Extracts from oil seeds and methods for processing oil seeds

Abstract

To provide methods for extracting materials from oil seeds.SOLUTION: An example method may include extracting a material from an oil seed with an extraction solution to form a mixture. The extraction solution may be free of an organic solvent. The method may also include filtering the mixture into a retentate and a permeate. The method may also include drying the retentate.SELECTED DRAWING: None

Description

Technical Field

[0001] The present disclosure relates to extracts obtained from oilseed grains and methods for treating oilseed grains.

Background Art

[0002] Numerous methods for treating oilseed grains are known. Among these methods, each has several advantages and disadvantages. The need for different new methods for treating oilseed grains continues to exist.

Summary of the Invention

Problems to be Solved by the Invention

[0003] The present disclosure provides a method for treating oilseed grains.

Means for Solving the Problems

[0004] A method for extracting a material from oilseed grains is disclosed. The method includes a step of extracting a material from the oilseed grains using an extraction solution to form a mixture, wherein the extraction solution does not contain an organic solvent, a step of filtering the mixture into a retentate and a permeate, and a step of drying the retentate.

[0005] Alternatively or additionally to any of the above embodiments, the method further includes a step of hulling the oilseed grains. Alternatively or additionally to any of the above embodiments, the method further includes a step of cold pressing the oilseed grains.

[0006] Alternatively or additionally to any of the above embodiments, the method further includes a step of grinding the hulled oilseed grains. Alternatively or additionally to any of the above embodiments, the extraction solution contains water.

[0007] Alternatively or additionally to any of the above embodiments, the extraction solution contains a salt. Alternatively or additionally to any of the above embodiments, the extraction solution contains an acid. Alternatively or additionally to any of the above embodiments, the method further includes separating the mixture into an aqueous phase and a wet meal.

[0008] Alternatively or additionally to any of the above embodiments, the step of separating the mixture into an aqueous phase and a wet meal includes decanting. Alternatively or additionally to any of the above embodiments, the method further includes removing seed oil from the aqueous phase.

[0009] Alternatively or additionally to any of the above embodiments, the method further includes centrifuging the aqueous phase. Alternatively or additionally to any of the above embodiments, the step of centrifuging the aqueous phase includes separating oil from the aqueous phase.

[0010] Alternatively or additionally to any of the above embodiments, the step of filtering the mixture includes ultrafiltration. Alternatively or additionally to any of the above embodiments, the step of filtering the mixture includes diafiltration.

[0011] Alternatively or additionally to any of the above embodiments, the step of drying the retained component includes evaporating the retained component. Alternatively or additionally to any of the above embodiments, the step of drying the retained component includes spray-drying the retained component.

[0012] Alternatively or additionally to any of the above embodiments, the retained component includes soluble proteins. Alternatively or additionally to any of the above embodiments, the retained component includes low molecular weight proteins.

[0013] Alternatively or additionally to any of the above embodiments, the method further includes filtering the permeate component. Alternatively or additionally to any of the above embodiments, the step of filtering the permeate component includes nanofiltration.

[0014] Alternatively or additionally to any of the above embodiments, the step of filtering the permeate component separates the permeate component into a second permeate component and a second retained component. Alternatively or additionally to any of the above embodiments, the method further includes a step of drying the second retained component.

[0015] Alternatively or additionally to any of the above embodiments, the step of drying the second retained component includes evaporating the second retained component. Alternatively or additionally to any of the above embodiments, the step of drying the second retained component includes spray-drying the second retained component.

[0016] Alternatively or additionally to any of the above embodiments, the second retained component contains chlorogenic acid. Alternatively or additionally to any of the above embodiments, the method further includes a step of passing the second permeate component through a reverse osmosis membrane.

[0017] Alternatively or additionally to any of the above embodiments, passing the second permeate component through a reverse osmosis membrane produces purified water. Alternatively or additionally to any of the above embodiments, passing the second permeate component through a reverse osmosis membrane produces a brine solution.

[0018] Alternatively or additionally to any of the above embodiments, the method further includes a step of extracting undried meal. Alternatively or additionally to any of the above embodiments, the step of extracting undried meal is an extraction without an organic solvent.

[0019] Alternatively or additionally to any of the above embodiments, the method further includes a step of separating the undried meal into a second aqueous phase and a second undried meal. Alternatively or additionally to any of the above embodiments, the step of separating the undried meal into a second aqueous phase and a second undried meal includes decanting.

[0020] Alternatively or additionally to any of the above embodiments, the method further includes centrifuging the second aqueous phase. Alternatively or additionally to any of the above embodiments, centrifuging the second aqueous phase includes separating oil from the second aqueous phase.

[0021] Alternatively or additionally to any of the above embodiments, the method further includes precipitating the second aqueous phase. Alternatively or additionally to any of the above embodiments, precipitating the second aqueous phase includes lowering the pH of the second aqueous phase.

[0022] Alternatively or additionally to any of the above embodiments, the method further includes separating a precipitate from the second aqueous phase. Alternatively or additionally to any of the above embodiments, separating a precipitate from the second aqueous phase includes decanting.

[0023] Alternatively or additionally to any of the above embodiments, the method further includes washing the precipitate. Alternatively or additionally to any of the above embodiments, the method further includes filtering the second aqueous phase to obtain a third retained component and a third permeate component.

[0024] Alternatively or additionally to any of the above embodiments, the method further includes passing the third permeate component through a reverse osmosis membrane. By passing the third permeate component through a reverse osmosis membrane, purified water is produced, alternatively or additionally to any of the above embodiments.

[0025] By passing the third permeate component through a reverse osmosis membrane, a brine solution is produced, alternatively or additionally to any of the above embodiments. Alternatively or additionally to any of the above embodiments, the method further includes drying the third retained component, the third permeate component, or both.

[0026] Alternatively or additionally to any of the above embodiments, the drying of the third holding component, the precipitate, or both, includes flash drying of the third holding component. Alternatively or additionally to any of the above embodiments, the third holding component, the precipitate, or both, include insoluble proteins.

[0027] Alternatively or additionally to any of the above embodiments, the third holding component, the precipitate, or both, include high molecular weight proteins. Alternatively or additionally to any of the above embodiments, the oilseed includes sunflower seeds.

[0028] A method for extracting a plurality of target materials from oilseeds is disclosed. The method includes: performing a first extraction on the oilseed material to form an aqueous phase and a solid phase, wherein the first extraction is an extraction without an organic solvent; filtering the aqueous phase to form a holding component and a permeating component; drying the holding component, wherein the dried holding component includes a first target material; filtering the permeating component to form a second holding component; and drying the second holding component, wherein the second dried holding component includes a second target material.

[0029] Alternatively or additionally to any of the above embodiments, the first target material includes proteins. Alternatively or additionally to any of the above embodiments, the second target material includes chlorogenic acid.

[0030] Alternatively or additionally to any of the above embodiments, the method further includes adding a precipitation material to the permeating component to form a precipitate. Alternatively or additionally to any of the above embodiments, the precipitation material includes calcium chloride.

[0031] Alternatively or additionally to any of the above embodiments, the precipitate includes phytic acid. A method for extracting a plurality of target materials from oil and grain seeds is disclosed. The method includes a step of performing a first extraction on the oil and grain seed material by adding water and salt to the oil and grain seed material, the first extraction forming an aqueous phase and a solid phase; a step of filtering the aqueous phase to form a retained component and a permeate component; a step of drying the retained component, the dried retained component containing a first target material; a step of filtering the permeate component to form a second retained component; and a step of drying the second retained component, the second dried retained component containing a second target material.

[0032] Alternatively or additionally to any of the above embodiments, the first target material contains protein. Alternatively or additionally to any of the above embodiments, the second target material contains chlorogenic acid.

[0033] Alternatively or additionally to any of the above embodiments, the method further includes a step of adding a precipitation material to the permeate component to form a precipitate. Alternatively or additionally to any of the above embodiments, the precipitation material contains calcium chloride.

[0034] Alternatively or additionally to any of the above embodiments, the precipitate contains phytic acid. A food is disclosed. The food includes an emulsion; and a sunflower-based emulsifier mixed with the emulsion.

[0035] A food is disclosed. The food includes a liquid, and a soluble sunflower protein dissolved in the liquid. A method for extracting a sweet protein from sunflower seeds is disclosed. The method includes a step of extracting a material derived from sunflower seeds with an extraction solution to form a mixture, the extraction solution not containing an organic solvent; a step of filtering the mixture into a retained component and a permeate component; and a step of drying the retained component to extract the sweet protein.

[0036] A method for extracting proteins from sunflower seeds is disclosed. The method includes a step of extracting a material derived from sunflower seeds with an extraction solution to form a mixture, wherein the extraction solution does not contain an organic solvent; a step of filtering the mixture into a retained component and a permeate component; and a step of drying the retained component to form a protein having a natural three-dimensional structure.

[0037] A method for extracting a plurality of materials from oilseed grains is disclosed. The method includes a step of extracting a material from oilseed grains with an extraction solution to form a mixture, wherein the extraction solution does not contain an organic solvent; a step of filtering the mixture into a retained component and a permeate component; a step of drying the retained component to form a first material; a step of filtering the permeate component into a second retained component and a second permeate component; and a step of drying the second retained component to form a second material, wherein at least one of the first material and the second material includes a nutritional supplement.

[0038] A method for extracting a material from oilseed grains is disclosed. The method includes a step of mixing an extraction solution with a certain amount of oilseed grains that have been dehulled, crushed, and pulverized to form a mixture, wherein the extraction solution contains water and salt and the pH of the extraction solution is 3 to 6; a step of extracting the mixture at a temperature in the range of 10 to 93 °C for 0.5 to 6 hours to form an extracted mixture; a step of filtering the extracted mixture into a retained component and a permeate component; and a step of drying the retained component.

[0039] A method for extracting a material from oilseed grains is disclosed. The method includes a step of mixing an extraction solution with a certain amount of oilseed grains that have been dehulled, pressed, and crushed to form a mixture, wherein the extraction solution contains water and salt and the pH of the extraction solution is 3 to 6; a step of extracting the mixture at a temperature in the range of 10 to 93 °C for 0.5 to 6 hours to form an extracted mixture; a step of filtering the extracted mixture into a retained component and a permeate component; and a step of drying the retained component.

[0040] A method for extracting a plurality of target materials from oil and grain seeds is disclosed. The method includes a step of performing a first extraction on the oil and grain seed material to form an aqueous phase and a solid phase, where the first extraction is an extraction without an organic solvent; a step of filtering the aqueous phase to form a retained component and a permeate component; a step of drying the retained component, where the dried retained component contains the first target material; a step of filtering the permeate component to form a second retained component; and a step of drying the second retained component, where the second dried retained component contains the second target material.

[0041] Alternatively or additionally to any of the above embodiments, the first target material includes a first protein. Alternatively or additionally to any of the above embodiments, the first protein includes an insoluble protein.

[0042] Alternatively or additionally to any of the above embodiments, the second target material includes a second protein. Alternatively or additionally to any of the above embodiments, the second protein includes a soluble protein.

[0043] Alternatively or additionally to any of the above embodiments, the step of filtering the permeate component to form a second retained component includes forming a second permeate component. Alternatively or additionally to any of the above embodiments, the method further includes a step of filtering the second permeate component to form a third retained component.

[0044] Alternatively or additionally to any of the above embodiments, the method further includes a step of drying the third retained component, and the third dried retained component contains a third target material. Alternatively or additionally to any of the above embodiments, the third target material includes chlorogenic acid.

[0045] Alternatively or additionally to any of the above embodiments, the method further includes a step of adding a precipitation material to the permeate component, the second permeate component, or both to form a precipitate. Alternatively or additionally to any of the above embodiments, the precipitation material comprises calcium chloride.

[0046] Alternatively or additionally to any of the above embodiments, the precipitate comprises phytic acid. A method for extracting materials from oilseed grains is disclosed. The method includes the steps of extracting materials from oilseed grains using an extraction solution to form a mixture, wherein the extraction solution does not contain an organic solvent; filtering the mixture into a retention component and a permeate component; and drying the retention component.

[0047] Alternatively or additionally to any of the above embodiments, the extraction solution comprises water and salts. Alternatively or additionally to any of the above embodiments, the method further includes separating the mixture into an aqueous phase and an undried meal by decanting.

[0048] Alternatively or additionally to any of the above embodiments, the method further includes removing seed oil from the aqueous phase. Alternatively or additionally to any of the above embodiments, the step of filtering the mixture includes ultrafiltration.

[0049] Alternatively or additionally to any of the above embodiments, the retention component comprises soluble proteins. Alternatively or additionally to any of the above embodiments, the method further includes filtering the permeate component into a second permeate component and a second retention component.

[0050] Alternatively or additionally to any of the above embodiments, the step of filtering the permeate component includes nanofiltration. Alternatively or additionally to any of the above embodiments, the second retention component comprises chlorogenic acid.

[0051] Alternatively or additionally to any of the above embodiments, the method further includes passing the second permeate component through a reverse osmosis membrane. Alternatively or additionally to any of the above embodiments, the method further includes a step of extracting undried meal and a step of separating the undried meal into a second aqueous phase and a second undried meal.

[0052] Alternatively or additionally to any of the above embodiments, the method further includes a step of precipitating the second aqueous phase and a step of separating the precipitated material from the aqueous phase. Alternatively or additionally to any of the above embodiments, the method further includes a step of filtering the second aqueous phase into a third retained component and a third permeate component.

