Patent Application
20140127381
The present disclosure provides liquid food compositions which comprise soy whey proteins recovered or isolated in accordance with the processes disclosed herein to form a soup, sauce, dressing, gravy, dip or spread composition (hereafter referred to as liquid food composition or “soup or sauce”). Specifically, the present disclosure provides a liquid food composition comprising soy whey proteins that have been recovered from soy processing streams, along with other ingredients to form a liquid food product. Specifically, the present soy recovery process utilizes one or more membrane or chromatographic separation operations for isolating and removing soy proteins, including novel soy whey proteins and purified target proteins, as well as sugars, minerals, and other constituents to form a purified waste water stream. Methods for making the liquid food products are also disclosed.
Food scientists in the industry continually work to develop novel processes and the resulting products that deliver improved nutritional characteristics that consumers desire. The inclusion of soy protein is a cost-effective way to reduce fat, increase protein content and improve overall characteristics of a food product such as soup, sauces, dressing, gravy, dips or spreads. Soy protein is also a cost-effective way to enhance the nutritional profile of many liquid food products such as fluid, semi-fluid, or pliable solid matrix food products.
Soy proteins are typically in one of three forms when consumed by humans. These include soy protein flour (grits), soy protein concentrates, and soy protein isolates. All three types are made from defatted soybean flakes. Flours and grits contain at least 50% protein and are prepared by milling the flakes.
Soy protein concentrates contain 65 wt. % to 90 wt. % protein on a dry weight basis, with the major non-protein component being fiber. Soy protein concentrates are made by repeatedly washing the soy flakes with water, which may optionally contain low levels of food grade alcohols or buffers. The effluent from the repeated washings is discarded and the solid residue is dried, thereby producing the desired concentrate. The yield of concentrates from the starting material is approximately 60-70%.
The preparation of soy protein concentrate generally results in two streams: soy isolate and a soy molasses stream, which may contain up to 55 wt. % soy protein. On a commercial scale, significant volumes of this molasses are generated that must be discarded. The total protein content may contain up to 15 wt. % of the total protein content of the soybeans from which they are derived. Thus, a significant fraction of soy protein is discarded during processes typically used for soy protein concentrate preparation.
Soy protein isolates are the most highly refined soy protein products commercially available, as well as the most expensive to obtain. However, as with soy protein concentrates, current processing known in the industry results in many of the valuable minerals, vitamins, isoflavones, and phytoestrogens being drawn off to form a waste stream along with the low-molecular weight sugars in making the isolates.
Soy protein isolates contain a minimum of 90 wt. % protein on a dry weight basis and little or no soluble carbohydrates or fiber. Isolates are typically made by extracting defatted soy flakes or soy flour with a dilute alkali (pH <9) and centrifuging. The extract is adjusted to pH 4.5 with a food grade acid such as sulfuric, hydrochloric, phosphoric or acetic acid. At a pH of 4.5, the solubility of the proteins is at a minimum so they will precipitate out. The protein precipitate is then dried after being adjusted to a neutral pH or is dried without any pH adjustment to produce the soy protein isolate. The yield of the isolate is 30% to 50% of the original soy flour and 60% of the protein in the flour. This extremely low yield along with the many required processing steps contributes to the high costs involved in producing soy protein isolates.
Due at least in part to their relatively high protein content, soy protein isolates are desired for a variety of applications. In conventional soy protein isolate manufacture, the aqueous stream (i.e., soy whey stream) remaining after precipitation of the soy protein isolate fraction is typically discarded. On a commercial scale, considerable costs are incurred with the handling and disposing of this aqueous waste stream. For example, the soy whey stream is relatively dilute (e.g., less than about 5 wt. % solids, typically about 2 wt. % solids). Thus, on a commercial scale, significant volumes of the soy whey stream are generated that must be treated and/or discarded. In addition, it has been observed that the soy whey stream may contain a substantial proportion of the total protein content of the soybeans used in preparation of soy protein isolates. In fact, the soy whey stream may contain up to 45 wt. % of the total protein content of the soybeans from which soy protein isolates are derived. Thus, a significant fraction of soy protein is typically discarded during conventional soy protein isolate production.
Despite the high proportion of the soy whey protein that is typically lost in the processing stream, recovery of the proteins has not generally been considered to be economically feasible. At least in part, the loss of these potentially valuable proteins has been heretofore deemed acceptable because of the relatively low concentrations of total protein in the whey, and the consequently large volumes of aqueous waste that must be processed for each unit of mass of protein recovered, which generates a large amount of pollution. Recovery attempts have also been deterred by the complex mixture of proteins and other components present in the soy whey, and the absence of commercial applications for crude mixtures of the protein solids. While soy whey has been known to contain certain bioactive proteins, the commercial value of these has been limited for lack of processes to recover them in high purity form.
Methods for recovering products from soy whey are known in the art. For example, a process for separating specific isoflavone fractions from soy whey and soy molasses feed streams is described in U.S. Pat. Nos. 6,033,714; 5,792,503; and 5,702,752. In another method, soy molasses (also referred to as soy solubles) is obtained when vacuum distillation removes the ethanol from an aqueous ethanol extract of defatted soy meal. The feed stream is heated to a temperature chosen according to the specific solubility of the desired isoflavone fraction. The stream is then passed through an ultrafiltration membrane, which allows isoflavone molecules below a maximum molecular weight to permeate. The permeate may then be concentrated using a reverse osmosis membrane. The concentrated stream is then put through a resin adsorption process using at least one liquid chromatography column to further separate the fractions.
Methods for the removal of oligosaccharides from soybean wastes are also known in the art. For example, Matsubara et al [Biosci. Biotech. Biochem. 60:421 (1996)] describe a method for recovering soybean oligosaccharides from steamed soybean wastewater using reverse osmosis and nanofiltration membranes. JP 07-082,287 teaches the recovery of oligosaccharides from soybean oligosaccharide syrup using solvent extraction. That method comprises adding an organic solvent to the aqueous solution containing the oligosaccharides, heating the mixture to give a homogeneous solution, cooling the solution to form two liquid layers, and separating and recovering the bottom layer.
Canadian Patent Applications 2,006,957 and 2,013,190 describe ion-exchange processes carried out in aqueous ethanol to recover small quantities of high value by-products from cereal grain processing waste. According to CA 2,013,190, an alcoholic extract from a cereal grain is processed through either an anionic and/or cationic ion-exchange column to obtain minor but economically valuable products.
Soy whey and soy molasses also contain a significant amount of protease inhibitors. Protease inhibitors are known to at least inhibit trypsin, chymotrypsin and potentially a variety of other key transmembrane proteases that regulate a range of key metabolic functions. Topical administration of protease inhibitors finds use in such conditions as atopic dermatitis, a common form of inflammation of the skin, which may be localized to a few patches or involve large portions of the body. The depigmenting activity of protease inhibitors and their capability to prevent ultraviolet-induced pigmentation have been demonstrated both in vitro and in vivo (See e.g., Paine et al., J. Invest. Dermatol., 116: 587-595 [2001]). Protease inhibitors have also been reported to facilitate wound healing. For example, secretory leukocyte protease inhibitor was demonstrated to reverse the tissue destruction and speed the wound healing process when topically applied. In addition, serine protease inhibitors can also help to reduce pain in lupus erythematosus patients (See e.g., U.S. Pat. No. 6,537,968). Naturally occurring protease inhibitors can be found in a variety of foods such as cereal grains (oats, barley, and maize), brussels sprouts, onion, beetroot, wheat, finger millet, and peanuts. One source of interest is the soybean.
Two broad classes of protease inhibitor superfamilies have been identified from soybean and other legumes with each class having several isoinhibitors. Kunitz-trypsin inhibitor (KTI) is major member of the first class whose members have approximately 170-200 amino acids, molecular weights between 20-25 kDa, and act principally against trypsin. Kunitz-trypsin proteinase inhibitors are mostly single chain polypeptides with 4 cysteines linked in two disulfide bridges, and with one reactive site located in a loop defined by disulfide bridge. The second class of inhibitors contains 60-85 amino acids, has a range in molecular weight of 6-10 kDa, has a higher number of disulfide bonds, is relatively heat-stable, and inhibits both trypsin and chymotrypsin at independent binding sites. Bowman-Birk inhibitor (BBI) is an example of this class. The average level of protease inhibitors present in soybeans is around 1.4 percent and 0.6 percent for KTI and BBI, respectively. Notably, these low levels make it impractical to isolate the natural protease inhibitor for clinical applications.
Preparing pure BBI, however, involves costly techniques. Moreover, because the average level of BBI present in soybeans is only around 0.6 wt. %, this low level makes it impractical and cost prohibitive to isolate the natural protease inhibitor for clinical applications. Purification methods currently used in the art vary. Some methods use affinity purification with immobilized trypsin or chymotrypsin. Immobilized trypsin will bind both BBI and Kunitz trypsin inhibitor (KTI) so a particularly pure BBI product is not isolated. Alternatively, a process involving use of immobilized chymotrypsin, while it does not bind KTI, has several problems, such as not being cost effective for scale-up and the possibility of chymotrypsin leaching from the resin following numerous uses and cleaning steps. Many older BBI purification methods use anion exchange chromatography, which technique can result in subfractionation of BBI isomers, In addition, it has been difficult with anion exchange chromatography to obtain a KTI-free BBI fraction without significant loss of BBI yield. Accordingly, all of the methods currently known for isolating BBI are problematic due to slow processing, low yield, low purity, and/or the need for a number of different steps which results in an increase of time and cost requirements.
Methods of purification which only utilize filtration are not effective as sole methods due to membrane fouling, incomplete and/or imperfect separation of non-protein components from BBI proteins, and ineffective separation of BBI proteins from other proteins. Methods of purification which only utilize chromatography are also not effective as sole methods due to binding capacity and overloading issues, incomplete and/or imperfect separation issues (e.g. separation of BBI from KTI), irreversible binding of protein to resin issues, resin lifetime issues, and it is relatively expensive compared to other techniques. Methods of purification which involve only ammonium sulfate precipitation are not effective as sole methods due to the possibility of irreversible precipitation of BBI proteins, potential loss of activity of BBI proteins, incomplete precipitation of BBI proteins (i.e. loss of yield), and the need to remove the ammonium sulfate from the final product, which adds an additional step and cost.
Current methods known in the art for obtaining purified BBI proteins suffer from lower purity levels due to the contamination of the BBI with Kunitz Trypsin Inhibitor (KTI) proteins. Depending on the isolation method used, endotoxin levels can also be an issue. Current methods use whole soybean as the starting material, which is then defatted by various means. In contrast, the processes of the present invention use defatted soy white flake as the starting material. As a result, the prior art has not described a BBI product having high purity levels that is obtained from a soy protein source, without acid or alcohol extraction, or acetone precipitation. Thus, there is a need for methods and compositions suitable for the production of high purity BBI and variants.
Thus, there is a need in the art for food products which incorporate as an ingredient the soy whey proteins recovered from soy processing streams pursuant to the methods disclosed herein. Accordingly, the present invention describes food compositions which comprise soy whey proteins that have been recovered in accordance with the methods described herein. Along with the recovered soy whey proteins, the food compositions may additionally comprise at least one other ingredient and are formed into a liquid food product. The liquid food products that contain recovered soy whey protein as an ingredient have been found to have an increased amount of protein and overall nutritional profile that a consumer desires, while retaining the same taste, structure, aroma and mouthfeel of typical liquid food products currently on the market.
