Natural crystalline colorants and methods of manufacture

Abstract

To provide a more concentrated natural coloring agent that can be added to various kinds of food, medicine and cosmetic product, and a method for producing the agent.SOLUTION: Provided is a unique dried coloring agent obtained from a natural source that is a plant such as fruit and vegetable and algae for example. In some embodiments, the coloring agent is obtained from squeezed juice or squeezed juice concentrate and / or extract of fruit and / or vegetable. In further embodiments, the coloring agent is obtained from red grape squeezed juice and / or purple carrot squeezed juice. A method for producing the dried coloring agent includes: a process of purifying coloring pigment by using various purifying techniques; and subsequently, a process of removing water by using a low-temperature drying method. The novel combination of the purifying technique and the low-temperature drying produces unique natural coloring agent having high color intensity and / or low sugar.SELECTED DRAWING: None

Description

[Technical Field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This application claims the benefit of and priority to U.S. Provisional Patent Application No. 61 / 503,557, filed June 30, 2011, entitled "Natural Crystalline Colorant and Method of Making," the contents of which are incorporated herein by reference.

[0002] The present disclosure relates generally to purified natural color pigments and colorants and methods for making and processing the pigments and colorants. [Background technology]

[0003] Natural pigments and dyes are primarily derived from pigments found in plants, such as fruits, flowers, and vegetables. Based on their chemical composition, natural plant-source pigments can be classified into structural groups, including, but not limited to, anthocyanins, betalains, carotenoids, curcumin, carminic acid and derivatives, chlorophyll and its derivatives, etc. Carotenoids include, but are not limited to, β-carotene, α-carotene, apocartinal, lycopene, bixin, norbixin, canthaxanthin, and zeaxanthin. Derivatives of chlorophyll and chlorophyllin include, but are not limited to, copper complexes. In another non-limiting embodiment, the pigment may be complexed with a metal ion, such as, but not limited to, a copper ion.

[0004] One goal of the manufacturing industry is to concentrate the pigmented parts of plants to provide more concentrated natural colorants that can be added to various food, pharmaceutical, and cosmetic products. These concentrated colorants are produced by removing other compounds through a separation process.

[0005] Natural colorants are often recovered from the juices of fruits and vegetables, which have high sugar content relative to the pigmented compound composition. These sugar-based colors are typically concentrated by removing water and used as concentrates with greater than 60 percent sugar on a dry weight basis and low pigment levels. It will be understood by those skilled in the art that the concentrate may have a higher or lower percentage of sugars on a dry weight basis depending on the fruit or vegetable. Low color content liquids can be costly to store (often requiring refrigeration), can be prone to spoilage over time, have a high calorie content relative to their color contribution in food or beverage applications due to their high sugar content, and / or can add undesirable organoleptic properties.

[0006] The industry has offered these natural colorants from fruit and vegetable juices in two different forms: liquid and powder. Sugar-based pigments are often difficult to dry and typically require a carrier such as maltodextrin or microcrystalline cellulose to offset the hygroscopic nature of the sugar.

[0007] Furthermore, the liquids subjected to drying typically have a moisture content of about 50% to 80% by weight, and few techniques are available to efficiently dry such products. The most common technique available for drying liquids with low levels of soluble solids is spray drying.

[0008] Unfortunately, spray drying has several drawbacks in terms of handling the dried product. Typical problems include, but are not limited to, significant deterioration of product quality due to the high temperatures and pressures to which the liquid is exposed during drying, the formation of amorphous particles with low bulk density due to rapid drying rates in fine droplets, and poor water solubility or wetting properties and moisture absorption tendency due to the presence of sugars in an amorphous rather than crystalline state, resulting in a tendency for the powder to clump or cake. Furthermore, successful spray drying of fruit or vegetable concentrates with high sugar content typically requires the presence of a carrier, which reduces the pigment concentration and incorporation efficiency of the final product.

[0009] Another goal of the manufacturing industry is to significantly reduce the sugar content of standard fruit and vegetable-based color concentrates to produce higher-concentration natural color concentrates with lower caloric density, which can be further dried to produce products with improved storage and handling characteristics. Refined color concentrates are typically produced by removing non-pigment components from fruit and vegetable juices and extracts, thereby significantly increasing the concentration of color compounds in the material. Because refined color concentrates contain low levels of sugar, they can be dried using a wide variety of drying methods, including spray dryers, drum dryers, refractive window dryers, and freeze dryers. The method of the present invention combines purification and drying techniques to provide a technology for producing high-concentration natural color concentrates that can be dried without a carrier. The high-concentration natural color concentrates described herein have higher color intensity and / or improved sensory, stability, and handling properties compared to other dried color concentrates known in the art.

[0010] The above-described examples of the related art and limitations thereto are illustrative and not exhaustive. Other limitations of the related art will become apparent to those skilled in the art upon reading this specification and studying the drawings. Summary of the Invention [Means for solving the problem]

[0011] The following aspects and embodiments thereof described and illustrated below are intended to be exemplary and illustrative, not limiting in scope.

[0012] The present disclosure relates to unique dried colorants derived from natural sources, such as plants, including fruits and vegetables and algae. In some embodiments, the colorants are derived from fruit and / or vegetable juices or juice concentrates and / or extracts. In further embodiments, the colorant is obtained from red grape juice and / or purple carrot juice. Briefly, the method for producing the dried colorant involves purifying color pigments using various refining techniques, followed by removing water using low-temperature drying methods. This novel combination of refining techniques and low-temperature drying produces unique natural colorants with high color strength and / or low sugar content. In some embodiments, the colorants described herein exhibit excellent storage stability and / or handling properties, such as, but not limited to, density, flowability, water dispersibility, and / or hygroscopicity.