[0053] Alternatively or additionally to any of the above embodiments, the third retained component includes insoluble proteins. A method for extracting a plurality of target materials from oilseed grains is disclosed. The method includes a step of performing a first extraction on an oilseed grain material to form an aqueous phase and a solid phase, wherein the first extraction is an extraction without an organic solvent; a step of filtering the aqueous phase to form a retained component and a permeate component; a step of drying the retained component, wherein the dried retained component includes a first target material; a step of filtering the permeate component to form a second retained component; and a step of drying the second retained component, wherein the second dried retained component includes a second target material.

[0054] Alternatively or additionally to any of the above embodiments, the first target material includes proteins. Alternatively or additionally to any of the above embodiments, the second target material includes chlorogenic acid.

[0055] Alternatively or additionally to any of the above embodiments, the method further includes a step of adding a precipitating material to the permeate component to form a precipitate. Alternatively or additionally to any of the above embodiments, the precipitate includes phytic acid.

[0056] A method for extracting materials from oil and grain seeds is disclosed. The method includes the steps of: mixing an extraction solution with a certain amount of peeled and ground oil and grain seeds to form a mixture, wherein the extraction solution contains water and salt, and the pH of the extraction solution is 3 to 6; extracting the mixture at a temperature in the range of 10 to 93 °C for 0.5 to 6 hours to form an extracted mixture; filtering the extracted mixture into a retention component and a permeate component; and drying the retention component.

[0057] A method for extracting materials from oil and grain seeds is disclosed. The method includes the steps of: mixing an extraction solution with a certain amount of peeled, pressed, and ground oil and grain seeds to form a mixture, wherein the extraction solution contains water and salt, and the pH of the extraction solution is 3 to 6; extracting the mixture at a temperature in the range of 10 to 93 °C for 0.5 to 6 hours to form an extracted mixture; filtering the extracted mixture into a retention component and a permeate component; and drying the retention component.

[0058] A composition is disclosed. The composition includes a first component containing sunflower protein extract; and a second component containing phytic acid. Alternatively or additionally to any of the above embodiments, the first component accounts for 91.7 to 99% by weight of the composition.

[0059] Alternatively or additionally to any of the above embodiments, the second component accounts for 0.28 to 7.7% by weight of the composition. Alternatively or additionally to any of the above embodiments, the second component accounts for 2 to 6% by weight of the composition.

[0060] Alternatively or additionally to any of the above embodiments, the composition has a sweetness substantially equal to that of sucrose. Alternatively or additionally to any of the above embodiments, the composition has a sweetness sweeter than that of sucrose.

[0061] Alternatively or additionally to any of the above embodiments, the composition has a sweetness that is 2 to 10 times sweeter than the sweetness of sucrose. Alternatively or additionally to any of the above embodiments, the composition has a sweetness that is 2 to 5 times sweeter than the sweetness of sucrose.

[0062] A method for extracting a plurality of target materials from oilseed grains is disclosed. The method includes a step of performing extraction on an oilseed grain material to form an aqueous phase and a solid phase, where the extraction is performed in an extraction without an organic solvent; a step of separating insoluble solids from the aqueous phase; a step of filtering the aqueous phase to form a retained component and a permeate component; a step of drying the retained component to form a dried retained component, where the dried retained component contains a first target material; a step of filtering the permeate component to form a second retained component and a second permeate component; a step of drying the second retained component to form a second dried retained component, where the second dried retained component contains a second target material; a step of filtering the second permeate component to form a third retained component; and a step of drying the third retained component to form a third dried retained component, where the third dried retained component contains a third target material.

[0063] Alternatively or additionally to any of the above embodiments, the first target material contains protein. Alternatively or additionally to any of the above embodiments, the second target material contains a second protein fraction.

[0064] Alternatively or additionally to any of the above embodiments, the method further includes a step of adding a precipitation material to the permeate component to form a precipitate. Alternatively or additionally to any of the above embodiments, the precipitate contains phytic acid.

[0065] Alternatively or additionally to any of the above embodiments, the precipitation material is calcium chloride. Alternatively or additionally to any of the above embodiments, the step of adding a precipitation material to the permeate component to form a precipitate includes the step of adding calcium chloride at a molar ratio of 5.6 to 6.0:1 to phytic acid in the permeate component.

[0066] Alternatively or additionally to any of the above embodiments, the third target material includes chlorogenic acid. Plant-based cheese is disclosed. The plant-based cheese includes water-soluble sunflower protein; one or more of almond milk, coconut, potato starch, and tapioca flour; and a thickened agar solution.

[0067] Alternatively or additionally to any of the above embodiments, the plant-based cheese includes two or more of almond milk, coconut, potato starch, and tapioca flour. Alternatively or additionally to any of the above embodiments, the plant-based cheese includes three or more of almond milk, coconut, potato starch, and tapioca flour.

[0068] Alternatively or additionally to any of the above embodiments, the plant-based cheese includes almond milk, coconut, potato starch, and tapioca flour. Alternatively or additionally to any of the above embodiments, it further includes one or more of nutritional yeast, xanthan gum, and salt.

[0069] Alternatively or additionally to any of the above embodiments, the plant-based cheese includes two or more of nutritional yeast, xanthan gum, and salt. Alternatively or additionally to any of the above embodiments, the plant-based cheese includes nutritional yeast, xanthan gum, and salt.

[0070] Plant-based ice cream is disclosed. The plant-based ice cream includes soluble sunflower protein; insoluble sunflower protein; one or more of pea starch, almond milk, coconut water blend, sugar, and allulose; and sunflower oil.

[0071] Alternatively or additionally to any of the above embodiments, the plant-based ice cream contains two or more of pea starch, almond milk, coconut water blend, sugar, and allulose.

[0072] Alternatively or additionally to any of the above embodiments, the plant-based ice cream contains three or more of pea starch, almond milk, coconut water blend, sugar, and allulose.

[0073] Alternatively or additionally to any of the above embodiments, the plant-based ice cream contains four or more of pea starch, almond milk, coconut water blend, sugar, and allulose.

[0074] Alternatively or additionally to any of the above embodiments, the plant-based ice cream contains pea starch, almond milk, coconut water blend, sugar, and allulose.

[0075] Protein-enriched chocolate milk is disclosed. The protein-enriched chocolate milk contains soluble sunflower protein containing 2-6 wt% phytic acid; milk; and one or more of cocoa, calcium carbonate, and cellulose gel.

[0076] Alternatively or additionally to any of the above embodiments, the soluble sunflower protein containing 2-6 wt% phytic acid has a sweetness substantially equal to that of sucrose. Alternatively or additionally to any of the above embodiments, the soluble sunflower protein containing 2-6 wt% phytic acid has a sweetness 2-5 times sweeter than sucrose.

[0077] Protein-enriched sports drink is disclosed. The protein-enriched sports drink contains soluble sunflower protein containing 2-6 wt% phytic acid; water; and an electrolyte solution.

[0078] Alternatively or additionally to any of the above embodiments, the soluble sunflower protein containing 2 to 6% by weight of phytic acid has a sweetness substantially equal to that of sucrose. Alternatively or additionally to any of the above embodiments, the soluble sunflower protein containing 2 to 6% by weight of phytic acid has a sweetness 2 to 5 times sweeter than sucrose.

[0079] Alternatively or additionally to any of the above embodiments, the protein-enriched sports drink does not contain added sugar and does not contain added sugar substitutes. Alternatively or additionally to any of the above embodiments, the protein-enriched sports drink contains 0.75 to 1.5 grams of protein per about 28 grams (1 ounce).

[0080] Alternatively or additionally to any of the above embodiments, the protein-enriched sports drink contains substantially 1 gram of protein per about 28 grams (1 ounce). The above summary of some embodiments is not intended to describe every disclosed embodiment or every implementation of the present disclosure. The figures and detailed description that follow illustrate these embodiments in more detail.

[0081] The present disclosure can be more fully understood by considering the following detailed description in connection with the accompanying drawings.

Brief Description of the Drawings

[0082]

Figure 1

Figure 2

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Modes for Carrying Out the Invention

[0083] While various modifications and alternative forms can be applied to the present disclosure, their details are shown by way of example in the drawings and are described in detail. However, it should be understood that the present invention is not intended to be limited to the specific embodiments described. On the contrary, it is intended to cover all modifications, equivalents, and alternatives that fall within the spirit and scope of the present disclosure.

[0084] For the following defined terms, these definitions shall apply unless different definitions are given in the claims or elsewhere in this specification. In this specification, all numerical values are assumed to be modified by the term "about", whether explicitly indicated or not. The term "about" generally refers to a range of numerical values that a person skilled in the art would consider to be equal to the recited value (e.g., having the same function or result). In many cases, the term "about" can include numbers that are rounded to the nearest significant digit.

[0085] The recitation of a numerical range by endpoints includes all numerical values within that range (e.g., 1 to 5 includes 1, 1.5, 2, 2.75, 3, 3.80, 4, and 5). As used in this specification and the appended claims, unless the context clearly indicates otherwise, the singular forms "a", "an", and "the" include plural referents. As used in this specification and the appended claims, the term "or" is generally used in the sense of "and / or" unless the context clearly indicates otherwise.

[0086] References to "one embodiment", "some embodiments", "other embodiments", etc. in this specification are to be noted as indicating that the described embodiments can include one or more specific features, structures, and / or characteristics. However, such listings do not necessarily mean that all embodiments include the specific features, structures, and / or characteristics. Further, when a specific feature, structure, and / or characteristic is described in relation to one embodiment, it is to be understood that such feature, structure, and / or characteristic can also be used in relation to other embodiments, whether or not explicitly described, unless otherwise specifically stated.

[0087] The following detailed description should be read in consideration of the drawings in which like elements in different drawings are given the same number. The drawings are not necessarily to scale and are illustrative of exemplary embodiments and are not intended to limit the scope of the present invention.

[0088] Many plants produce seeds that contain extractable oils and other materials. For the purposes of this disclosure, such plants and / or, more particularly, the seeds of such plants can be referred to as oilseed plants and / or oilseeds. Examples of plants that produce oilseeds can include almonds, argan, borrage, rapeseed, castor, cherry, coconut, corn, cotton, flax, grape, hemp, jojoba, macadamia, mango, mustard, indigo, oil palm, rape, safflower, sesame, shea tree, sunflower, tonka bean, moringa, rice (and / or rice bran) and tung tree. These are but one example. By extracting oil from the seeds of such plants, vegetable oil is produced. For example, by extracting oil from rapeseed seeds, canola oil is produced.

[0089] In addition to oil, there are also numerous substances of interest present in oilseed crops. Some examples of such materials include proteins (such as soluble proteins, insoluble proteins, albumin, helianthinin, etc.), one or more meals (such as sunflower meal with reduced oil and protein content and / or sunflower meal with chlorogenic acid removed that can have a beneficial effect on the color of the meal), phenols, chlorogenic acid, phytic acid, combinations thereof, and / or the like. In some cases, organic solvents such as hexane, alcohol, and / or the like are used to extract proteins from oilseed crops. However, such solvents may have an impact on the environment and / or human health. Furthermore, such solvents may affect other materials present in the oilseed crops. Therefore, it may be desirable to extract proteins from oilseed crops in a manner that minimizes the impact on the environment, improves human health, and / or also extracts other desired substances. Methods for treating oilseed crops are disclosed herein. These methods can be utilized to extract materials from the oilseed crops. Such materials can include seed oil, proteins, one or more meals, phenols, chlorogenic acid, phytic acid, combinations thereof, and / or other materials.

[0090] Currently, there is a lack of such further overall perspectives on oilseed crop processing in this field, and since oilseed crops are processed as oil, other valuable nutrients in the oilseed crops are often degraded during processing. As the understanding of the nutrients necessary for maintaining human health and a healthy mind and body progresses, it becomes necessary to develop new technologies to supply these nutrients in a sustainable manner. The present disclosure enables the treatment of seeds in a way that allows for extraction as many nutrients valuable to human health as are available.

[0091] Protein is one of the major nutrients, especially with increasing relevance to plant proteins. As the interest and desire for the intake of plant proteins increase, the need for new and novel sources of plant proteins is also increasing. A new plant protein source with good taste, which is not a major allergen and / or has functional aspects (such as foaming, gelation, solubility, etc.) is desirable. The present disclosure aims to provide at least some of these traits and others.

[0092] Furthermore, micronutrients, such as minerals, vitamins, antioxidants, polyphenols, etc., are becoming increasingly important as tools are developed to understand what is necessary for an individual's daily nutrition, which varies from person to person. Many oilseeds contain useful micronutrients that are mainly composed of polyphenols. Sunflower seeds have two useful micronutrients, chlorogenic acid and phytic acid. Both can still be extracted and isolated in a nutritionally useful form as long as strong stimulants or extreme processing conditions (such as high temperature, very low or high pH) are avoided.

[0093] Figure 1 is a flowchart showing an example of a method for processing oilseeds, generally referred to by reference numeral 10. The method can include receiving oilseeds 12 (such as unprocessed oilseeds) from a supplier (such as an agricultural product supplier). The unprocessed oilseeds 12 can, for example, undergo a dehulling process 14 where the unprocessed oilseeds 12 are brought into a processing facility and taken into a dehulling unit. When taken into the dehulling unit, the seeds are cracked and the husks are separated from the "pulp" or material 16 of the seeds. After the dehulling process, more than 90% of the husks are removed from the oilseeds, or about 99% or more of the husks are removed from the oilseeds, or about 99.9% or more of the husks are removed from the oilseeds. The husks may be discarded or transferred to separate / different processing. The pulp or dehulled oilseed material 16 can be further processed.