The present disclosure relates to liquid food compositions which comprise soy whey proteins that have been recovered in accordance with the novel methods for purifying soy processing streams disclosed herein. The liquid food composition is broadly defined as a fluid, semi-fluid, or pliable solid matrix food product. The liquid food compositions disclosed herein can include soups, sauces, gravy, dips, or spread compositions and the like. Specifically, the present disclosure provides liquid food products that contain recovered soy whey protein, which products have been found to have an improved nutritional profile including increased amount of protein, while retaining the same taste, structure, aroma and mouthfeel of typical liquid food products currently on the market and desired by consumers. The liquid food compositions which contain the soy whey proteins of the present disclosure may be combined with at least one other ingredient to form the desired liquid food product.
The liquid food products of the present disclosure incorporate soy whey protein that has been recovered from processing streams in accordance with novel processing methods. To recover the soy whey protein, a sequence of membrane or chromatographic separation operations steps, which are described below in further detail, are combined in varying order to comprise the overall process for recovering soy whey protein and other constituents from a processing stream. The present processing method results in the isolation and removal of one or more soy whey proteins, sugars, and minerals from a soy processing stream, the soy processing stream comprising the soy whey proteins, one or more soy storage proteins, one or more sugars, and one or more minerals. The removal of the soy whey proteins from the processing streams in accordance with the novel processing methods allows the soy whey protein to be used in food compositions to produce the liquid food products.
The present invention provides food compositions comprising soy whey proteins recovered from a variety of leguminous plant processing streams (including soy whey streams and soy molasses streams) generated in the manufacture of soy protein isolates. The recovered soy whey proteins are useful as an ingredient in food compositions which can then be used to form liquid food products. The resultant liquid food products have been shown to exhibit improved nutritional characteristics, including an increased amount of protein, while retaining the same taste, structure, aroma, and mouthfeel of typical liquid food products currently on the market.
Generally, the purification of the soy processing stream comprises one or more operations (e.g. membrane separation operations) selected and designed to provide recovery of the desired proteins or other products, or separation of various components of the soy whey stream, or both. Recovery of soy whey proteins (e.g. Bowman-Birk inhibitor (BBI) and Kunitz trypsin inhibitor (KTI) proteins) and one or more other components of the soy whey stream (e.g. various sugars, including oligosaccharides) may utilize a plurality of separation techniques, (e.g. membrane, chromatographic, centrifugation, or filtration). The specific separation technique will depend upon the desired component to be recovered by separating it from other components of the processing stream.
For example, a purified fraction is typically prepared by removal of one or more impurities (e.g. microorganisms or minerals), followed by removal of additional impurities including one or more soy storage proteins (i.e. glycinin and β-conglycinin), followed by removal of one or more soy whey proteins (including, for example, KTI and other non-BBI proteins or peptides), and/or followed by removal of one or more additional impurities including sugars from the soy whey. Recovery of various target components in high purity form is improved by removal of other major components of the whey stream (e.g. storage proteins, minerals, and sugars) that detract from purity by diluents, while likewise improving purity by purifying the protein fraction through removal of components that are antagonists to the proteins and/or have deleterious effects (e.g. endotoxins). Removal of the various components of the soy whey typically comprises concentration of the soy whey prior to and/or during removal of the components of the soy whey. The methods of the present invention also will reduce pollution generated from processing large quantities of aqueous waste.
Removal of storage proteins, sugars, minerals, and impurities yields fractions that are enriched in the individual, targeted proteins and free of impurities that may be antagonists or toxins, or may otherwise have a deleterious effect. For example, typically a soy storage protein-enriched fraction may be recovered, along with a fraction enriched in one or more soy whey proteins. A fraction enriched in one more sugars (e.g. oligosaccharides and/or polysaccharides) is also typically prepared. Thus, the present methods provide a fraction that is suitable as a substrate for recovery of individual, targeted proteins, and also provide other fractions that can be used as substrates for economical recovery of other useful products from aqueous soy whey. For example, removal of sugars and/or minerals from the soy whey stream produces a useful fraction from which the sugars can be further separated, thus yielding additional useful fractions: a concentrated sugar and a mineral fraction (that may include citric acid), and a relatively pure aqueous fraction that may be disposed of with minimal, if any, treatment or recycled as process water. Process water thus produced may be especially useful in practicing the present methods. Thus, a further advantage of the present methods may be reduced process water requirements as compared to conventional isolate preparation processes.
Methods of the present disclosure provide advantages over conventional methods for manufacture of soy protein isolates and concentrates in at least two ways. As noted, conventional methods for manufacturing soy protein materials typically dispose of the soy whey stream (e.g. aqueous soy whey or soy molasses). Thus, the products recovered by the methods of the present disclosure represent an additional product, and a revenue source not currently realized in connection with conventional soy protein isolate and soy protein concentrate manufacture. Furthermore, treatment of the soy whey stream or soy molasses to recover saleable products preferably reduces the costs associated with treatment and disposal of the soy whey stream or soy molasses. For example, as detailed elsewhere herein, various methods of the present invention provide a relatively pure soy processing stream that may be readily utilized in various other processes or disposed of with minimal, if any, treatment, thereby reducing the environmental impact of the process. Certain costs exist in association with the methods of the present disclosure, but the benefits of the additional product(s) isolated and minimization of waste disposal are believed to compensate for any added costs.
The soy whey proteins recovered in accordance with the processes of the present disclosure represent a significant advance in the art over other soy proteins and isolates. As noted herein, the soy whey proteins of the present disclosure, which are recovered from a processing stream, possess unique characteristics as compared to other soy proteins found in the art.
Soy protein isolates are typically precipitated from an aqueous extract of defatted soy flakes or soy flour at the isoelectric point of soy storage proteins (e.g. a pH of about 4.1). Thus, soy protein isolates generally include proteins that are not soluble in acidic liquid media. Similarly, the proteins of soy protein concentrates, the second-most refined soy protein material, are likewise generally not soluble in acidic liquid media. However, soy whey proteins recovered by the processes of the present disclosure differ in that they are generally acid-soluble, meaning they are soluble in acidic liquid media.
The present disclosure provides soy whey protein compositions derived from an aqueous soy whey that exhibit advantageous characteristics over soy proteins found in the prior art. For example, the soy whey proteins isolated according to the methods of the present invention possess high solubility (i.e. SSI % greater than 80) across a relatively wide pH range of the aqueous (typically acidic) medium (e.g. an aqueous medium having a pH of from about 2 to about 10, from about 2 to about 7, or from about 2 to about 6) at ambient conditions (e.g. a temperature of about 25° C.). As shown in Table 1 and graphically illustrated in
In addition to solubility, the soy whey proteins of the present disclosure also possess much lower viscosity than other soy whey proteins. As shown in Table 1 and as graphically illustrated in
As Table 2 illustrates, the other physical characteristics, with the exception of the viscoelastic properties and solubility, of the soy whey protein recovered in accordance with the methods of the present disclosure were found to be very similar to that of soy isolate.
Aqueous whey streams and molasses streams, which are types of soy processing streams, are generated from the process of refining a whole legume or oilseed. The whole legume or oilseed may be derived from a variety of suitable plants. By way of non-limiting example, suitable plants include leguminous plants, including for example, soybeans, corn, peas, canola, sunflowers, sorghum, rice, amaranth, potato, tapioca, arrowroot, canna, lupin, rape, wheat, oats, rye, barley, and mixtures thereof. In one embodiment, the leguminous plant is soybean and the aqueous whey stream generated from the process of refining the soybean is an aqueous soy whey stream.
Aqueous soy whey streams generated in the manufacture of soy protein isolates are generally relatively dilute and are typically discarded as waste. More particularly, the aqueous soy whey stream typically has a total solids content of less than about 10 wt. %, typically less than about 7.5 wt. % and, still more typically, less than about 5 wt. %. For example, in various aspects, the solids content of the aqueous soy whey stream is from about 0.5 to about 10 wt. %, from about 1 wt. % to about 4 wt. %, or from about 1 to about 3 wt. % (e.g. about 2 wt. %). Thus, during commercial soy protein isolate production, a significant volume of waste water that must be treated or disposed is generated.
Soy whey streams typically contain a significant portion of the initial soy protein content of the starting material soybeans. As used herein the term “soy protein” generally refers to any and all of the proteins native to soybeans. Naturally occurring soy proteins are generally globular proteins having a hydrophobic core surrounded by a hydrophilic shell. Numerous soy proteins have been identified including, for example, storage proteins such as glycinin and β-conglycinin. Soy proteins likewise include protease inhibitors, such as the above-noted BBI proteins. Soy proteins also include hemagglutinins such as lectin, lipoxygenases, β-amylase, and lunasin. It is to be noted that the soy plant may be transformed to produce other proteins not normally expressed by soy plants. It is to be understood that reference herein to “soy proteins” likewise contemplates proteins thus produced.
On a dry weight basis, soy proteins constitute at least about 10 wt. %, at least about 15 wt. %, or at least about 20 wt. % of the soy whey stream (dry weight basis). Typically, soy proteins constitute from about 10 to about 40 wt. %, or from about 25 to about 30 wt. % of the soy whey stream (dry weight basis). Soy protein isolates typically contain a significant portion of the storage proteins of the soybean. However, the soy whey stream remaining after isolate precipitation likewise contains one or more soy storage proteins.
In addition to the various soy proteins, the aqueous soy whey stream likewise comprises one or more carbohydrates (i.e. sugars). Generally, sugars constitute at least about 25%, at least about 35%, or at least about 45% by weight of the soy whey stream (dry weight basis). Typically, sugars constitute from about 25% to about 75%, more typically from about 35% to about 65% and, still more typically, from about 40% to about 60% by weight of the soy whey stream (dry weight basis).
The sugars of the soy whey stream generally include one or more monosaccharides, and/or one or more oligosaccharides or polysaccharides. For example, in various aspects, the soy whey stream comprises monosaccharides selected from the group consisting of glucose, fructose, and combinations thereof. Typically, monosaccharides constitute from about 0.5% to about 10 wt. % and, more typically from about 1% to about 5 wt. % of the soy whey stream (dry weight basis). Further in accordance with these and various other aspects, the soy whey stream comprises oligosaccharides selected from the group consisting of sucrose, raffinose, stachyose, and combinations thereof. Typically, oligosaccharides constitute from about 30% to about 60% and, more typically, from about 40% to about 50% by weight of the soy whey stream (dry weight basis).
The aqueous soy whey stream also typically comprises an ash fraction that includes a variety of components including, for example, various minerals, isoflavones, phytic acid, citric acid, saponins, and vitamins. Minerals typically present in the soy whey stream include sodium, potassium, calcium, phosphorus, magnesium, chloride, iron, manganese, zinc, copper, and combinations thereof. Vitamins present in the soy whey stream include, for example, thiamine and riboflavin. Regardless of its precise composition, the ash fraction typically constitutes from about 5% to about 30% and, more typically, from about 10% to about 25% by weight of the soy whey stream (dry weight basis).
The aqueous soy whey stream also typically comprises a fat fraction that generally constitutes from about 0.1% to about 5% by weight of the soy whey stream (dry weight basis). In certain aspects of the invention, the fat content is measured by acid hydrolysis and is about 3% by weight of the soy whey stream (dry weight basis).
In addition to the above components, the aqueous soy whey stream also typically comprises one or more microorganisms including, for example, various bacteria, molds, and yeasts. The proportions of these components typically vary from about 100 to about 1×109 colony forming units (CFU) per milliliter. As detailed elsewhere herein, in various aspects, the aqueous soy whey stream is treated to remove these component(s) prior to protein recovery and/or isolation.