[0013] In one aspect, a natural colorant composition is contemplated, comprising a crystalline pigment or mixture of pigments derived from plants and / or algae. In one embodiment, the composition has a color strength greater than that of the crude juice or unrefined pigment or composition. In a further embodiment, the composition of the above aspect and / or embodiment has reduced sugars on a dry weight basis compared to the crude juice or unrefined pigment composition. In another embodiment, the composition of the above aspect and / or embodiment contains less than about 5-20% sugars on a dry weight basis. In a further embodiment, the composition of the above aspect and / or embodiment has a total sugar content of less than about 20% by dry weight. In yet another embodiment, the composition of the above aspect and / or embodiment has a color strength greater than about 40,000 color units. In another embodiment, the pigment of the above aspect and / or embodiment is red grape anthocyanin, and the composition has a color strength of about 40,000-55,000 color units. In further embodiments, the pigment of any of the above aspects and / or embodiments is purple carrot anthocyanin and the composition has a color strength of about 90,000 to 125,000 chromaticity.In additional embodiments, the pigment of any of the above aspects and / or embodiments is selected from the group consisting of anthocyanins, carotenoids, betalains, curcumin, carminic acid, carminic acid derivatives, chlorophyll, and chlorophyll derivatives.

[0014] Another aspect contemplates a method for producing a purified crystalline natural pigment. The method includes (a) purifying a juice or extract containing the pigment by removing at least a portion of non-pigment compounds to produce a purified pigment, and (b) drying the purified pigment. In one embodiment, the purified pigment is crystalline and has increased color intensity and / or reduced sugar content on a dry weight basis compared to the crude juice. In another embodiment, the pigment of the above aspect and / or embodiment is selected from the group consisting of anthocyanins, carotenoids, betalains, curcumin, carminic acid, carminic acid derivatives, chlorophyll, and / or chlorophyll derivatives. In a further embodiment, the purification step in the method of the above aspect and / or embodiment includes ultrafiltration and diafiltration through a polymeric membrane device. In yet another embodiment, the polymeric membrane device of the above aspect and / or embodiment includes a polyethersulfone (PES) spiral ultrafiltration membrane. In a further embodiment, the PES spiral ultrafiltration membrane of the above aspect and / or embodiment has a nominal molecular weight cut-off of about 5000 Daltons. In yet another embodiment, the purification process of the above aspect and / or embodiment comprises circulating the juice or extract through a membrane device, the process comprising: (a) filtering the juice or extract through the membrane device; (b) recovering the retentate; (c) reconstituting the retentate; and (d) repeating steps (a) through (b) until the retentate reaches a desired color intensity on a dry weight basis. In an additional embodiment, the purification process of the above aspect and / or embodiment comprises adsorption / desorption chromatography. In another embodiment, the purification process of the above aspect and / or embodiment comprises a fermentation process. In a further embodiment, the purification process of the above aspect and / or embodiment comprises a subcritical or supercritical fluid extraction method. In yet another embodiment, the drying process of the above aspect and / or embodiment is accomplished with a refractive window dryer. In a further embodiment, the drying step of the above aspects and / or embodiments comprises freeze-drying. In another embodiment, the method of the above aspects and / or embodiments further comprises the step of grinding the dried product.

[0015] In a further embodiment, a composition formed by the method of any of the above aspects or embodiments, alone or in any combination, is contemplated.

[0016] Additional embodiments of the methods, combinations, and the like of the present invention will be apparent from the following description, drawings, examples, and claims. As can be understood from the above and below description, every feature described herein, and every combination of two or more such features, is encompassed within the scope of the present disclosure, unless the features included in such combinations are mutually inconsistent. Furthermore, any feature or combination of features may be specifically excluded from any embodiment of the present invention. Additional aspects and advantages of the present invention are described in the following specification and claims, particularly when considered in conjunction with the accompanying examples and drawings. [Brief explanation of the drawings]

[0017] [Figure 1] 1 is a flow diagram illustrating an exemplary method for purifying and drying natural fruit and vegetable based pigments, according to one embodiment. [Figure 2] 1 is a flow diagram illustrating an exemplary method for purifying a colorant using ultrafiltration and diafiltration, according to one embodiment. [Figure 3] 1 is a flow diagram illustrating an exemplary method for concentrating, drying, and grinding a purified dye liquid, according to one embodiment. [Figure 4A] FIG. 1 is a side view of a refractive window dryer according to one embodiment. [Figure 4B] FIG. 1 is a cross-sectional view of a refractive window dryer according to one embodiment. [Figure 5] 1 is a flow diagram illustrating an exemplary method for purifying a dye using an adsorption resin separation technique, according to one embodiment. [Figure 6] 1 is a flow diagram illustrating an exemplary method for purifying a pigment using fermentation techniques, according to one embodiment. [Figure 7]1 is a flow diagram illustrating an exemplary method for purifying a dye using solvent extraction techniques, according to one embodiment. [Figure 8] 1 is a flow diagram illustrating an exemplary method for drying a purified dye using freeze-drying techniques, according to one embodiment. [Figure 9A] A microscope image of the refractive window dried purified grape pigment at 5x magnification. [Figure 9B] 1 is a microscopic image of freeze-dried purified grape pigment at 5x magnification. [Figure 9C] 1 is a microscope image of spray-dried purified grape pigment at 5x magnification. [Figure 9D] 1 is a microscopic image of drum-dried purified grape pigment at 5x magnification. [Figure 10A] 9B is a microscopic image of FIG. 9A at 20x magnification. [Figure 10B] FIG. 9B is a microscopic image of FIG. 9B at 20× magnification. [Figure 10C] FIG. 9C is a microscopic image at 20× magnification. [Figure 10D] FIG. 9D is a microscopic image at 20x magnification. DETAILED DESCRIPTION OF THE INVENTION

[0018] Various aspects will now be described in more detail below. However, because such aspects may be embodied in various forms, they should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey its scope to those skilled in the art.

[0019] It will be understood that for simplicity and clarity of illustration, where considered appropriate, reference numerals may be repeated among the figures to indicate corresponding or analogous elements. Furthermore, numerous specific details are set forth in order to provide a thorough understanding of the implementation of the examples described herein. However, it will be understood by those skilled in the art that the implementation of the examples described herein may be practiced without these specific details.