[0094] In some cases, before extracting the dehulled oilseed material 16, the dehulled oilseed material 16 can be pressed (e.g., cold pressed) to remove a portion of the oil from the dehulled oilseed material 16. The cold pressing process can be carried out at a temperature in the range of about 70 - 140°F (20 - 60°C) or about 130 - 138°F (54 - 59°C). Pressing at such temperatures (e.g., pressing at relatively low temperatures) can help preserve nutrients (e.g., vitamin E) in the oil as well as preserve the integrity and / or higher-order structure of the proteins in the dehulled oilseed material 16. Further, pressing at relatively low temperatures can also help preserve the integrity of other materials (e.g., chlorogenic acid, etc.) of interest in the dehulled oilseed material 16.

[0095] The dehulled oilseed material 16 can be subjected to a grinding process 18 to produce a ground material 20. Grinding can include grinding using any one (or more) of various types of grinders including, for example, hammer mills, knife mills, colloid mills, stone mills, and / or the like. The grinding process can reduce the particle size such that D90 is less than about 3 mm, or D90 is about 1 - 2 mm or less, or the like.

[0096] In some cases, when the temperature conditions are not controlled, grinding can result in the release / liberation of oil from the dehulled seed oil material and / or the degradation of one or more components (e.g., chlorogenic acid). To limit the release / liberation of oil from the dehulled seed oil raw material and / or the degradation of one or more components, grinding can be carried out under temperature-controlled conditions. For example, in some cases, grinding is carried out at a temperature of about 80 - 140°F (26 - 60°C), or about 120 - 140°F (48 - 60°C), or about 140°F (60°C) or less, or about 130 - 138°F (54 - 59°C).

[0097] The comminuted material 20 can be subjected to one or more extractions. A flowchart showing a process 22 including a first extraction of the comminuted material 20 and the recovery of one or more materials from the comminuted material 20 is shown in FIG. 2. The process 22 can include a step of mixing the comminuted material 20 with an extraction solution to form a mixture 26. The mixing is generally designated by reference numeral 24 in FIG. 2. In at least some cases, the extraction solution includes water, and the step of mixing the comminuted material 20 with the extraction solution can include adding water in an appropriate ratio. For example, the comminuted material 20 can be mixed with water at a ratio of water to the comminuted material 20 (e.g., the dry weight of the comminuted material 20) of about 6:1 to 20:1, or a ratio of water to the comminuted material 20 (e.g., the dry weight of the comminuted material 20) of about 10:1 to 15:1. In some cases, this ratio can be about 10:1 of water to comminuted material 20. The mixture 26 can be heated to a temperature of about 50 to 200°F (10 to 93°C), or about 100 to 140°F (37 to 60°C), or about 140°F (60°C), or about 130 to 138°F (54 to 59°C). In some cases, the pH is adjusted to about pH 3 to 6 or pH about 4 using a suitable acid / base (e.g., an acid such as HCl, a base such as NaOH, and / or other suitable acid / base). Also, a salt can be added to the mixture 26. In some cases, the salt can be NaCl. The salt can be added such that the mixture 26 has a salt concentration of about 0.05 to 2.0 M NaCl, or about 0.1 to 1.0 M NaCl, or about 0.25 to 0.5 M NaCl, or about 0.25 M NaCl. With the mixture 26 adjusted to the desired temperature and salt concentration, the mixture 26 can be held (e.g., held during the extraction period) in a suitable container (e.g., a batch tank, a continuous stirred tank, a continuous mixed flow reactor, etc.) for about 0.5 to 6 hours or about 2 hours to extract the target material. For example, low molecular weight proteins (e.g., having a molecular weight in the range of about 10 to 18 kDa), chlorogenic acid, and / or other target materials can be extracted into the aqueous phase. The step of holding the mixture to enable extraction of the target material (e.g., the first extraction) is generally designated by reference numeral 28 in FIG. 2. The result of the first extraction 28 is the extracted mixture 30.

[0098] In at least some cases, it can be understood that the first extraction 28 is carried out without using an organic solvent that may affect (e.g., decompose) other materials present in the comminuted material 20, affect the environment, and / or affect human health. Thus, the first extraction 28 can be carried out without using an organic solvent, or if not, can be considered to be free of organic solvents (e.g., the extraction process is carried out without using an organic solvent). That is, the first extraction 28 may be an extraction without an organic solvent. For example, the first extraction 28 can be carried out without using hexane, or if not, can be considered to be free of hexane (e.g., the extraction process is carried out without using hexane). In other words, the first extraction 28 may be an extraction without hexane. In some and other cases of these, the first extraction 28 can be carried out using materials that reduce or minimize the impact on the target substance in the comminuted material 20, reduce the impact on the environment, and / or reduce the impact on human health. For example, the first extraction 28 can be carried out using materials that reduce or minimize the impact on chlorogenic acid in the comminuted material 20 (e.g., the possibility of chlorogenic acid decomposing during the first extraction 28 is reduced or minimized). For the purposes of the present disclosure, water is not considered an organic solvent.

[0099] In some cases, one or more additional processes may be added to, incorporated into, and / or otherwise used in conjunction with the first extraction 28 (e.g., and / or other extractions disclosed herein). For example, 0.1 to 2 wt% ascorbic acid can be added during the extraction process. This can help reduce and / or prevent the formation of undesirable colors that may occur due to the interaction between polyphenol oxidase, chlorogenic acid, and proteins. In some and other cases of these, adsorbent polymer beads and / or activated carbon can be utilized to improve the separation of chlorogenic acid from proteins. For example, chlorogenic acid can bind to the beads and can later be eluted using a solvent such as ethanol or water and / or by adjusting the pH. The eluted chlorogenic acid can be dried to form a powder (e.g., chlorogenic acid powder). Activated carbon can also be used to facilitate the removal of any materials not sufficiently removed by membrane filtration during the steps after protein isolation. This can include color compounds, trace amounts of chlorogenic acid, trace amounts of metals, etc. The use of activated carbon can include passing the liquid protein stream through an activated carbon layer. However, other uses / processes can also be utilized.

[0100] Solvent-free extraction may be desirable for many reasons. For example, organic solvents may affect the native three-dimensional structure of proteins present in oilseed grains. For example, extraction / processing with such solvents can disrupt the higher-order structure of the protein and / or cause the protein to denature. In processes for extracting proteins for use in industries such as the food industry, disruption of the higher-order structure of the protein can affect the physical properties of the protein, including the physical properties and taste of the protein. For example, sunflower protein may tend to have a relatively sweet flavor, such as can be felt when consuming sunflower seeds. Extracting the protein from sunflower seeds using organic solvents, at more extreme pHs, at higher temperatures, and / or combinations thereof, can result in a protein that does not retain the natural sweetness of sunflower protein. By extraction as disclosed herein, performed at non-extreme pHs and lower temperatures without using organic solvents, protein materials are surprisingly isolated that retain their native three-dimensional structure and have a surprising sweetness.

[0101] The sweetness of sunflower protein can be utilized, for example, in product development and formulations where sweetness is desired. Compared to sucrose with a reference sweetness of 1, the extracted sunflower protein provides an approximate sweetness of 2 - 10 (2 - 10 times sweeter than sucrose) or about 2 - 5 (2 - 5 times sweeter than sucrose). This is different from other carbohydrate-based sweeteners, which have a sweetness similar to that of sucrose and are compared to intense-sweetness sweeteners (or non-nutritive sweeteners) that have a sweetness hundreds of times that of sucrose. Thus, sunflower protein provides a sweetness without the undesirable flavors and aftertastes that may be associated with intense-sweetness sweeteners. Furthermore, the use of such proteins enables the addition of sweetness without dilution (e.g., as bulking agents, fillers, and / or the like), enables the use of less sweetener (e.g., in a lesser amount), enables the addition of sweetness to the product together with / simultaneously with the protein, has a desirable effect on the creaming or whitening color effect, and can provide a longer profile of sweetness perception from the initial sweetness to the completion of the flavor (e.g., without a lingering aftertaste).

[0102] After the first extraction 28, the extracted mixture 30 can be separated using a separation / decanting process. An example of the separation / decanting of the extraction mixture 30 is shown in FIG. 2 using reference numerals 32a, 32b, 32c. The step of separating / decanting the extracted mixture 30 includes transporting the mixture / slurry to a suitable solid / liquid separation unit for a separation / decanting process that separates the extracted mixture 30 into a liquid or aqueous phase 34 (e.g., reference numeral 32a indicates the separation / decanter of the aqueous phase 34) and a solid or undried meal 36 (e.g., reference numeral 32b indicates the separation of the undried meal 36). In some cases, the separation / decanting process can include the use of a decanter centrifuge.

[0103] In some cases, the undried meal 36 can be dried to form a vegetable meal or vegetable powder. Alternatively, the undried meal 36 can be further processed / extracted as discussed herein. In some and other cases of these, the undried meal 36 can be washed one or more times, for example, to increase the yield of the target material and / or to desalt the undried meal 36. For example, water can be mixed with the undried meal and the mixture can be separated / decanted again (e.g., in a manner similar to that disclosed herein). At that time, the aqueous phase (e.g., this phase can contain one or more target materials) can be added to the aqueous phase 34. In some cases, the washed undried meal can be dried to form a vegetable meal or vegetable powder. In other cases, the washed undried meal can be further processed as disclosed herein.

[0104] In addition to the step of separating the aqueous phase 34 from the undried meal 36, the separation / decanting process may separate the seed oil 40 from the extraction mixture 30 (e.g., the aqueous phase of the extraction mixture 30), as indicated by reference numeral 32c. For example, it can be understood that other separation / decanting processes can be utilized, including the use of one or more filters, disk stack centrifuges, sedimentation chambers, combinations thereof, and / or the like. In some cases, an additional centrifugation process 38 (e.g., using a disk stack centrifuge) can be used to remove additional seed oil 40 from the aqueous phase 34. However, this process is considered optional.

[0105] In some cases, the aqueous phase 34 can be mixed with divalent ions such as calcium chloride (CaCl 2 ). At that time, the calcium ions can bind to phytic acid that may be present in the aqueous phase 34 and form an insoluble compound that can precipitate. The resulting solid / precipitate can be separated using a suitable separation device such as a centrifuge, filter, and / or the like. The collected solid (e.g., phytic acid) can be dried using appropriate treatments such as those disclosed herein.

[0106] Adding a specific amount of divalent ions to the starting material results in different levels of phytic acid in the final soluble protein product. As an example, when the feed to the extraction step is 33% protein, 25% oil, 2% CGA, and 3.8% phytic acid, and the divalent ion is calcium chloride, adding calcium chloride at the levels shown in Table 1 below will result in the associated levels of phytic acid being included in the soluble protein product.

[0107]

Table 1

[0108] For proteins extracted / isolated from sunflower seeds disclosed in this specification (e.g., insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (e.g., residual albumin), combinations thereof, and / or the like; and / or soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like, etc.), the amount of phytic acid present in the protein product may correlate with sweetness. More specifically, the more phytic acid present in the protein, the less sweet the protein product. For example, a protein product having a phytic acid content of about 5.5 - 6.5% or about 6% may have a sweetness similar to sucrose. A protein product having a phytic acid content of about 3.5 - 4.5% or about 4% may have a sweetness approximately twice that of sucrose. A protein product having a phytic acid content of about 1.5 - 2.5% or about 2% may have a sweetness approximately five times that of sucrose.

[0109] The aqueous phase 34 can be subjected to one or more filtration processes shown in Figure 2 using reference numerals 42a, 42b. In at least some cases, the filtration process can include ultrafiltration. For example, the filtration process can include a step of using a filter membrane with a nominal pore size of about 600 to 8000 Daltons or about 800 to 2000 Daltons. At that time, the aqueous phase 34 can be separated into a retained component or retained component stream 44 (e.g., material retained on the filter membrane or not passing through the filter membrane by other means) and a permeate component or permeate component stream 46 (e.g., material passing through the filter membrane). The retained component stream 44 can include proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like), and the permeate component stream 46 can include other materials (e.g., chlorogenic acid, minerals, other low molecular weight compounds, and / or the like). In some cases, diafiltered water can be added to further purify the retained component stream 44. In some cases, the retained component stream 44 may be concentrated to have a solids content of about 10 to 40%. 70 to 99% (or more) of the solids may be composed of proteins, about 80 to 95% of the solids may be composed of proteins, or about 85 to 95% of the solids may be composed of proteins. In some cases, the pH of the retained component stream 44 can be adjusted to a pH of about 4 to 7, or a pH of about 5 to 6.5, or a pH of about 5 to 5.5. This can include the addition of a base such as KOH, NaOH, and / or the like or an acid such as H 3 PO 4 , and / or the like.

[0110] The holding component stream 44 can undergo one or more drying processes. For example, the holding component stream 44 can undergo an evaporation process 48. This can include transporting / moving the holding component stream 44 to an evaporator to concentrate the solids. The evaporator can have a liquid output with a solids content of about 20 - 50 wt%. In some cases, the evaporator operates at a temperature of about 120 - 160°F (48 - 72°C) and the vacuum pressure can be about 0.1 - 10 psi.

[0111] The holding component stream 44 (and / or the evaporated holding component stream indicated using reference numeral 50) can undergo one or more additional drying processes such as a drying process 52 (e.g., a spray drying process). For example, the holding component stream 44 and / or the evaporated holding component stream 50 can be transported / moved to a drying device such as a spray dryer, drum dryer, flash dryer, pan dryer, combinations thereof, and / or the like. In some cases, the drying device can reduce the water content to about 10% or less, or about 6% or less, or about 3 - 6% or less. As a result of the drying process 52, a solid product 54 is obtained that includes proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like).

