequent embodiment, wherein the dry, free flowing particulate mixture comprises less than 1 wt. % of betaine.

[0205] Embodiment 74 is the betaine-poor product of any previous or subsequent embodiment, wherein the betaine has an average particle size of 100 nm to 1.5 pm.

[0206] Embodiment 75 is a method for obtaining dry powder betaine-poor extract, comprising:

[0207] purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-poor fraction; concentrating the betaine-poor fraction by performing falling film plate evaporation to form a concentrated betaine-poor fraction; and drying the concentrated betaine-poor fraction by conical ribbon vacuum drying to obtain a dry powder betaine-poor extract.

[0208] Embodiment 76 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

[0209] Embodiment 77 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

[0210] Embodiment 78 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

[0211] Embodiment 79 is the method of any previous or subsequent embodiment, wherein the purifying is accomplished by a single step ion exchange chromatography.

[0212] Embodiment 80 is the method of any previous or subsequent embodiment, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography.

[0213] Embodiment 81 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with a crosslinking agent.

[0214] Embodiment 82 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0215] Embodiment 83 is the method of any previous or subsequent embodiment, wherein the crosslinking agent is divinyl benzene.

[0216] Embodiment 84 is the method of any previous or subsequent embodiment, further comprising a decolorizing step after the purifying step and before the concentrating step.

[0217] Embodiment 85 is the method of any previous or subsequent embodiment, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine- containing fraction.

[0218] Embodiment 86 is the method of any previous or subsequent embodiment, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in thedecolorizing step.

[0219] Embodiment 87 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed under vacuum and / or with heating.

[0220] Embodiment 88 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

[0221] Embodiment 89 is the method of any previous or subsequent embodiment, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

[0222] Embodiment 90 is the method of any previous or subsequent embodiment, wherein the drying step is performed under vacuum and / or with heating.

[0223] Embodiment 91 is the method of any previous or subsequent embodiment, wherein the drying step is performed to achieve a percent humidity of less than 1%.

[0224] Embodiment 92 is the method of any previous or subsequent embodiment, wherein the conical ribbon vacuum drying is performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45 mmHg.

[0225] Embodiment 93 is a polyphenol product, comprising: a dry, free flowing particulate mixture comprising: 6000 mgGAE / lOOg total phenolic content; less than 10 wt. % water; and optionally one or more additional components.

[0226] Embodiment 94 is the polyphenol product of any previous or subsequent embodiment, wherein the one or more additional components comprises an anti-caking agent.

[0227] Embodiment 95 is the polyphenol product of any previous or subsequent embodiment, wherein the anti-caking agent comprises a silicon-containing compound.

[0228] Embodiment 96 is the polyphenol product of any previous or subsequent embodiment, wherein the silicon-containing compound comprises fume silicate or silicon dioxide.

[0229] Embodiment 97 is a method for obtaining dry powder polyphenol extract, comprising: purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-poor fraction; adsorbing the betaine-poor fraction by adsorbent resin column chromatography to obtain a polyphenol fraction; concentrating the polyphenol fraction by performing falling film plate evaporation to form a concentrated polyphenol fraction; and drying the concentrated polyphenol fraction by conical ribbon vacuum drying to obtain a dry powder polyphenol extract.

[0230] Embodiment 98 is the method of any previous or subsequent embodiment, whereinthe sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

[0231] Embodiment 99 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

[0232] Embodiment 100 is the method of any previous or subsequent embodiment, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

[0233] Embodiment 101 is the method of any previous or subsequent embodiment, wherein the purifying is accomplished by a single step ion exchange chromatography and / or the adsorbing step is accomplished by a single step adsorbent resin column chromatography.

[0234] Embodiment 102 is the method of any previous or subsequent embodiment, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography and / or wherein a polymeric, nonionic, macroporous adsorbent resin is used in the adsorbent resin column chromatography.

[0235] Embodiment 103 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin and the polymeric, nonionic, macroporous resin are crosslinked with a crosslinking agent.

[0236] Embodiment 104 is the method of any previous or subsequent embodiment, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

[0237] Embodiment 104 is the method of any previous or subsequent embodiment, wherein the crosslinking agent is divinyl benzene.

[0238] Embodiment 106 is the method of any previous or subsequent embodiment, further comprising a decolorizing step after the purifying step and before the concentrating step.