[0020] As used herein, the terms "colorant" and "pigment" refer to any substance used to change the color of an object by altering its spectral transmittance or its spectral reflectance. As used herein, "colorants" and "pigments" generally refer to colorants and pigments obtained from natural sources, such as, but not limited to, plants and algae. "Colorants" and "pigments" are used interchangeably herein.

[0021] As used herein, "concentrate" refers to a juice or extract from which at least a portion of the water has been removed.

[0022] As used herein, "juice" refers to a liquid obtained from a fruit, vegetable, or other plant. Juice may also refer to a liquid obtained from algae. As used herein, "juice" includes concentrates and extracts. As used herein, "crude juice" refers to juice that has not yet been refined.

[0023] "Increased color intensity" refers to an increase in color intensity compared to the color intensity of the crude juice and / or unrefined pigment composition.

[0024] "Reduced sugar content" refers to a reduction in sugar content on a dry weight basis compared to the crude juice and / or crude pigment.

[0025] Concentrations, amounts, pH values, and the like are often presented herein in range format. The range format is merely for convenience and brevity and should not be construed as an inflexible limitation on the scope of the invention. Accordingly, the description of a range should be construed as specifically disclosing all possible subranges within that range, as well as each individual numerical value. For example, the description of a range such as 10-15% should be construed as specifically disclosing subranges such as 10-11%, 10-12%, 10-13%, 10-14%, 11-12%, 11-13%, etc. Colorant manufacturing method

[0026] In one aspect, a method for producing a colorant is described. It will be understood that the method of the present invention can be used to produce either a pigment or a colorant, and these two terms are used interchangeably herein. Briefly, the method of the present invention includes (i) optional reconstitution and pasteurization of a juice concentrate or extract, (ii) purification of the juice concentrate or extract, for example, by ultrafiltration and diafiltration, (iii) concentration of the purified juice concentrate or extract, for example, by falling film evaporation, (iv) drying, and (v) grinding. While traditional dry colorants in the food industry are spray-dried powders, the dry colorants of the present invention use low-temperature drying methods, such as refractive window drying technology or freeze-drying, to produce crystalline solid color additives that are 100% natural, high in antioxidants, highly concentrated in color, and / or completely soluble in water.

[0027] FIG. 1 illustrates a typical manufacturing process for producing the unique crystalline product described above. Fruit and / or vegetable juice and / or extract 100 is typically, but not always, reconstituted (diluted with water) prior to purification. In one non-limiting embodiment, a concentrate at about 68°Brix is ​​reconstituted to about 18-22°Brix. In one embodiment, the concentrate is reconstituted with about 3 parts water to 1 part concentrate. Once reconstituted, the juice may be more susceptible to fermentation by any yeast that may be present in the starting material. Because the juice is maintained at a low solids level throughout all subsequent liquid processing steps, the juice may optionally be immediately pasteurized to enhance microbial stability from the beginning of the manufacturing process. The juice or extract can be pasteurized according to methods known in the art. According to one non-limiting embodiment, the juice or extract is pasteurized by heating to about 185°F (85°C) for about 30 seconds and then immediately cooling to about 55°F (12.8°C). The juice or extract is typically, but not always, pasteurized into a jacketed vessel, which serves as a feed vessel for subsequent membrane filtration. All vessels used in the manufacturing process can be jacketed and / or temperature controlled, using, for example, food-grade propylene glycol as a refrigerant.

[0028] The juice / extract is then purified (step 200). By increasing the pigment concentration relative to the sugars and organic acids, the pigment-enriched liquid can be efficiently converted, under appropriate drying conditions, into a crystalline form with superior properties, such as excellent handling.

[0029] The juice / extract can be purified by any suitable method known in the art. In one preferred embodiment, purification step 200 is accomplished using ultrafiltration and diafiltration through a polymeric membrane. Ultrafiltration (and subsequent repetition with diafiltration) produces a retentate that is concentrated in pigments, such as anthocyanin or carotenoid pigments, while simultaneously containing reduced amounts of sugars and acids that more readily permeate the membrane. Removal of sugars increases pigment concentration or color intensity on a dry weight basis and produces a product with superior storage and handling characteristics compared to other colorants known in the industry. Other methods for purifying pigments include, but are not limited to, column chromatography using adsorbent resins, fermentation, and extraction, including, but not limited to, subcritical fluid extraction, supercritical fluid extraction, and / or solvent extraction.

[0030] In the case of pigment purification using membrane separation, the purified pigment, low in sugars and organic acids, is concentrated by removing water using evaporation (step 300). Depending on the membrane separation process, it may be possible to immediately dry the purified product without concentrating it. Once a liquid of the appropriate composition and solids content is prepared, the liquid is dried under appropriate conditions effective to produce a product with the morphology and properties described above (step 400). These conditions allow for a water removal rate suitable to achieve crystallization of the solids while avoiding significant thermal damage to the pigment compounds.

[0031] FIG. 2 illustrates a typical process for purifying color pigments using ultrafiltration and diafiltration to remove natural sugars and other low molecular weight dissolved solids, such as organic acids, from the retentate, according to one embodiment. In this embodiment, the feedstock 100 to the membrane device is preferably a fruit or vegetable juice / extract, less than about 40°Brix, preferably about 12-22°Brix. In one embodiment, the membrane device 203 includes a polymeric membrane known in the art. In one embodiment, the membrane device 203 used is constructed from polyethersulfone (PES) with a molecular weight cutoff in the range of about 5,000-10,000 Daltons, such as those manufactured by Koch Membrane Systems or Hydranautics. This type of membrane provides suitable rejection characteristics to produce a permeate stream 205 containing concentrated sugars and acids, and a retentate stream 204 containing pigment compounds, such as anthocyanins and polyphenols, further enriched relative to the sugar and acid concentrations. In another exemplary embodiment, a PES spiral ultrafiltration membrane device with a nominal molecular weight cutoff of approximately 5,000 daltons is used. Ultrafiltration 202 can be carried out over any operating temperature and pressure range specified by the membrane manufacturer that avoids damage to the membrane and provides sufficient crossflow. However, in this embodiment, maintaining the temperature below approximately 70°F (21.1°C), or more preferably below approximately 40°F (4.4°C), maintains product quality by slowing the rate of pigment color degradation. The retentate 204 from membrane device 203 is returned to feed tank 201 and recirculated through ultrafiltration membrane 202 until a critical viscosity and flux is reached, typically a retentate solids concentration of approximately 20-25% by weight. Further purification can be continued by adding water to retentate 206 and circulating it through membrane 203 to concentrate it again to a critical solids concentration. The diafiltration 206 series is repeated until the desired pigment purity is achieved in the retentate. According to one embodiment, the retentate has a pigment concentration of greater than about 45,000 color degrees on a dry weight basis compared to a base extract / juice of about 3,000 color degrees on a dry weight basis.