As noted, conventional production of soy protein isolates typically includes disposal of the aqueous soy whey stream remaining following isolation of the soy protein isolate. In accordance with the present disclosure, recovery of one or more proteins and various other components (e.g. sugars and minerals) results in a relatively pure aqueous whey stream. Conventional soy whey streams from which the protein and one or more components have not been removed generally require treatment prior to disposal and/or reuse. In accordance with various aspects of the present disclosure the aqueous whey stream may be disposed of or utilized as process water with minimal, if any, treatment. For example, the aqueous whey stream may be used in one or more filtration (e.g. diafiltration) operations of the present disclosure.
In addition to recovery of BBI proteins from aqueous soy whey streams generated in the manufacture of soy protein isolates, it is to be understood that the processes described herein are likewise suitable for recovery of one or more components of soy molasses streams generated in the manufacture of a soy protein concentrate, as soy molasses streams are an additional type of soy processing stream.
The following is a general description of the various steps that make up the overall process. A key to the process is to start with the whey protein pretreatment step, which uniquely changes the soy whey and protein properties. From there, the other steps may be performed using the raw material sources as listed in each step, as will be shown in the discussion of the various embodiments to follow.
It is understood by those skilled in the art of separation technology that there can be residual components in each permeate or retentate stream since separation is never 100%. Further, one skilled in the art realizes that separation technology can vary depending on the starting raw material.
Step 0 (as shown in FIG. 4A)—Whey protein pretreatment can start with feed streams including but not limited to isolated soy protein (ISP) molasses, ISP whey, soy protein concentrate (SPC) molasses, SPC whey, functional soy protein concentrate (FSPC) whey, and combinations thereof. Processing aids that can be used in the whey protein pretreatment step include but are not limited to, acids, bases, sodium hydroxide, calcium hydroxide, hydrochloric acid, water, steam, and combinations thereof. The pH of step 0 can be between about 3.0 and about 6.0, preferably 4.5. The temperature can be between about 70° C. and about 95° C., preferably about 85° C. Temperature hold times can vary between about 0 minutes to about 20 minutes, preferably about 10 minutes. Products from the whey protein pretreatment include but are not limited to soluble components in the aqueous phase of the whey stream (pre-treated soy whey) (molecular weight of equal to or less than about 50 kiloDalton (kD)) in stream 0a (retentate) and insoluble large molecular weight proteins (between about 300 kD and between about 50 kD) in stream 0b (permeate), such as pre-treated soy whey, storage proteins, and combinations thereof.
Step 1 (as shown in FIG. 4A)—Microbiology reduction can start with the product of the whey protein pretreatment step, including but not limited to pre-treated soy whey. This step involves microfiltration of the pre-treated soy whey. Process variables and alternatives in this step include but are not limited to, centrifugation, dead-end filtration, heat sterilization, ultraviolet sterilization, microfiltration, crossflow membrane filtration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 1 can be between about 2.0 and about 12.0, preferably about 5.3. The temperature can be between about 5° C. and about 90° C., preferably about 50° C. Products from step 1 include but are not limited to storage proteins, microorganisms, silicon, and combinations thereof in stream 1a (retentate) and purified pre-treated soy whey in stream 1b (permeate).
Step 2 (as shown in FIG. 4A)—A water and mineral removal can start with the purified pre-treated soy whey from stream 1b or 4a, or pre-treated soy whey from stream 0b. It includes a nanofiltration step for water removal and partial mineral removal. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, reverse osmosis, evaporation, nanofiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 2 can be between about 2.0 and about 12.0, preferably about 5.3. The temperature can be between about 5° C. and about 90° C., preferably about 50° C. Products from this water removal step include but are not limited to purified pre-treated soy whey in stream 2a (retentate) and water, some minerals, monovalent cations and combinations thereof in stream 2b (permeate).
Step 3 (as shown in FIG. 4A)—the mineral precipitation step can start with purified pre-treated soy whey from stream 2a or pretreated soy whey from streams 0a or 1b. It includes a precipitation step by pH and/or temperature change. Process variables and alternatives in this step include but are not limited to, an agitated or recirculating reaction tank. Processing aids that can be used in the mineral precipitation step include but are not limited to, acids, bases, calcium hydroxide, sodium hydroxide, hydrochloric acid, sodium chloride, phytase, and combinations thereof. The pH of step 3 can be between about 2.0 and about 12.0, preferably about 8.0. The temperature can be between about 5° C. and about 90° C., preferably about 50° C. The pH hold times can vary between about 0 minutes to about 60 minutes, preferably about 10 minutes. The product of stream 3 is a suspension of purified pre-treated soy whey and precipitated minerals.
Step 4 (as shown in FIG. 4A)—the mineral removal step can start with the suspension of purified pre-treated whey and precipitated minerals from stream 3. It includes a centrifugation step. Process variables and alternatives in this step include but are not limited to, centrifugation, filtration, dead-end filtration, crossflow membrane filtration and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Products from the mineral removal step include but are not limited to a de-mineralized pre-treated whey in stream 4a (retentate) and insoluble minerals with some protein mineral complexes in stream 4b (permeate).
Step 5 (as shown in FIG. 4B)—the protein separation and concentration step can start with purified pre-treated whey from stream 4a or the whey from streams 0a, 1b, or 2a. It includes an ultrafiltration step. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, ultrafiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 5 can be between about 2.0 and about 12.0, preferably about 8.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 5a (retentate) include but are not limited to, soy whey protein, BBI, KTI, storage proteins, other proteins and combinations thereof. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. Products from stream 5b (permeate) include but are not limited to, peptides, soy oligosaccharides, minerals and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Minerals include but are not limited to calcium citrate.
Step 6 (as shown in FIG. 4B)—the protein washing and purification step can start with soy whey protein, BBI, KTI, storage proteins, other proteins or purified pre-treated whey from stream 4a or 5a, or whey from streams 0a, 1b, or 2a. It includes a diafiltration step. Process variables and alternatives in this step include but are not limited to, reslurrying, crossflow membrane filtration, ultrafiltration, water diafiltration, buffer diafiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Processing aids that can be used in the protein washing and purification step include but are not limited to, water, steam, and combinations thereof. The pH of step 6 can be between about 2.0 and about 12.0, preferably about 7.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 6a (retentate) include but are not limited to, soy whey protein, BBI, KTI, storage proteins, other proteins, and combinations thereof. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. Products from stream 6b (permeate) include but are not limited to, peptides, soy oligosaccharides, water, minerals, and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Minerals include but are not limited to calcium citrate.
Step 7 (as shown in FIG. 4C)—a water removal step can start with peptides, soy oligosaccharides, water, minerals, and combinations thereof from stream 5b and/or stream 6b. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. It includes a nanofiltration step. Process variables and alternatives in this step include but are not limited to, reverse osmosis, evaporation, nanofiltration, water diafiltration, buffer diafiltration, and combinations thereof. The pH of step 7 can be between about 2.0 and about 12.0, preferably about 7.0. The temperature can be between about 5° C. and about 90° C., preferably about 50° C. Products from stream 7a (retentate) include but are not limited to, peptides, soy oligosaccharides, water, minerals, and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Products from stream 7b (permeate) include but are not limited to, water, minerals, and combinations thereof.
Step 8 (as shown in FIG. 4C)—a mineral removal step can start with peptides, soy oligosaccharides, water, minerals, and combinations thereof from streams 5b, 6b, 7a, and/or 12a. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. It includes an electrodialysis membrane step. Process variables and alternatives in this step include but are not limited to, ion exchange columns, chromatography, and combinations thereof. Processing aids that can be used in this mineral removal step include but are not limited to, water, enzymes, and combinations thereof. Enzymes include but are not limited to protease, phytase, and combinations thereof. The pH of step 8 can be between about 2.0 and about 12.0, preferably about 7.0. The temperature can be between about 5° C. and about 90° C., preferably about 40° C. Products from stream 8a (retentate) include but are not limited to, de-mineralized soy oligosaccharides with conductivity between about 10 milli Siemens (mS) and about 0.5 mS, preferably about 2 mS, and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Products from stream 8b include but are not limited to, minerals, water, and combinations thereof.
Step 9 (as shown in FIG. 4C)—a color removal step can start with de-mineralized soy oligosaccharides from streams 8a, 5b, 6b, and/or 7a). It utilizes an active carbon bed. Process variables and alternatives in this step include but are not limited to, ion exchange. Processing aids that can be used in this color removal step include but are not limited to, active carbon, ion exchange resins, and combinations thereof. The temperature can be between about 5° C. and about 90° C., preferably about 40° C. Products from stream 9a (retentate) include but are not limited to, color compounds. Stream 9b is decolored. Products from stream 9b (permeate) include but are not limited to, soy oligosaccharides, and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof.
Step 10 (as shown in FIG. 4C)—a soy oligosaccharide fractionation step can start with soy oligosaccharides, and combinations thereof from streams 9b, 5b, 6b, 7a, and/or 8a. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. It includes a chromatography step. Process variables and alternatives in this step include but are not limited to, chromatography, nanofiltration, and combinations thereof. Processing aids that can be used in this soy oligosaccharide fractionation step include but are not limited to acid and base to adjust the pH as one know in the art and related to the resin used. Products from stream 10a (retentate) include but are not limited to, soy oligosaccharides such as sucrose, monosaccharides, and combinations thereof. Products from stream 10b (permeate) include but are not limited to soy oligosaccharides such as, raffinose, stachyose, verbascose, and combinations thereof.
Step 11 (as shown in FIG. 4C)—a water removal step can start with soy oligosaccharides such as, raffinose, stachyose, verbascose, and combinations thereof from streams 9b, 5b, 6b, 7a, 8a, and/or 10a. It includes an evaporation step. Process variables and alternatives in this step include but are not limited to, evaporation, reverse osmosis, nanofiltration, and combinations thereof. Processing aids that can be used in this water removal step include but are not limited to, defoamer, steam, vacuum, and combinations thereof. The temperature can be between about 5° C. and about 90° C., preferably about 60° C. Products from stream 11a (retentate) include but are not limited to, water. Products from stream 11b (permeate) include but are not limited to, soy oligosaccharides, such as, raffinose, stachyose, verbascose, and combinations thereof.
Step 12 (as shown in FIG. 4C)—an additional protein separation from soy oligosaccharides step can start with peptides, soy oligosaccharides, water, minerals, and combinations thereof from stream 7b. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. It includes an ultrafiltration step. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, ultrafiltration with pore sizes between about 50 kD and about 1 kD, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Processing aids that can be used in this protein separation from sugars step include but are not limited to, acids, bases, protease, phytase, and combinations thereof. The pH of step 12 can be between about 2.0 and about 12.0, preferably about 7.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 12a (retentate) include but are not limited to, soy oligosaccharides, water, minerals, and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Minerals include but are not limited to calcium citrate. This stream 12a stream can be fed to stream 8. Products from stream 12b (permeate) include but are not limited to, peptides, and other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Step 13 (as shown in FIG. 4C)—a water removal step can start with, peptides, and other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. It includes an evaporation step. Process variables and alternatives in this step include but are not limited to, reverse osmosis, nanofiltration, spray drying and combinations thereof. Products from stream 13a (retentate) include but are not limited to, water. Products from stream 13b (permeate) include but are not limited to, peptides, other proteins, and combinations thereof. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Step 14 (as shown in FIG. 4B)—a protein fractionation step may be done by starting with soy whey protein, BBI, KTI, storage proteins, other proteins, and combinations thereof from streams 6a and/or 5a. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. It includes an ultrafiltration (with pore sizes from 100 kD to 10 kD) step. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, ultrafiltration, nanofiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 14 can be between about 2.0 and about 12.0, preferably about 7.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 14a (retentate) include but are not limited to, storage proteins. Products from stream 14b (permeate) include but are not limited to, soy whey protein, BBI, KTI and, other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Step 15 (as shown in FIG. 4B)—a water removal step can start with soy whey protein, BBI, KTI and, other proteins from streams 6a, 5a, and/or 14b. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. It includes an evaporation step. Process variables and alternatives in this step include but are not limited to, evaporation, nanofiltration, RO, and combinations thereof. Products from stream 15a (retentate) include but are not limited to, water. Stream 15b (permeate) products include but are not limited to soy whey protein, BBI, KTI and, other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Step 16 (as shown in FIG. 4B)—a heat treatment and flash cooling step can start with soy whey protein, BBI, KTI and, other proteins from streams 6a, 5a, 14b, and/or 15b. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. It includes an ultra high temperature step. Process variables and alternatives in this step include but are not limited to, heat sterilization, evaporation, and combinations thereof. Processing aids that can be used in this heat treatment and flash cooling step include but are not limited to, water, steam, and combinations thereof. The temperature can be between about 129° C. and about 160° C., preferably about 152° C. Temperature hold time can be between about 8 seconds and about 15 seconds, preferably about 9 seconds. Products from stream 16 include but are not limited to, soy whey protein.