[0112] In some cases, the holding component stream 44 and / or the solid product 54 can be treated with a decolorizing material (e.g., an activated carbon bed, adsorbent, ionic adsorbent, combinations thereof, and / or the like) to remove color compounds from the proteins.

[0113] (For example, the) permeate stream 46 (obtained from filtration process 42b) can be subjected to further filtration processes, indicated in Figure 2 by reference numerals 56a and 56b. In some cases, the filtration process can include nanofiltration. For example, the permeate stream 46 can be conveyed to a nanofiltration membrane having a nominal pore size of about 200 to 800 Daltons or about 300 to 600 Daltons. At that time, the nanofiltration membrane can separate the permeate stream into a second retentate or second retentate stream 58 and a second permeate or second permeate stream 60. In at least some cases, the second retentate 58 can include a target material such as chlorogenic acid. The second permeate 60 can include minerals, salts, and / or the like. In some cases, diafiltered water can be added to further purify the second retentate stream 58. The second retentate 58 can have a solids concentration of about 2 to 20% or more by solids, about 10% or more by solids, or about 5% or more by solids. The solids composition can be about 40 to 80% chlorogenic acid, or about 50 to 80% chlorogenic acid, or about 70 to 80% chlorogenic acid.

[0114] In some cases, the second retentate 58 can undergo one or more drying processes. For example, the second retentate 58 can undergo an evaporation process 62. This can include conveying the second retentate 58 to an evaporator to concentrate the solids. The evaporator can have a liquid output that is about 20 to 50% by weight or about 10 to 20% by weight of solids. In some cases, the evaporator operates at a temperature of about 120 to 160°F (48 to 72°C) and the vacuum pressure can be about 0.1 to 10 psi.

[0115] The second holding component 58 (and / or the evaporated second holding component indicated using reference numeral 64) can undergo one or more additional drying processes such as a drying process 66 (e.g., a spray drying process). For example, the second holding component 58 and / or the evaporated second holding component 64 can be conveyed / transferred to a drying device such as a spray dryer, a drum dryer, a flash dryer, a pan dryer, combinations thereof, and / or the like. In some cases, the drying device can reduce the water content to about 10% or less, or about 6% or less. As a result of the drying process, a solid product 68 containing chlorogenic acid is obtained.

[0116] In some cases, the second permeate 60 can undergo a reverse osmosis process indicated using reference numerals 70a, 70b in FIG. 2. For example, the second permeate component 60 can be sent to a reverse osmosis membrane to separate the salt 72 from the water 74. Thereby, the water 74 can be reused in one or more of the processes disclosed herein, reducing the overall water usage. In some cases, the reverse osmosis membrane can take the form of a high salt concentration retention membrane (e.g., 95% or more). Similar to the water 74, the retained salt 72 can also be reused in one or more of the processes disclosed herein, thereby reducing the overall salt usage.

[0117] The undried meal 36 (e.g., from the separation / decanting process 32b) can be subjected to one or more additional extractions. A flowchart showing a process 76 including a second extraction of the undried meal 36 and recovery of one or more materials from the undried meal 36 is shown in FIG. 3. The process 76 can include a step of mixing the undried meal 36 with an extraction solution to form a mixture 80. The mixing is generally referred to by reference numeral 78 in FIG. 3. In at least some cases, the extraction solution can include water, and the step of mixing the undried meal 36 with the extraction solution can include the step of adding water in a suitable ratio. For example, the undried meal 36 can be mixed with water at a water to undried meal material (e.g., dry weight of the undried meal material) ratio of about 6:1 to 20:1, or at a water to undried meal material (e.g., dry weight of the undried meal material) ratio of about 10:1 to 15:1. In some cases, this ratio can be about 10:1 water to undried meal material. The mixture can be heated to a temperature of about 50 to 200°F (10 to 93°C), or about 100 to 140°F (37 to 60°C), or about 140°F (60°C), or about 130 to 138°F (54 to 59°C). In some cases, the pH is adjusted to about pH 5 to 8 or pH about 5.5 using a suitable acid / base (e.g., a base such as NaOH, KOH, and / or other suitable acid / bases). Salt can also be added to the mixture 80. In some cases, the salt can be NaCl. The salt can be added such that the mixture 80 has a salt concentration of about 0.05 to 2.0 M NaCl, or about 0.1 to 1.0 M NaCl, or about 0.25 to 0.5 M NaCl, or about 0.25 M NaCl. With the mixture 80 adjusted to the desired temperature and salt concentration, the mixture can be held (e.g., held during the extraction period) for about 0.5 to 6 hours or about 2 hours in a suitable container (e.g., a batch tank, a continuous stirred tank, a continuous mixed flow reactor, or the like) to extract the target materials. For example, proteins (e.g., insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (e.g., residual albumin), combinations thereof, and / or the like), chlorogenic acid, and / or other target materials can be extracted into the aqueous phase.The step of holding the mixture to enable extraction of the target material (e.g., the second extraction) is generally denoted using reference numeral 82 in FIG. 3. The result of the second extraction 82 is the extraction mixture 84.

[0118] Similar to the first extraction, in at least some cases, it can be understood that the second extraction 82 is carried out without using an organic solvent that can affect (e.g., decompose) other materials present in the pulverized material. Thus, the second extraction 82 can be carried out without using an organic solvent, or if not, can be considered to be free of organic solvents (e.g., the extraction process is carried out without using an organic solvent). That is, the second extraction may be an extraction without an organic solvent. For example, the second extraction 82 can be carried out without using hexane, or if not, can be considered to be free of hexane (e.g., the extraction process is carried out without using hexane). That is, the second extraction 82 may be an extraction without hexane. In some and other cases of these, the second extraction 82 can be carried out using materials that reduce or minimize the impact on the target substance in the undried meal 36, reduce the environmental impact, and / or reduce the impact on human health. For example, the second extraction can be carried out using a material that reduces or minimizes the impact on chlorogenic acid in the undried meal 36 (e.g., the possibility of decomposition of chlorogenic acid during the second extraction 82 is reduced or minimized). For the purposes of the present disclosure, water is not considered an organic solvent.

[0119] After the second extraction 82, the extracted mixture 84 can be separated using a separation process. The separation process is indicated using reference numerals 86a, 86b, 86c in FIG. 3. The step of separating the extracted mixture 84 involves transporting the mixture / slurry to a suitable solid / liquid separation unit for separation / decanting processing to separate the extracted mixture 84 into a liquid or aqueous phase 88 (e.g., the process is indicated by reference numeral 86a) and a solid or undried meal 90 (e.g., the process is indicated by reference numeral 86b; the undried meal 90 may be further processed). In some cases, the separation process can include the use of decanting and / or a decanter centrifuge. In addition to the step of separating the aqueous phase 88 from the undried meal 90, the separation / decanting process may separate the seed oil 40 from the extracted mixture 84 as indicated by reference numeral 32c. It can be understood that other separation / decanting processes, including the use of one or more filters, disk stack centrifuges, sedimentation chambers, combinations thereof, and / or the like, may also be utilized. In some cases, additional centrifugation processing 92 (e.g., using a disk stack centrifuge) can be used to remove additional seed oil 40 from the aqueous phase 88. However, this processing is considered optional.

[0120] The undried meal 90 can be washed, for example, to reduce the salt content. At that time, water can be added in a ratio of 5:1 to 20:1 or about 10:1. The washed undried meal 90 can then be sent to a solid-liquid separation process and then the meal can be dried to form, for example, vegetable powder. The drying step can include the use of a roll dryer, flash dryer, ring dryer, combinations thereof, and / or the like.

[0121] The aqueous phase 88 can be subjected to a precipitation treatment 92. For example, the pH of the aqueous phase 88 can be adjusted to about 3 - 5 or about 4 - 4.25 by adding a suitable acid / base (e.g., HCl). Proteins present in the aqueous phase 88 can be insolubilized and precipitated. The materials are mixed and conveyed / transferred to a liquid-solid separation unit. The precipitated protein stream indicated by reference numeral 94 can be separated into a liquid 98 (e.g., the separation process is indicated by reference numeral 96a) and a solid, protein precipitate 100 (e.g., this process is indicated by reference numeral 96b). This can include steps of using a filter, a centrifuge, combinations thereof, and / or the like. The solid fraction 100 can be recovered and further washed. The liquid 98 can undergo further filtration treatment. For example, the liquid 98 can undergo microfiltration and / or ultrafiltration treatment (e.g., indicated by reference numerals 102a, 102b in Figure 3). This can include the use of an ultrafiltration membrane with a pore size of about 10 - 2000 kDa or about 30 - 80 kDa that can separate the liquid into a permeate component 104 and a retained component 106. The retained component 106 can include additional proteins obtained from the liquid that did not precipitate during the precipitation treatments 96a, 96b. The permeate component 104 can be subjected to a reverse osmosis membrane treatment (e.g., indicated by reference numerals 108a, 108b in Figure 3). For example, the permeate component 104 can be sent to a reverse osmosis membrane to separate the salt 72 from the water 74. Thereby, the water 74 can be reused in one or more of the processes disclosed herein, reducing the overall water usage. In some cases, the reverse osmosis membrane can be in the form of a high salt retention membrane (e.g., 95% or more). Similar to the water 74, the retained salt 72 can also be reused in one or more of the processes disclosed herein, thereby reducing the overall salt usage.

[0122] The solid content 100 obtained from the separation process 96b can be washed using the washing process 110 to form a washed protein slurry 112. At that time, a step of adding water to remove salts and other substances from the protein can also be included. In some cases, water may be added to a water-to-dry weight ratio of 10:1 to 100:1, or a water-to-dry weight ratio of about 50:1. The pH may be adjusted according to the conditions from the precipitation state, and the slurry can be further subjected to a separation process. In some cases, the washing process 110 and the separation process 96b can be combined in a single step.

[0123] The washed protein slurry 112 can be further subjected to a separation process (e.g., indicated by reference numerals 114a, 114b in FIG. 3). The separation can separate the washed protein slurry 112 into a solid fraction 116 and a liquid 122. This can include steps of using filters, centrifuges, combinations thereof, and / or the like. When a centrifuge is used, the solid fraction 116 can be subjected to a drying process 118. For example, the solid fraction 116 can be conveyed / moved to a drying device such as a spray dryer, drum dryer, flash dryer, pan dryer, combinations thereof, and / or the like. The solid fraction 106 (e.g., obtained from the filtration process 102a) can also be subjected to the same or a similar drying process 118. In some cases, the drying process can reduce the water content to about 10% or less, or about 6% or less. The products resulting from the drying process 118 can be combined to form a solid product 120 containing proteins (e.g., insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (e.g., residual albumin), combinations thereof, and / or the like). The liquid 122 obtained from the separation process 114b can be subjected to a reverse osmosis membrane. Thereby, water can be reused one or more times in the processes disclosed herein, thereby reducing the overall water usage. In some cases, the reverse osmosis membrane can be in the form of a high salt retention membrane (e.g., 95% or more). Similar to water, the retained salt can also be reused one or more times in the processes disclosed herein, thereby reducing the overall salt usage amount.

[0124] Referring to FIGS. 1-3, the extraction process described above can be described as a two-step extraction process. For example, by the first extraction, proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like) and chlorogenic acid are separated from the aqueous phase 34, and by the second extraction, proteins (e.g., insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (e.g., residual albumin), combinations thereof, and / or the like) are separated from the undried meal 36.

[0125] Other processes using fewer or more extractions are also conceivable. For example, as shown in FIG. 4, a single extraction process 123 is conceivable. In such a process, many steps similar to those described above (some of which are not shown in FIG. 4) can be performed. For example, the raw oilseed 12 can be processed as described with reference to FIG. 1 to form a pulverized material 20. The pulverized material 20 can be mixed with an extraction mixture (e.g., similar to those described above) and extracted. The extracted mixture 30 can be separated into an aqueous phase 34 and an undried meal 36 through a separation / decanting process (e.g., similar to those described above).

[0126] In some cases, the aqueous phase 34 can be mixed with divalent ions such as calcium chloride (CaCl 2 ). At this time, the calcium ions can bind to phytic acid that may be present in the aqueous phase 34 and become an insoluble compound that can precipitate. The resulting solid / precipitate can be separated by a suitable separation device such as a centrifuge, filter, and / or the like. The collected solid (e.g., phytic acid) can be dried using an appropriate treatment such as those disclosed herein.

[0127] In a single extraction process 123, the aqueous phase 34 can undergo a series of filtration processes that can be similar to those disclosed herein to isolate the target substance. For example, a first filtration process (indicated by reference numerals 124a, 124b) can filter the aqueous phase (forming a permeate component or filtered aqueous phase 126) and remove insoluble particles and / or oil 128 (which can be recovered, for example, as a processed meal) from the aqueous phase 34. The first filtration process can be considered a microfiltration process using a filter with a pore size in the range of about 0.05 to 2 microns, or about 0.2 microns. In some cases, the filter can be a cross-flow filtration unit, a dead-end filter, and / or the like. When using a cross-flow filtration unit, diafiltration can be used to increase the recovery of the target material in the filtered aqueous phase 126.