[0032] The diafiltration process can be modified by adding water 206 at a rate approximately equal to the rate of permeate 205 exiting the membrane device, thereby performing continuous diafiltration until the desired retentate composition is achieved.

[0033] After each concentration run, a sample of the retentate can be analyzed for residual sugars and color strength (color strength is expressed as liquids divided by solids weight percent) on a dry weight basis. If the retentate reaches a color strength that produces a product within the desired specifications on a dry basis, the product is concentrated product 300. Due to natural variations in the composition of the feedstock to this process, the amount of diafiltration required can vary, typically about 2-4 diafiltration volumes.

[0034] As a non-limiting example of a batch size, a 5,000-gallon (18.9 kiloliter) feedstock tank of reconstituted, pasteurized juice at approximately 18-20°Brix is ​​circulated through a membrane device, with the retentate recycled to the feedstock tank until the tank reaches a solids level of approximately 30°Brix, at which point further concentration is typically prevented by reduced flux. This results in a reduction in the volume of the feedstock liquid by approximately four-fold, leaving a retentate of approximately 1,500 gallons (5.7 kiloliters). Because this initial concentration may not increase the ratio of pigments, e.g., anthocyanin pigment molecules, to sugars sufficiently to achieve the target color intensity, the retentate can undergo several rounds of diafiltration to reach a sufficient dissolved solids composition. According to one embodiment, for each diafiltration, the retentate is reconstituted with water in a 1:1 volumetric ratio of water to concentrate, and approximately 3,000 gallons (11.4 kiloliters) of reconstituted material is circulated through the membrane device and concentrated back to the original retentate volume of approximately 1,500 gallons.

[0035] In a non-limiting embodiment, throughout the ultrafiltration and diafiltration steps, the permeate can be pumped through a small surge tank attached to the membrane skid to a 20,000 gallon (75.7 kiloliter) permeate accumulation tank in the plant basement where it is concentrated and used in the concentrate blend.

[0036] Once the desired color strength on a dry weight basis is achieved by adjusting the pigment to sugar ratio, membrane processing is terminated and the retentate liquid can be further concentrated in solids without adjusting the solids composition.

[0037] Pigment purification can also be carried out using adsorption resin separation techniques. In this embodiment, as shown in FIG. 5, a water-based fruit or vegetable juice / extract 100 (feedstock liquid 501) is passed through a packed bed of adsorbent resin 502. Pigment compounds are preferentially adsorbed onto the resin relative to other dissolved solids, such as sugars and acids 503. The adsorbed pigment is then recovered from the resin using an ethanol / water eluent 508 of varying composition. The purified, pigment-rich eluate 504 is distilled 505 to recover ethanol 507. The alcohol-free, high-purity pigment 506 is concentrated according to the process shown in FIG. 3.

[0038] In another embodiment, pigment purification can be achieved using fermentation to convert free sugars to alcohol, followed by recovery of the alcohol using conventional distillation methods. In this embodiment, shown in FIG. 6, fruit / vegetable sugars from fruit / vegetable juice / extract 100 (feedstock liquid 601) are fermented to alcohol using active yeast 603 in a suitable fermenter 602 at a suitable temperature (approximately 50°F (10°C) to 100°F (37.8°C)). It will be understood that other temperature ranges may be suitable for fermentation, as known to those skilled in the art. The fermentation by-product 604, consisting of approximately 8 to 25 percent alcohol, is distilled 605 to recover ethanol 607, leaving behind purified color pigment 606. The alcohol-free liquid is then concentrated by removing water according to the method shown generally in FIG. 3.

[0039] In yet another embodiment, pigment purification is carried out using supercritical fluid or solvent-solvent extraction techniques. In this embodiment, shown in FIG. 7, a water-based fruit / vegetable juice / extract 100 (feedstock liquid 701) is contacted with a non-polar, water-immiscible extraction liquid (e.g., hexane), i.e., solvent 702, that preferentially absorbs pigment compounds. This absorption process is repeated to produce a pigment-enriched extract fraction 705 and a carbohydrate and / or other non-pigment-enriched fraction 704. A batch or continuous extraction tank 703 can be used to recover and concentrate the pigments. The extraction solvent 705 is then distilled (706) to recover the solvent 708 for reuse and produce a solvent-free, pigment-enriched water-based liquid 707, which is subsequently concentrated by removing water according to the method shown schematically in FIG. 3.

[0040] Figure 3 shows an exemplary process for concentrating (300) and drying (400) a purified dye liquid using a refractive window dryer in an exemplary embodiment. The dried crystalline material is then milled (500) to produce a powder form having a range of particle sizes. The purified liquid can be produced using membrane filtration techniques, such as ultrafiltration / diafiltration, adsorption resins, fermentation, solvent extraction, and / or supercritical fluid extraction. Depending on the solids content in the purified liquid, it may be necessary to concentrate the solids to 20-35% by weight prior to drying.

[0041] Concentration of the purified liquid dye (300) may be carried out in one embodiment by feeding the final retentate from the previous step to a falling film evaporator. Other types of evaporators, such as forced circulation evaporators or plate evaporators, can also be used.

