WO2021154766A1 - Methods of extracting starch or protein from agricultural products - Google Patents

Abstract

Methods are described for extracting starch and/or protein from agricultural products, such as wheat, potatoes, and maize. The methods include utilizing continuous or semi-continuous dosages of monochloramine at various stages of the methods. The methods can result in an increase of the amount of starch and/or protein extracted as well as one or more other benefits.

Description

METHODS OF EXTRACTING STARCH OR PROTEIN FROM AGRICULTURAL PRODUCTS

BACKGROUND OF THE INVENTION

[0001] This application claims the benefit under 35 U.S.C. §119(e) of prior U.S. Provisional Patent Application No. 62/966,700 filed January 28, 2020, which is incorporated in its entirety by reference herein.

[0002] The present invention relates to methods for extracting starch and/or protein from agricultural products, which includes, but is not limited to, bacterial control during the starch and/or protein extraction process steps.

[0003] Starch is extracted from a wide range of agricultural products. These include maize, wheat, potatoes, and cassava and to a lesser extent rice, barley, sorghum, sago, and plants of the legume family. No matter which particular crop the starch is to be extracted from, the production processes involved are essentially the same. They are all based on making the raw material disintegrate (milling), followed by mechanically separating the different component parts. Cereals such as maize and wheat are milled by grinding whereas tubers/roots such as potatoes and cassava/manioc are shredded using raspers. The subsequent separation of the component elements is carried out either on the basis of their different sizes - using screens or filters - or different weights - using gravitational forces in centrifugal separators (decanter centrifuges, nozzle centrifuges or hydrocyclones) in the presence of water.

[0004] One problem facing the industry in general is the efficacy of the separation process, product quality, and the yield, which generally depends on a variety of factors. In wheat, long polymers that include non-starch polysaccharides are responsible for high viscosities due to their high water-binding capacity. Typically, enzymes such as xylanase and beta-glucanase are added in dough preparation to break down these polymers and lower dough viscosity for optimized separation of the starch and gluten (or protein) phases, resulting in high cost with limited performance depending on the conditions in the mixing tank (temperature, pH).

[0005] Another problem in the industry is in the wet processing of starches. Temperatures between 30 - 40°C, and the availability of dextrans and polysaccharides in an aqueous solution during such starch processes, provides an ideal environment for the growth of microorganisms. The microorganisms are equipped with an enzymatic system to break these molecules down into sugars and will ferment the sugars into a variety of organic acids, e.g., lactic acid, causing the pH value of the process water to drop considerably beyond the optimum pH for processing (about pH 4). This lactic acid formation can be associated with premature disintegration of starch due to the formation of microbial amylases, resulting in yield losses and reduced starch quality. The application of strong oxidizing agents to prevent bacterial growth often results in undesirable oxidation of the organic materials. If the dough is over-oxidized, the structure of the starch and the gluten may be modified, and the quality of the end-products can be diminished.

[0006] A further problem facing the industry relates to the agglomeration process that is utilized to obtain both high-quality gluten and high-quality starch in parallel. Intense mixing, high shear, good hydration, and operation at a pH of the isoelectric point can be useful parameters. The pH level of the gluten can be adjusted to the isoelectric point (pH 5.2-6.2) by adding a caustic solution. This increases the dewatering ability and the yield by reducing the water absorption of the gluten. A screw press can be used to remove excess water from wet feed material in preparation for drying. The solubility of cereal proteins is a function of the pH-value. Poor dewatering, high water retention, and/or inhomogeneous moisture distribution due to process acidification can result in reduced dryer evaporation load and high energy demand. Accordingly, large quantities of alkaline are typically used, such as caustic soda or sodium bicarbonate, to stabilize the pH value close to the isoelectric point of gluten for optimized gluten agglomeration, resulting in high chemical costs and a more complicated process.

[0007] An additional problem in the industry relates to the presence of microbial cells on surfaces resulting in the formation of biofilms, which may also give rise to microbiologically influenced corrosion. Biofilms accumulate on all submerged industrial and environmental surfaces. Fouling on the surfaces of pipes and tanks in a wet separation plant calls for frequent cleaning. This presents a significant problem as the cost of water and chemical disposal increases. Fouling is considered the unwanted buildup of material on a surface and includes protein and mineral deposition, product solidification, growth of biofilm, and accumulation of material in stagnant or low-flow areas of equipment. Cleaning operations such as CIP are ubiquitously applied to remove unwanted fouling layers in a processing plant to maintain product safety and process efficiency. The economic penalties of fouling in wet separation can be expressed as maintenance costs and cost due to production loss besides the cost of cleaning agents and water.

[0008] A further problem in the industry relates to vegetable or plant washing, that generates waters with high loads of particulate matter and some dissolved organics. Annually, within the European Union, over 2 million tons of juice from the potato starch production is generated. This stream consists mainly of water with a high concentration of potassium and has a high COD (minimally 20 000 mg O/l) due to the presence of, among others, proteins, amino acids, and sugars. Within the grain and vegetable food-processing industry, wastewater is high, and organic sugars and starches and may contain residual pesticides.

[0009] Water and energy consumption in this industry can also be very high. In wheat starch production, just during deglutination, the water consumption can be 11- 15 m³ G¹ wheat flour and then discharged as a wastewater.

[0010] Thus, the present inventors determined that improved methods are needed for the starch production industry, to address one or more of the problems identified above, but which do not adversely affect the quality of the starch recovered.

SUMMARY OF THE PRESENT INVENTION [0011] It is therefore a feature of the present invention to provide a method for microbiological control in a starch extraction process or protein extraction process.

[0012] An additional feature of the present invention is to provide a method for microbiological control such that the pH of the treated environment is not altered by the treatment (e.g., the pH of the treated area or environment or material can be a pH of 6 or about 6, which provides optimum conditions for extraction or separation processes and can avoid or minimize the reliance on pH control agents or pH control steps, such as the use of caustic). [0013] Another feature of the present invention is to provide a method of using a monochloramine in a starch extraction process or protein extraction process.

[0014] A further feature of the present invention is to provide a method that can increase the amount of starch recovered and/or the amount of protein (or gluten) recovered.

[0015] Additional features and advantages of the present invention will be set forth in part in the description that follows, and in part will be apparent from the description, or may be learned by practice of the present invention. The objectives and other advantages of the present invention will be realized and attained by means of the elements and combinations particularly pointed out in the description and appended claims.

[0016] To achieve these and other advantages, and in accordance with the purposes of the present invention, as embodied and broadly described herein, the present invention relates to a method for extracting starch and/or protein from an agricultural product. The method comprises, consist essentially of, consist of, or includes obtaining a processed product that is a starting agricultural product that is milled, grated, shredded, or any combination thereof. The method further includes conducting one or more separation steps (e.g., solid-liquid separations) to the processed product or a fraction thereof, to obtain at least a first wet solid that comprises, consists essentially of, consists of, or includes starch or protein, or both. The method further includes drying the first wet solid to obtain a dried solid that comprises, consists essentially of, consists of, or includes dry starch, dry protein or both. In the process, at a point prior to conducting and/or during a first of the one or more separation steps, the method further comprises or includes the step(s) of treating the processed product or feed line(s) with monochloramine. The treating comprises or includes a continuous, or nearly continuous, or non-continuous dosage(s) of the monochloramine (MCA) to provide a MCA concentration in an amount of from about 40 ppm to about 800 ppm (this can be achieved for instance by adding 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product). The treating with MCA can also comprise dosing with an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% (such as 0.1 wt% to 1 wt%) monochloramine (based on the total weight of the aqueous monochloramine solution).

[0017] The present invention also relates to a method for extracting starch or protein or both from an agricultural product that includes processing a starting agricultural product to obtain a processed product that is milled, grated, shredded, or any combination thereof. The method then includes wetting the processed product to obtain a wet product, and then conducting one or more solid-liquid separation steps to the wet product or a fraction thereof, to obtain at least a first wet solid that comprises starch or protein or both. The method then includes the step of drying the first wet solid to obtain a dried solid that comprises starch or protein or both. In the method, during and/or after the wetting step, and prior to conducting and/or during the first of the one or more solid-liquid separation steps, the method includes the step of treating the wet product and/or feed line(s) with monochloramine (“MCA”). This treating step includes or is a continuous or nearly continuous, or non-continuous dosage of the monochloramine to provide a MCA concentration. The treating comprises or includes a continuous or nearly continuous, or non-continuous dosage(s) of the monochloramine (MCA) to provide a MCA concentration in an amount of from about 40 ppm to about 800 ppm (this can be achieved for instance by adding 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product). The treating with MCA also comprises dosing with an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% (such as 0.1 wt% to 1 wt%) monochloramine (based on the total weight of the aqueous monochloramine solution).

[0018] The present invention further relates to a method for extracting starch or protein or both from wheat. The method includes the steps of milling wheat to obtain milled wheat, and then wetting the milled wheat to obtain a wet product. The method also includes the steps of conducting at least two wet separation steps to the wet product and/or to a fraction thereof. The wet separation steps are separations based on weight, size, or both of the wet product or fraction thereof. A first wet separation step at least partially separates A-type starches from at least gluten (or a protein) and some non-type A starches in the wet product, and a second wet separation step at least partially separates A-type starches from non-A type starches, such as B-type starches, in at least one fraction from the wet product. The method further includes the step of drying at least the A-type starches to obtain a dried starch. Further, in this method, during and/or after the wetting, and prior to conducting and/or during a first of the two wet separation steps, the method further includes treating the wet product and/or feed line(s) with monochloramine, and includes treating the fraction with monochloramine immediately prior to and/or during the second wet separation step. The treating preferably is or includes a continuous or nearly continuous, or non-continuous dosage of the monochloramine (MCA) to provide a MCA concentration. The treating comprises or includes a continuous or nearly continuous, or non-continuous dosage(s) of the monochloramine (MCA) to provide a MCA concentration in an amount of from about 40 ppm to about 800 ppm (this can be achieved for instance by adding 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product). Preferably, the treating with MCA also comprises dosing with an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% (such as 0.1 wt% to 1 wt%) monochloramine (based on the total weight of the aqueous monochloramine solution).