[0128] The filtered aqueous phase 126 can undergo another filtration process (indicated by reference numerals 130a, 130b) to separate the filtered aqueous phase 126 into a retained component 132 and a permeate component 134. The filtration processes 130a, 130b can take the form of ultrafiltration processes. The retained component 132 can be processed by an evaporation process 136 to form an evaporated retained component 138 and / or can undergo a drying process 140 to form a dried material 142. The dried material 142 can include proteins (such as insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (such as residual albumin), combinations thereof, and / or the like).

[0129] The permeate component 134 may be separated into a retained component 146 and a permeate component 148 through another filtration process (indicated by reference numerals 144a, 144b). The filtration processes 144a, 144b can take the form of ultrafiltration and / or nanofiltration processes. The retained component 146 can be processed by an evaporation process 150 to form an evaporated retained component 152 and / or can pass through a drying process 154 to form a dried material 156. The dried material 156 may contain proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like).

[0130] The permeate component 148 may be separated into a retained component 160 and a permeate component 162 through another filtration process (indicated by reference numerals 158a, 158b). The filtration processes 158a, 158b can take the form of nanofiltration processes. The retained component 160 can be processed by an evaporation process 164 to form an evaporated retained component 166 and / or can pass through a drying process 168 to form a dried material 170. The dried material 170 may contain chlorogenic acid.

[0131] It can be understood that the various processes constituting the single extraction process 123 can utilize the processes disclosed herein, such as oil removal, centrifugation, diafiltration, reverse osmosis for recovering water and / or salts, and / or the like.

[0132] Also, as shown in FIG. 5, three extraction processes 172 are also conceivable. For example, the raw oilseed 12 can be processed as described with reference to FIG. 1 to form a ground material 20. The ground material 20 can be mixed with an extraction mixture (e.g., similar to those described above) and extracted. The extracted mixture 30 can be separated into an aqueous phase 34 and an undried meal 36 (e.g., as indicated by reference numeral 32a) through a separation / decanting process (e.g., similar to those described above).

[0133] In some cases, the aqueous phase 34 can undergo a centrifugation step as described above, which can help remove oil from the aqueous phase 34. In some cases, the aqueous phase 34 can be mixed with divalent ions such as calcium chloride (CaCl 2 ). At this time, calcium ions can bind to phytic acid that may be present in the aqueous phase 34, resulting in an insoluble compound that can precipitate. The resulting solid / precipitate can be separated by a suitable separation device such as a centrifuge, filter, and / or the like. The collected solid (e.g., phytic acid) can be dried using appropriate treatments such as those disclosed herein.

[0134] The aqueous phase 34 may undergo a filtration process 174. In some cases, the filtration process 174 can be a nanofiltration process and / or an ultrafiltration process. For example, the aqueous phase 34 can be carried / moved to a nanofiltration member having a nominal pore size of about 200 - 800 Daltons or about 300 - 600 Daltons. At this time, the nanofiltration membrane can separate the retained component 176 from the aqueous phase 34. In at least some cases, the retained component 176 can contain a target material such as chlorogenic acid. The retained component 176 can have a solid concentration of about 2 - 20% or more by solids content, about 10% or more by solids content, or about 5% or more by solids content. The composition of the solids content can be about 40 - 80% chlorogenic acid, or about 50 - 80% chlorogenic acid, or about 70 - 80% chlorogenic acid.

[0135] In some cases, the retained component 176 can undergo one or more drying treatments. For example, the retained component 176 can undergo an evaporation process 178. This can include the step of carrying / moving the retained component 176 to an evaporator to concentrate the solids content. The evaporator can have a liquid output of about 20 - 50% by weight or about 10 - 20% by weight of solids content. In some cases, the evaporator operates at a temperature of about 120 - 160°F (48 - 72°C) and the vacuum pressure can be about 0.1 - 10 psi.

[0136] The holding component 176 (and / or the evaporated holding component represented using reference numeral 180) can undergo one or more additional drying processes such as a drying process 182 (e.g., a spray drying process). For example, the holding component 176 and / or the evaporated holding component 180 can be conveyed / transferred to a drying device such as a spray dryer, a drum dryer, a flash dryer, a pan dryer, combinations thereof, and / or the like. In some cases, the drying device can reduce the water content to about 10% or less, or about 6% or less. As a result of the drying process, a solid product 184 containing chlorogenic acid is obtained.

[0137] The undried meal 36 can undergo a second extraction process. The second extraction process can be similar to other extraction processes disclosed herein. For example, the undried meal 36 can be mixed with water at a water to undried meal material (e.g., dry weight of the undried meal material) ratio of about 6:1 to 20:1, or a water to undried meal material (e.g., dry weight of the undried meal material) ratio of about 10:1 to 15:1. In some cases, this ratio can be about 10:1 water to undried meal material. The mixture can be heated to a temperature of about 50 to 200°F (10 to 93°C), or about 100 to 140°F (37 to 60°C), or about 140°F (60°C), or about 130 to 138°F (54 to 59°C). In some cases, the pH is adjusted to about pH 2 to 8, or about pH 3 to 6, or about pH 4.0 using a suitable acid / base (e.g., an acid such as HCl, a base such as NaOH or KOH, and / or other suitable acid / bases). Salt can also be added to the mixture. In some cases, the salt can be NaCl. The salt can be such that the mixture is about 0.05 to 2.0 M NaCl, or about 0.1 to 1.0 M NaCl, or about 0.25 to 0.5 M NaCl, or about 0.25 M It can be added to have the salt concentration of NaCl. With the mixture adjusted to the desired temperature and salt concentration, the mixture is held (e.g., held during the extraction period) in a suitable container (e.g., a batch tank, a continuous stirred tank, a continuous mixed flow reactor, or the like) for about 0.5 to 6 hours or about 2 hours to extract the target material. For example, proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like) and / or other target materials can be extracted into the aqueous phase.

[0138] The extracted undried meal 36 can be separated into an aqueous phase 188 and a second undried meal 189 (as shown, for example, by reference numeral 186a) through a separation / decanting process (similar to those described above, for example).

[0139] The filtration process 190 can filter the aqueous phase 188 to form a retained component 192. The filtration process 190 can be considered a nanofiltration process using a filter with a pore size in the range of about 200 to 800 Daltons or about 300 to 600 Daltons.

[0140] The retained component 192 is processed by an evaporation process 194 to form an evaporated retained component 196 and / or is subjected to a drying process 198 to form a dried material 200. The dried material 200 may contain proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like).

[0141] The second undried meal 189 may undergo a third extraction similar to that described above. For example, the second undried meal 189 can be mixed with water at a water to undried meal material (e.g., dry weight of the undried meal material) ratio of about 6:1 to 20:1, or a water to undried meal material (e.g., dry weight of the undried meal material) ratio of about 10:1 to 15:1. In some cases, this ratio can be about 10:1 water to undried meal material. The mixture can be heated to a temperature of about 50 - 200°F (10 - 93°C), or about 100 - 140°F (37 - 60°C), or about 140°F (60°C), or about 130 - 138°F (54 - 59°C). In some cases, the pH is adjusted to about pH 5 - 8 or pH about 5.5 using a suitable acid / base (e.g., an acid such as HCl, a base such as NaOH or KOH, and / or other suitable acid / base). Salt may also be added to the mixture. In some cases, the salt can be NaCl. The salt can be added such that the mixture has a salt concentration of about 0.05 - 2.0M NaCl, or about 0.1 - 1.0M NaCl, or about 0.25 - 0.5M NaCl, or about 0.25M NaCl. With the mixture adjusted to the desired temperature and salt concentration, the mixture can be held (e.g., held during the extraction period) for about 0.5 - 6 hours or about 2 hours in a suitable container (e.g., a batch tank, a continuous stirred tank, a continuous mixed flow reactor, or the like) to extract the target material. For example, proteins (e.g., insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (e.g., residual albumin), combinations thereof, and / or the like), chlorogenic acid, and / or other target materials can be extracted into the aqueous phase.

[0142] The extracted second undried meal 189 can be separated, via a separation / decanting process (e.g., similar to that described above), into an aqueous phase 204 and a third undried meal 206 (e.g., as indicated by reference number 202a and 202b, respectively). The third undried meal can be dried to form a vegetable meal or vegetable powder.

[0143] The filtration process 208 can filter the aqueous phase 204 to form the retained component 210. The filtration process 208 can be considered an ultrafiltration process using a filter with a pore size in the range of about 10 to 2000 kDa or about 30 to 80 kDa. When using a cross-flow filtration unit, diafiltration can be used to increase the recovery of the target material in the retained component 210.

[0144] The retained component 210 is processed by an evaporation process 212 to form the evaporated retained component 214 and / or is dried through a drying process 216 to form a dried material 218. The dried material 218 may contain proteins (such as insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (such as residual albumin), combinations thereof, and / or the like).

[0145] In some cases, the permeate component of the filtration process 208 can be sent to an adsorption column filled with adsorption beads, such as adsorption beads that selectively adsorb chlorogenic acid and allow most other substances to pass through. Then, chlorogenic acid can be eluted from the column using a pH swing or another solvent such as ethanol. Other permeate components disclosed herein can be treated similarly, such as the permeate component through a microfiltration membrane / filter or the permeate component through an ultrafiltration membrane / filter.

[0146] Many uses for the extraction / isolation substances disclosed herein and / or for the processes disclosed herein are contemplated. Possible uses include the use of the extracted and isolated substances in food.

[0147] As an example of use, it is a vegetable cheese. The vegetable cheese can contain soluble sunflower proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like) isolated / extracted from sunflower seeds using the processes disclosed herein. The soluble sunflower proteins (e.g., about 0.5 - 5%, or about 1 - 3%, or about 2.0%) can be combined with one or more of other materials such as almond milk (e.g., about 20 - 40%, or about 25 - 35%, or about 31.8%), coconut oil (e.g., about 2 - 10%, or about 4 - 6%, or about 5.2%), potato starch (e.g., about 2 - 10%, or about 4 - 6%, or about 5.2%), tapioca flour (e.g., 2 - 10%, or about 3 - 5%, or about 4.0%), nutritional yeast (e.g., about 1 - 3%, or about 1.5 - 1.8%, or about 1.6%), xanthan gum (e.g., about 0.01 - 1%, or about 0.05 - 0.15%, or about 0.1%), and salt (e.g., about 0.1 - 2%, or about 0.5 - 1.5%, or about 0.6%) (e.g., using a blender or other suitable mixing device). The given percentages are weight percentages relative to all starting materials. This combination (e.g., the almond milk mixture) can be mixed / blended until it reaches the desired creamy consistency.

[0148] Separately, the agar solution can be formed by combining water (e.g., about 30 - 60%, or about 40 - 50%, or about 45.7%) and agar (e.g., about 2 - 6%, or about 3 - 4.5%, or about 3.9%) and heating until the agar dissolves. The agar solution can be further cooked (e.g., simmer with a lid) until thickened.

[0149] The almond milk mixture may be combined with a thickened agar solution. This can include adding a portion (e.g., about half) of the almond milk mixture to the thickened agar solution while mixing, and then adding the remainder of the almond milk mixture. This is done over low heat until the mixture peels away from the sides of the heating vessel, whereby a plant-based cheese can be formed. The plant-based cheese can be cooled (e.g., placed in a suitable container and refrigerated).

[0150] Another example of use is a plant-based ice cream. The plant-based ice cream can contain soluble sunflower proteins (e.g., soluble proteins, low molecular weight proteins, albumin, combinations thereof, and / or the like) isolated / extracted from sunflower seeds using the processes disclosed herein and insoluble sunflower proteins (e.g., insoluble proteins, high molecular weight proteins, helianthinin, globulin, albumin (e.g., residual albumin), combinations thereof, and / or the like) isolated / extracted from sunflower seeds using the processes disclosed herein. The insoluble sunflower protein (e.g., about 1-8%, or about 2-6%, or about 4%) and the soluble sunflower protein (e.g., about 0.5-5%, or about 1-3%, or about 2%) can be combined with a stabilizer (e.g., GRINDSTED stabilizer blend; about 0.1-1%, or about 0.2-0.6%, or about 0.4%), pea starch (e.g., about 0.1-3%, or about 0.5-1.5%, or about 1%) while vigorously shaking until completely incorporated. Other ingredients such as almond milk (e.g., about 10-50%, or about 20-40%, or about 30%), coconut water blend (e.g., about 5-30%, or about 10-20%, or about 14%), sugar (e.g., about 1-10%, or about 4-8%, or about 6%), and allulose (1-30%, or about 5-15%, or about 10%) etc. can be added and thoroughly mixed. Sunflower oil (e.g., about 1-30%, or about 5-15%, or about 10%) can be added and stirred with a powerful impeller type stirrer / mixer to form an emulsion. This emulsion was slowly heated while stirring and heated to 163°F (73°C). Then, the emulsion was quenched to a temperature below 70°F while stirring using an ice bath.

[0151] The cooled mixture was then placed into a personal or commercially available ice cream machine (e.g., according to the manufacturer's guidelines) to form ice cream. Another example of use is protein - fortified chocolate milk. The protein - fortified chocolate milk can contain soluble sunflower proteins (e.g., soluble proteins, low - molecular - weight proteins, albumin, combinations thereof, and / or the like) isolated / extracted from sunflower seeds using the processes disclosed herein. The soluble sunflower proteins can be combined with milk, cocoa (e.g., about 0.5 - 5%, or about 1 - 3%, or about 1.5%), calcium carbonate (e.g., about 0.1 - 2%, or about 0.2 - 0.8%, or about 0.5%), cellulose gel (e.g., about 0.05 - 1%, or about 0.1 - 0.5%, or 0.3%), natural and artificial flavorings (e.g., about 0.05 - 1%, or about 0.1 - 0.5%, or about 0.2%), salts (e.g., about 0.05 - 1%, or about 0.1 - 0.5%, or about 0.15%), carrageenan (e.g., about 0.01 - 0.5%, or about 0.08 - 0.12%, or about 0.1%) and cellulose gum (e.g., about 0.01 - 0.5%, or about 0.08 - 0.12%, or about 0.1%).