Step 17 (as shown in FIG. 4B)—a drying step can start with soy whey protein, BBI, KTI and, other proteins from streams 6a, 5a, 14b, 15b, and/or 16. It includes a drying step. The liquid feed temperature can be between about 50° C. and about 95° C., preferably about 82° C. The inlet temperature can be between about 175° C. and about 370° C., preferably about 290° C. The exhaust temperature can be between about 65° C. and about 98° C., preferably about 88° C. Products from stream 17a (retentate) include but are not limited to, water. Products from stream 17b (permeate) include but are not limited to, soy whey protein which includes, BBI, KTI and, other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
The soy whey protein products of the current application include raw whey, a soy whey protein precursor after the ultrafiltration step of Step 17, a dry soy whey protein that can be dried by any means known in the art, and combinations thereof. All of these products can be used as is as soy whey protein or can be further processed to purify specific components of interest, such as, but not limited to BBI, KTI, and combinations thereof.
Embodiment 1 starts with Step 0 (See
Step 5 (See
Embodiment 2—starts with Step 0 (See
Next Step 5 (See
Finally Step 6 (See
Embodiment 3 starts with Step 0 (See
Step 3 (See
Step 4 (See
Finally, Step 5 (See
Embodiment 4 starts with Step 0 (See
Step 3 (See
Step 4 (See FIG. 4A)—the mineral removal step can start with the suspension of purified pre-treated whey and precipitated minerals from stream 3. It includes a centrifugation step. Process variables and alternatives in this step include but are not limited to, centrifugation, filtration, dead-end filtration, crossflow membrane filtration and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Products from the mineral removal step include but are not limited to a de-mineralized pre-treated whey in stream 4a (retentate) and insoluble minerals with some protein mineral complexes in stream 4b (permeate).
Step 5 (See FIG. 4B)—the protein separation and concentration step can start with purified pre-treated whey from stream 4a. It includes an ultrafiltration step. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, ultrafiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 5 can be between about 2.0 and about 12.0, preferably about 8.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 5a (retentate) include but are not limited to, soy whey protein, BBI, KTI, storage proteins, other proteins and combinations thereof. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. Products from stream 5b (permeate) include but are not limited to, peptides, soy oligosaccharides, minerals and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Minerals include but are not limited to calcium citrate.
Finally, Step 6 (See
Embodiment 5 starts with Step 0 (See
Step 3 (See
Step 4 (See FIG. 4A)—the mineral removal step can start with the suspension of purified pre-treated whey and precipitated minerals from stream 3. It includes a centrifugation step. Process variables and alternatives in this step include but are not limited to, centrifugation, filtration, dead-end filtration, crossflow membrane filtration and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Products from the mineral removal step include but are not limited to a de-mineralized pre-treated whey in stream 4a (retentate) and insoluble minerals with some protein mineral complexes in stream 4b (permeate).
Step 5 (See
Step 6 (See FIG. 4B)—the protein washing and purification step can start with soy whey protein, BBI, KTI, storage proteins, other proteins or purified pre-treated whey from stream 5a. It includes a diafiltration step. Process variables and alternatives in this step include but are not limited to, reslurrying, crossflow membrane filtration, ultrafiltration, water diafiltration, buffer diafiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Processing aids that can be used in the protein washing and purification step include but are not limited to, water, steam, and combinations thereof. The pH of step 6 can be between about 2.0 and about 12.0, preferably about 7.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 6a (retentate) include but are not limited to, soy whey protein, BBI, KTI, storage proteins, other proteins, and combinations thereof. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. Products from stream 6b (permeate) include but are not limited to, peptides, soy oligosaccharides, water, minerals, and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Minerals include but are not limited to calcium citrate.
Step 16 (See
Finally, Step 17 (See FIG. 4B)—a drying step can start with soy whey protein, BBI, KTI and, other proteins from stream 16. It includes a drying step. The liquid feed temperature can be between about 50° C. and about 95° C., preferably about 82° C. The inlet temperature can be between about 175° C. and about 370° C., preferably about 290° C. The exhaust temperature can be between about 65° C. and about 98° C., preferably about 88° C. Products from stream 17a (retentate) include but are not limited to, water. Products from stream 17b (permeate) include but are not limited to, soy whey protein which includes, BBI, KTI and, other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Embodiment 6 starts with Step 0 (See
Step 3 (See
Step 4 (See
Step 5 (See
Step 6 (See
Step 15 (See
Step 16 (See
Finally, Step 17 (See FIG. 4B)—a drying step can start with soy whey protein, BBI, KTI and, other proteins from stream 16. It includes a drying step. The liquid feed temperature can be between about 50° C. and about 95° C., preferably about 82° C. The inlet temperature can be between about 175° C. and about 370° C., preferably about 290° C. The exhaust temperature can be between about 65° C. and about 98° C., preferably about 88° C. Products from stream 17a (retentate) include but are not limited to, water. Products from stream 17b (permeate) include but are not limited to, soy whey protein which includes, BBI, KTI and, other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Embodiment 7 starts with Step 0 (See
Step 2 (See
Finally, Step 5 (See
Embodiment 8 starts with Step 0 (See
Step 2 (See
Step 5 (See
Finally, Step 6 (See
Embodiment 9 starts with Step 0 (See
Step 2 (See
Step 3 (See
Step 4 (See
Step 5 (See
Embodiment 10 starts with Step 0 (See
Step 2 (See
Step 3 (See
Step 4 (See
Step 5 (See
Finally, Step 6 (See
Embodiment 11 starts with Step 0 (See
Step 2 (See
Step 3 (See
Step 4 (See FIG. 4A)—the mineral removal step can start with the suspension of purified pre-treated whey and precipitated minerals from stream 3. It includes a centrifugation step. Process variables and alternatives in this step include but are not limited to, centrifugation, filtration, dead-end filtration, crossflow membrane filtration and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Products from the mineral removal step include but are not limited to a de-mineralized pre-treated whey in stream 4a (retentate) and insoluble minerals with some protein mineral complexes in stream 4b (permeate).
Step 5 (See FIG. 4B)—the protein separation and concentration step can start with purified pre-treated whey from stream 4a. It includes an ultrafiltration step. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, ultrafiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 5 can be between about 2.0 and about 12.0, preferably about 8.0. The temperature can be between about 5° C. and about 90° C., preferably about 75° C. Products from stream 5a (retentate) include but are not limited to, soy whey protein, BBI, KTI, storage proteins, other proteins and combinations thereof. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof. Products from stream 5b (permeate) include but are not limited to, peptides, soy oligosaccharides, minerals and combinations thereof. Soy oligosaccharides include but are not limited to sucrose, raffinose, stachyose, verbascose, monosaccharides, and combinations thereof. Minerals include but are not limited to calcium citrate.
Step 6 (See
Step 16 (See
Finally, Step 17 (See FIG. 4B)—a drying step can start with soy whey protein, BBI, KTI and, other proteins from stream 16. It includes a drying step. The liquid feed temperature can be between about 50° C. and about 95° C., preferably about 82° C. The inlet temperature can be between about 175° C. and about 370° C., preferably about 290° C. The exhaust temperature can be between about 65° C. and about 98° C., preferably about 88° C. Products from stream 17a (retentate) include but are not limited to, water. Products from stream 17b (permeate) include but are not limited to, soy whey protein which includes, BBI, KTI and, other proteins. Other proteins include but are not limited to lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
Embodiment 12 starts with Step 0 (See
Step 2 (See
Step 3 (See
Step 4 (See
Step 5 (See
Step 6 (See
Step 15 (See
Step 16 (See
Finally, Step 17 (See
Embodiment 13 starts with Step 0 (See
Step 3 (See
Step 4 (See
Step 2 (See
Finally, Step 5 (See
Embodiment 14 starts with Step 0 (See
Step 3 (See
Step 4 (See
Step 2 (See
Step 5 (See
Finally, Step 6 (See
Embodiment 15 starts with Step 0 (See
Step 3 (See
Step 4 (See
Step 2 (See
Step 5 (See
Step 6 (See
Step 16 (See
Finally, Step 17 (See
Embodiment 16 starts with Step 0 (See
Step 3 (See
Step 4 (See
Step 2 (See
Step 5 (See
Step 6 (See
Step 15 (See
Step 16 (See
Finally, Step 17 (See
Embodiment 17 starts with Step 0 (See
Step 1 (See
Step 3 (See
Step 4 (See
Step 2 (See FIG. 4A)—A water and mineral removal can start with the purified pre-treated soy whey from stream 4a. It includes a nanofiltration step for water removal and partial mineral removal. Process variables and alternatives in this step include but are not limited to, crossflow membrane filtration, reverse osmosis, evaporation, nanofiltration, and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. The pH of step 2 can be between about 2.0 and about 12.0, preferably about 5.3. The temperature can be between about 5° C. and about 90° C., preferably about 50° C. Products from this water removal step include but are not limited to purified pre-treated soy whey in stream 2a (retentate) and water, some minerals, monovalent cations and combinations thereof in stream 2b (permeate).
Step 5 (See
Step 6 (See
Step 15 (See
Step 16 (See
Finally, Step 17 (See
Embodiment 18 starts with Step 0 (See
Step 1 (See
Step 2 (See
Step 3 (See
Step 4 (See FIG. 4A)—the mineral removal step can start with the suspension of purified pre-treated whey and precipitated minerals from stream 3. It includes a centrifugation step. Process variables and alternatives in this step include but are not limited to, centrifugation, filtration, dead-end filtration, crossflow membrane filtration and combinations thereof. Crossflow membrane filtration includes but is not limited to: spiral-wound, plate and frame, hollow fiber, ceramic, dynamic or rotating disk, nanofiber, and combinations thereof. Products from the mineral removal step include but are not limited to a de-mineralized pre-treated whey in stream 4a (retentate) and insoluble minerals with some protein mineral complexes in stream 4b (permeate).