[0239] Embodiment 107 is the method of any previous or subsequent embodiment, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine- containing fraction.

[0240] Embodiment 108 is the method of any previous or subsequent embodiment, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

[0241] Embodiment 109 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed under vacuum and / or with heating.

[0242] Embodiment 110 is the method of any previous or subsequent embodiment, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

[0243] Embodiment I l l is the method of any previous or subsequent embodiment, whereinthe falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

[0244] Embodiment 112 is the method of any previous or subsequent embodiment, wherein the drying step is performed under vacuum and / or with heating.

[0245] Embodiment 113 is the method of any previous or subsequent embodiment, wherein the drying step is performed to achieve a percent humidity of less than 1%.

[0246] Embodiment 114 is the method of any previous or subsequent embodiment, wherein the conical ribbon vacuum drying is performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45 mmHg.

[0247] The compositions and methods of the appended claims are not limited in scope by the specific compositions and methods described herein, which are intended as illustrations of a few aspects of the claims and any compositions and methods that are functionally equivalent are within the scope of this disclosure. Various modifications of the compositions and methods in addition to those shown and described herein are intended to fall within the scope of the appended claims. Further, while only certain representative compositions, methods, and aspects of these compositions and methods are specifically described, other compounds and methods are intended to fall within the scope of the appended claims. Thus, a combination of steps, elements, components, or constituents can be explicitly mentioned herein; however, all other combinations of steps, elements, components, and constituents are included, even though not explicitly stated.

Claims

WHAT IS CLAIMED IS:

1. A purified betaine product, comprising: a dry, free flowing particulate mixture comprising: at least 70 wt. % betaine; less than 10 wt. % water; and optionally one or more additional components.

2. The purified betaine product of claim 1 , wherein the one or more additional components comprises an anti -caking agent.

3. The purified betaine product of claim 2, wherein the anti-caking agent comprises a stearate salt.

4. The purified betaine product of claim 3, wherein the stearate salt comprises calcium stearate or magnesium stearate.

5. The purified betaine product of claim 2, wherein the anti-caking agent comprises a silicon-containing compound.

6. The purified betaine product of claim 5, wherein the silicon-containing compound comprises fume silicate or silicon dioxide.

7. The purified betaine product of any one of claims 1-6, wherein the one or more additional components comprises sucrose.

8. The purified betaine product of claim 7, wherein the sucrose is present in an amount of less than 0.5 wt. % based on the weight of the dry, free flowing particulate mixture.

9. The purified betaine product of any one of claims 1-8, wherein the dry, free flowing particulate mixture comprises at least 75 wt. % of betaine.

10. The purified betaine product of any one of claims 1-9, wherein the dry, free flowing particulate mixture comprises at least 85 wt. % betaine.

11. The purified betaine product of any one of claims 1-10, wherein the dry, free flowing particulate mixture comprises at least 95 wt. % betaine.

12. The purified betaine product of any one of claims 1-11, wherein the betaine has an average particle size of 100 nm to 1.5 pm.

13. A method for obtaining dry powder betaine, comprising: purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-containing fraction; concentrating the betaine-containing fraction by performing falling film plate evaporation to form a concentrated betaine fraction; and drying the concentrated betaine fraction by conical ribbon vacuum drying to obtain a dry powder betaine.

14. The method of claim 13, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

15. The method of claim 13 or 14, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

16. The method of any one of claims 13-15, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

17. The method of any one of claims 13-16, wherein the purifying step is accomplished by a single step ion exchange chromatography.

18. The method of any one of claims 13-17, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography.

19. The method of claim 18, wherein the strong acidic cation exchange resin is crosslinked with a crosslinking agent.

20. The method of claim 19, wherein the strong acidic cation exchange resin is crosslinkedwith the crosslinking agent at a degree of 1 to 20 %.

21. The method of claim 19 or 20, wherein the crosslinking agent is divinyl benzene.

22. The method of any one of claims 13-21, further comprising a decolorizing step after the purifying step and before the concentrating step.

23. The method of claim 22, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine-containing fraction.

24. The method of claim 23, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

25. The method of any one of claims 13-24, wherein the concentrating step is performed under vacuum and / or with heating.