[0152] In some cases, the amount of phytic acid in the soluble sunflower protein can be controlled to adjust the sweetness of the protein-enriched chocolate milk. For example, the soluble sunflower protein can have a phytic acid content of about 1 to 8 wt%, or about 2 to 6 wt%. In some cases, a soluble sunflower protein having a sweetness approximately equal to sucrose and containing 6 wt% phytic acid (e.g., about 1 to 10%, or about 4 to 5%, or about 4.4%) can be combined with milk (e.g., 1% milk; about 80 to 96% or about 90 to 95% or about 92.75%) and the remaining components described above. In some cases, a soluble sunflower protein having a sweetness approximately twice that of sucrose and containing 4 wt% phytic acid (e.g., about 0.5 to 5%, or about 1 to 3%, or about 2.17%) can be combined with milk (e.g., 1% milk; about 85 to 98%, or about 94 to 96%, or about 94.98%) and the remaining components described above. In some cases, a soluble sunflower protein having a sweetness approximately five times that of sucrose and containing 2 wt% phytic acid (e.g., about 0.1 to 2%, or about 0.5 to 1.5%, or about 0.8%) can be combined with milk (e.g., 1% milk; about 85 to 99%, or about 94 to 97%, or about 96.35%) and the remaining components described above. These are just examples. Other compositions are contemplated.

[0153] Another example of use is a protein-enriched sports drink. The protein-enriched sports drink can include a soluble sunflower protein isolated / extracted from sunflower seeds (e.g., soluble protein, low molecular weight protein, albumin, combinations thereof, and / or the like) using the processes disclosed herein. The soluble sunflower protein can be combined with water, electrolytes (e.g., electrolyte solutions and / or suitable salts), and other substances (e.g., natural and / or artificial flavors, natural and / or artificial colorants, sugars and / or sugar substitutes, and / or the like).

[0154] In some cases, the amount of phytic acid in the soluble sunflower protein can be controlled to adjust the sweetness of the protein - fortified sports drink. In some cases, the amount of sugar and / or sugar substitute added to the protein - fortified sports drink can be reduced. In some of these cases and other cases, due to the sweetness of the soluble sunflower protein, it may be possible to substantially add no sugar or sugar substitute to the protein - fortified sports drink. For example, the soluble sunflower protein can have a phytic acid content of about 1 - 8 wt%, or about 2 - 6 wt%. In some cases, a soluble sunflower protein having a sweetness approximately equal to sucrose and containing 6 wt% phytic acid can be combined with water, electrolytes, and other desirable components. In some cases, a soluble sunflower protein having a sweetness approximately twice that of sucrose and containing 4 wt% phytic acid can be combined with water, electrolytes, and other desirable components. In some cases, a soluble sunflower protein having a sweetness approximately five times that of sucrose and containing 2 wt% phytic acid can be combined with water, electrolytes, and other desirable components. These are just examples. Other compositions are conceivable.

[0155] The resulting protein - fortified sports drink can have a desirable transparency (e.g., be free of turbidity or generally have a reduced level of turbidity). Further, by using the soluble sunflower protein, it may be possible to have a higher level of protein per about 28 grams (1 ounce). For example, the resulting protein - fortified sports drink can have about 0.75 - 1.5 grams of protein per about 28 grams (1 ounce) of the sports drink, or about 1 gram of protein per about 28 grams (1 ounce) of the sports drink.

Example

[0156] The present disclosure may be further clarified by reference to the following examples, some of which are anticipatory in nature, serve to illustrate some embodiments, and in no way limit the present disclosure in any case.

[0157] Example 1 Extraction of Albumin, Chlorogenic Acid (CGA), Phytic Acid, and Helianthin from Sunflower Seeds Sunflower seeds were obtained as a commercial product. The sunflower seeds were dehulled, cold-pressed, and ground. The ground material was substantially subjected to an extraction process as disclosed herein with reference to FIG. 4. At that time, albumin, chlorogenic acid, phytic acid, and helianthinin were isolated from the sunflower seeds.

[0158] The ground seeds were mixed with water at a water to dry weight ratio of 10:1, NaCl was added to make a 0.5 M NaCl solution, and the mixture was heated to about 59 °C (138 °F) and mixed for 2 hours. After 2 hours, the slurry was separated using a decanter centrifuge. The solid stream was mixed with water at a water to dry weight ratio of 10:1 and decanted again while combining the liquid streams from the first and second decanters. The solid stream was dried to form sunflower meal. This liquid stream was CaCl at 2.5 wt% of the meal in the first extraction slurry 2It was mixed. Next, the pH was raised to 5.8 using NaOH, and it was sent to a three-phase disk stack centrifuge. The oil / oil:water emulsion was recovered as the light stream, an aqueous stream containing proteins (albumin and helianthinin) and CGA was recovered, and a wet solid stream was discharged. The aqueous stream was sent to a 0.2-micron precision filtration membrane, and after concentrating the stream up to 4 times, diafiltration water was added. The diafiltration water was added in an amount 0.25 times the initial volume of the stream sent to the membrane. The retained components were composed of large particles (mainly sunflower meal and oil not separated by the disk stack centrifuge), and the clarified permeate components contained proteins and CGA. Then, the permeate components were sent to a 30 kDa ultrafiltration membrane. The retained components were concentrated up to 5 times the starting volume, and diafiltration water was added in an amount 0.5 times the amount of the material sent to the ultrafiltration membrane. The retained components contained helianthinin, and the permeate components contained albumin and CGA. The retained components were sent to an evaporator to concentrate the solids to 15%, and then sent to a flash dryer to create a dried insoluble sunflower protein powder with 90% by weight of protein. The permeate components were sent to a 1 kDa ultrafiltration membrane. The retained components were concentrated up to 10 times the starting volume, and diafiltration water was added in an amount 0.5 times the amount of the material sent to the membrane. The retained components contained albumin, and the permeate components contained CGA. The retained components were sent to an evaporator to concentrate the solids to 40% by weight, and then sent to a spray dryer to create a dried soluble sunflower protein with 90% by weight of protein. The permeate components were sent to a 300 Da nanofiltration membrane and concentrated up to 20 times. Diafiltration water was added in an amount 0.25 times the amount of the material sent to the membrane. The permeate components mainly contained NaCl, and the retained components contained CGA. A large amount of the CGA retained components was sent to an evaporator to concentrate the solids to 10%, and then sent to a spray dryer to produce a dried CGA powder with 60% by weight of CGA.

[0159] Example 2 Extraction of Albumin, Chlorogenic Acid (CGA), Phytic Acid, and Helianthinin from Sunflower Seeds Sunflower seeds were obtained as a commercial product. The sunflower seeds were dehulled, cold-pressed, and ground. The ground material was substantially subjected to an extraction process as disclosed herein with reference to FIGS. 1-3. At that time, albumin, chlorogenic acid, phytic acid, and helianthinin were isolated from the sunflower seeds.

[0160] The ground and pressed seeds were mixed with water at a water to dry weight ratio of 10:1, NaCl was added to make a 0.5 M NaCl solution, the pH was adjusted to 4.0 and maintained, and it was heated to about 59 °C (138 °F) and mixed for 2 hours. After 2 hours, the slurry was separated using a decanter centrifuge. The solid stream was mixed with water at a water to dry weight ratio of 10:1 and decanting was performed again while combining the liquid streams from the first and second decanters. The solid stream was retained for further extraction. The liquid streams from both decanters were sent to a three-phase clarifying disk stack centrifuge to remove residual oil and residual insoluble solids. The clarified stream was sent to a 0.1 micron precision filtration membrane to remove any residual oil or insoluble species. The permeate component was mixed with calcium chloride and sent to a disk stack centrifuge to remove precipitated phytic acid. The collected solids were dried in a fluidized bed dryer to form a dry calcium phytate powder. Next, the liquid stream obtained from the disk stack centrifuge was sent to a 1 kDa ultrafiltration membrane, and diafiltration water was added at a rate of 0.5 times the amount of the material sent to the membrane to pass chlorogenic acid through the permeate component. The retained component contained albumin and the permeate component contained CGA. The retained component was sent to an evaporator to concentrate the solids to 40 wt% and then sent to a spray dryer to create a dried soluble sunflower protein with 90 wt% protein. The permeate component was sent to a 300 Da nanofiltration membrane and concentrated up to 20 times. Diafiltration water was added at 0.25 times the amount of the material sent to the membrane. The permeate component mainly contained NaCl and the retained component contained CGA. A large amount of the CGA retained component was sent to an evaporator to concentrate the solids to 10% and then sent to a spray dryer to produce a dried CGA powder with 60 wt% CGA.

[0161] The retained solid stream obtained from the second decanter was mixed with water at a ratio of 15:1, NaCl was added to make a 0.5 M NaCl solution, the pH was adjusted to 5.8 and maintained, and it was heated to about 59 °C (138 °F) and mixed for 2 hours. After 2 hours, the slurry was separated using a decanter centrifuge. The solid stream was mixed with water at a water to dry weight ratio of 10:1, and decanting was performed again while combining the liquid streams from the first and second decanters. The solid stream was dried to form sunflower meal. The combined liquid streams were passed through a 0.1 micron precision filtration membrane to remove any lipids / oils and insoluble species. The permeate component was mixed with hydrochloric acid to adjust the pH to 4.0, and the precipitate was recovered using a decanter centrifuge. The solid stream was retained. The liquid stream was sent to a 30 kDa ultrafiltration membrane to retain the remaining protein and pass the salts through as the permeate component. Diafiltration water was added in an amount 0.5 times that of the feed. The retained component was sent to an evaporator to concentrate the solids to 15%, and then it was mixed with the retained solids obtained from the precipitation step and sent to a flash dryer to create a dried insoluble sunflower protein powder that was 90% by weight protein.

[0162] Example 3 Emulsification Soluble proteins were isolated / extracted from sunflower seeds using the processes disclosed herein. The proteins may be used as emulsifiers. For example, the proteins can be mixed with many different oils to form vegetable mayonnaise, creamy dressings, milk without dairy components, and / or the like. For example, 6 g of protein isolated from sunflower seeds using the processes disclosed herein was mixed with 14 g of water. The mixture was added to a hood processor. The hood processor was switched on, and 1 / 2 cup of canola oil was slowly added to the mixture over approximately 2 minutes. After all the oil was added, the resulting mixture, which could take the form of mayonnaise, was processed for an additional 30 seconds.

[0163] Example 4 Bubble stability Soluble proteins were isolated / extracted from sunflower seeds using the processes disclosed herein. Using this protein, the ability to form stable foam was tested. The foam stability test was conducted at three pH levels, namely pH 4, natural pH (5.5), and pH 7. To test the foam stability, 20 mL of a 0.5% solids solution of the soluble protein was placed in a 400 mL beaker. The 0.5% solids solution contained soluble proteins isolated / extracted from sunflower seeds using the processes disclosed herein. The liquid was frothed for 1 minute using a Bodum Schiuma handheld Milk Frother. Then, the foam was transferred to a 250 mL graduated cylinder. The initial foam volume was recorded. The foam volume was recorded every minute for 10 minutes. The foam stability test was conducted at room temperature (21 °C).

[0164] The first trial was conducted to determine the foam stability of the soluble protein. In the first trial, it was demonstrated that the soluble protein was able to maintain stable foam over a long period of time. In particular, at pH 4 and pH 5.5, the soluble protein was able to maintain 72% and 76% of the original foam volume, respectively, after 10 minutes. The results of this foam stability test are shown in Table 2.

[0165]

Table 2

[0166] The second trial was conducted to determine the foam stability of the soluble protein. In the second trial as well, it was demonstrated that the soluble protein was able to maintain stable foam over a long period of time. In particular, at pH 4, the soluble protein was able to maintain 56% of the original foam volume after 10 minutes. The results of this foam stability test are shown in Table 3.

[0167]

Table 3

[0168] Example 5 Mixed beverage Soluble protein was isolated / extracted from sunflower seeds using the processes disclosed herein. An isolated protein (78.3%), cocoa powder (11.6%), sugar (5.8%), xanthan gum (2.0%), salt (1.2%), vanilla extract (0.9%), and lacanka extract (0.2%) were combined to form a powder mix. 35 g of the powder mix was mixed / blended with approximately 340 grams (12 ounces) of water to form a beverage.

[0169] Example 6 High-protein cracker Soluble protein was isolated / extracted from sunflower seeds using the processes disclosed herein. A mixture was formed by combining soluble protein (12.2%), wheat flour (49.3%), unsalted butter (20.10%), water (15.8%), and baking soda (2.5). More specifically, the wheat flour, soluble protein, and baking soda were mixed until well combined, and then the chilled butter was incorporated until well combined. Water (room temperature) was added and the dough was kneaded until smooth. The dough was shaped into a desired shape (e.g., rectangle), wrapped in vinyl, and allowed to rest for 30 minutes. The shaped dough was rolled out to a thickness of approximately 1.6 millimeters (about 1 / 16 inch) and then baked for about 7 minutes. In some cases, the rolled-out dough was lightly coated with olive oil and sprinkled with sea salt before baking.