Step 5 (See
Step 6 (See
Step 15 (See
Step 16 (See
Finally, Step 17 (See
Embodiment 19 encompasses Step 7 (See
Embodiment 20 starts with Step 7 (See
Finally, Step 11 (See
Embodiment 21 starts with Step 7 (See
Finally, Step 8 (See
Embodiment 22 starts with Step 7 (See
Step 8 (See
Finally, Step 11 (See
Embodiment 23 starts with Step 7 (See
Step 8 (See
Step 9 (See
Step 10 (See
Finally, Step 11 (See
The soy whey proteins that have been recovered from soy processing streams in accordance with the methods of the present disclosure and that possess the novel characteristics described in more detail in A., above, may further be used in food compositions. Specifically, the food compositions of the present invention comprise the soy whey proteins described herein combined with at least one additional ingredient to form a liquid food product. As will be appreciated by a skilled artisan, a variety of ingredients may be combined with the soy whey proteins of the present invention to produce a mix or pre-mix, which is then formed into a liquid food product. Specifically, the food products discussed herein are liquid food products, that include fluid, semi-fluid, or pliable solid matrix food products. Non-limiting examples of liquid food products include the following ready-to serve or ready-to-eat soups, canned condensed and dry mix soups; clear, thick, broths, cream, bisques, chowders, purees, meat and vegetable soups, soups with particulates, cold or chilled soups, dessert soups, fish soups, beverage soups and fermented soups. Examples of sauces include, without limitation, ready made sauces, salad sauces, pan sauces, vegetable sauces, dessert sauces, chocolate sauces, caramel sauces, white sauces, brown sauces, emulsified sauces, sweet sauces, fruit sauces, nut pastes including peanut, soy, and almond paste, jellies, jams, preserves, chutney, compotes, apple sauce, puddings, gelatin, mole sauces, sauce bases, such as espangole, velouté, Béchamel, Hollandaise, salsas, relishes, and cooked sauces. Non-limiting examples of gravies include, without limitation, various types of pan gravies, thickened style gravies and ready-to-serve gravies.
The liquid food products of the present invention will comprise, as one of the ingredients, soy whey protein which has been recovered from soy processing streams in accordance with the methods of the current invention. The amount of soy whey protein present in the ingredient(s) utilized can and will vary depending on the desired product and processing methods being used to produce the desired end product. For example, the amount of soy whey protein present in the ingredient(s) utilized for the liquid food products may range from about 0.01% to about 90% by weight. In another embodiment, the amount of soy whey protein present in the ingredient(s) utilized for the liquid food products may range from about 5% to about 30% by weight. In an additional embodiment, the amount of soy whey protein present in the ingredient(s) utilized for the liquid food products may range from about 10% to about 25% by weight.
The soy whey protein may be added at the initial hydration step or to the pre-mix or at a subsequent processing step in the preparation of the liquid food composition. For example, dry ingredients (i.e., dry blend pre-mix) or alternatively may be added to the composition with the liquid ingredients. In one embodiment, the soy whey protein is added in water as part of the initial hydration of the protein followed by addition of other formula ingredients. In an additional embodiment, the soy whey protein is added to the dry ingredients in a dry form as part of the dry blend pre-mix before adding to the liquid ingredients.
In addition to the soy whey protein obtained through the methods of the present disclosure, other optional protein-containing material may also be present in the ingredient(s) utilized for the liquid food products. While ingredients comprising proteins derived from plants are typically used, it is also envisioned that proteins derived from other sources, such as animal sources, may be utilized without departing from the scope of the invention. For example, a dairy protein selected from the group consisting of casein, caseinates, whey protein, and mixtures thereof, may be utilized. By way of further example, an egg protein selected from the group consisting of ovalbumin, ovoglobulin, ovomucin, ovomucoid, ovotransferrin, ovovitella, ovovitellin, albumin globulin, and vitellin may be used.
In an exemplary embodiment, at least one ingredient derived from a variety of suitable plants will be present in the ingredient(s) used to form the liquid food products. By way of non-limiting example, suitable plants include legumes, corn, peas, peanut, almonds, and various treenuts, canola, sunflower, sorghum, rice, amaranth, potato, tapioca, arrowroot, canna, lupin, rape, wheat, oats, rye, barley, and mixtures thereof. In a preferred embodiment, the additional protein-containing material is isolated from soybeans. In another exemplary embodiment, the additional protein-containing material is isolated from wheat. Suitable wheat-derived protein-containing ingredients include wheat gluten, wheat flour and mixtures thereof. In a further exemplary embodiment, the additional protein-containing material is isolated from rice and corn.
Suitable soybean derived protein-containing ingredients (“soy protein material”) which may be present in the ingredient(s) used to form the liquid food products include soy protein isolate, soy protein concentration, soy protein flour, soy protein hydrolysate, and mixtures thereof. Generally speaking, when soy isolate is used, an isolate is preferably selected that is not a highly hydrolyzed soy protein isolate. In certain embodiments, highly hydrolyzed soy protein isolates may be used in combination with other soy protein isolates. Examples of commercially available soy protein material that may be utilized in the invention include, for example and among them include SUPRO® 670, SUPRO® 120, SUPRO® PLUS 651, SUPRO® PLUS 3000, SUPRO® XF 8020, and combinations thereof, all of which are available from Solae, LLC (St. Louis, Mo.). The amount of protein present in the ingredient(s) utilized can and will vary depending upon the product and processing methods used.
The amount of additional protein-containing material that optionally may be present in the ingredient(s) utilized for the liquid food product may range from about 0% to about 80% by weight. In another embodiment, the amount of additional protein-containing material present in the ingredient(s) utilized for the liquid food products may range from about 10% to about 70% by weight. In an additional embodiment, the amount of additional protein-containing material that may be present in the ingredient(s) utilized for the liquid food products may range from about 20% to about 60% by weight. In another embodiment, no additional protein-containing material except for the soy whey protein is included in the food composition.
Soy cotyledon fiber may also be used as a fiber source. Soy cotyledon fiber may be present in the ingredient(s) utilized for the liquid food product in an amount ranging from about 0% to about 40%, preferably from about 1% to about 20%, and most preferably, from about 1.5% to about 5% by weight. Suitable soy cotyledon fiber is commercially available. For example, FIBRIM® 1270 is a soy cotyledon fiber material that is commercially available from Solae, LLC (St. Louis, Mo.).
The additional protein-containing material detailed above can be combined with at least one carbohydrate source. Generally, the carbohydrate source is starch (pre-gelatinized starch or a modified food starch) or flour (wheat, potato, rice, corn, konjac). Suitable starches are known in the art and may include starches derived from vegetables (including legumes) or grains. Non-limiting examples of suitable starches may include starch derived from corn, potato, rice, wheat, arrowroot, guar gum, locust bean, tapioca, arracacha, buckwheat, banana, barley, cassava, konjac, kudzu, oca, sago, sorghum, sweet potato, taro, yams, and mixtures thereof. Edible legumes, such as favas, lentils and peas are also rich in suitable starches.
Regardless of the specific starch used, the percentage of starch utilized in the liquid food product will be determined based on the desired end product and desired characteristics of the end product. For example, the amount of starch present in the ingredient(s) utilized for the liquid product may range from about 0.5% to about 80% by weight. In another embodiment, the amount of starch present in the ingredient(s) utilized for the liquid food products may range from about 1% to about 70% by weight. In an additional embodiment, the amount of starch that may be present in the ingredient(s) utilized for the liquid food products may range from about 2% to about 10% by weight.
As will be appreciated by the skilled artisan, the moisture content of the pre-mix can and will vary depending on the type of product being made and the process by which that product is produced. Generally speaking, the moisture content may range from about 0% to about 99% by weight.
In addition to the ingredients detailed in (a)-(c) above, a variety of other ingredients may be added to the pre-mix or at a subsequent processing step without departing from the scope of the invention. For example, dietary fiber, antioxidants, antimicrobial agents, leavening agents, emulsifiers, phospholipids, preservatives, flavoring agents, sweetening agents, coloring agents, pH-adjusting agents, other nutrients, and combinations thereof may be included.
In one embodiment, the pre-mix may comprise a vegetable oil. Non-limiting examples of suitable vegetable oils include palm oil, rapeseed oil, soybean oil, sunflower oil, canola oil, corn oil, coconut oil, lecithin, soy lecithin, and combinations thereof. The percent of the pre-mix comprised of a vegetable oil will depend, in part, on the vegetable oil used and desired product. Generally, a vegetable oil may comprise between about 0.1% and 45% by weight of the pre-mix. Preferably, a vegetable oil may comprise between about 1% and 30% by weight of the pre-mix.
In one embodiment, the pre-mix may comprise an emulsifier. Non-limiting examples of suitable emulsifiers include distilled mono and di-glycerides, propylene glycol monoesters, sodium stearoyl-2-lactylate, polsorbate 60, lecithin, hydroxylated lecithin, and combinations thereof. The percent of the pre-mix comprised of an emulsifier will depend, in part, on the emulsifier used and desired product. Generally, an emulsifier may comprise between about 0.01% and 10% by weight of the pre-mix. Preferably, an emulsifier may comprise between about 0.05% and 5% by weight of the pre-mix. More preferably, an emulsifier may comprise between about 0.5% to 2% by weight of the pre-mix.
Antioxidant additives include BHA, BHT, TBHQ, vitamins A, C, and E and derivatives, and various plant extracts such as those containing cartenoids, tocopherols or flavonoids having antioxidant properties, may be included to increase the shelf-life or nutritionally enhance the liquid food product. The antioxidants may have a presence at levels from about 0.01% to about 10%, preferably from about 0.05% to about 5%, and more preferably from about 0.1% to about 2% by weight of the ingredients.
[The liquid food composition may optionally include a thickening agent depending on the desired dessert product to be produced. Suitable thickening agents may include carrageenan, cellulose gum, cellulose gel, starch, maltodextrin, gum arabic, xanthan gum, and any other thickening agent known and used in the industry. The thickening agent may be present in the dessert composition at levels from about 0.01% to about 10%, preferably from about 0.05% to about 5%, and more preferably from about 0.1% to about 2% by weight of the ingredients. As will be appreciated by a skilled artisan, the amount of thickening agent, if any, added to the dessert composition can and will depend upon the type of dessert product desired.
In some embodiments, it may be desirable to lower or raise the pH of the liquid food composition depending on the type of end product desired. Thus, the liquid food composition may be contacted with a pH-adjusting agent. In one embodiment, the pH of the liquid food composition may range from about 3.0 to about 7.5. In another embodiment, the pH of the liquid food composition may be higher than about 7.2. Several pH-adjusting agents are suitable for use in the invention. The pH-adjusting agent may be organic or alternatively, it may be inorganic. In exemplary embodiments, the pH-adjusting agent is a food grade edible acid. Non-limiting acids suitable for use in the invention include acetic, lactic, hydrochloric, phosphoric, citric, tartaric, malic, glucono, deltalactone, gluconic, and combinations thereof. In an exemplary embodiment, the pH-adjusting agent is citric acid. In an alternative embodiment, the pH-adjusting agent may be a pH-raising agent, such as but not limited to disodium diphosphate and potassium hydroxide. As will be appreciated by a skilled artisan, the amount of pH-adjusting agent contacted with the liquid food composition can and will vary depending on several parameters, including, the agent selected and the desired pH.
The liquid food composition may optionally include a variety of flavorings, spices, or other ingredients to naturally enhance the final food product. As will be appreciated by a skilled artisan, the selection of ingredients added to the food composition can and will depend upon the final food product desired.
In one embodiment, the liquid food composition may further comprise a flavoring agent. The flavoring agent may include any suitable edible flavoring agent known in the art including, but not limited to, salt, an flower flavor, any spice flavor, vanilla, any fruit flavor, caramel, nut flavor, beef, poultry (e.g. chicken or turkey), pork or seafood flavors, dairy flavors such as butter and cheese, any vegetable flavor and combinations thereof.
The flavoring may also be sweet. Sugar, sweet dairy whey, soy molasses, corn syrup, corn syrup solids, stevia, monk fruit extract, honey, and fructose may be used for sweet flavors. Also, a sweetened flavor may include artificial flavor, such as sucralose and acesulfame potassium. Additionally, other sweet flavors may be used (e.g., chocolate, chocolate mint, caramel, toffee, butterscotch, mint, and peppermint flavorings). Sugar alcohols may also be used as sweeteners.