26. The method of any one of claims 13-25, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

27. The method of any one of claims 13-26, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

28. The method of any one of claims 13-27, wherein the drying step is performed under vacuum and / or with heating.

29. The method of any one of claims 13-28, wherein the drying step is performed to achieve a percent humidity of less than 1%.

30. The method of any one of claims 13-29, wherein the conical ribbon vacuum drying is performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45 mmHg.

31. A purified betaine liquid product, comprising a liquid solution comprising:at least 45 wt. % betaine; less than 50 wt. % water; and optionally one or more additional components.32 The purified betaine liquid product of claim 31, wherein the one or more additional components comprises a de-icing agent.

33. The purified betaine liquid product of claim 32, wherein the de-icing agent comprises a glycol.

34. The purified betaine liquid product of claim 33, wherein the glycol comprises propylene glycol or glycerol.

35. The purified betaine liquid product of any one of claims 31-34, wherein the one or more additional components comprises sucrose.

36. The purified betaine liquid product of claim 35, wherein the sucrose is present in an amount of less than 0.5 wt. % based on the weight of the liquid solution.

37. The purified betaine liquid product of any one of claims 31-36, wherein the liquid solution comprises at least 55 wt. % of betaine.

38. The purified betaine liquid product of any one of claims 31-37, wherein the liquid solution comprises at least 57 wt. % of betaine.

39. The purified betaine liquid product of any one of claims 31-38, wherein the liquid solution comprises at least 60 wt. % of betaine.

40. A method for obtaining a betaine liquid product, comprising: purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-containing fraction; and concentrating the betaine-containing fraction by performing falling film plate evaporation to obtain a betaine liquid product.

41. The method of claim 40, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

42. The method of claim 40 or 41, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

43. The method of any one of claims 40-42, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

44. The method of any one of claims 40-43, wherein the purifying step is accomplished by a single step ion exchange chromatography.

45. The method of any one of claims 40-44, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography.

46. The method of claim 45, wherein the strong acidic cation exchange resin is crosslinked with a crosslinking agent.

47. The method of claim 46, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

48. The method of claim 46 or 47, wherein the crosslinking agent is divinyl benzene.

49. The method of any one of claims 40-48, further comprising a decolorizing step after the purifying step and before the concentrating step.

50. The method of claim 49, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine-containing fraction.

51. The method of claim 50, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

52. The method of any one of claims 40-51, wherein the concentrating step is performedunder vacuum and / or with heating.

53. The method of any one of claims 40-52, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

54. The method of any one of claims 40-53, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

55. A betaine-poor product, comprising: a dry, free flowing particulate mixture comprising:750 mgGAE / 100 g total phenolic content; less than 10 wt. % betaine; less than 10 wt. % water; and optionally one or more additional components.

56. The betaine-poor product of claim 55, wherein the one or more additional components comprises an anti -caking agent.

57. The betaine-poor product of claim 56, wherein the anti-caking agent comprises a silicon-containing compound.

58. The betaine-poor product of claim 57, wherein the silicon-containing compound comprises fume silicate or silicon dioxide.

59. The betaine-poor product of any one of claims 55-58, wherein the one or more additional components comprises sucrose.

60. The betaine-poor product of claim 59, wherein the sucrose is present in an amount of less than 10 wt. % based on the weight of the dry, free flowing particulate mixture.

61. The betaine-poor product of any one of claims 55-60, wherein the dry, free flowing particulate mixture comprises less than 9 wt. % of betaine.

62. The betaine-poor product of any one of claims 55-61, wherein the dry, free flowing particulate mixture comprises less than 5 wt. % of betaine.

63. The betaine-poor product of any one of claims 55-62, wherein the dry, free flowing particulate mixture comprises less than 1 wt. % of betaine.

64. The betaine-poor product of any one of claims 55-63, wherein the betaine has an average particle size of 100 nm to 1.5 pm.

65. A method for obtaining dry powder betaine-poor extract, comprising: purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-poor fraction; concentrating the betaine-poor fraction by performing falling film plate evaporation to form a concentrated betaine-poor fraction; and drying the concentrated betaine-poor fraction by conical ribbon vacuum drying to obtain a dry powder betaine-poor extract.

66. The method of claim 65, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

67. The method of claim 65 or 66, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

68. The method of any one of claims 65-67, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

69. The method of any one of claims 65-68, wherein the purifying is accomplished by a single step ion exchange chromatography.