[0019] The present invention further relates to optionally processing the starch, or refining the starch, so as to obtain glucose, sugar, polyols, and/or other sweeteners. As a further option, the starch or parts of the starch can be fermented to obtain fermentation products such as ethanol and/or organic acids.

[0020] The present invention further relates to products obtained from one or more of the methods of the present invention, including but not limited to, starch and/or gluten (or a protein) and/or byproducts from the one or more the methods.

[0021] It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are intended to provide a further explanation of the present invention, as claimed.

[0022] The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate some of the features of the present invention and together with the description, serve to explain the principles of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] The present invention may be more fully understood with reference to the accompanying figures. The figures are intended to illustrate exemplary features of the present invention without limiting the scope of the invention.

[0024] FIG. 1 is a process flow chart illustrating a method for extracting starch and/or protein according to an example of the present invention.

[0025] FIG. 2 is a process flow chart illustrating a method for extracting starch and/or protein according to an example of the present invention.

[0026] FIG. 3 is a process flow chart illustrating a method according to an example of the present application wherein the agricultural product is maize.

[0027] FIG. 4 is a process flow chart illustrating a method according to an example of the present application wherein the agricultural product is wheat.

[0028] FIG. 5 is a process flow chart illustrating a method according to an example of the present application wherein the agricultural product is tubers.

[0029] FIG. 6 is a process flow chart illustrating a method according to an example of the present application.

[0030] FIG. 7 is a process flow chart illustrating a method according to an example of the present application wherein the agricultural product is wheat.

[0031] FIG. 8 is a process flow chart illustrating a method according to a further example of the present application wherein the agricultural product is wheat.

[0032] FIG. 9 is a process flow chart illustrating options of further steps once the starch is extracted such as, but not limited to, starch conversion and obtaining glucose or fermentation.

[0033] FIG. 10 is a process flow chart illustrating the starch conversion process to one or more types of dextrins. [0034] FIG. 11 is a process flow chart illustrating in more detail, an embodiment of the production of starch slurry.

[0035] FIG. 12 is a process flow chart illustrating the production of starch products.

[0036] FIG. 13 is a process flow chart illustrating the production of sweeteners and ethanol from starch products.

[0037] FIG.14 is a process flow chart illustrating the production of starch from wheat showing one possible embodiment.

[0038] FIG. 15 is a process flow chart illustrating the production of starch from potato showing on possible embodiment.

DETAILED DESCRIPTION OF THE PRESENT INVENTION [0039] In accordance with the present invention, a method is provided to extract starch or protein or both from agricultural products, utilizing chloramine, such as monochloramine. [0040] A key point in achieving effective control of the problems detailed above is using the correct biocidal treatment, and this involves using the correct biocide, the correct dosage, the correct application point(s), pH stabilization, maintaining the correct residual biocidal levels, and to keep doing this over an extended period of time. The biocide can be considered an antimicrobial processing aid.

[0041] Accordingly, methods of extracting starch and/or protein from agricultural sources (e.g., agricultural products) are strategically treated at certain points of the process with one or more chloramines, for example monochloramine (MCA), dichloramine (DCA), or a combination thereof. Preferably, monochloramine is primarily utilized. A majority (by weight) of the chloramine can be MCA (such as at least 50.1%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 99% or 100% by weight of the chloramine present). The treatment can be performed in any suitable manner. The treatment can be continuous, substantially continuous, intermittent, cyclic, batch, or any combination thereof. The treatment is performed at certain locations in a starch extraction process, as further described herein. [0042] The agricultural product can be a starch-containing plant material. The agricultural product can be a starch-containing tree material. The term “plant” is used herein botanically unless indicated otherwise. Examples of the agricultural product include, but are not limited to, is wheat, potatoes, maize, cassava, tapioca, rice, sorghum, barley, sago, manioc, or a plant from the legume family, or any combinations thereof thereof or any portion thereof. The starting agricultural product can be a raw agricultural product, such as, but not limited to, raw wheat, potatoes, maize, cassava, tapioca, rice, sorghum, barley, sago, m manioc or a plant from the legume family, or any combinations thereof. The starting agricultural product can be a fraction or part of wheat, potatoes, maize, cassava, tapioca, rice, sorghum, barley, sago, manioc, or a plant from the legume family, or any combinations thereof. The starting agricultural product can be a washed and/or peeled and/or cut or diced or shredded or pulped raw agricultural product. Generally, the agricultural product prior to being milled and/or grated is not cooked or subject to high temperatures, such as above 100 deg C.

[0043] A key point with the present invention and to obtaining one or more benefits, such as increased starch production, is using the chloramine treatment (hereinafter, referred to at times as a monochloramine treatment (or MCA treatment)) at appropriate dosage points in the starch and/or protein extraction process. Accordingly, not only is the use of monochloramine important, but the location of the monochloramine dosages, the frequency of the monochloramine dosages, and the amount (concentration) of the monochloramine dosages.

[0044] Also, important or helpful is a treatment that provides pH stabilization. Most other biocides or antimicrobial processing aids that are used in extracting starch and/or proteins do not control the pH that well despite controlling the microbiology. For instance, with peracetic acid, the environment is still acidic despite inhibition of lactic acid formation and the addition of caustic and close monitoring of pH becomes a necessity. With the present invention and processes, one real differentiator with monochloramine is the stabilization of the pH around pH 6 (within 15% or within 10% of a pH of 6), which provides optimum conditions for separation processes and without relying on the need for pH control and/or the overdosing/underdosing of caustic or other pH agents.

[0045] In one aspect of the present invention, the present invention relates to a method for extracting starch or protein or both from an agricultural product (as described herein). The method comprises, consist essentially of, consist of, or includes obtaining a processed product that is a starting agricultural product that is milled, diced, grated, shredded, in pulp form, or any combination thereof. This processed product can take the form or include the form that is a flour, mash, pulp, and/or fiber, and the like.

[0046] The method further includes conducting one or more separation steps (e.g., solid-liquid separations) to the processed product or a fraction thereof, to obtain at least a first wet solid that comprises, consists essentially of, consists of, or includes starch or protein or both. The method further includes drying the first wet solid to obtain a dried solid that comprises, consists essentially of, consists of, or includes dry starch or dry protein or both. Prior to the one or more of the separation steps, intermediate processing steps may occur, and after one or more of the separation steps, one or more processing steps may occur prior to drying to obtain the starch and/or protein. This general process is shown in FIG. 1 which sets forth a flow chart of steps. For all figures, “MCA” in the figures are dosing locations of the chloramine (e.g., MCA) with the MCA concentrations and dosing in the manner described herein. The “optional MCA” in the figures are optional dosing locations of the chloramine (e.g., MCA) with the MCA concentrations and dosing in the manner described herein. The “MCA or MCA” in the figures indicate that the dosing location can be in one of two or multiple locations or in both of the two or multiple locations.

[0047] In the processes of the present invention, at least at a point immediately prior to conducting and/or during a first of the one or more separation steps, the method further comprises or includes the step(s) of treating the processed product and/or feed line(s) used for the processed product, with chloramine, such as monochloramine. The treating preferably comprises or includes a non-continuous, or a continuous or nearly continuous dosage(s) of the monochloramine (MCA) to provide a MCA concentration in an amount of from about 40 ppm to about 800 ppm (this can be achieved for instance by adding 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product). The treating with MCA also comprises dosing with an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% (such as 0.1 wt% to 1 wt%) monochloramine (based on the total weight of the aqueous monochloramine solution). The MCA concentration in an amount of about 40 ppm to about 800 ppm is with respect to the concentration in the material being treated (e.g., the processed product or the water being used).

[0048] Also, as an option, in the present invention, the material being treated can have a maximum residual chloramine or MCA amount of 10 ppm, 7 ppm, 5 ppm, 3 ppm, or 2.5 ppm, or 2 ppm, or 1.5 ppm or 1 ppm, or 0.5 ppm. This residual amount can be determined based on the total chlorine detected in the material being tested for residual amount. As an option, this residual amount can be present once the first dosing of MCA occurs in the process, and can either continue to be present throughout the entire process until the starch or fraction thereof (or protein) is dried, or alternatively can continue at a point right after the last separation step occurs to further concentrate a starch or fraction thereof (or protein). When a starch or fraction thereof (or protein) is going to be further processed with some type of enzyme and/or microbial treatment (e.g., starch conversion such as hydrolysis or fermentation), the residual amount can be reduced to an amount below 0.5 ppm or to about 0 ppm or to 0 ppm prior to the further processing with an enzyme and/or microbial treatment. This can be done by stopping the MCA treatment upstream of this further processing.

[0049] As a more specific example, as set forth in FIG. 2, which can be more applicable to certain starting agricultural products, the present invention relates to a method for extracting starch or protein or both from an agricultural product (as described herein). The method comprises, consist essentially of, consist of, or includes processing a starting agricultural product to obtain a processed product that is milled, grated, diced, shredded, in pulp form, or any combination thereof. The method includes the wetting of the processed product to obtain a wet product. The method further includes conducting one or more separation steps (e.g., solid-liquid separations) to the wet product or to a fraction thereof, to obtain at least a first wet solid that comprises, consists essentially of, consists of, or includes starch or protein or both. The method further includes drying the first wet solid to obtain a dried solid that comprises, consists essentially of, consists of, or includes dry starch or dry protein or both. In the process, at a point during and/or after the wetting, and prior to conducting and/or during a first of the one or more separation steps, the method further comprises or includes the step(s) of treating the wet product (and/or feed line(s) of the wet product) with chloramine, such as monochloramine (“MCA”). The treating preferably comprises or includes a non-continuous, or continuous or nearly continuous dosage(s) of the monochloramine (MCA) to provide a MCA concentration in an amount of from about 40 ppm to about 800 ppm (this can be achieved for instance by adding 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product). The treating with MCA also comprises dosing with an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% (such as 0.1 wt% to 1 wt%) monochloramine (based on the total weight of the aqueous monochloramine solution).