A wide variety of fruit or citrus flavors may also be used. Non-limiting examples of fruit or citrus flavors include strawberry, banana, pineapple, coconut, cherry, orange, and lemon flavors.
A wide variety of spice flavors may also be used. Non-limiting examples include herb and garlic, sour cream and onion, honey mustard, hot mustard, dry roast, barbecue, jalapeno, red pepper, garlic, chili, sweet and sour seasoning, sweet seasoning, hot and spicy seasoning, savory flavor seasoning, vegetable seasonings, and combinations thereof.
In an additional embodiment, the liquid food composition may further comprise a coloring agent. The coloring agent may be any suitable food coloring, additive, dye or lake known to those skilled in the art. Suitable food colorants may include, but are not limited to, for example, Food, Drug and Cosmetic (FD&C) Blue No. 1, FD&C Blue No. 2, FD&C Green No. 3, FD&C Red No. 3, FD&C Red No. 40, FD&C Yellow No. 5, FD&C Yellow No. 6, Orange B, Citrus Red No. 2 and combinations thereof. Other coloring agents may include annatto extract, b-apo-8′-carotenal, beta-carotene, beet powder, canthanxantin, caramel color, carrot oil, cochineal extract, cottonseed flour, ferrous gluconate, fruit juice, grape color extract, paprika, riboflavin, saffron, titanium dioxide, turmeric, and vegetable juice. These coloring agents may be combined or mixed as is common to those skilled in the art to produce a final coloring agent.
In a further embodiment, the liquid food composition may further comprise a nutrient such as a vitamin, a mineral, an antioxidant, an omega-3 fatty acid, or an herb. Suitable vitamins include Vitamins A, C and E, which are also antioxidants, and Vitamins B and D. Examples of minerals that may be added include the salts of aluminum, ammonium, calcium, magnesium, and potassium. Suitable omega-3 fatty acids include docosahexanenoic acid (DHA). Herbs that may be added include basil, celery leaves, chervil, chives, cilantro, parsley, oregano, tarragon, and thyme.
As referenced herein, the food compositions comprising soy whey proteins recovered from processing streams may undergo typical processing known in the industry to produce the desired liquid food product end product. Generally speaking, any method of processing known in the industry can be used to produce the desired liquid end product.
To facilitate understanding of the invention, several terms are defined below.
The term “acid soluble” as used herein refers to a substance having a solubility of at least about 80% with a concentration of 10 grams per liter (g/L) in an aqueous medium having a pH of from about 2 to about 7.
The terms “soy protein isolate” or “isolated soy protein,” as used herein, refer to a soy material having a protein content of at least about 90% soy protein on a moisture free basis.
The term “other proteins” as used herein referred to throughout the application are defined as including but not limited to: lunasin, lectins, dehydrins, lipoxygenase, and combinations thereof.
The term “soy whey protein” as used herein is defined as including protein soluble at those pHs where soy storage proteins are typically insoluble, including but not limited to BBI, KTI, lunasin, lipoxygenase, dehydrins, lectins, and combinations thereof. Soy whey protein may further include storage proteins.
The term “subject” or “subjects” as used herein refers to a mammal (preferably a human), bird, fish, reptile, or amphibian, in need of treatment for a pathological state, which pathological state includes, but is not limited to, diseases associated with muscle, uncontrolled cell growth, autoimmune diseases, and cancer.
The term “processing stream” as used herein refers to the secondary or incidental product derived from the process of refining a whole legume or oilseed, including an aqueous or solvent stream, which includes, for example, an aqueous soy extract stream, an aqueous soymilk extract stream, an aqueous soy whey stream, an aqueous soy molasses stream, an aqueous soy protein concentrate soy molasses stream, an aqueous soy permeate stream, and an aqueous tofu whey stream, and additionally includes soy whey protein, for example, in both liquid and dry powder form, that can be recovered as an intermediate product in accordance with the methods disclosed herein.
The term “liquid food product” as used herein refers to a fluid, semi-fluid, or pliable solid matrix food product formed by typical processing standards known in the industry.
When introducing elements of the present invention or the preferred embodiments(s) thereof, the articles “a,” “an,” “the” and “said” are intended to mean that there are one or more of the elements. The terms “comprising,” “including” and “having” are intended to be inclusive and mean that there may be additional elements other than the listed elements.
As various changes could be made in the above compounds, products and methods without departing from the scope of the invention, it is intended that all matter contained in the above description and in the examples given below, shall be interpreted as illustrative and not in a limiting sense.
145 liters of aqueous raw soy whey (not pre-treated) with a total solids content of 3.7% and dry basis protein content of 19.8% was microfiltered using two different membranes in an OPTISEP® 7000 module, manufactured by SmartFlow Technologies. The first membrane, BTS-25, was a polysulfone construction with 0.5 um pore size manufactured by Pall. Aqueous soy whey was concentrated to a 1.6× factor, at an average flux of 30 liters/meter2/hr (LMH). The concentrated aqueous soy whey was then passed through a modified polysulfone microfiltration membrane, MPS 0.45, manufactured by Pall. The aqueous soy whey was concentrated from 1.6× to 11× at an average flux of 28 LMH.
Permeate from the microfiltration process, 132 liters total, was then introduced into an OPTISEP® 7000 module with ultrafiltration membranes, RC100, which are 100 kDa regenerated cellulose membranes manufactured by Microdyn-Nadir. The microfiltered aqueous soy whey was concentrated to about 20× using a 20 L tank setup at an average flux of 30 LMH before being transferred to a 5 L tank setup in order to minimize the hold-up volume of the system. In the smaller tank, the aqueous soy whey was concentrated from 20× to 66× at an average flux rate of 9 LMH, reaching a final retentate volume of 2 liters. The final retentate was 24.0% total solids, and 83.0% dry basis protein content.
128 liters of sugar and mineral enriched RC100 permeate was then introduced into an OPTISEP® 7000 module with polysulfone thin film nanofiltration membranes with a 35% NaCl rejection rate, NF20, manufactured by Sepro. The feed was concentrated 18× at an average flux rate of 4.7 LMH. The retentate from this process step, 9 liters, was enriched in the various sugar species. The permeate stream from the NF20 separation process, 121 liters, contained the minerals and water.
The permeate of the NF20 process was then introduced into an OPTISEP® 3000 module with thin film reverse osmosis membranes with a 98.2% NaCl rejection rate, SG, manufactured by GE. The feed was concentrated 12× at an average flux rate of 8 LMH. The permeate of the SG membrane, 9.2 liters, consisted primarily of water, suitable for re-use in a process with minimal further treatment. The retentate of the SG process, 0.8 liters, consisted predominantly of a concentrated mineral fraction.
61.7 liters of soy molasses with a total solids content of 62.7% and dry basis protein content of 18.5% was diluted with 61.7 liters of water prior to microfiltration. The diluted soy molasses was then microfiltered using an OPTISEP® 7000 module, manufactured by SmartFlow Technologies. The diluted soy molasses passed through a modified polysulfone microfiltration membrane, MPS 0.45, manufactured by Pall. The diluted soy molasses was concentrated to a 1.3× factor, at an average flux of 6 liters/meter2/hr (LMH).
Permeate from the microfiltration process, 25 liters total, was then introduced into an OPTISEP® 7000 module with ultrafiltration membranes, RC100, which are 100 kDa regenerated cellulose membranes manufactured by Microdyn-Nadir. The microfiltered diluted soy molasses was diafiltered with 2 volumes of water prior to being concentrated to 7.6× at an average flux of 20 LMH, reaching a final retentate volume of 2 liters. The final retentate was 17.5% total solids, and 22.0% dry basis protein content.
72 liters of sugar and mineral enriched RC100 permeate was then introduced into an OPTISEP® 7000 module with polysulfone thin film nanofiltration membranes with a 35% NaCl rejection rate, NF20, manufactured by Sepro. The feed was concentrated 3× at an average flux rate of 4.0 LMH. The retentate from this process step, 23 liters, was enriched in the various sugar species. The permeate stream from the NF20 separation process, 48 liters, contained the minerals and water.
A portion of the permeate of the NF20 process, 10 liters, was then introduced into an OPTISEP® 3000 module with thin film reverse osmosis membranes with a 98.2% NaCl rejection rate, SG, manufactured by GE. The feed was concentrated 6.7× at an average flux rate of 7.9 LMH. The permeate of the SG membrane, 8.5 liters, consisted primarily of water, suitable for re-use in a process with minimal further treatment. The retentate of the SG process, 1.5 liters, consisted predominantly of a concentrated mineral fraction.
Defatted soy flour (DSF) was extracted by adding a 15:1 ratio of water to DSF at a pH of 7.8 and stirring for 20 minutes prior to filtration. The extract was microfiltered using an OPTISEP® 800 module, manufactured by SmartFlow Technologies. The microfiltration membrane, MMM-0.8, was a polysulfone and polyvinylpropylene construction with 0.8 um pore size manufactured by Pall. Aqueous soy extract was concentrated to a 2.0× factor, at an average flux of 29 liters/meter2/hr (LMH). Permeate from the microfiltration process was then introduced into an OPTISEP® 800 module with ultrafiltration membranes, RC100, which are 100 kDa regenerated cellulose membranes manufactured by Microdyn-Nadir. The microfiltered aqueous soy extract was concentrated to about 6.3× at an average flux rate of 50 LMH. The final retentate measured 84.7% dry basis protein content.
CSEP experiments were performed by passing feed material (soy whey) through a column (ID 1.55 cm, length 9.5 cm, volume 18 mL) packed with SP GibcoCel resin. The column was connected to a positive displacement pump and samples of flow through and eluates were collected at the outlet of the column. Different experimental conditions were used to determine the effect of feed concentration, feed flow rate and elution flow rate on the binding capacity of the resin.
Feed Concentration
Soy whey was prepared from the defatted soy flake. Briefly, one part of defatted flake was mixed with 15 parts of water at 32° C. The pH of the solution was adjusted to 7.0 using 2 M NaOH and proteins were extracted into the aqueous phase by stirring the solution for 15 min. The protein extract was separated from the insoluble material by centrifugation at 3000×g for 10 min. The pH of the collected supernatant was adjusted to 4.5 using 1 M HCl and the solution was stirred for 15 min followed by heating to a temperature of 57° C. This treatment resulted in precipitation of the storage proteins while the whey proteins remained soluble. The precipitated proteins were separated from the whey by centrifugation at 3000×g for 10 min.
In some cases, the soy whey was concentrated using a Lab-Scale Amicon DC-10LA ultrafiltration unit and Amicon 3K membrane. Prior to ultrafiltration, pH of soy whey was adjusted to 5.5 with 2 M NaOH to avoid membrane fouling at acidic conditions. 10 L of whey was processed with the flux at ˜100 mL/min. Once the concentration factor of 5 in the retentate was reached, both retentate and permeate streams were collected. Soy whey concentrates 2.5×, 3×, and 4× were prepared by mixing a known amount of permeate and 5× whey concentrate. The pH of all soy concentrates was readjusted if necessary to 4.5.
Feed Flow Rate
During dynamic adsorption, as fluid flows through the resin bed, the proteins are adsorbed by the resin and reach equilibrium with the liquid phase. As the whey is loaded onto the column, the bound protein band extends down the column and reaches equilibrium with the liquid phase. When the resin is saturated with adsorbed proteins, the concentration of the proteins in the liquid phase exiting the column will be similar to the protein concentration in the feed. The curve describing the change in the flow through concentration compared to the feed concentration with the passage of fluid is the breakthrough curve. The concentration of protein in the solid phase increases as the breakthrough curve is developed, and the adsorption wave moves through the bed. As more fluid is passed through the bed, the flow through concentration increases asymptotically to the incoming fluid stream and at the same time a similar phenomena is achieved with the solid phase.