70. The method of any one of claims 65-69, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography.

71. The method of claim 70, wherein the strong acidic cation exchange resin is crosslinkedwith a crosslinking agent.

72. The method of claim 71, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

73. The method of claim 71 or 72, wherein the crosslinking agent is divinyl benzene.

74. The method of any one of claims 71-73, further comprising a decolorizing step after the purifying step and before the concentrating step.

75. The method of claim 74, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine-containing fraction.

76. The method of claim 75, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

77. The method of any one of claims 65-76, wherein the concentrating step is performed under vacuum and / or with heating.

78. The method of any one of claims 65-77, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

79. The method of any one of claims 65-78, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

80. The method of any one of claims 65-79, wherein the drying step is performed under vacuum and / or with heating.

81. The method of any one of claims 65-80, wherein the drying step is performed to achieve a percent humidity of less than 1%.

82. The method of any one of claims 65-81, wherein the conical ribbon vacuum drying is performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45mmHg.

83. A polyphenol product, comprising: a dry, free flowing particulate mixture comprising:6000 mgGAE / lOOg total phenolic content; less than 10 wt. % water; and optionally one or more additional components.

84. The polyphenol product of claim 83, wherein the one or more additional components comprises an anti -caking agent.

85. The polyphenol product of claim 84, wherein the anti -caking agent comprises a silicon- containing compound.

86. The polyphenol product of claim 85, wherein the silicon-containing compound comprises fume silicate or silicon dioxide.

87. A method for obtaining dry powder polyphenol extract, comprising: purifying sugar beet molasses by ion exchange chromatography to obtain one or more separated fractions, wherein the one or more separated fractions comprises a betaine-poor fraction; adsorbing the betaine-poor fraction by adsorbent resin column chromatography to obtain a polyphenol fraction; concentrating the polyphenol fraction by performing falling film plate evaporation to form a concentrated polyphenol fraction; and drying the concentrated polyphenol fraction by conical ribbon vacuum drying to obtain a dry powder polyphenol extract.

88. The method of claim 87, wherein the sugar beet molasses in the purifying step contains from 25-50 wt. % betaine.

89. The method of claim 87 or 88, wherein the sugar beet molasses in the purifying step contains 1-6 wt. % sucrose.

90. The method of any one of claims 87-89, wherein the sugar beet molasses in the purifying step contains 10-30 % colored impurities, salts, and / or amino acids.

91. The method of any one of claims 87-90, wherein the purifying is accomplished by a single step ion exchange chromatography and / or the adsorbing step is accomplished by a single step adsorbent resin column chromatography.

92. The method of any one of claims 87-91, wherein a strong acidic cation exchange resin is used in the ion exchange chromatography and / or wherein a polymeric, nonionic, macroporous adsorbent resin is used in the adsorbent resin column chromatography.

93. The method of claim 92, wherein the strong acidic cation exchange resin and the polymeric, nonionic, macroporous resin are crosslinked with a crosslinking agent.

94. The method of claim 93, wherein the strong acidic cation exchange resin is crosslinked with the crosslinking agent at a degree of 1 to 20 %.

95. The method of claim 93 or 94, wherein the crosslinking agent is divinyl benzene.

96. The method of any one of claims 87-95, further comprising a decolorizing step after the purifying step and before the concentrating step.

97. The method of claim 96, wherein the decolorizing step comprises performing ion exchange chromatography on the betaine-containing fraction.

98. The method of claim 97, wherein a strong basic anion exchange resin is used in the ion exchange chromatography in the decolorizing step.

99. The method of any one of claims 87-98, wherein the concentrating step is performed under vacuum and / or with heating.

100. The method of any one of claims 87-99, wherein the concentrating step is performed to obtain a solids content of 60 % to 85 % by weight.

101. The method of any one of claims 87-100, wherein the falling film plate evaporation in the concentrating step is performed at a temperature of 50 °C or greater and at a vacuum pressure of 40 mmHg to 60 mmHg.

102. The method of any one of claims 87-101, wherein the drying step is performed under vacuum and / or with heating.

103. The method of any one of claims 87-102, wherein the drying step is performed to achieve a percent humidity of less than 1%.

104. The method of any one of claims 87-103, wherein the conical ribbon vacuum drying is performed at a temperature of 90 °C to 125 °C and at a vacuum pressure of 30 mmHg to 45 mmHg.

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