[0050] The processing of the starting agricultural product (the ‘processing’ step) can comprise, consist essentially of, consist of, include or is milling, grated, dicing, pulping, shredding, and/or otherwise reducing in size the starting agricultural product. This can be achieved with mills, rotary graters, raspers, and the like. This processing step and how to achieve this processing are known to those skilled in the art. This processing can form a flour, mash, pulp, and/or fiber, and the like. As an option, prior to this processing step, the starting agricultural product can be subjected to a cleaning step, such as with water and/or scrubbers and/or screens. As an option, prior to the processing step, the starting agricultural product can be subjected to a steeping step, to for instance, soften the starting agricultural product (e.g., maize). These options and a more detailed flow chart of the general process is set forth in FIG. 6. The water or liquid used for any option cleaning or washing step can be pre-treated and/or post-treated with the MCA treatment as described herein.

[0051] After the processing step (milling, grating, shredding, and/or otherwise reducing in size the starting agricultural product) and, for instance, prior to a separation step (e.g., a solid-liquid separation step), the processed product, as an option, can be subjected to one or more of the following steps, which can depend on the type of starting agricultural product: juice separation, the use of hydrocyclones and/or screens to remove a component from the processing step (e.g., germ from the kernel), and the like. For any one or more of these optional steps, the material entering the optional step and/or the material exiting the optional step (and/or the feed line(s)) and/or during the optional step, the material can receive or can be subjected to a MCA treatment as described herein. Put another way, upstream (or immediately upstream) and/or downstream (or immediately downstream), and/or during the one or more optional steps, the material or part of the material can receive or can be subjected to a MCA treatment as described herein. This option to have a MCA treatment at one or more optional steps is further reflected in part in FIG. 6.

[0052] For purposes of the present invention, it is to be understood that the ‘processing’ step can include or be the feeding or unloading of an already processed product, such as an already milled, grated, diced, or shredded agricultural product. It is within the scope of the present invention to have the milling, grating, dicing, pulping, and/or shredding occur at another location or processing plant and then transferred to a location that conducts the subsequent steps of the present invention. As a more specific example, wheat flour can be formed at another location and then transferred or transported to the location that conducts the subsequent steps of the present invention, and this previous preparation of the processed product and transferring/transporting can embrace the step of processing, unless stated otherwise.

[0053] Depending on the starting agricultural product, the method can include the step of wetting of the processed product. The wetting step can comprise, consists of, consist essentially of, include combining or adding at least water to the processed product to form a slurry or mixture or wetted product. It is to be understood that prior to the wetting step, the processed product may be either in a dry state (e.g., wheat flour) or wet state (e.g., potato pulp or maize fiber). The wetting step with water can include or be a dilution step. The wetting step can include or be a washing step with water. The water can optionally contain one or more other components or ingredients. The techniques used and devices used and amounts of water used to wet the processed product are conventional in the art and known to those skilled in the art.

[0054] Any water or portions thereof utilized in the methods of the present invention

(e.g., one of the streams and/or more than one stream) can be treated with chloramine, such as monochloramine, prior to, during, and/or after the combining or adding of the water to the processed product. The techniques and dosages can be as described herein. Thus, as an option, the treating can comprise treating water with monochloramine prior to, during, and/or after the adding of water to the milled wheat or other processed product or fraction thereof.

[0055] The one or more separation steps can include or be one or more solid-liquid separation steps.

[0056] The one or more separation steps can be achieved with utilizing at least one centrifuge, at least one decanter (e.g., 2-phase decanter or 3 -phase decanter), at least one sieve (e.g., a curved sieve), at least one separation tank, at least one screen, at least one hydrocyclone, or any combinations thereof. The one or more separation steps can be considered or result in the concentration of one or more particular components or fractions of the processed product. Ultimately, at least one or more of the separation steps result in the isolation or concentration of starch or a species of starch and/or the isolation or concentration of protein or a species of protein.

[0057] More specific examples of the centrifuge include, but are not limited to, a nozzle centrifuge, a decanter centrifuge, and a three-phase decanter centrifuge. Certain centrifuges are considered more desirable depending on the processed product. For instance, a nozzle centrifuge is more common in a maize separation process. Decanter centrifuges are more common in wheat and potato separation processes. The separation step, especially utilizing one or more centrifuges is known to those skilled in the art and the centrifuges are commercially available, for instance from such sources as, but not limited to, Alfa Laval (e.g., Alfa Laval Merco centrifuge and Alfa Laval STNX 944 centrifuge), or a Hiller DecaPress decanter centrifuge, or a Centri-Force decanter centrifuge or Flottweg decanter (2- or 3 -phase decanters, centrifuges and the like).

[0058] The one or more separation steps can comprise or include at least a first separation step and a second separation step, wherein at least a portion of the product separated in the first separation step is processed through the second separation step, and prior (and preferably, immediately prior) to and/or during each of the first separation step and the second separation step, the treating (as described herein) of the processed product or fraction thereof, with monochloramine occurs.

[0059] As a more specific example, the one or more separation steps can be one or more solid-liquid separation steps, which can comprise or include at least a first solid-liquid separation step and a second solid-liquid separation step, wherein at least a portion of the liquid separated in the first solid-liquid separation step is processed through the second solid-liquid separation step, and prior to and/or during each of the first solid-liquid separation step and the second solid-liquid separation step, the treating (as described herein) of the processed product or fraction thereof, with monochloramine occurs.

[0060] With reference to examples of agricultural products and as reflected in FIG. 3, a first separation step can separate, in the case of maize processing, at least a portion of the starch from the gluten (or protein), known as a primary separation, and the second separation step can separate at least a portion of the gluten (or protein) from water. After the primary separation, the recovered starch can optionally be washed with water and subjected to a further separation step to optionally remove at least a portion of proteins that still are present and/or other impurities. This can be done with one or more centrifuges and/or hydrocyclones. The second separation step can further include other processing such as, but not limited to, dewatering steps to remove further water from the gluten (or a protein), for instance, utilizing one or more filters, such as one or more vacuum filters. As indicated, prior to and/or during the first and second separation steps, the processed product or fraction thereof is treated with the MCA treatment as described herein, and preferably immediately before and/or during each of the first and second separation steps. [0061] With further reference to examples of agricultural products and as reflected in FIG. 4, wheat in flour or milled form can be formed into a slurry with water. The slurry can then be subjected to a first separation step that can separate, in the case of wheat processing, at least a portion of the type A-starch (also known as the prime A starch or A starch) from one or more other fractions in the processed product (e.g., at least a portion of the B starch and gluten) and from one or more additional fractions in the processed product (e.g., at least a portion of C starch and optionally pentosanes and/or other solubles). Thus, the first separation in the case of wheat processing can be a separation into at least three fractions (a first fraction that is primarily A starch, a second fraction that is primarily B-starch and gluten, and a third fraction that is primarily C-starch and/or pentosanes). The second separation can be one or more of the following: a) separating the second fraction such that at least a portion of the B-starch is separated from the gluten, b) separating the first fraction further by separating at least a portion of the A-starch from non-A-starch components and/or water, c) separating at least a portion of fibers present in the first fraction from A- starch. The second separation can be one of a) or b) or c), or can be a) and b), or can be a) and c), or can be b) and c). As indicated, prior to and/or during the first and second separation steps, the processed product or fraction thereof is treated with the MCA treatment as described herein, and preferably immediately before and/or during each of the first and second separation steps.

[0062] With further reference to examples of agricultural products and as reflected in FIG. 5, in the case of tuber or potato processing, a first separation step can be one or more of the following: a) separating at least a portion of the starch (first fraction) from soluble proteins and water, and/or b) separating at least a portion of the starch (first fraction) from pulp fibers. The second separation can be one or more of the following: a) separating at least a portion of the starch from the first fraction from water and/or non-starch components, b) separating proteins that have been converted to insoluble proteins (e.g., by heat and/or pH adjustments) from water and/or non-protein components, c) separating at least a portion of the fiber pulp (that was separated away in the first fraction) from water. The second separation can be one of a) or b) or c), or can be a) and b), or can be a) and c), or can be b) and c). As indicated, prior to and/or during the first and second separation steps, the processed product or fraction thereof is treated with the MCA treatment as described herein, and preferably immediately before and/or during each of the first and second separation steps.

[0063] It is to be understood that for any of the figures, the drying step which dries the starch or a component thereof or a by-product thereof is not shown. Other steps, not shown or described can further be included. The figures are meant to show the most relevant steps for purposes of the present invention along with preferred MCA dosing points and optional MCA dosing points.

[0064] As an option, the method of the present invention can include or comprise at least three separate separations of the wet product and/or a fraction thereof utilizing separators (e.g., the same or different types of centrifuges, such as nozzle centrifuges and/or decanter centrifuges and/or decanters and/or 3-phase separators and/or 2-phase separators, and/or screens, and/or sieves, and/or separation tanks, and/or hydrocyclones) located at three different processing points of the method, and the method further comprises dosing with the chloramine (e.g., monochloramine) immediately before and/or during each of said at least three separations.