[0170] Example 7 High-protein chocolate chip cookie The soluble protein was isolated / extracted from sunflower seeds using the processes disclosed herein. A mixture was formed by combining soluble protein (13.29%), wheat flour (27.79%), semi-sweet chocolate chips (18.92%), eggs (11.98%), unsalted butter (11.19%), granulated sugar (8.13%), light brown sugar (8.13%), vanilla extract (0.21%), baking soda (0.21%), and salt (0.15%). More specifically, the granulated sugar, butter, vanilla, and eggs were mixed together, and then the wheat flour, soluble protein, baking soda, and salt were added to form the dough. The chocolate chips were added. The dough was formed into balls and baked at about 180 °C (350 °F) for about 8 - 9 minutes.

[0171] Example 8 Chocolate Peanut Butter Protein Bar The soluble protein was isolated / extracted from sunflower seeds using the processes disclosed herein. A mixture was formed by combining soluble protein (22.6%), quick oats (15.13%), almonds (15.13%), peanut butter (12.10%), chocolate chips (10.92%), dates (9.43%), maple syrup (5.26%), water (4.52%), cocoa powder (3.77%), vanilla extract (0.66%), and salt (0.53%). More specifically, the dates, quick oats, and almonds were processed using a food processor until the dates were in pea-sized pieces. The soluble protein and cocoa powder were added and the mixture was processed further. The chocolate chips were melted and added to the mixture along with the remaining ingredients. The mixture was processed until well combined. The processed mixture was placed between two sheets of cooking parchment and rolled out to a thickness of about 1.3 centimeters (half an inch). Then, using a knife, the material was cut into bars.

[0172] Example 9 Food / Beverage Using Soluble Protein Soluble proteins were isolated / extracted from sunflower seeds using the processes disclosed herein. Using this protein, a number of different beverages can be formed, including plant-based milks, protein drinks, nutritional / protein bars, confections, and / or the like.

[0173] Example 10 Other Uses The protein isolated / extracted from sunflower seeds using the processes disclosed herein can be used as an emulsifier (i.e., a food component that aids in the formation and stabilization of emulsions). An emulsion is a stable, water-in-oil or oil-in-water mixture that imparts texture and flavor to a food system. Foods that can utilize such isolated / extracted sunflower protein can include mayonnaise, creamy dressings, milk without dairy components, and beverages containing oil as a component.

[0174] The protein isolated / extracted from sunflower seeds using the processes disclosed herein can be used as a foam stabilizer. Foams are stable mixtures of air in a liquid where the protein helps to form and stabilize the structure. Foods that can utilize such isolated / extracted sunflower protein can include meringue, whipped cream, dairy foams (such as the foam on cappuccino coffee, mousse, dairy desserts, etc.), and ice cream (e.g., those with foam structure elements).

[0175] The protein isolated / extracted from sunflower seeds using the processes disclosed herein can be used as a gelling agent. When the protein cross-links and imparts viscosity and stability to a solution, a protein gel is formed, including in solid form. Foods that can utilize such isolated / extracted sunflower protein can include salad dressings, gelatin snacks, and the like.

[0176] The proteins isolated / extracted from sunflower seeds using the processes disclosed herein can be used as a thickening agent. The proteins form cross-links and interact with other food components to impart viscosity. Foods that can utilize such isolated / extracted sunflower proteins include beverages, sauces, dairy analogs, flavor enhancers, enhancers that affect the mouthfeel, etc.

[0177] The proteins isolated / extracted from sunflower seeds using the processes disclosed herein can be used as a flavor enhancer. The proteins isolated / extracted from sunflower seeds using the processes disclosed herein can be used as a soluble protein product that can affect the taste, texture, and appearance of the resulting food and / or beverage. Foods that can utilize such isolated / extracted sunflower proteins include plant-based milk, protein beverages (e.g., ready-to-drink beverages), nutrition bars, protein confectioneries, etc.

[0178] The proteins isolated / extracted from sunflower seeds using the processes disclosed herein can be used for their water retention properties. Water retention is the ability of a food to hold itself or added water during the application of force, pressure, centrifugation, heating, etc. to the food. Foods that can utilize such isolated / extracted sunflower proteins include meat substitutes, soy substitutes, etc.

[0179] The proteins isolated / extracted from sunflower seeds and / or other materials isolated / extracted from sunflower seeds using the processes disclosed herein can be used to add nutrition to foods (e.g., enhance the protein content of foods). Nutritional components can include the addition of proteins and / or other components of sunflower seeds such as phenols, phytic acid, chlorogenic acid, and / or the like. The isolated / extracted components can be understood to be dietary supplements.

[0180] For other uses, it can include bread-making applications (e.g., products leavened by yeast and / or chemically fermented), cereals, puff snacks, meat analogs, taffy, nuggets, chocolate products, protein bits, gluten-free flour blends, batters, coatings, etc.

[0181] Example 11 Plant-based cheese Soluble proteins were isolated / extracted from sunflower seeds using the processes disclosed herein.

[0182] A given percentage is a weight percentage based on all starting materials. To formulate the plant-based cheese, almond milk (31.8%), coconut oil (5.2%), potato starch (5.2%), tapioca flour (4.0%), soluble proteins isolated / extracted from sunflower seeds (2.0%), nutritional yeast (1.6%), xanthan gum (0.1%), salt (0.6%) were added to a blender and blended until creamy. This process formed an almond milk mixture.

[0183] In a small saucepan, water (45.7%) was combined with agar (3.9%) and heated over low-medium heat until the agar dissolved. Then, the saucepan was covered, the heat was turned down low, and the mixture was boiled for an additional 2 minutes while stirring occasionally until it thickened. This process formed an agar mixture.

[0184] Half of the almond milk mixture was added to the agar mixture and mixed quickly. Then, the remaining almond milk mixture was added while mixing continuously. The mixture was continuously mixed over low-medium heat for approximately 5 - 10 minutes until the cheese peeled off the sides of the saucepan without sticking.

[0185] Then, the cheese was placed in a glass container and chilled in the refrigerator for at least 6 hours before slicing thinly and / or dicing finely. Example 12 Plant-based ice cream Using the processes disclosed herein, insoluble and soluble proteins were isolated / extracted from sunflower seeds.

[0186] A given percentage is a weight percentage relative to all starting materials. To formulate the plant-based ice cream, water (22.2%), insoluble protein isolated / extracted from sunflower seeds (4.0%), soluble protein isolated / extracted from sunflower seeds (2.0%), GRINDSTED stabilizer blend (0.4%) and pea starch (1%) were thoroughly mixed together with strong agitation until fully incorporated. Almond milk (30%), coconut water blend (14%), sugar (6%), and allulose (10%) were added and mixed thoroughly. Sunflower oil (10%) was added and agitated with a powerful impeller-type stirrer / mixer to form an emulsion. This emulsion was slowly heated with stirring to 163°F (73°C). The emulsion was then quenched to a temperature below about 21°C (70°F) with agitation using an ice bath.

[0187] The cooled mixture was then placed into a pre-chilled ice cream maker (Breville BCI600) and frozen with agitation in the ice cream machine until a semi-hard consistency was achieved (the overrun target was 30%). The ice cream can be solidified in a standard freezer.

[0188] Example 13 Extraction of Albumin, Chlorogenic Acid (CGA), Phytic Acid, and Helianthin from Sunflower Seeds Sunflower seeds were obtained as a commercial product. The sunflower seeds were dehulled, cold pressed, and ground. The dehulled, pressed, and ground seeds contained 33% protein, 25% oil, 2% CGA, and 3.8% phytic acid. The ground material was subjected to a substantially extraction process as disclosed herein with reference to Figure 4. In so doing, albumin, chlorogenic acid, phytic acid, and helianthin were isolated from sunflower seeds.

[0189] The ground seeds were mixed with water at a water to dry weight ratio of 10:1, NaCl was added to make a 0.5 M NaCl solution, and it was heated to about 59 °C (138 °F) and mixed for 2 hours. After 2 hours, the slurry was separated using a decanter centrifuge. The solid stream was mixed with water at a water to dry weight ratio of 10:1 and decanting was carried out again while combining the liquid streams from the first and second decanters. The solid stream was dried to form sunflower meal. This liquid stream was 3.86 wt% CaCl with respect to the meal in the initial extraction slurry 2It was mixed. Then, the pH was raised to 5.8 using NaOH, and it was sent to a three-phase disk stack centrifuge. The oil / oil:water emulsion was recovered as the light stream, an aqueous stream containing proteins (albumin and helianthinin) and CGA was recovered, and a wet solid stream was discharged. The solid stream contains >99% phytic acid from the extraction stream. The aqueous stream was sent to a 0.2-μm precision filtration membrane, concentrated up to 4-fold, and then diafiltration water was added. The diafiltration water was added in an amount 0.25 times the initial volume of the stream sent to the membrane. The retained components consisted of large particles (mainly sunflower meal and oil not separated by the disk stack centrifuge), and the clarified permeate components contained proteins and CGA. Thereafter, the permeate components were sent to a 30-kDa ultrafiltration membrane. The retained components were concentrated up to 5-fold the starting volume, and diafiltration water was added in an amount 0.5 times the amount of material sent to the membrane. The retained components contained helianthinin, and the permeate components contained albumin and CGA. The retained components were sent to an evaporator to concentrate the solids to 15%, and then sent to a flash dryer to create a dried insoluble sunflower protein powder with 90 wt% protein. The permeate components were sent to a 1-kDa ultrafiltration membrane. The retained components were concentrated up to 10-fold the starting volume, and diafiltration water was added in an amount 0.5 times the amount of material sent to the ultrafiltration membrane. The retained components contained albumin, and the permeate components contained CGA. The retained components were sent to an evaporator to concentrate the solids to 40 wt%, and then sent to a spray dryer to create a dried soluble sunflower protein with 90 wt% protein. The permeate components were sent to a 300-Da nanofiltration membrane and concentrated 20-fold. Diafiltration water was added in an amount 0.25 times the amount of material sent to the membrane. The permeate components mainly contained NaCl, and the retained components contained CGA. The large amount of CGA retained components were sent to an evaporator to concentrate the solids to 10%, and then sent to a spray dryer to produce a dried CGA powder with 60 wt% CGA.

[0190] In some cases, the aqueous phase 34 is calcium chloride (CaCl 2) can be mixed with divalent ions such as calcium ions. In this case, the calcium ions bind to phytic acid that may be present in the aqueous phase 34, resulting in an insoluble compound that can precipitate. The resulting solid / precipitate can be separated using a suitable separation device such as a centrifuge, filter, and / or the like. The collected solid (e.g., phytic acid) can be dried using appropriate treatments such as those disclosed herein.

[0191] Adding a specific amount of divalent ions to the starting material results in different levels of phytic acid in the final soluble protein product. As an example, when the feed to the extraction step is 33% protein, 25% oil, 2% CGA, 3.8% phytic acid, and the divalent ion is calcium chloride, adding calcium chloride at the levels shown in Table 1 (as disclosed herein) results in the relevant levels of phytic acid in the soluble protein product.

[0192] Example 14 Content / Removal Amount of Phytic Acid The sweetness level of sunflower soluble protein can be adjusted by the amount of phytic acid (PA) remaining in the powder. When the PA content is 4 wt% (dry basis) of the protein powder, the sweetness is reduced by up to 20% compared to the protein powder with a base of 0.28 wt% PA. When the PA content is 7.7 wt% (dry basis) of the protein powder, the sweetness is reduced by up to 60% compared to the base protein powder. The phytic acid attached to it has no notable flavor.

[0193] The PA content in the protein powder can be controlled by adjusting the removal of PA from this treatment. If no PA is removed at all, the PA content in the final protein powder is as high as 40 wt%. By the removal treatment, it can be adjusted to 0.1 - 40.0 wt% of the final powder.

[0194] The base protein powder, which had 0.28 wt% phytic acid, was 10 times sweeter than sucrose when compared in a 0.5 wt% solution. When the protein solution contained 4 wt% phytic acid based on the protein powder, the sweetness compared to sucrose was only 2.5 times. When the level of phytic acid was even higher, up to 8 wt%, as shown herein, the sweetness further decreased.

[0195] This unique feature of the interaction between phytic acid and sunflower albumin protein allows the sweetness of the protein to be adjusted for desired applications. For example, an alternative sweetener that can substantially reduce the sucrose level in a product may be desired. This should be a preferred use for the 10 - times - sweeter protein. In alternative applications, higher levels of protein may be desired, and in that case, since it is necessary to make the protein product less sweet, it is possible to include more protein without having an overwhelming sweetness. This should be a preferred use for products containing phytic acid at levels up to 8 wt%.

[0196]

Table 4

[0197] Phytic acid is naturally present in dehulled sunflower seeds at 2 - 3 wt%. The protein is 20 - 25 wt% in dehulled seeds and 4.0 - 6.25 wt% in the soluble protein fraction. Before the treatment of extracting and purifying the soluble protein and removing PA from the system, the soluble protein and PA can be in a high ratio of 4:3 (protein to PA).

[0198] PA removal was carried out by adding calcium chloride to the system at a molar ratio to phytic acid of 6:1 or more and removing all of the PA. By adjusting the pH to 5.5 or more, the PA was precipitated. As a result, this precipitate could be removed by a filter or a centrifuge. What remained was a combination of protein and sodium chloride, hydrogen chloride, and any excess calcium chloride. These non-protein compounds could then be removed by utilizing nanofiltration. In some cases, the calcium chloride in molar ratio to phytic acid (e.g., in the permeate component) was about 5.6 - 6.0:1.