[0042] In one non-limiting embodiment, the retentate is concentrated in a falling film evaporator prior to drying. One typical falling film evaporator is a small (single-effect) falling film evaporator. In one embodiment using a falling film evaporator, the retentate having a final solids content of about 15-20% by weight and about 25-30° Brix is ​​circulated through the evaporator until the feed tank solids concentration reaches about 25-30% by weight solids or about 40-45° Brix. This concentration, according to one embodiment, results in a volume reduction of approximately 45% and takes approximately 12 hours. The resulting liquid is now ready as feedstock material for drying, for example, in a refractive window dryer. The liquid can also be further pasteurized and packaged in transportable metal cans so that it can be stored without damage and shipped in small quantities as needed.

[0043] Because the final concentrated liquor fed to the dryer may not yet have reached the solids concentration required for long-term shelf stability of the concentrate (which may require concentrations up to above 68°Brix), and because some drying embodiments may feed the liquor to the dryer at a rate of about 9-12 gallons (34.1-45.4 liters) per hour, an optional pasteurization step may be required at the end of the liquor processing. This pasteurization step can kill any yeast that may have been introduced during the processing before the liquor is stored and / or gradually fed to the dryer. Any pasteurization method known in the art can be used. A typical method of pasteurization involves heating the liquor to about 185°F (85°C) for about 30 seconds, cooling the liquor to about 55°F (12.8°C), and placing it in a surge tank. From this surge tank, the liquid can be quickly pumped to a barrel filler, where it is poured without air exposure into bags lining the inside of a barrel (e.g., a 54-gallon (204 liter) drum). According to one embodiment, barrels of finished liquid feedstock are stored at approximately 40-50° F. (4.4-10° C.). The barrels can be transported in groups (up to four per pallet) to a dryer, where they are gradually consumed one at a time.

[0044] Purification of natural pigments ensures that the final dried product exhibits excellent long-term storage stability and handling properties, such as density, flowability, water dispersibility, and hygroscopicity. The purified pigment extract has improved drying properties and can therefore be dried using a variety of standard drying techniques, such as spray drying, drum drying, belt drying, and atmospheric / vacuum tray drying. These techniques can subject the pigment to excessively high temperatures or residence times, resulting in color degradation and / or adverse sensory effects. These drying techniques can also result in various crystalline morphologies and associated differences in the quality or handling characteristics of the material. To produce crystalline products with excellent quality, handling, and / or solubility properties, the pigment concentrate must be dried slowly, as in the case of refractive drying and freeze-drying, to allow for the formation of large crystal lattices, including possible crystallization of residual sugars. In one embodiment, the method of the present invention uses a refractive window dryer, which significantly reduces the temperature requirements and high-temperature exposure time for effective drying. In contrast, spray drying and drum drying operate at higher temperatures and dry for very short periods of time, leaving the components in an amorphous state. Freeze drying can also be used to form large crystal lattices, provided the raw material is purified before drying.

[0045] After concentration, the liquid is dried to produce a crystalline solid pigment. In one embodiment, as shown in FIG. 3, the liquid can then be passed through a refractive window dryer 400 to remove most of the residual water and produce a crystalline solid with less than about 8% moisture. The dryer 400 includes a long tunnel, typically constructed from stainless steel. The liquid product passes through the tunnel as a thin layer spread across the upper surface of a thin plastic conveyor belt 403. In this drying method, in one embodiment, hot water circulates in a shallow heating tray below the conveyor belt, heating the liquid layer. Heat energy from the hot water is transferred through the conveyor belt by conduction and radiation. In one embodiment, the hot water is at a temperature of up to about 210° F. (98.9° C.). It will be understood that the hot water can be at any temperature suitable for heating the liquid layer to the desired temperature. A fan continuously blows water vapor away from the surface of the thin layer to maximize the rate of water evaporation. The combination of evaporative cooling and the limited heat transfer of the plastic belt prevents the thin liquid layer from reaching the temperature of the hot water in the heating tray, which would otherwise adversely affect product quality. The product exits the tunnel as a layer of dried, solid product, which can be cut off by a sharp plastic blade placed against the belt at the end of the dryer. Contact with the blade cuts the layer of dried product into thin, crystalline pieces of various sizes.

[0046] The solid product exits the dryer in a form that can be described as sheets, flakes, or granules of various particle sizes. These particles can then be milled through a sieve mill 500 or other suitable particle size reduction device, such as an impact mill, to produce particles of a desired size range. The desired particle size range can be determined by the specific industrial application. In embodiments where the pigment is produced as a food colorant, the desired particle size comprises at least about 90% of all particle sizes between about 50 and 425 μm for purposes of optimizing handling characteristics and standardizing bulk density. In other embodiments, about 90% of the total particle size is smaller than about 100-200 μm, smaller than about 100-250 μm, smaller than about 100-300 μm, smaller than about 100-400 μm, smaller than about 200-250 μm, smaller than about 200-300 μm, smaller than about 250-300 μm, smaller than about 200-400 μm, or smaller than about 250-400 μm.

[0047] In one embodiment, the concentrated liquid feed material 300 is passed through a dryer, such as a refractive window dryer, to remove water and produce a crystalline solid having less than about 8% moisture by weight. In another embodiment, the crystalline solid has less than about 5-10% moisture by weight.

[0048] In one non-limiting embodiment, the present disclosure relates to a unique dry colorant made from red grape juice concentrate and purple carrot juice concentrate. A particular embodiment is a crystalline red colorant from grapes having a color value of at least about 40,000. In other embodiments, the crystalline red colorant has a color value of about 40,000-55,000, about 42,000-55,000, about 45,000-55,000, about 40,000-50,000, or about 42,000-50,000. In further embodiments, the crystalline red colorant has a color value greater than about 40,000, greater than about 42,000, greater than about 45,000, greater than about 50,000, or greater than about 55,000. Another specific embodiment is a crystalline purple colorant from carrots having a color intensity of at least about 90,000. In other embodiments, the crystalline purple colorant has a color intensity of about 85,000 to 130,000, about 85,000 to 125,000, about 90,000 to 130,000, about 90,000 to 125,000, about 95,000 to 130,000, about 95,000 to 125,000, about 100,000 to 130,000, or about 100,000 to 125,000. In further embodiments, the crystalline violet colorant has a color value greater than 85,000, greater than 90,000, greater than 95,000, greater than 100,000, greater than 125,000, or greater than 130,000.