[0065] In general, with respect to ‘immediately’ treating the processed product or fraction thereof with chloramine (e.g., monochloramine) before a separation step, for instance, this can mean that the MCA treatment occurs after any previous mechanical processing step that occurs prior to a separation step (e.g., after slurry formation but before a separation step) and/or can mean that the MCA treatment occurs anywhere from 1 second to 5 minutes prior to conducting the separation step(s), such as from 5 seconds to 3 minutes, or from 10 seconds to 1 minute prior to the separation step(s).

[0066] In general, with respect to treating the processed product or fraction thereof with chloramine (e.g., monochloramine) ‘during’ a separation step, this can mean that the chloramine is directly added to the separation device or location (e.g., directly dosed into the decanter) and this can be done with chloramine present in water or any other dosing techniques mentioned herein. The ‘during’ can be continuously, non-continuously, intermittently, before the start of separation, during the separation and/or after the separation. Any combination of dosing times is possible.

[0067] If the method includes the step of forming the processed product (e.g., by milling or grating or shredding), which is before the first separation step, any MCA treatment can occur within 20 minutes or within 10 minutes of this forming step, such as within 5 minutes or within 1 minute, or within 30 seconds, or immediately after this forming step.

[0068] When the wetting step is included in the method(s) of the present invention, the MCA treatment can occur during and/or within 20 minutes or within 10 minutes of this wetting step, such as within 5 minutes or within 1 minute of this wetting step, or within 30 seconds of this wetting step, or the water used to wet the processed product can be pre treated with MCA with the dosages/concentrations as described herein.

[0069] As an option, the method(s) of the present invention can include pH control, such that a pH of from about 5 to about 7 is maintained with respect to the wet product or wet fractions thereof.

[0070] In conventional methods for extracting starch (or protein) from agricultural products, it is typical to add alkaline agents to the process (e.g., to the process water and/or agricultural product or fraction thereof) so as to maintain a desirably pH environment, such as from a pH of 5 to about 7. With the present invention, especially in wheat processing but not limited to wheat, the methods of the present invention, due to the strategic use of the MCA treatment as described herein, can reduce the amount (of pH control agents) needed to maintain a pH environment, such as a pH of about 5 to about 7. The reduction in amount of alkaline agents can be at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% by weight (based on the comparison described above).

[0071] Also, with the present invention, the MCA treatment as described herein, can eliminate the need of adding alkaline agent(s) to the starch extraction process or parts of the process, or stages of the process can be conducted in the absence of adding alkaline agents to maintain a pH environment.

[0072] As indicated, the methods of the present invention involve the strategic dosing of MCA at multiples points of a starch and/or protein extraction process. Preferably, the dosage of monochloramine can comprise or include at least 2 dosage points or at least 3 dosage points (that are separate from each other and that are at different processing stages of the starch and/or protein extraction method), or can comprise or include at least 4 dosage points or at least 5 dosage points (that are separate from each other and that are at different processing stages of the starch and/or extraction method), or can comprise or include at least 8 dosage points (that are separate from each other and that are at different processing stages of the starch and/or protein extraction method).

[0073] As an option, the treating with monochloramine can comprise or include multiple dosing points throughout the starch and/or protein extraction method such that the MCA concentration (±20%, or ±10% or ±5%) is maintained with respect to any point from the formation of the wet product to prior to obtaining the dried starch or dried protein or both.

[0074] The starch and/or protein extraction process generally can further include utilizing multiple tanks to hold liquid that comprise primarily water (e.g., the liquid is at least 51% by weight water, such as at least 70% by weight, at least 80% by weight, at least 90% by weight, at least 95% by weight, at least 99% by weight, at least 99.5% by weight or 100% by weight). The liquid can comprise or be process water, pulp press water, wash water, or any combinations thereof. The multiple tanks include feed lines to and/or from each of the multiple tanks. The liquid in the feed lines and in the multiple tanks can have the MCA concentration and/or is a dosage point for the MCA.

[0075] The term “feed line(s)” or “feed lines” is used at times to describe what is treated. For instance, as described herein, “at a point immediately prior to conducting or during a first of the one or more separation steps, the method further comprises treating the processed product or feed line(s) or both.” The “feed line(s)” here is a reference to the piping or conduits or tanks used to transport the processed product or fraction thereof to the separation zone or area or device. In one aspect of the present invention, the hardware used to transport or hold the processed product or fraction thereof is treated with MCA as described herein, and by doing so, the one or more features and/or benefits as described herein can be achieved. In one sense, by treating the processed product or fraction thereof, as described herein, the hardware used to transport or hold the processed product is likewise treated since the MCA is present with the processed product. Similarly, by treating the hardware itself with the MCA as described herein, in one sense, the processed product or fraction thereof passing through the hardware is likewise treated.

[0076] In the present invention, the method can further comprise, consists essentially of, consists of, or includes utilizing multiple tanks to hold liquid that comprises primarily water, wherein the liquid comprises process water, pulp press water, wash water, or any combinations thereof, and the multiple tanks include feed lines to and/or from each of said multiple tanks, and the liquid can have the MCA concentration (as described herein) in the multiple tanks and in the feed lines.

[0077] As indicated, the figures that form a part of the present invention, show examples of flow charts of the starch (and/or protein) extraction process and non-limiting exemplary MCA dosage points. FIG. 7 and FIG. 8 show more specific examples of a starch extraction process for wheat and preferred MCA dosage points. FIG 7 includes “Monochloramine” with arrows to show locations of preferred MCA dosing points in the process. FIG. 7 shows one preferred process scheme where B-starch is being used for ethanol processing/animal feed and as a result, the dosing with MCA for the ‘middle flow’ occurs after a further 3 phase separation step. FIG. 8 shows one preferred process scheme where B-starch is being used for a refinery and as a result, the dosing with MCA for the ‘middle flow’ can occur prior to this particular 3 phase separation step. It is to be understood that when “Monochloramine” is shown with an arrow in FIG. 7 and FIG. 8 adjacent to the “3 -phase Decanter”, the introduction of MCA or dosing of MCA can occur either prior to and/or during this separation step (such as by dosing directly into the separation device or zone) before, during, and/or after conducting the separation but in the separation device or zone.

[0078] It is to be understood the in the methods of the present invention, at least a first and at least a second separation step include a MCA treatment prior to that separation step or during the first and second separation step or both prior and during, but that in the event that there are more than two separation steps, these other separation steps, may or may not include a MCA dosing point or may include a MCA dosing after the separation instead of before (and/or during) the separation step.

[0079] In starch post-processing, once the starch is concentration or divided into fractions, as an option, the starch or fraction thereof can be subjected to a starch conversion step(s), which can convert the starch or a fraction thereof to a glucose or dextrin (which can be used as a sweetener) or the starch converted product can be subjected to a conventional fermentation process to make one or more bioproducts, such as ethanol. FIG. 9 and FIG. 10 show these general process steps in flow charts. The starch conversion can be a hydrolysis process using one or enzymes and/or one or more acids. The enzymes are conventional and can be a glucose isomerase, a glucoamylase, an alpha-amylase, a papain, a trypsin, and/or other food proteases. The post-starch processing can include, but is not limited to, the steps of liquefaction, saccharification, purification (to maltose syrups, to glucose syrups, to mixed syrups), isomerization, and/or conventional refining steps to form/obtain fructose syrups. [0080] Further details of the starch (and/or protein) extraction process are provided here (along with some optional post-starch (or post-protein) processing steps) and the description provided here is one possible embodiment with the understanding that additional steps can be used and other recited here omitted. The process described herein is especially applicable to starch extraction from com. The corn in the form of kernels is subjected to a steeping process. During steeping, the kernels absorb water, increasing their moisture levels, for instance from 15 percent to 45 percent, can more than double in size. Conventional processes have used the addition of 0.1 percent sulfur dioxide to the water so as to prevent excessive bacterial growth in the warm environment. However, instead of this biocide, an MCA treatment, as described herein can be utilized. As the corn swells and softens, the mild acidity of the steepwater begins to loosen the gluten bonds within the corn and release the starch. After steeping, the corn is coarsely ground to break the germ loose from other components. Steepwater is condensed to capture nutrients in the water for use in animal feeds and for a nutrient for later fermentation processes. The ground com, in a water slurry, flows to the germ separators. Then, in one process, cyclone separators spin the low-density com germ out of the slurry. The germs, containing oil, for instance about 85 percent of corn's oil, are pumped onto screens and washed repeatedly to remove any starch left in the mixture. Here, this washing step can optionally have an MCA treatment as described herein. A combination of mechanical and solvent processes can be used to extract the oil from the germ. The oil is then refined and filtered into finished com oil. The germ residue is saved as another useful component of animal feeds. Then, the corn and water slurry leave the germ separator for a second, more thorough, grinding in an impact or attrition-impact mill to release the starch and gluten from the fiber in the kernel. The suspension of starch, gluten, and fiber flows over fixed concave screens, which catch fiber but allow starch and gluten to pass through. The fiber is collected, slurried, and screened again to reclaim any residual starch or protein, then piped to the feed house as a major ingredient of animal feeds. The starch-gluten suspension, called mill starch, is piped to the starch separators. Gluten has a low density compared to starch. By passing mill starch through a centrifuge, the gluten is readily spun out for use in animal feeds. As indicated, prior (or just prior) to this centrifuge stage, an MCA treatment can be utilized. The starch, with just one or two percent protein remaining, is diluted, washed (one or more times such as eight to 14 times), rediluted, and washed again in hydroclones to remove the last trace of protein and produce high quality starch, typically more than 99.5 percent pure. The washing step or right before this washing step, an MCA treatment can be utilized as described herein. Some of the starch can be dried and marketed as unmodified com starch, the starch or a portion thereof can be modified into specialty starches, and/or the starch or a portion thereof can be converted into com syrups and glucose.