The flow through protein concentration data at three different linear velocity rates were plotted against the column volumes of soy whey loaded (see
The profile of the breakthrough curve, where soy whey and soy whey concentrated by a factor of 3 and 5 was applied to an SP Gibco resin bed at 15 mL/min (8.5 cm/min linear flow rate), was similar with all three concentrations (see
Based on the dynamic adsorption data (see
Elution Flow Rate
The effect of elution flow rate was investigated at three different flow rates and the recovery data are shown in Table 3. The recovery of protein at low flow rates in duplicate experiments resulted in recoveries of over 164% and 200%. The data indicate that eluting at 20 and 30 mL/min (11.3 and 17.0 cm/min, respectively) did not significantly affect the recoveries. Moreover, operating at higher flow rates achieved much faster elution (see
The feed stream to the process, pre-treated whey protein, (also referred to PT whey) had approximately 1.4%-2.0% solids. It was comprised of approximately 18% minerals, 18% protein, and 74% sugars and other materials. Implementation of a Nanofiltration (NF) process allowed for water removal while retaining most of the sugars and protein, and other solid material, in the process to be recovered downstream. The NF membranes (Alfa Laval NF99 8038/48) for the trial were polyamide type thin film composite on polyester membranes with a 2 kDa molecular weight cutoff (MWCO) that allowed water, monovalent cations, and a very small amount of sugars and protein to pass through the pores. The membrane housing held 3 membrane elements. Each element was 8 inches in diameter and had 26.4 square meters of membrane surface area. The total membrane surface area for the process was 79.2 square meters. These membranes were stable up to 1 bar of pressure drop across each membrane element. For the entire module containing 3 membrane elements, a pressure drop of 3 bar was the maximum allowable. The NF feed rate of PT whey was approximately 2,500 L/hour. The temperature of this feed was approximately 45-50° C., and the temperature of the NF operation was regulated to be in this range using cooling water. Initial product flux rates were approximately 16-22 liters per meter squared per hour (LMH). The feed pressure at the inlet of the module was approximately 6 bar. Through the duration of the 6 hour run, the flux dropped as a result of fouling. The feed pressure was increased incrementally to maintain higher flux, but as fouling occurred, the pressure was increased to the maximum, and the flux slowly tapered from that point. Volumetric concentration factors were between 2× and approximately 4×.
A Precipitation step was performed to separate, e.g., phosphorous and calcium salts and complexes from the PT whey. Precipitation conditions were at pH 9 while maintaining the temperature at 45° C. with a residence time of approximately 15 minutes. The precipitation process occurred in a 1000 liter. This tank had multiple inlets and outlets where materials can be piped into and out of it. A small centrifugal pump circulated product out of the tank and back into the side of the tank to promote agitation and effective mixing of the 35% NaOH added to the system to maintain the target pH. This pump also sent product into the centrifuge when one of the T-valves connected to this recirculation loop was opened. Concentrated PT whey from the NF was fed directly into the top of the tank. 35% NaOH was connected into the feed line from the NF in order to control the pH at the target value. PT whey was fed into this mixing tank at approximately 2,500 L/hour and fed out at the same rate.
In following process step, an Alfa Laval Disc Centrifuge (Clara 80) with intermittent solids ejection system was used to separate precipitated solids (including insoluble soy fiber, insoluble soy protein) from the rest of the sugar- and protein-containing whey stream. In this process, concentrated PT whey from the precipitation tank was pumped into a disc-centrifuge where this suspension was rotated and accelerated by centrifugal force. The heavier fraction (precipitated solids) settles on the walls of the rotating centrifuge bowl with the lighter fraction (soluble liquid) was clarified through the use of disc-stacks and continuously discharged for the next step of the process. The separated precipitated solids was discharged at a regular interval (typically between 1 and 10 minutes). The clarified whey stream was less then 0.2% solids on a volumetric basis. The continuous feed flow rate was approximately 2.5 m3/hr, with a pH of 9.0 and 45° C. The insoluble fraction reached Ash=30-60%; Na=0.5-1.5% dry basis, K=1.5-3% dry basis, Ca=6-9% dry basis, Mg=3-6% dry basis, P=10-15% dry basis, Cl=1-2% dry basis, Fe, Mn, Zn, Cu<0.15% dry basis. Changes to the soluble fraction were as follows: Phytic acid was approximately 0.3% dry basis (85% reduction, P=0.2-0.3% dry basis (85-90% reduction), Ca=0.35-0.45% dry basis (80-85% reduction), Mg=0.75-0.85% dry basis (15-20% reduction).
The next step was an Ultrafiltration (UF) membrane. Protein was concentrated by being retained by a membrane while other smaller solutes pass into the permeated stream. From the centrifuge a diluted stream the containing protein, minerals and sugars was fed to the UF. The UF equipment and the membrane were supplied from Alfa Laval while the CIP chemicals came from Ecolab, Inc. The tested membrane, GR70PP/80 from Alfa-Laval, had a MWCO of 10 kD and was constructed of polyethersulfone (PES) cast onto a polypropylene polymer backing. The feed pressure varied throughout the trial from 1-7 bar, depending upon the degree of fouling of the membranes. The temperature was controlled to approximately 65° C. The system was a feed and bleed setup, where the retentate was recycled back to the feed tank while the permeate proceeded on to the next step in the process. The system was operated until a volume concentration factor of 30× was reached. The feed rate to the UF was approximately 1,600 L/hour. The setup had the ability to house 3 tubes worth of 6.3″ membrane elements. However, only one of the three tubes was used. The membrane skid had an automatic control system that allowed control of the temperature, operating pressures (inlet, outlet, and differential) and volume concentration factor during process. Once the process reached the target volume concentration factor, typically after 6-8 hours of operation, the retentate was diafiltered (DF) with one cubic meter of water, (approximately 5 parts of diafiltration water per part of concentrated retentate) to yield a high protein retentate. After a processing cycle, the system was cleaned with a typical CIP protocol used with most protein purification processes. The retentate contained about 80% dry basis protein after diafiltration.
The permeate of the UF/DF steps contained the sugars and was further concentrated in a Reverse Osmosis Membrane system (RO). The UF permeate was transferred to an RO system to concentrate the feed stream from approximately 2% total solids (TS) to 20% TS. The process equipment and membranes (RO98pHt) for the RO unit operation were supplied by Alfa-Laval. The feed pressure was increased in order to maintain a constant flux, up to 45 bar at a temperature of 50° C. Typically each batch started at a 2-3% Brix and end at 20-25% Brix (Brix=sugar concentration).
After the RO step the concentrated sugar stream was fed to an Electrodialysis Membrane (ED). Electrodialysis from Eurodia Industrie SA removes minerals from the sugar solution. The electrodialysis process has two product streams. One is the product, or diluate, stream which was further processed to concentrate and pasteurize the SOS concentrate solution. The other stream from the electrodialysis process is a brine solution which contains the minerals that were removed from the feed stream. The trial achieved >80% reduction in conductivity, resulting in a product stream that measured <3 mS/cm conductivity. The batch feed volume was approx 40 liters at a temperature of 40° C. and a pH of 7. The ED unit operated at 18V and had up to 50 cells as a stack size.
The de-mineralized sugar stream from the ED was further processed in an Evaporation step. The evaporation of the SOS stream was carried out on Anhydro's Lab E vacuum evaporator. SOS product was evaporated to 40-75% dry matter with a boiling temperature of approximately 50-55° C. and a ΔT of 5-20° C.
A Spray Dryer was used to dry UF/DF retentate suspension. The UF diafiltrate retentate, with a solids content of approximately 8%, was kept stirred in a tank. The suspension was then fed directly to the spray dryer where it was combined with heated air under pressure and then sprayed through a nozzle. The dryer removed the water from the suspension and generated a dry powder, which was collected in a bucket after it was separated from the air stream in a cyclone. The feed suspension was thermally treated at 150° C. for 9 seconds before it entered the spray dryer to kill the microbiological organisms. The spray dryer was a Production Minor from the company Niro/GEA. The dryer was set up with co-current flow and a two fluid nozzle. The drying conditions varied somewhat during the trial. Feed temperatures were about 80° C., nozzle pressure was about 4 bars, and inlet air temperatures was about 250° C.
Approximately 8000 lbs of aqueous soy whey (also referred to as raw whey) at 110° F. and 4.57 pH from an isolated soy protein extraction and isoelectric precipitation continuous process was fed to a reaction vessel where the pH was increased to 5.3 by the addition of 50% sodium hydroxide. The pH-adjusted raw whey was then fed to a second reaction vessel with a 10 minute average residence time in a continuous process where the temperature was increased to 190° F. by the direct injection of steam. The heated and pH-adjusted raw whey was then cooled to 90 degrees F. by passing through a plate and frame heat exchanger with chilled water as the cooling medium. The cooled raw whey was then fed into an Alfa Laval VNPX510 clarifying centrifuge where the suspended solids, predominantly insoluble large molecular weight proteins, were separated and discharged in the underflow to waste and the clarified centrate proceeded to the next reaction vessel. The pH of the clarified centrate, or pre-treated whey protein, was adjusted to 8.0 using 12.5% sodium hydroxide and held for 10 minutes prior to being fed into an Alfa Laval VNPX510 clarifying centrifuge where the suspended solids, predominantly insoluble minerals, were separated and discharged in the underflow to waste. The clarified centrate proceeded to a surge tank prior to ultrafiltration. Ultrafiltration of the clarified centrate proceeded in a feed and bleed mode at 90° F. using 3.8″ diameter polyethersulfone spiral membranes, PW3838C, made by GE Osmonics, with a 10 kDa molecular weight cut-off. Ultrafiltration continued until a 60× concentration of the initial feed volume was accomplished, which required about 4.5 hrs. The retentate, 114 lbs at 4.5% total solids and 8.2 pH, was transferred to a reaction vessel where the pH was adjusted to 7.4 using 35% hydrochloric acid. The retentate was then heated to 305° F. for 9 seconds via direct steam injection prior to flash cooling to 140° F. in a vacuum chamber. The material was then homogenized by pumping through a homogenizing valve at 6000 psi inlet and 2500 outlet pressure prior to entering the spray drier through a nozzle and orifice combination in order to atomize the solution. The spray drier was operated at 538° F. inlet temperature and 197° F. outlet temperature, and consisted of a drying chamber, cyclone and baghouse. The spray dried soy whey protein, a total of 4 lbs, was collected from the cyclone bottom discharge.