[0049] 4A and 4B show a side view and a cross-sectional view, respectively, of a typical refractive window dryer 400. Dryer 400 includes a long tunnel 401, typically constructed from stainless steel, suitable for rapid evaporation of water. Liquid product passes through tunnel 401 as a thin layer 402 spread across the upper surface of a thin plastic conveyor belt 403.

[0050] In one non-limiting embodiment, liquid colorant is applied to the belt using an air pump with a suction hose inserted into the feed barrel. The air pump pumps the liquid from the barrel through a filter, such as a 75 micron in-line filter, and into a small feed balance tank. The air pump is typically controlled by the level in the feed balance tank. A valve at the feed outlet(s) directs the product onto an applicator tray, forming a thin layer on the moving surface of the belt.

[0051] Hot water, according to one embodiment, circulates in shallow heating trays 404 below conveyor belt 403, heating liquid layer 402. Thermal energy from the hot water is transferred by conduction and radiation through conveyor belt 403. In one embodiment, the hot water is at a temperature of up to about 210° F. It will be appreciated that the hot water may be at any temperature suitable to heat liquid layer 402 to the desired temperature.

[0052] A blower continuously blows water vapor away from the thin layer surface 402, maximizing the rate of water evaporation. The combination of evaporative cooling and the limited heat transfer of the plastic belt prevents the thin liquid layer surface 402 from reaching the temperature of the hot water in the heating tray 404, which could otherwise adversely affect product quality.

[0053] The product exits tunnel 401 as a dried solid product layer 405, which can be cut off by a sharp plastic blade 406 located against belt 403 at the bull nose end of the dryer. Contact with the blade cuts the dried product layer into thin crystalline pieces of various sizes. In one embodiment, the crystalline product falls off the end of the belt and is collected. In one embodiment, a plastic bag stretched over the inside of a plastic barrel and supported on a removable stainless steel frame is placed to collect the crystalline product from the belt.

[0054] Softened water can also be used in the heating trays below the belt to avoid staining and deposits on the stainless steel. The water is typically held in tanks below the belt. In one embodiment, each tank is connected to a heat exchanger through which the water circulates, using steam to reach and maintain an adjustable set-point temperature.

[0055] In another embodiment, the purified liquid concentrate is dried using a vacuum freeze-drying process to produce a dried powder with a large crystal structure that exhibits excellent color stability and / or pigment handling properties. In this embodiment, shown in Figure 8, the purified liquid is placed in a vacuum chamber of a freeze dryer 801. Air and water vapor are removed from the chamber under vacuum until the liquid in the trays is frozen. The frozen trays are then indirectly heated using an external source (i.e., steam, hot water, electricity) while the trays remain under vacuum. Residual water is sublimated from the frozen material until the moisture content is less than about 7 percent. This water sublimation process is carried out for about 8 to 24 hours at plate temperatures ranging from about 40°C to 100°C, depending on the water content and composition of the pigment. Once the water has sublimed, the trays are removed from the vacuum chamber, and the dried crystals are collected as granules of various sizes. The granules are milled in a sieve mill 802 or other size reduction device known in the art, such as an impact mill, to produce particles in the desired size range 803. This milling process produces a more coherent particle size and higher packing density for better storage and / or shipping efficiency. Crystalline Colorants / Pigments

[0056] In another aspect, crystalline pigments or colorants are described. Preferably, the crystalline pigments or colorants are derived from natural plant or algae sources. A novel combination of purification techniques and drying produces unique natural colorants with high color strength and / or low sugar content, which exhibit excellent long-term storage stability and / or handling properties, such as density, flowability, water dispersibility, and / or lower moisture absorption. As such, the crystalline pigments or colorants of the present invention overcome several fundamental problems the industry has previously encountered when using dried natural colorants.

[0057] In some embodiments, derivatization and / or modification of the crystalline pigments of the present invention are contemplated, including, but not limited to, co-pigmentation, saponification, complexation, and / or exfoliation. The pigments of the present invention can be modified and then formulated into a dye composition.

[0058] As shown in Figures 9A-9D, the crystalline pigments of the present invention are crystalline rather than amorphous. The natural dry colorants of the present invention are not spray-dried and therefore are not inherently low bulk density amorphous and do not require additives to enable drying or to make them less hygroscopic. Instead, the natural dry colorants of the present invention are dried using gentler drying techniques, such as, but not limited to, a refractive window dryer or a freeze dryer.

[0059] The crystalline colorants or pigments of the present invention can be produced from any suitable plant or algae that produces the desired pigment. In some embodiments, the pigments are comprised of anthocyanins, carotenoids, curcumin, betalains, carminic acid and derivatives, and / or chlorophyll and derivatives. Carotenoids include, but are not limited to, β-carotene, α-carotene, apocarotenal, lycopene, bixin, norbixin, canthaxanthin, and zeaxanthin. Derivatives of chlorophyll and chlorophyllin include, but are not limited to, copper complexes. In another non-limiting embodiment, the pigments of the present invention can be complexed with metal ions, such as, but not limited to, copper ions. In some non-limiting embodiments, the crystalline colorants or pigments of the present invention are obtained from grapes or carrots. It will be understood that the pigment composition may contain one or more crystalline pigments.

[0060] The purified natural dry colorants of the present invention are produced using gentler drying techniques that result in crystalline pigments that are non-hygroscopic and, due to their hygroscopicity, have excellent dispersibility and solubility properties and do not require agglomeration or granulation to improve solubility.