[0081] For corn based or any starch recovered, the following processes can be used. Starch, suspended in water, is liquefied in the presence of acid and/or enzymes which convert the starch to a low-glucose solution. Prior to, during, and/or after this liquefication process, an MCA treatment can be utilized. Treatment with another enzyme continues the conversion process. Throughout the process, refiners can halt acid or enzyme actions at key points to produce the right mixture of sugars like glucose and maltose for syrups to meet different needs. In some syrups, the conversion of starch to sugars is halted at an early stage to produce low-to medium sweetness syrups. In others, the conversion is allowed to proceed until the syrup is nearly all glucose. The syrup is refined in filters, centrifuges, and ion- exchange columns, and excess water is evaporated. Syrups are sold directly, crystallized into pure glucose, or processed further to create high fructose corn syrup. And, as an option, a fermentation process can then be utilized.

[0082] Glucose is one of the most fermentable of all of the sugars. Following conversion of starch to glucose, the glucose can be used at glucose to fermentation facilities where the glucose is converted to alcohol by traditional yeast fermentation or to amino acids and other bioproducts through either yeast or bacterial fermentation. After fermentation, the resulting broth is distilled to recover alcohol or concentrated through membrane separation to produce other bioproducts. Carbon dioxide from fermentation is recaptured for sale and nutrients remaining after fermentation are used as components of animal feed ingredients. [0083] Wheat starch granules can be divided in two groups (A-starches and B-starches) or can be divided in to three groups by size, B-starch (e.g., 15 - 20 % by vol) is 1 - 15 micron diameter (or 1 -10 microns), the larger A-starch granules (e.g., 80 - 85 % by vol) are 10-35 microns (or 20 - 35 microns), and C-starch can have sizes that are below B-starch sizes, and/or can be below 5.3 microns in size. B-starch and/or C-starch can be contaminated with pentosans, fibers, lipids and protein to an extent requiring further treatment. Gluten is proteins of the wheat. Gluten forms long molecules insoluble in water. This gives dough its characteristic texture and permits breads and cakes to rise because the carbon dioxide released by the yeast is trapped in the gluten superstructure. Gluten is particular important in the manufacture of starch from wheat because gluten is a most valuable by-product representing half the turnover. If the gluten is extracted and gently dried in hot air at moderate temperatures the gluten maintains the gluten characteristics. If so, it is designated "vital gluten". Vital gluten may be added as a dry powder to flour otherwise low in gluten and thereby improve the baking qualities of the flour. Commercial gluten can be dried to minimum 90% dry matter and a typical composition is (by wt):

• 70 - 80 % crude protein,

• 6 - 8 % crude lipids,

• 10 - 14 % carbohydrates,

• 0.8 - 1.4 % minerals.

[0084] Gluten is used in bread-making as a component to add to the dough so to improve properties of the bread dough such as with respect to elasticity and rise. Also, gluten can be used as a meat extender in both food and feed. Gluten can be used by the fermentation industry using an acid hydrolysis or enzyme hydrolysis. The gluten can be used for production of hydrolyzed vegetable protein and glutamic acid.

[0085] Wheat grain may be taken in as raw material as is the case with corn, but typically the starch manufacturer can use already prepared flour from a flour mill. Composition of the wheat kernel can be (by wt):

Bran 12 %

Germ 2 %

Endosperm 82 %.

[0086] The number of parts by weight of flour that is produced from 100 parts of wheat is termed the extraction rate. Flour extraction ranges from 73 to 77% resulting in an average mill feed production of about 25%. It is apparent that the mill feed contains, in addition to the bran, a significant portion of the starchy endosperm.

[0087] A typical flour composition on dry matter basis can be (by wt):

Moisture content: 13.5 %

Total protein content: 13 %

Fiber content: 1.0 %

Ash content: 0.75 %. [0088] The amounts can vary by 1% to 20% of the value provided. The flour used is generally suitable for human consumption and is milled to a specific particle size distribution. Slurry processes (batter processes) are more industry friendly and make closed continuous handling possible. Several variants have been practiced over time, but the Scandinavian Process is by far the most elegant and efficient.

[0089] The Scandinavian process is based on wheat flour as raw material and it is designed to process even weak (soft) Scandinavian wheat difficult to process otherwise and nevertheless obtain vital gluten of excellent properties. The Scandinavian process also works well with completely fresh and unconditioned flour minimizing storage capacity requirement. Flour is pneumatically conveyed from intermediate silos into a feeding bin equipped with means to separate air and flour. The control system continuously discharges flour into a stream of warm water. Water and flour are mixed in-line and the slurry obtained is homogenized in a high-speed in-line disintegrator. As indicated, a MCA treatment can be uses at this stage, where the water and/or the slurry are treated with MCA as described herein.

[0090] The homogenized slurry can then be right away separated. As indicated, the MCA treatment can occur prior to this separation and/or during this separation. The slurry can be separated into the following fractions by a three-phase decanter (tricanter):

• Starch - Heavy phase

• Gluten (or protein) - Middle phase

• Pentosanes - Light phase.

[0091] Or, the homogenized slurry can then be right away separated into the following fractions by a three-phase decanter (tricanter):

• A type starch - Heavy phase

• B type starch and Gluten (or protein) - Middle phase

• C type starch and Pentosanes - Light phase. [0092] And as stated, prior to this separation and/or during this separation, a MCA treatment can be utilized. The “starch” fraction is the heavy phase containing the major part of A-starch. It is re-slurried and refined - much in the same way as starch of any other origin. The ‘pentosane’ fraction is the light phase from the tricanter - and can contain various gums. It can be mixed with other by-products and used as a wet feed. The wet feed may be dried, mixed with bran or sold as such. The ‘gluten’ fraction is the complex middle phase. It contains the gluten, fibers, solubles, B-starch and some A-starch. After maturing of the gluten, these constituents are split into sub-fractions. With respect to gluten maturing, before separating the gluten fraction, the stream is treated in a maturing reactor. The reactor is specially designed for the maturing of gluten. During maturing the “gluten matrix” of wheat flour is softened and bound starch granules are released. Glutenin and gliadin proteins can now start to form long molecular chains i.e., gluten formation can take place. And with respect to gluten agglomeration and recovery, the gluten maturing step is followed by a treatment in gluten agglomerators. In the agglomerators, the matured gluten is combined into lumps formed of glutenin and gliadin. The gluten lumps are screened off and washed on bend screens. This washing step can optionally receive an MCA treatment as described herein. The wet gluten is dewatered on screw presses and dried. By gentle drying in hot air in a ring dryer the gluten retains its vital properties. After in-line milling and classification the product leaves the dryer ready for packing and sale as vital gluten.

[0093] In B-starch recovery, after gluten recovery, the residual fraction is separated on hydrocyclones. This separation step can optionally receive an MCA treatment as described herein (before and/or during and/or after the separation step). The heavy A-starch goes in the underflow and the lighter B-starch goes with the overflow.

[0094] The A-starch recovered with the underflow can be concentrated and combined with the A-starch main stream. The B-starch can be recovered from the overflow by special recovery cyclones and dewatered on a decanter. The B-starch can be dried in hot air in a ring dryer or drum dried and used as pre-gelatinized starch. With respect to the solubles, a clarifier can remove the last bit of starch from the overflow and essentially solubles and water remains. The clarified overflow leaves the factory as an effluent to be disposed of by landspreading or biogas digestion. The effluent can optionally receive a MCA treatment.

[0095] With regards to A-starch refining, starch is refined by washing with fresh clean water. This washing step can receive a MCA treatment as described herein. With hydrocyclones (a separation step), it is feasible to reduce fiber and solubles including soluble protein to low levels with a minimum of fresh water. To save water, the wash is done counter currently, i.e., the incoming fresh water is used on the very last step and the overflow is reused for dilution on the previous step, and so on. This separation step can receive a MCA treatment and/or the overflow can receive a MCA treatment.

[0096] By using multi stage hydrocyclones, soluble materials and fine cell residues can be removed in a water saving process. The refined starch milk contains an almost 100% pure starch slurried in pure water.

[0097] With respect to A-starch dewatering, the purified A-starch milk is discharged to a peeler centrifuge for dewatering. This separation step can receive a MCA treatment. The peeler filtrate is recycled to the process. The dewatered starch is batch-wise peeled off and discharged by gravity to the moist starch hopper.

[0098] With respect to A-starch drying, from the moist starch hopper, the A-starch is fed by a metering screw conveyor into a flash dryer and dried in hot air. The inlet air temperature can be moderate. The dried starch is pneumatically transported to a starch silo ready for screening and bagging. The moisture of starch after drying can be normally 12-13 wt%. The starch can then be screened on a fine sieve in order to remove any scale formed in screw conveyors, and the like. The starch can optionally be modified, for instance, using a three-step wet modification.