[0199] To adjust the amount of PA in the final powder, the amount of calcium chloride added to the system can be adjusted so that only a certain amount of PA is removed. By measuring the exact amounts of phytic acid and protein in the system (which can be done with analytical instruments), the protein and PA content in the final product can be controlled, and thus the sweetness level of the final product can be controlled.

[0200] Example 15 Protein - fortified chocolate milk Soluble protein was isolated / extracted from sunflower seeds using the processes disclosed herein.

[0201] A given percentage is a weight percentage relative to all starting materials. Three different protein - fortified chocolate milk products were formed. Each product contained coca (1.5%), calcium carbonate (0.5%), cellulose gel (0.3%), natural and artificial flavorings (0.2%), salt (0.15%), carrageenan (0.1%), and cellulose gum (0.1%).

[0202] Protein - fortified chocolate milk formulation A also contained 1% milk (92.75%) and soluble protein (4.4%) isolated / extracted from sunflower seeds having a sweetness approximately equal to sucrose and containing 6% by weight of phytic acid.

[0203] Protein-enriched chocolate milk formulation B also had a sweetness approximately twice that of 1% milk (94.98%) and sucrose, and contained soluble protein (2.17%) isolated / extracted from sunflower seeds containing 4% by weight of phytic acid.

[0204] Protein-enriched chocolate milk formulation C also had a sweetness approximately five times that of 1% milk (96.35%) and sucrose, and contained soluble protein (0.8%) isolated / extracted from sunflower seeds containing 2% by weight of phytic acid.

[0205] It should be understood that the present disclosure is merely illustrative in many respects. Details, particularly matters regarding shape, size, and arrangement of steps, can be changed without departing from the scope of the present disclosure. This may include, within an appropriate range, the use of any of the features of an exemplary embodiment in other embodiments. Of course, the scope of the present invention is defined by the language expressed in the appended claims. embodiment) in other embodiments. Of course, the scope of the present invention is defined by the language expressed in the appended claims. (Appendix) Describe the technical idea that can be grasped from the above embodiments and modification examples. [Item 1] A first component comprising a sunflower protein extract; and A second component comprising phytic acid A composition comprising. [Item 2] The composition according to item 1, wherein the first component accounts for 91.7 to 99% by weight of the composition. [Item 3] The composition according to item 1 or 2, wherein the second component accounts for 0.28 to 7.7% by weight of the composition. [Item 4] The composition according to any one of items 1 to 3, wherein the second component accounts for 2 to 6% by weight of the composition. [Item 5] The composition according to any one of items 1 to 4, having a sweetness substantially equal to that of sucrose. [Item 6] The composition according to any one of items 1 to 4, having a sweetness sweeter than that of sucrose. [Item 7] The composition according to any one of items 1 to 4, having a sweetness 2 to 10 times sweeter than that of sucrose. [Item 8] The composition according to any one of items 1 to 4, having a sweetness 2 to 5 times sweeter than that of sucrose. [Item 9] A method for extracting a plurality of target materials from oilseed grains, comprising: A step of performing extraction on an oilseed grain material to form an aqueous phase and a solid phase, wherein the extraction is performed without an organic solvent; A step of separating insoluble solids from the aqueous phase; A step of filtering the aqueous phase to form a retained component and a permeated component; A step of drying the retained component to form a dried retained component containing a first target material; A step of filtering the permeated component to form a second retained component and a second permeated component; A step of drying the second retained component to form a second dried retained component containing a second target material; A step of filtering the second permeated component to form a third retained component, and A step of drying the third retained component to form a third dried retained component containing a third target material. A method comprising the above steps. [Item 10] The method according to item 9, wherein the first target material contains protein. [Item 11] The method according to item 9 or 10, wherein the second target material contains a second protein fraction. [Item 12] The method according to any one of items 9 to 11, further comprising a step of adding a precipitating material to the permeated component to form a precipitate. [Item 13] The method according to item 12, wherein the precipitate contains phytic acid. [Item 14] The method according to item 12 or 13, wherein the precipitation material is calcium chloride. [Item 15] The method according to item 12 or 13, wherein the step of adding a precipitation material to the permeation component to form a precipitate includes adding calcium chloride at a molar ratio of 5.6 to 6.0:1 to phytic acid in the permeation component. [Item 16] The method according to any one of items 12 to 15, wherein the third target material contains chlorogenic acid. [Item 17] A method for extracting a material from oilseed grains, comprising: mixing an extraction solution having a pH of 3 to 6 containing water and salt with a certain amount of oilseed grains that have been dehulled, cold-pressed, and pulverized to form a mixture; extracting the mixture at a temperature in the range of 10 to 93 °C for 0.5 to 6 hours to form an extracted mixture; filtering the extracted mixture into a retention component and a permeation component; and drying the retention component A method comprising the above steps. [Item 18] Soluble sunflower protein; One or more of almond milk, coconut, potato starch, and tapioca flour; and A thickened agar solution A plant-based cheese comprising the above components. [Item 19] The plant-based cheese according to item 18, comprising two or more of almond milk, coconut, potato starch, and tapioca flour. [Item 20] The plant-based cheese according to item 18, comprising three or more of almond milk, coconut, potato starch, and tapioca flour. [Item 21] The plant-based cheese according to item 18, comprising almond milk, coconut, potato starch, and tapioca flour. [Item 22] The vegetable cheese according to any one of Items 18 to 21, further comprising at least one of nutritional yeast, xanthan gum, and salt. [Item 23] The vegetable cheese according to Item 22, comprising two or more of nutritional yeast, xanthan gum, and salt. [Item 24] The vegetable cheese according to Item 22, comprising nutritional yeast, xanthan gum, and salt. [Item 25] Soluble sunflower protein; Insoluble sunflower protein; At least one of pea starch, almond milk, coconut water blend, sugar, and allulose, and Sunflower oil comprising a vegetable ice cream. [Item 26] The vegetable ice cream according to Item 25, comprising two or more of pea starch, almond milk, coconut water blend, sugar, and allulose. [Item 27] The vegetable ice cream according to Item 25, comprising three or more of pea starch, almond milk, coconut water blend, sugar, and allulose. [Item 28] The vegetable ice cream according to Item 25, comprising four or more of pea starch, almond milk, coconut water blend, sugar, and allulose. [Item 29] The vegetable ice cream according to Item 25, comprising pea starch, almond milk, coconut water blend, sugar, and allulose. [Item 30] Soluble sunflower protein containing 2 to 6% by weight of phytic acid; Milk; and at least one of cocoa, calcium carbonate, and cellulose gel comprising a protein - fortified chocolate milk. [Item 31] The protein-enriched chocolate milk according to item 30, wherein the soluble sunflower protein containing 2 to 6% by weight of phytic acid has a sweetness substantially equal to that of sucrose. [Item 32] The protein-enriched chocolate milk according to item 30 or 31, wherein the soluble sunflower protein containing 2 to 6% by weight of phytic acid has a sweetness 2 to 5 times sweeter than that of sucrose. [Item 33] A soluble sunflower protein containing 2 to 6% by weight of phytic acid; Water, and An electrolyte solution A protein-enriched sports drink containing the same. [Item 34] The protein-enriched sports drink according to item 33, wherein the soluble sunflower protein containing 2 to 6% by weight of phytic acid has a sweetness substantially equal to that of sucrose. [Item 35] The protein-enriched sports drink according to item 33 or 34, wherein the soluble sunflower protein containing 2 to 6% by weight of phytic acid has a sweetness 2 to 5 times sweeter than that of sucrose. [Item 36] A protein-enriched sports drink according to any one of items 33 to 35, which does not contain added sugar or a sugar substitute. [Item 37] A protein-enriched sports drink according to any one of items 33 to 36, which contains 0.75 to 1.5 grams of protein per about 28 grams (1 ounce). [Item 38] A protein-enriched sports drink according to any one of items 33 to 37, which contains substantially 1 gram of protein per about 28 grams (1 ounce).

Claims

1. a first component comprising a sunflower protein extract; and The second ingredient contains phytic acid. A composition comprising:

2. The composition of claim 1 , wherein the first component comprises 91.7 to 99% by weight of the composition.

3. The composition of claim 1 or 2, wherein the second component comprises 0.28 to 7.7% by weight of the composition.

4. The composition of any one of claims 1 to 3, wherein the second component comprises 2 to 6% by weight of the composition.

5. The composition according to any one of claims 1 to 4, having a sweetness substantially equivalent to that of sucrose.

6. The composition according to any one of claims 1 to 4, which has a sweetness greater than that of sucrose.

7. The composition according to any one of claims 1 to 4, which has a sweetness that is 2 to 10 times sweeter than that of sucrose.

8. The composition according to any one of claims 1 to 4, which has a sweetness that is 2 to 5 times sweeter than that of sucrose.

9. 1. A method for extracting multiple target materials from oil seeds, comprising: subjecting the oil seed material to an extraction to form an aqueous phase and a solid phase, said extraction being an organic solvent-free extraction; separating insoluble solids from said aqueous phase; filtering the aqueous phase to form a retentate and a permeate component; drying the retention component to form a dry retention component comprising a first target material; filtering the permeate component to form a second retentate component and a second permeate component; drying the second retention component to form a second dry retention component comprising a second target material; filtering the second permeate component to form a third retentate component; and drying the third retention component to form a third dry retention component comprising a third target material; A method comprising:

10. The method of claim 9 , wherein the first target material comprises a protein.

11. The method of claim 9 or 10, wherein the second target material comprises a second protein fraction.

12. The method of any one of claims 9 to 11, further comprising adding a precipitating material to the permeated component to form a precipitate.

13. The method of claim 12 , wherein the precipitate comprises phytic acid.

14. 14. The method of claim 12 or 13, wherein the precipitating material is calcium chloride.

15. 14. The method of claim 12 or 13, wherein adding a precipitating material to the permeation component to form a precipitate comprises adding calcium chloride in a molar ratio of 5.6 to 6.0:1 to phytic acid in the permeation component.

16. The method of any one of claims 12 to 15, wherein the third target material comprises chlorogenic acid.

17. 1. A method for extracting material from an oil seed, comprising: mixing a quantity of dehulled, cold pressed and crushed oil seeds with an extraction solution having a pH of 3-6 comprising water and salt to form a mixture; extracting the mixture at a temperature ranging from 10 to 93° C. for 0.5 to 6 hours to form an extracted mixture; filtering the extracted mixture into a retained component and a permeated component; and drying the retained component A method comprising:

18. Soluble sunflower protein; one or more of almond milk, coconut, potato starch, and tapioca flour; and Thickened agar solution Plant-based cheese, including:

19. 20. The plant-based cheese of claim 18 comprising two or more of almond milk, coconut, potato starch, and tapioca flour.

20. 20. The plant-based cheese of claim 18 comprising three or more of almond milk, coconut, potato starch, and tapioca flour.

21. 20. The plant-based cheese of claim 18 comprising almond milk, coconut, potato starch, and tapioca flour.

22. The plant-based cheese of any one of claims 18 to 21, further comprising one or more of nutritional yeast, xanthan gum, and salt.

23. 23. The plant-based cheese of claim 22, comprising two or more of nutritional yeast, xanthan gum, and salt.

24. 23. The plant-based cheese of claim 22 comprising nutritional yeast, xanthan gum, and salt.

25. Soluble sunflower protein; Insoluble sunflower protein; one or more of pea starch, almond milk, coconut water blend, sugar, and allulose; and Sunflower oil Including, plant-based ice cream.

26. 26. The plant-based ice cream of claim 25, comprising two or more of pea starch, almond milk, coconut water blend, sugar, and allulose.

27. 26. The plant-based ice cream of claim 25, comprising three or more of the following: pea starch, almond milk, coconut water blend, sugar, and allulose.

28. 26. The plant-based ice cream of claim 25, comprising four or more of the following: pea starch, almond milk, coconut water blend, sugar, and allulose.

29. 26. The plant-based ice cream of claim 25 comprising pea starch, almond milk, coconut water blend, sugar, and allulose.

30. soluble sunflower protein containing 2-6% by weight of phytic acid; Milk; and At least one of the following: coca, calcium carbonate, cellulose gel Protein-enriched chocolate milk, including:

31. 31. The protein-enriched chocolate milk of claim 30, wherein said soluble sunflower protein containing 2-6% by weight of phytic acid has a sweetness substantially equivalent to that of sucrose.

32. Protein-enriched chocolate milk according to claims 30 or 31, wherein the soluble sunflower protein containing 2-6% by weight of phytic acid has a sweetness 2-5 times sweeter than sucrose.

33. soluble sunflower protein containing 2-6% by weight of phytic acid; Water, and electrolyte solution Protein-enhanced sports drinks, including:

34. 34. The protein-fortified sports drink of claim 33, wherein the soluble sunflower protein containing 2-6% by weight of phytic acid has a sweetness substantially equivalent to that of sucrose.

35. 35. The protein-fortified sports drink of claim 33 or 34, wherein the soluble sunflower protein containing 2-6% by weight of phytic acid has a sweetness 2-5 times sweeter than sucrose.

36. 36. The protein-enriched sports drink of any one of claims 33 to 35, which contains no added sugar and no added sugar substitutes.

37. 37. The protein-enhanced sports drink of any one of claims 33 to 36, comprising 0.75 to 1.5 grams of protein per ounce.

38. 38. The protein-enhanced sports drink of any one of claims 33 to 37, comprising substantially 1 gram of protein per ounce.

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