[0061] When refining fruit and vegetable pigment juices and extracts, according to one embodiment, the sugar composition is reduced from about 70%-95% on a dry weight basis to about 10-20% on a dry weight basis. In other embodiments, the sugar content is reduced to less than 10%, less than 15%, less than 20%, 15-20%, or 10-15% on a dry weight basis. In further embodiments, the crystalline pigments described herein have a total sugar content of about 5-20% on a dry weight basis. In other embodiments, the crystalline pigments have a total sugar content of about 5-10% on a dry weight basis, about 5-15% on a dry weight basis, about 10-20% on a dry weight basis, about 10-15% on a dry weight basis, or about 15-20% on a dry weight basis. According to one embodiment, reducing the sugar concentration relative to the total dry solids also concentrates the pigment fraction to about 7-15 times its original concentration on a dry weight basis. In some embodiments, the pigmentary portion is concentrated to 7-10 or 10-15 times its original concentration on a dry weight basis. There are several techniques for purifying colorants, including ultrafiltration / diafiltration, adsorption resins, solvent extraction, fermentation, and supercritical or subcritical fluid extraction.

[0062] As noted above, the crystalline colorants or pigments of the present invention have high color strength. Table 1 shows the color strength of purified grape and carrot pigments compared to standard sugar-based natural dyes. The color strength measurements for Table 1 are as follows: TIFF0007731407000001.tif18170

[0063] As shown in Table 1, typical color intensities of unrefined fruit and vegetable juice concentrates are between 2,000 and 12,000 color intensities. The purified pigments exhibit color intensities of about 40,000 to 55,000 color intensities for grape anthocyanins and about 90,000 to 125,000 color intensities for purple carrot anthocyanins. In one embodiment, the purified pigments have a color intensity greater than about 40,000 color intensities for grape anthocyanins. In another embodiment, the purified pigments have a color intensity greater than about 90,000 color intensities for purple carrot anthocyanins. In one embodiment, the color value is equal to: TIFF0007731407000002.tif18170

[0064] In further embodiments, the purified pigment exhibits increased color intensity compared to the crude juice and / or unrefined pigment or pigment composition. In non-limiting embodiments, increased color intensity refers to an increase in color intensity of at least about 5-200%. In further embodiments, increased color intensity refers to an increase in color intensity of at least about 5%, 10%, 20%, 25%, 50%, 75%, 100%, 150%, 200% or more.

[0065] The range of residual sugar and color intensity values ​​are provided for illustrative purposes only and represent nominal purification levels achievable using membrane purification processes. Lower residual sugar levels (down to less than 1 percent) are possible using additional or different types of membrane filtration and / or different purification processes, such as fermentation, adsorption resins, and solvent extraction.

[0066] Table 1: Purified pigment color strength of extracts, purified concentrates, and purified powders [Table 1]

[0067] As can be seen from Table 1, the purified pigment powders had significantly increased color intensity compared to the crude fruit extract / concentrate. Also, as can be seen from Table 1, the purified pigment powders had reduced sugar content compared to the crude fruit extract / concentrate. The grape pigments had at least 4 times less sugar than the crude fruit extract / concentrate, and the carrot pigments had at least 2.8 times less sugar. The purified crystalline red grape pigments had 13 to 17 times stronger color intensity on a dry basis than the crude grape juice concentrate. The purified crystalline purple carrot pigments had 6 to 9 times stronger color intensity on a dry basis than the crude carrot juice concentrate. In some embodiments, the purified crystalline pigments have 5 to 20 times stronger color intensity on a dry basis compared to the crude juice concentrate. In further embodiments, the purified crystalline pigments have 5 to 10 times, 5 to 15 times, or 10 to 20 times stronger color intensity on a dry basis compared to the crude juice concentrate.

[0068] The data presented in Table 1 reflect the use of membrane filtration to purify natural pigments. Inherent with membrane filtration is that there is a practical lower limit to sugar content based on the amount of diafiltration required, and that increasing diafiltration reduces the yield of purified pigment. Other purification methods, such as fermentation or adsorption resin methods, potentially have the potential to achieve lower sugar contents and therefore higher relative degrees of purification. It will be understood that lower sugar contents and higher pigment purity may be obtained using other purification methods.

[0069] Table 2 summarizes the differences in physical properties between refractory window-dried, freeze-dried, and spray-dried powders produced from the same purified grape anthocyanin pigment. As shown, the crystals dried by refractory window-dried and freeze-dried methods exhibit significantly different microscopic images, particle size distributions, and particle densities compared to the spray-dried powder.

[0070] Table 2: Physical properties of purified grape pigments [Table 2] 1 0.5 bar dispersion pressure 2 The terms D10, D50 and D90 refer to the size below which 10%, 50% and 90% of the particles in the sample are smaller, respectively. NOTE: The moisture content of the products dried by refractive window drying and spray drying was 3.0% and 3.5%, respectively.

[0071] As can be seen in Figures 9A-9B and 10A-10B, the refractive window dried or freeze-dried powders exhibit glassy, ​​angular crystals, reflecting relatively slow crystal growth compared to the spray-dried powders. The refractive window crystals also exhibit micropores within the basic crystal structure (Figure 10A). The angular, glassy morphology of the refractive window dried or freeze-dried crystals confers superior physical and flow properties, as discussed further below.

[0072] In contrast, the spray-dried powder is spherical and glassy (Figures 9C and 10C).

[0073] The crystal size of the refractive window-dried or freeze-dried powder is approximately seven times larger than that of the spray-dried powder produced from the same purified grape pigment. Ninety percent of the refractive window-dried or freeze-dried powder crystals were less than 277-287 μm in diameter, while 90 percent of the spray-dried particles were less than 38 μm in diameter. As a result of these larger average particle sizes, the crystalline powders produced by refractive window drying or freeze-drying exhibit less dust during handling when compared to comparable spray-dried powders, resulting in less airborne product loss in the manufacturing environment and cleaner, safer use.

[0074] The particle density of the refractive window dried or freeze dried powder is 50 percent greater than that of the spray dried powder, i.e., 1.5 g / cm 3 vs. 0.9g / cm 3 is.

[0075] Table 3 summarizes powder flow properties for refined grape anthocyanin pigments dried using either refractive window drying or spray drying. As shown, refined powders produced using refractive window drying exhibit less stickiness, lower wall friction, and higher air permeability compared to their spray-dried counterparts. These properties result in smaller hopper exit requirements, more gradual hopper angle requirements, and higher steady-state discharge flow rates, respectively.