[0099] Starch sweeteners are an important outlet for starch, including wheat starch and in many plants, starch is not dried at all. Instead, the refined A-starch slurry is further processed into starch syrups. For wheat starch, the glucose is particular important. Basic and typical units of operation are: LIQUEFACTION. The refined A-starch slurry is pH-adjusted and enzymes are added. The prepared slurry is heated by direct steam in a steam jet. The liquefaction is typically a two-stage process. The combination of heat and enzymes gelatinizes and thins the starch. The enzyme does the work by cutting the long starch molecules into pieces by hydrolysis. A low DE hydrolysate is formed and at this point the starch has been converted into a maltodextrin. (DE= Dextrose Equivalent). SACCHARIFICATION. The low DE hydrolysate is pH and temperature adjusted once again and new enzymes added to produce glucose with a higher DE. Glucose of different composition can be made depending on the enzymes added and the process applied - even products close to pure dextrose. A cross-flow membrane filtration of the hydrolysate can be done. By dia-filtration, glucose may be recovered from the filter residue leaving a protein rich mud to be discharged as animal feed. The glucose hydrolysate is heated and treated with activated carbon to remove impurities and color bodies and then filtered. The glucose hydrolysate is demineralized with ion exchange resins in a "merry go round" arrangement. Cation resins remove various ions as sodium, calcium, traces of iron and some amino acids. Anion resins remove ions like chloride, sulphate, phosphate and most residual amino acids. The refined glucose syrup is concentrated by evaporation to its final commercial dry matter content. The syrup is now ready for drumming off or for road tanker transport. By varying the procedures, a range of commercial products can be made and the pure dextrose syrups may even form basis for further processing into high fructose Syrups utilizing sophisticated techniques like enzymatically isomerizing and chromatography. [00100] FIG. 11 provides a further example of the process, in the form of a flow chart, showing the production of a starch slurry, wherein an MCA treatment (as described herein) can be utilized in any of these process steps and especially just prior to and/or during the separation step(s).

[00101] FIG. 12 provides a further example of the process, in the form of a flow chart, showing the post-starch processing, wherein an MCA treatment (as described herein) can be utilized in any of these process steps and especially just prior to, during, or after the starch slurry step.

[00102] FIG. 13 provides a further example of a process, in the form of a flow chart, showing the production of sweeteners from starch, wherein an MCA treatment (as described herein) can be utilized in any of these process steps and especially just prior to and/or during the separation step(s).

[00103] FIG. 14 provides a further example of a process, in the form of a flow chart, showing the production of wheat starch, wherein a MCA treatment (as described herein) can be utilized in any of these process steps, and especially just prior to and/or during the dough mixing step, the washing and screening step, the gluten (or protein) washing step, the screen, and/or centrifuging and cyclone separation step(s).

[00104] FIG. 15 provides a further example of a process, in the form of a flow chart, showing the production of potato starch, wherein a MCA treatment (as described herein) can be utilized in any of these process steps, and especially just prior to and/or during the potato washer, the screen, the filtration and Redispersion in Water, and/or the dewatering step(s). [00105] The methods of the present invention can provide one or more beneficial results. These one or more beneficial results can be more apparent in comparing the method of the present invention with a method that is otherwise identical except that the MCA treatment is completely omitted (and no other biocide is utilized) or the MCA treatment (as described herein) is omitted prior to and during any first and second separation steps, as described herein. This comparison as described here is, at times, referred to as ‘in the absence of monochloramine’ or ‘in the absence of MCA’ or ‘due to the MCA treatment.’

[00106] An example of one potential benefit is that method results in a reduced chemical oxygen demand (COD) in an effluent stream not containing starch or a fraction thereof. The effluent stream can be a reference to the by-product after conducting one or more stages of the method of the present invention, and while this effluent stream can be recycled, at least a portion may ultimately be removed or discharged. The effluent stream that is a by product originates from any washing and/or cleaning steps and/or from the formation of the wetting of the processed product and/or from water or juice from the starting agricultural product. The reduction in COD can be at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00107] A further example of a potential benefit of the present invention is that the wet product (e.g., a slurry of milled wheat and water) is a slurry that has a viscosity that is lower due to the MCA treatment. The viscosity can be lowered by at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00108] A further example of a potential benefit of the present invention is that the wet product (e.g., a slurry of milled wheat and water) is a slurry that is oxidized less due to the MCA treatment. The reduction can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above). [00109] A further example of a potential benefit of the present invention is when the gluten (or protein) is recovered as an option, and the method requires less alkaline additions to maintain a pH value within 10% of the isoelectric point of the gluten due to the MCA treatment. The reduction in addition amounts can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00110] A further example of a potential benefit of the present invention is that the starch yields are increased compared to when the MCA treatment is not used. The increase (by weight) can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00111] A further example of a potential benefit of the present invention is that the addition of xylanases and/or cellulases for viscosity reduction is reduced or eliminated. The reduction in addition amounts can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00112] A further example of a potential benefit of the present invention is that the mineral scale up is reduced. This reduction can be especially seen when mineral scale up occurs with the formation of biofilm. The reduction can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00113] A further example of a potential benefit of the present invention is that the MCA treatment removes biofilms or prevents biofilm formation. The improvement in removing biofilms can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00114] A further example of a potential benefit of the present invention is that there is an improvement in the gluten agglomeration and an improved dewatering is achieved compared to when the MCA treatment is not used. Wet vital gluten can enter a drainage hopper of a press. The tumbling allows free moisture to be drained from the screen sides and the base of the hopper. A conical screw can then compress the gluten against a perforated screen, forcing water from the gluten and through the screen before discharge onto an angled drainage screen. This drainage screen removes excess surface water before passing the gluten to the dryer feed system. With faster dewatering, less wash water or even no wash water is required at this stage and the pressure in the nozzles before passing the gluten to the dryer will increase. Ultimately it is a gain in gluten yield. The increase in gluten agglomeration can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above). The increase in dewatering can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00115] A further example of a potential benefit of the present invention is that when the gluten is recovered as an option, the gluten has an increased number of disulfide bonds compared to when the MCA treatment is not used. This increased number can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00116] A further example of a potential benefit of the present invention is that when the gluten is recovered as an option, the gluten has an increased amount of protein compared to when the MCA treatment is not used. This increased amount can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00117] A further example of a potential benefit of the present invention is that any fouling in the method, due to at least biofilm formation, is reduced due to the MCA treatment, as compared to when MCA treatment is not used. This reduction can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00118] A further example of a potential benefit of the present invention is that yields of fermentables (starch, fibers, and preferably non-type A starches) are increased compared to when no MCA treatment is used. This increase can be at least 1%, at least 5%, at least 10%, or at least 20%, such as from 1% to 20% or 5% to 20% (based on the comparison described above).

[00119] As an option, in the methods of the present invention, the microbial activity can be controlled throughout all points in the process such that the CFU/g is maintained (meaning, microbial activity is not increasing) or reduced by at least 1 log or at least 2 log (such as a microbial activity reduction of 1 to 2 log). The reduction can be based on a comparison of using MCA treatments pursuant to the present invention compared to no MCA treatment as described herein.

[00120] With the present invention, the microbial lactic acid formation can be below 1.5 g/1. This amount can be an average (at one wet separation stage or more than one or all combined and averaged) and determined after each wet separation stage, if desired. This amount of microbial lactic acid is based on one or more measurements of the processed agricultural product, for instance, after a separation step. This amount of microbial lactic acid formation can be especially relevant with respect to extracting starch from wheat. [00121] The monochloramine treatments of the present invention can reduce or prevent pH drops, increases in lactic acid concentrations, or both, which can adversely impact wet product separations and/or pressability or cause other problems if not controlled.

[00122] Control of the population of at least one species of bacteria can be provided, which reduces the population to a desired level (even to undetectable limits), and/or at least partially inhibits the growth of the bacteria. [00123] Further, as a potable approved material, the monochloramine can be dosed in non- topical or topical manners, or both, which expands the potential addition points of the treatment agent within the starch extraction system.

[00124] The monochloramine can be used to treat the starting agricultural product, and/or a component derived therefrom, and/or a medium containing the starting agricultural product and/or the component, or any combinations thereof and/or can be used to treat any process water before, during, and/or after contacting the starting agricultural product or a fraction thereof.

[00125] Monochloramine can be added in water dilution form, which can facilitate its introduction into a wide variety of aqueous process streams, masses, and materials at different locations in a starch extraction system.

[00126] Further, chloramine lacks a distinct chlorine odor, and so does not have an adverse effect on taste or other sensory attributes (unlike, e.g., chlorine treatments), and thus is more food-processing compatible.

[00127] The method for extracting starch and/or protein from a starting agricultural product can involve dosing a starch extraction system (or protein extraction process) at a total dosage (combined dosages, all addition points) of from about 1 g to about 1000 g monochloramine, or from about 3 g to about 1000 g monochloramine, or from about 10 g to about 1000 g monochloramine, or from about 50 g to about 1000 g monochloramine, or from about 100 g to about 1000 g monochloramine, or from about 1 g to about 500 g monochloramine, or from about 3 g to about 500 g monochloramine, or from about 10 g to about 500 g monochloramine, or from about 50 g to about 500 g monochloramine, or from about 1 g to about 300 g monochloramine, or from about 3 g to about 300 g monochloramine, or from about 10 g to about 300 g monochloramine, or from about 20 g to about 300 g monochloramine, or from about 30 g to about 300 g monochloramine, or from about 40 g to about 300 g monochloramine, or from about 50 g to about 300 g monochloramine, or other amounts, per ton (2000 lb.) of the starting agricultural product processed in the starch extraction and/or protein extraction methods. The dosage can be constant or can vary in these ranges during production. The monochloramine amount (and/or the desired MCA concentration) can be an average monochloramine amount based on a 24-hour period, or other time period. The indicated treatment ranges are on a monochloramine basis. Other chloramines may be used in addition to monochloramine.

[00128] The monochloramine can be added in an aqueous diluted form at a concentration of from about 100 ppm to about 15,000 ppm, or from about 200 ppm to about 15,000 ppm, or from about 300 ppm to about 15,000 ppm, or from about 500 ppm to about 15,000 ppm, or from about 500 ppm to about 5000 ppm, or from about 1000 ppm to about 4500 ppm, or from about 1500 ppm to about 4000 ppm, or from about 2000 ppm to about 3500 ppm, or from about 2250 ppm to about 3250 ppm, or from about 2500 ppm to about 3000 ppm, or from about 500 ppm to about 13,000 ppm, or from about 600 to about 12,000 ppm, or from about 700 ppm to about 10,000 ppm, or from about 800 ppm to about 9,000 ppm, or from about 900 ppm to about 8000 ppm, or other ranges.