200 ml of aqueous raw soy whey (not pre-treated) with a total solids content of 1.92%, was adjusted to pH 4.5 with acetic acid and applied to a 1×25 cm column of Mimo6ME resin (UpFront Chromatography, Copenhagen Denmark) equilibrated in 10 mM sodium citrate, pH 4.5. Material was loaded onto the column from the bottom up at 20-25° C. using a linear flow rate of 7.5 cm/min. Samples of the column flow-through were collected at regular intervals for later analysis. Unbound material was washed free of the column with 10 column volumes of equilibration buffer, then bound material recovered by elution with 50 mM sodium hydroxide. 10 μls of each fraction recovered during EBA chromatography of aqueous soy whey were separated on a 4-12% SDS-PAGE gel and stained with Coomassie Brilliant Blue R 250 stain. SDS-PAGE analysis of the column load, flow-through, wash, and sodium hydroxide eluate samples is depicted in
Spray-dried soy whey powder was slurried to a concentration of 10 mg/ml in water and adjusted to pH 4.0 with acetic acid. 400 ml of the slurry was then applied directly to the bottom of a 1×25 cm column of Mimo-4SE resin (UpFront Chromatography, Copenhagen Denmark) that had been equilibrated in 10 mM sodium citrate, pH 4.0. Material was loaded at 20-25° C. using a linear flow rate of 7.5 cm/min. Samples of the column flow-through were collected at regular intervals for later analysis. Unbound material was washed free of the column using 10 column volumes of equilibration buffer. Bound material was eluted with 30 mM NaOH. 10 μls of each fraction recovered during EBA chromatography of a suspension of soy whey powder were separated on a 4-12% SDS-PAGE gel and stained with Coomassie Brilliant Blue R 250 stain. SDS-PAGE analysis of the column load, flow-thru, wash, and eluate are depicted in
Two procedures were used to remove the majority of contaminating KTI protein from the bulk of the soy whey protein by EBA chromatography. In the first, 200 ml of aqueous raw soy whey (not pre-treated) with a total solids content of 1.92%, was adjusted to pH 6.0 with sodium hydroxide and applied to a 1×25 cm column of Mimo6HE resin (UpFront Chromatography, Copenhagen Denmark) equilibrated in 10 mM sodium citrate, pH 6.0. Material was loaded onto the column from the bottom up at 20-25° C. using a linear flow rate of 7.5 cm/min. Samples of column flow-through were collected at regular intervals for later analysis. Unbound material was washed free of the column with 10 column volumes of equilibration buffer, then bound material recovered by elution with 30 mM sodium hydroxide. 10 μls of each fraction recovered during EBA chromatography of a suspension of soy whey powder were separated on a 4-12% SDS-PAGE gel and stained with Coomassie Brilliant Blue R 250 stain. SDS-PAGE analysis of the column load, flow-through, wash, and sodium hydroxide eluate samples is depicted in
In the second procedure, 160 mls of aqueous raw soy whey (not pre-treated) with a total solids content of 1.92%, was adjusted to pH 5.1 with acetic acid and applied to a 1×25 cm column of Mimo6ZE resin (UpFront Chromatography, Copenhagen Denmark) equilibrated in10 mM sodium citrate, pH 5.0. Material was loaded onto the column from the bottom up at 20-25° C. using a linear flow rate of 7.5 cm/min. Samples of column flow-through were collected at regular intervals for later analysis. Unbound material was washed free of the column with 10 column volumes of equilibration buffer, then bound material recovered by elution with 30 mM sodium hydroxide. 10 μls of each fraction recovered during EBA chromatography of a suspension of soy whey powder were separated on a 4-12% SDS-PAGE gel and stained with Coomassie Brilliant Blue R 250 stain. SDS-PAGE analysis of the column load, flow-through, wash, and sodium hydroxide eluate samples is depicted in
A tomato based red sauce was prepared using soy whey protein recovered from a soy processing stream as described in the present invention, SWP, according to typical industry processing techniques following the process below. Table 4 is the list of ingredients used to prepare the red sauce and the amount used in concentration (%) and total weight (grams).
The red sauce was formed by first adding the soy whey protein to water that had been pre-heated to a temperature of 37.8° C. and mixing in a conventional food processing kettle such as a stainless steel jacketed kettle equipped with air operated propeller mixer using moderate shear mixing. The soy whey protein was mixed slowly in the water for 10 minutes until it was allowed to hydrate and completely disperse. Next the tomato paste was added to the protein slurry and mixed at ambient temperature for time sufficient to thoroughly mix the components. After thoroughly mixing the temperature of the mixture was increased to 60° C. Upon reaching the desired temperature the SBO oil was added to the tomato paste mixture. In a separate container the sugar and potato starch were dry blended to form a mixture. Upon thoroughly mixing the sugar and potato starch mixture it was added to the tomato paste mixture. The mixture was then heated to 76° C.-82.2° C. and held at this temperature for 5 minutes. After this heating stage the remaining salt and seasoning (salt, garlic, basil, tomato flavor and natural pepper) ingredients were added to the tomato paste mixture to form the red sauce. Upon adding the remaining ingredients the pH of the red sauce was tested to ensure a pH between 4.0 and 4.1. The pH of the red sauce was 4.44 so to obtain the desired pH range 8 mL of citric acid was added to the red sauce, resulting in a pH of 3.9. (please note the amount of citric acid will be dependent on each specific batch). The red sauce was then held at a temperature of 82.2° C. for an amount of time sufficient to pasteurize before it was packaged.
The red sauce produced according to the method described above was higher in protein and enhanced in body and texture compared to the typical red sauces on the market, which have little or no protein. The prepared red sauce also retained the structure and aroma of a typical red sauce currently on the market.
An alfredo based white sauce was prepared using soy whey protein recovered from a soy processing stream as described in the present invention, SWP, according to typical industry processing techniques following the process below. Table 5 is the list of ingredients used to prepare the alfredo sauce and the amount used in concentration (%) and total weight (grams).
The alfredo sauce was formed by first heating the water in a suitable container to a temperature of approximately 60° C. The phosphate was then added and mixed until completely dissolved. The soy whey protein was then added to the water and mixed with a vortex at a moderate speed, until the soy whey protein was completely dispersed. The mixing was adjusted to a lower speed and continued for 6 to 10 minutes to thoroughly mix the ingredients. A dry blend of the maltodextrins, starch, flour and sugar were combined until thoroughly mixed. After dry blending the mixture the dry blended mixture was added to the protein slurry. Mixing was continued for 5 minutes after the blend was complete dispersed. Next the oil was added to the mixture and thoroughly mixed for 3 minutes. Finally the remaining ingredients including salt and flavors were added to the mixture and mixed for 3 additional minutes. After adding the remaining ingredients the pH of the mixture was measured to ensure a pH range of between 6.8 and 7.0. If adjustments to the pH are required, a basic or acidic component can be added to ensure the required range is met. The last step was to pasteurize and homogenize the alfredo sauce. Pasteurization was completed at standard industry settings (HTST 82.2° C.) or (UHT 141° C.) for 6 seconds. Homogenization was completed at standard industry settings (500 psi, 2nd stage; 2500 psi 1st stage).
The alfredo sauce produced according to the method described above had a higher amount of protein, while retaining the aroma and appearance of a typical alfredo sauce currently on the market.
A soy butter composition was prepared using soy whey protein recovered from a soy processing stream as described in the present invention, SWP, according to typical industry processing techniques using the step-by-step process described below. Table 6 is the list of ingredients that was used to prepare the soy butter composition and the amount used expressed in concentration (%) and weight (grams).
The soy butter was prepared by first heating the oil to 77° C. The emulsifier was added to the oil and mixed until it was completely dispersed within the oil. The ingredients that include coloring and flavoring were added to the oil mixture and mixed at low to moderate speed until the mixture is well blended. After the mixture was thoroughly blended the Soy Whey Protein was added and mixed until completely blended, about 5-10 minutes at a low to moderate speed. Finally, the powdered sugar and maltodextrin were added and mixed until thoroughly blended and the mixture was uniform, about 5-10 minutes and at low to moderate speed. The soy butter was then packaged according to typical industry standards.
The soy butter made by the method described above was found to have an increased amount of oil absorbtion capabilities, in addition to the following test specific characteristics set forth in Table 7.
A soup was prepared using soy whey protein recovered from a soy processing stream as described in the present invention, SWP, according to typical industry processing techniques used to create soup within the industry following the process below. Table 8 is the list of ingredients used to prepare the soup and the amount used expressed in both concentration (%) and weight (grams).
The soups were formed by first adding the citrate and phosphate. Next the soy whey protein was added to the water until hydrated and thoroughly mixed. During mixing the water and soy slurry was heated to 65.5° C. The soy slurry and water was allowed to mix and hydrate for 15 minutes to ensure uniform hydration and mixing of the slurry. In a separate container the oil and distilled mono & diglycerides blend was heated to between 40.5° C.-48.8° C. and the mixture was moderately agitated to ensure uniform mixing. Next the oil mixture was slowly added to the soy slurry and mixed for 5 minutes. Next the soy protein slurry was homogenized at 3000 psi (2500 psi first stage and 500 psi second stage). The mixture was weighed to ensure the correct amount of CHO ingredients were added in the next phase. After the mixture was weighed the carbohydrates and salt (sugar, corn syrup solids and maltodextrin) were added and thoroughly mixed for 3 minutes to ensure a uniform product. After thoroughly mixing the carbohydrates and sugar the remaining ingredients were added, including the vitamins and minerals. These ingredients were mixed for 5 minutes at low to moderate speed for thorough distribution within the mixture. The pH was measured to ensure the target pH of 6.8-7.0 was maintained. If needed an amount of a basic or acidic food grade component can be added to ensure the pH target range is met, such as 45% potassium hydroxide. Additionally an anti-foaming food grade agent may be required on an as needed basis. The mixture was then processed according to typical industry practice to aid in shelf stabilization including pasteurization and homogenization. Pasteurized at Ultra High Temperature of 142° C. for 6 seconds and Homogenized at 3000 psi (2500 psi first stage and 500 psi second stage). The product was then cooled and packaged and placed in a cold water bath and refrigerated until further testing.
The soups that were made by the method described above contained higher amounts of protein, while retaining the aroma and appearance of typical soups currently on the market.
A dressing composition can be prepared using soy whey protein recovered from a soy processing stream as described in the present invention, SWP, according to typical industry processing techniques using the step-by-step process described below. Table 9 is the list of ingredients that can be used to prepare the Fat-Free Pourable Dressing composition.
A creamy Italian fat free dressing can be prepared using the above recipe that incorporates soy whey protein. First the calcium disodium EDTA is dispersed within cold tap water using an Arde Barinco Mixer set at 1500 rpm until thoroughly mixed. Next the soy whey protein is added to the water and thoroughly mixed for 6 minutes until a complete dispersion is achieved and the mixture in uniform. All remaining dry ingredients (except for salt) are dry blended in a separate container. These ingredients are then added to the soy whey protein slurry and mixed at a speed of 3500 rpm for 10 minutes to create a thoroughly mixed slurry. Next the salt is added to the slurry mixture and mixing continued for an additional minute before the final step of slowly adding the vinegar to the mixture and continuing to mix for an additional 3 minutes. The dressing can then be packaged according typical industry standards.
A dressing made by the method described above will have an increased amount of protein, while retaining aroma and appearance of typical fat-free pourable dressing product currently on the market.
One skilled in the art would readily appreciate that the methods, compositions, and products described herein are representative of exemplary embodiments, and not intended as limitations on the scope of the invention. It will be readily apparent to one skilled in the art that varying substitutions and modifications may be made to the present disclosure disclosed herein without departing from the scope and spirit of the invention.
All patents and publications mentioned herein are herein incorporated by reference, including without limitation PCT Application No. PCT/US10/62591 as it relates to any and all teachings related to soy whey protein, to the same extent as if each individual publication was specifically and individually indicated as incorporated by reference.
The present disclosure illustratively described herein suitably may be practiced in the absence of any element or elements, limitation or limitations that are not specifically disclosed herein. Thus, for example, in each instance herein any of the terms “comprising,” “consisting essentially of,” and “consisting of” may be replaced with either of the other two terms. The terms and expressions which have been employed are used as terms of description and not of limitation, and there is no intention that in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the present disclosure claimed. Thus, it should be understood that although the present disclosure has been specifically disclosed by preferred embodiments and optional features, modification and variation of the concepts herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention as defined by the appended claims.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/US11/42405 | 6/29/2011 | WO | 00 | 12/20/2013 |