[0076] Table 3: Flow properties of purified grape pigments [Table 3] 1 The cohesive arch is the smallest outlet diameter that does not form an arch in the mass flow vessel. Smaller arch sizes allow for higher throughput and greater equipment design flexibility for the same outlet size. 2 Wall friction is the maximum mass flow angle required to maintain steady flow. Larger angles allow greater flexibility in equipment design. 3 Permeability measures the critical mass flow rate that can support flow without clogging.

[0077] Cohesion strength measures the tendency of a powder to form ratholes and cohesion arches. Cohesion arch measurements determine the minimum hopper outlet size required to maintain steady-state flow without clogging. Smaller minimum outlet diameters are preferred because they require smaller transport piping and mixing equipment. Refined grape pigment powder produced using refractory window drying can maintain steady flow in a cone-shaped outlet as small as 9 cm in diameter. This same refined pigment produced using a spray dryer requires a cone diameter as large as 55 cm to maintain steady flow, nearly six times larger.

[0078] Wall friction angle is another measure of a powder's resistance to discharge from a hopper or flow through a pipe and its tendency to clog. A larger angle indicates better flowability, since mass flow can occur with hopper walls that are significantly off-vertical, thereby reducing the space area required to achieve a given flow rate. Refined powders produced using refractive window drying had a wall friction angle of 18 degrees in a conical hopper, compared to 11 degrees for refined powders produced using spray drying and subjected to the same outlet size, wall material, and surface finish.

[0079] Powder permeability correlates with steady-state flow characteristics; the higher the permeability, the more stable the steady-state flow. Powders with high air permeability maintain their shape and a high flow rate through a restricted orifice, while powders with low permeability have problems interacting with the air and limiting their discharge rate. Flow characteristics are quantified by measuring the steady-state flow of the powder through a fixed orifice. Refined powders produced using refractory window drying can maintain a steady-state flow of nearly 700 kg / min through a 2-foot diameter conical orifice, compared to only 8 kg / min for refined powders produced using spray drying. Similar enhanced flow characteristics noted above for refined grape pigments are expected to hold true for other refined natural pigments purified using the same purification process and dried using freeze drying.

[0080] In some embodiments, the pigments or colorants of the present invention are formulated as compositions. The pigments or colorants may be formulated as aqueous solutions, emulsions, suspensions, and / or dispersions. The pigment or colorant compositions are contemplated for any suitable situation in which color is to be added or enhanced. In some embodiments, the pigment or colorant compositions are used in food, pharmaceutical, and / or cosmetic applications. Example

[0081] The following examples are for illustrative purposes and are not intended to limit the invention in any way. [Example]

[0082] Crystalline colorant formation

[0083] Red grape juice concentrate and purple carrot juice concentrate were separately reconstituted to approximately 18–22°Brix.

[0084] Red grape juice concentrate and purple carrot juice concentrate were purified separately by ultrafiltration and diafiltration through PES membrane devices.

[0085] The refined red grape juice concentrate and purple carrot juice concentrate were separately concentrated using a falling film evaporator and then dried using a refractory window dryer. The refinement data were measured and the results are shown in Table 5.

[0086] Table 5: Crystal purification data [Table 4]

[0087] While many exemplary aspects and embodiments have been discussed above, those skilled in the art will recognize certain modifications, permutations, additions, and subcombinations thereof. Accordingly, it is intended that the following appended claims and any subsequent claims be interpreted as including all such modifications, permutations, additions, and subcombinations that fall within the true spirit and scope of the claims.

Claims

1. 1. A system comprising:

1. A purification apparatus for purifying juice of a plant containing natural pigments by removing at least a portion of non-pigment compounds, including sugars and acids, from said juice to produce a liquid feedstock, said purification comprising at least one of ultrafiltration and diafiltration, adsorption / desorption chromatography, fermentation, a subcritical fluid extraction process, or a supercritical fluid extraction process; a conveyor belt having an upper surface configured to receive the liquid feedstock on the upper surface; a dispenser tray at a first end of the conveyor belt for receiving the liquid feedstock and dispensing the liquid feedstock onto the upper surface; and one or more heating trays below said conveyor belt for heating said liquid feedstock to facilitate production of a crystalline pigment product from said liquid feedstock, wherein hot water at up to about 210°F (98.9°C) is circulated through said one or more heating trays; Including, the system.

2. 10. The system of claim 1, further comprising an air pump and a feedstock barrel coupled to the air pump via a suction hose for delivering the liquid feedstock from the feedstock barrel and ultimately to the applicator tray.

3. 3. The system of claim 2, wherein the air pump pumps the liquid feedstock from the feedstock barrel into a feedstock balance tank.

4. 4. The system of claim 3, wherein the air pump is controlled by the level of the liquid feedstock in the feedstock balance tank.

5. 10. The system of claim 1, further comprising one or more feedstock outlet valves that cause the liquid feedstock to flow onto the applicator tray to form a thin layer of the liquid feedstock on the moving surface of the belt.

6. The system of claim 1 further comprising a tunnel through which the conveyor belt passes.

7. The system of claim 1 , wherein the liquid feedstock has a temperature that is less than the temperature of the hot water.

8. The system of claim 1 further comprising a blower for blowing water vapor away from the conveyor belt.

9. 10. The system of claim 1, further comprising a plastic blade to facilitate cutting the crystalline product from the conveyor belt.

10. 10. The system of claim 1, wherein the liquid feedstock comprises a pigment selected from the group consisting of anthocyanins, carotenoids, betalains, curcumin, carminic acid, carminic acid derivatives, chlorophyll, and chlorophyll derivatives.

11. The system of claim 1 further comprising a heat exchanger.

12. 10. The system of claim 1, wherein the purification device comprises a polymeric membrane system and the purification comprises performing the ultrafiltration and diafiltration through the polymeric membrane system.

13. The system of claim 1 further comprising a mill for grinding the crystalline product.

14. The system of claim 1 , wherein the conveyor belt is made of plastic.

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