[00129] For purposes of the present invention, the MCA treatment can optionally be a chloramine treatment agent that can be used, which comprises, consists essentially of, or consists of at least one chloramine. The chloramine(s) can be, for example monochloramine (MCA)(NH₂C1), di chloramine (DC A), or a combination thereof. A majority (by weight) of the chloramine can be MCA (such as at least 50.1%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 99%, 90% to 100%, 95% to 100%, 99% to 100%, or 100% by weight of the chloramine present). For purposes of the present invention, “MCA” treatment, unless stated otherwise, encompasses chloramine(s) as stated herein. [00130] The monochloramine treatment can be performed in any suitable manner at each addition point in the starch extraction process that is used. The treatment can be continuous, substantially continuous, intermittent, cyclic, batch, or any combination thereof. For purposes of the present invention, ‘nearly continuous’ means that the dosing with MCA to the agricultural product or a portion or fraction thereof occurs at least 75% of the time that material is being processed through the treatment dosing point. For instance, if the process is being operated for one hour, dosing with MCA occurs for at least 45 minutes during that one-hour period. For purposes of the present invention, ‘non-continuous’ means that the dosing with MCA to the agricultural product or a portion or fraction thereof occurs on non-continuously on a time basis. For instance, if the process is being operated for one hour, dosing with MCA does not occur for 60 minutes, but less than 60 minutes of that operation. The non-continuous dosing may comprise one or more dosings of the material at intermittent times. Thus, the doing with the MCA treatment may be interrupted at one or more times during the running of the method to extract starch or a fraction thereof.

[00131] The MCA treatment and dosing can be the same concentration and/or dosing amount or can be different when more than one dosing point exists in the process.

[00132] The treatment can be performed at one or more stages or locations in a starch and/or protein extraction process. In a processing plant, the treatment can be performed in a vessel through which processed material passes. The monochloramine can be added directly into the vessel, or can be introduced indirectly via a process stream that then is fed into the vessel, or combinations thereof. The treatment may be applied in-line to a flowing process stream or mass without any accompanying dwell or residence period in a process vessel. A process vessel in a starch and/or protein extraction process wherein the treatment can be applied is a holding tank, washer, grater, sheer, feed line, mixer, storage vessel, and/or other process vessel, or any combinations thereof. [00133] The monochloramine treatment(s) can occur directly on external surfaces of the raw agricultural product, such as by topical application of a treatment solution containing monochloramine. The treatment(s) can occur where process water or other process fluid can be pre-treated with the monochloramine prior to being combined with at least one of a raw agricultural product, a component thereof, a fraction thereof, or another medium in which the raw agricultural product and/or component thereof is contained, dispersed, or massed.

[00134] The microorganisms that are controlled can be bacteria, fungi, yeasts, and/or archaebacteria, and/or other microorganisms that can consume starch or affect the quality of the starch. The microorganisms that can be controlled with the monochloramine treatment can be predominantly bacteria, essentially entirely, or entirely bacteria. The bacteria that can be controlled can be classical aerobic bacteria, such as Leuconostoc mesenteroides , lactobalillus , coccus , or other bacterial species, or any combination thereof. Thermophilic microorganisms may be controlled with the monochloramine treatment. The thermophilic microorganisms that may be controlled are bacillus , thermos , and chlostridia species, or other species, or any combination thereof.

[00135] With the present invention, the starch, gluten, treated process water, fluid, juice, syrup, fibers, pulp, feed lines, and/or other material has very low bacteria count. The bacteria can be controlled, such that the bacteria count does not increase or the bacterial count. Compared to a process where no MCA treatment is utilized in the manner described herein or not utilized at all, or no biocide is utilized, the bacterial count can actually decrease, such as by at least one log or at least two log (such as a decrease of from 1 log to 2 log).

[00136] The monochloramine or other chloramine can be obtained from any suitable source. The monochloramine can be formed as a stock solution, such as an aqueous dilute form thereof, which can be introduced to process water and/or an aqueous medium containing sugar-containing plant material or sugar-containing components thereof. The monochloramine can be formed in-situ in stock solution or process water. The monochloramine can be formed on-site or off-site. For example, OCAMGNE 6150, BUSPERSE 2454 product, BUSAN 1215 product, and BUCKMAN 1250 product, available from Buckman Laboratories International, Inc., Memphis, Tennessee, can be used as precursors to form monochloramine. The monochloramine can be prepared accordingly to any suitable method. For example, monochloramine can be produced by one of the techniques described in U.S. Patent Nos. 4,038,372, 4,789,539, 6,222,071, 7,045,659, and 7,070,751, which are incorporated herein in their entireties. The monochloramine can be formed by reacting dilute ammonia solution or at least one ammonium salt or other nitrogen source with at least one chlorine-containing oxidant. The monochloramine can be formed by reacting a dilute ammonia solution with sodium hypochlorite, calcium hypochlorite, or other hypochlorite source, or any combination thereof. Monochloramine can be prepared by adding an ammonia solution and sodium hypochlorite to dilution water to achieve a 1 to 1 molar ratio of ammonia and sodium hypochlorite. Monochloramine can be prepared, for example, by combining about 1 fluid volume part OXAMINE 6150 to about 2.3-3 fluid volume parts of bleach. Commercial bleaches can contain concentrations of sodium hypochlorite which can be up to 18.0% wt/wt sodium hypochlorite, e.g., about 14%-18% wt/wt NaOCl, or other concentrations thereof. The monochloramine can be formed by reacting at least one ammonium salt with sodium hypochlorite or other hypochlorite source. For example, the ammonium salt can be ammonium bromide, ammonium sulfate, ammonium hydroxide, ammonium chloride, or a combination thereof. Monochloramine can be produced by reacting 1 to 1 molar ratio of the ammonium salt and chlorine. Monochloramine can be produced on-site at a sugar mill using such reactions, and used immediately or stored before use. Monochloramine can be produced off site, and transported on-site for use. [00137] For on-site production of monochloramine, a method and apparatus can be used for mixing at least two reactants or components, such as dilute ammonia solution and sodium hypochlorite, to form the desired reaction product. The apparatus can comprise preparatory makedown unit equipment. The apparatus can include a reactor, a reactor system, a generator, a small-volume generator, a vessel, an in-line mixer, or the like. The method and apparatus can be useful in controlling reactions that may be inherently dangerous, for example, wherein the mixing of the components has the potential to produce hazardous compounds or components. Precautions can be taken to ensure that the molar ratio of each reactant is precisely metered, as well as incoming makeup water if used in the reaction. As an example, the method and apparatus can be used for mixing an ammonia- containing chemical (e.g., ammonia) and a hypochlorite-containing chemical (e.g., hypochlorite), the nature of which is inherently dangerous. The mixing of an ammonia- containing chemical and a hypochlorite-containing chemical can be controlled carefully to avoid the production of hazardous compounds such as dichloramine, trichloramine, and chlorine gas.

[00138] The equipment used for mixing the at least two reactants or components, such as dilute ammonia solution and sodium hypochlorite, to form monochloramine, optionally can include an automated control mechanism. The control mechanism can relate one or more process control parameters to a monitored reaction condition, such as temperature. A differential temperature method of controlling an exothermic or endothermic chemical reaction optionally can be used. The chemical reaction can be an exothermic reaction, and the temperature difference can be a temperature increase. The chemical reaction can be an endothermic reaction, and the temperature difference is a temperature decrease. The method can include measuring a temperature of a first reactant flowing at a first flow rate, contacting the first reactant with a second reactant, and then measuring the temperature of a reaction product formed by a reaction between the first and second reactants. The temperature difference between the measured temperature of the first reactant and the measured temperature of the reaction product can be used to monitor the reaction, and adjustments can be made based on the temperature difference. The flow rate of the first reactant can be adjusted based on the temperature difference. The second reactant can be made to flow at a second flow rate, and the flow rate of the first reactant and/or the second reactant can be adjusted based on the temperature difference. The first temperature reading can optionally be right at the initial time that the reactants are brought together or some other time if desired. The second reading, used to obtain the temperature differential, can be a time where maximum temperature increase or decrease occurs from the reaction (e.g., the maximum increase from the exothermic reaction or maximum decrease from the endothermic reaction, whichever the case may be). This temperature difference from the reaction can be used to determine and/control the reaction to ensure that the reaction and the product from the reaction is the desired reaction product (e.g., monochloramine) and/or to ensure that reaction is proceeding in an efficient or correct manner. The apparatus can be configured to produce any amount of monochloramine including, but not limited to, 20 pounds or more of monochloramine per day, or less than this amount.

[00139] As indicated, the treating with monochloramine in the indicated process flow, such as illustrated in FIG. 1, but not limited thereto, can occur at one or more addition points within the system, such those locations or stages indicated by “MCA” in the figures, and/or right before these locations and/or right after these locations. Preferred addition points are those which can allow monochloramine to be added in a fluid medium, such as an aqueous form, e.g., a water dilution form, to contact the agricultural product or fraction thereof, a medium which contains agricultural product or an extract and/or other part(s) thereof, or other process materials or equipment, or any combination of these and/or other addition locations. [00140] The treatment of the agricultural product or related process waters with monochloramine can be continuous, substantially continuous, intermittent, cyclic, batch, or any combination thereof. Treatment can be repeated any desired number of times and treatments can be separated by constant or variable time periods. The rate of addition of monochloramine and/or precursors can be constant or variable. Monochloramine can be topically applied, non-topically applied, or both, to provide microbiological control. Monochloramine can be added in any manner to the starch-containing materials (or protein containing materials) or process water, for example, by pouring, by nozzle, by spraying, by misting, by curtain, by weir, by fountain, by percolation, by mixing, by injection, or by any combination thereof. For topical treatment, monochloramine can be sprayed in an aqueous form on the agricultural product raw material. The monochloramine can be added in an aqueous dilute form to process water used in the production process that contacts or is brought into contact with at least one of the agricultural product or the component derived therefrom.

[00141] The agricultural product or process water can be treated for any period of time. For instance, on a substantially continuous or continuous basis or on a non-continuous basis, such as at least about 6.0 hours, at least about 12 hours, at least about 24 hours, at least about 36 hours, or at least about at least 7 days, at least 2 weeks, at least 1 month, at least 2 months, at least 3 months, from 1 day to 6 months, from 1 day to 12 months or more. The amount of monochloramine added may be varied based on any one or combination of different process factors.

[00142] As an option, one or more other non-MCA or non-chloramine biocides can be used in addition to the MCA treatment as described herein.

[00143] As an option, in any of the methods of the present invention, no other biocide is used except for the chloramine (e.g., monochloramine) at any stage. [00144] As an option, in any of the methods of the present invention, if another biocide is used, in addition to a chloramine, the chloramine (e.g., monochloramine) is the predominate biocide by dosage amount (e.g., at least 60 wt%, at least 70 wt%, at least 80 wt%, at least 90 wt%, at least 95 wt%, at least 99 wt% of the total weight of all biocides used are chloramine or MCA at any stage).

[00145] As an option, in any of the methods of the present invention, no agent (e.g., chemical compound or agent) is added to potentiate the chloramine or monochloramine. [00146] The present invention includes the following aspects/embodiments/features in any order and/or in any combination:

1. The present invention relating to a method for extracting starch or protein or both from an agricultural product, said method comprising obtaining a processed product that is a starting agricultural product that is milled, grated, pulped, diced, shredded, or any combination thereof, conducting one or more separation steps to the processed product or to a fraction thereof to obtain at least a first wet solid that comprises starch or protein or both, and drying the first wet solid to obtain a dried solid that comprises dry starch or dry protein or both, wherein at a point immediately prior to conducting and/or during a first of the one or more separation steps, the method further comprises treating the processed product or feed line(s) or both with monochloramine.

2. The method of any preceding or following embodiment/feature/aspect, wherein the method further comprises at a point immediately prior to conducting and/or during a second of the one or more separation steps, the method further comprises treating the processed product or feed line(s) or both with monochloramine.

3. The present invention additionally or alternatively relates to a method for extracting starch or protein or both from an agricultural product, said method comprising processing a starting agricultural product to obtain a processed product that is milled, grated, shredded, or any combination thereof, wetting the processed product to obtain a wet product, conducting one or more separation steps to the wet product or a fraction thereof, to obtain at least a first wet solid that comprises starch or protein or both; and drying said first wet solid to obtain a dried solid that comprises starch or protein or both, and wherein after said wetting, and prior to conducting and/or during a first of said one or more separation steps, said method further comprises treating said wet product (and/or the feed line(s)) with monochloramine, wherein said treating comprises a non-continuous, continuous or nearly continuous dosage of said monochloramine (MCA) to provide a MCA concentration in an amount of from about 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product; and wherein said treating comprises an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% monochloramine.

4. The method of any preceding or following embodiment/feature/aspect, wherein said agricultural product is wheat, potatoes, maize, cassava, tapioca, rice, sorghum, barley, sago, or manioc or a plant from the legume family, or any combinations thereof.

5. The method of any preceding or following embodiment/feature/aspect, wherein said wetting comprising adding at least water to the processed product to form a slurry.

6. The method of any preceding or following embodiment/feature/aspect, wherein said wetting comprises treating said water with monochloramine prior to, during, and/or after said adding of water to the processed product.

7. The method of any preceding or following embodiment/feature/aspect, wherein said one or more separation steps comprises utilizing at least one centrifuge, at least one decanter (e.g., 2-phase decanter or 3-phase decanter), at least one separation tank, at least one sieve (e.g., a curved sieve), at least one screen, or at least one hydrocyclone, or any combinations thereof.

8. The method of any preceding or following embodiment/feature/aspect, wherein said one or more separation steps comprises at least a first solid-liquid separation step and a second solid-liquid separation step, wherein at least a portion of the liquid separated in said first solid-liquid separation step is processed through said second solid-liquid separation step, and prior to and/or during each of said first solid-liquid separation step and said second solid-liquid separation step, said treating with monochloramine occurs.

9. The method of any preceding or following embodiment/feature/aspect, wherein said method results in a reduced chemical oxygen demand in process water resulting from said method (e.g., one or more effluent streams not containing fractions of products, such as starch, protein and/or fibers).

10. The method of any preceding or following embodiment/feature/aspect, wherein starch yields or protein yields or both are increased compared to the same method except in the absence of monochloramine.

11. The method of any preceding or following embodiment/feature/aspect, wherein said treating with monochloramine comprises multiple dosing points throughout said method such that said MCA concentration is maintained with respect to any point from said wet product to prior to obtaining said dried solid.

12. The method of any preceding or following embodiment/feature/aspect, wherein said method further comprises utilizing multiple tanks to hold liquid that comprises primarily water, wherein said liquid comprises process water, pulp press water, wash water, or any combinations thereof, and said multiple tanks include feed lines to and/or from each of said multiple tanks, and said liquid has said MCA concentration in said multiple tanks and in said feed lines.

13. The method of any preceding or following embodiment/feature/aspect, wherein said treating with said monochloramine occurs within 20 minutes after forming said processed product.

14. The method of any preceding or following embodiment/feature/aspect, wherein said treating with said monochloramine occurs within 1 minute after forming said processed product.

15. The present invention in additional or alternatively relates to a method for extracting starch from wheat, said method comprising milling said wheat to obtain milled wheat, wetting the milled wheat to obtain a wet product, conducting at least two wet separation steps to the wet product or to a fraction thereof, based on weight, size, or both, wherein a first wet separation step at least partially separates A-type starches from at least gluten (or a protein) and some non-type A starches in said wet product, and a second wet separation step at least partially separates said A-type starches from non- A-type starch components in at least one fraction from said wet product, drying at least said A-type starches to obtain a dried starch, wherein after said wetting, and prior to conducting and/or during a first of said two wet separation steps, said method further comprises treating said wet product with monochloramine, and immediately prior to and/or during said second wet separation step, treating said fraction with monochloramine, wherein said treating comprises a non-continuous, continuous or nearly continuous dosage of said monochloramine (MCA) to provide a MCA concentration in an amount of from about 50 g to about 800 g MCA per 1 ton (2,000 lb) of wheat; and wherein said treating comprises an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% monochloramine.

16. The method of any preceding or following embodiment/feature/aspect, wherein said first wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter (e.g., 2-phase decanter or 3-phase decanter), at least one sieve (e.g., a curved sieve), at least one screen, or at least one hydrocyclone, or any combinations thereof.

17. The method of any preceding or following embodiment/feature/aspect, wherein said second wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter (e.g., 2-phase decanter or 3-phase decanter), at least one sieve (e.g., a curved sieve), at least one screen, or at least one hydrocyclone, or any combinations thereof.

18. The method of any preceding or following embodiment/feature/aspect, wherein said wetting comprising forming a slurry of milled wheat and water.

19. The method of any preceding or following embodiment/feature/aspect, said method further comprising a fiber screening prior to said second wet separation step, and said treating occurs after said fiber screening and prior to and/or during said second wet separation step.

20. The method of any preceding or following embodiment/feature/aspect, wherein no biocide except for the monochloramine is added at any stage.

21. The method of any preceding or following embodiment/feature/aspect, wherein no agent is added to potentiate the monochloramine.

22. The method of any preceding or following embodiment/feature/aspect, wherein said wet product is a slurry that has a viscosity that is lower due to the MCA treatment.

23. The method of any preceding or following embodiment/feature/aspect, wherein said wet product is a slurry that is oxidized less due to the MCA treatment. 24. The method of any preceding or following embodiment/feature/aspect, wherein said gluten (or a protein) is recovered, and said method requires less alkaline additions to maintain a pH value within 10% of the isoelectric point of the gluten (or protein) due to the MCA treatment (compared to when said MCA treatment is not used).

25. The method of any preceding or following embodiment/feature/aspect, wherein microbial activity is controlled throughout all points in the process such that the CFU/g is maintained or reduced by at least 1 log.

26. The method of any preceding or following embodiment/feature/aspect, wherein said method results in a reduced chemical oxygen demand in an effluent stream not containing starch, protein or fiber, or a fraction thereof

27. The method of any preceding or following embodiment/feature/aspect, wherein in said method, microbial lactic acid formation is below 1.5 g/1.

28. The method of any preceding or following embodiment/feature/aspect, wherein in said method, a pH of from about 5 to about 7 is maintained with respect to the wet product or wet fractions thereof.

29. The method of any preceding or following embodiment/feature/aspect, wherein starch yields (and/or protein yields) are increased compared to when said MCA treatment is not used.

30. The method of any preceding or following embodiment/feature/aspect, wherein the addition of xylanases and/or cellulases for viscosity reduction is reduced or eliminated.

31. The method of any preceding or following embodiment/feature/aspect, wherein mineral scale up is reduced.

32. The method of any preceding or following embodiment/feature/aspect, wherein said MCA treatment removes biofilms or prevents biofilm formation.

33. The method of any preceding or following embodiment/feature/aspect, wherein improved gluten agglomeration and dewatering is achieved compared to when said MCA treatment is not used.

34. The method of any preceding or following embodiment/feature/aspect, wherein said gluten is recovered and wherein the gluten has an increased number of disulfide bonds compared to when said MCA treatment is not used.

35. The method of any preceding or following embodiment/feature/aspect, wherein said gluten is recovered and wherein said gluten has an increased amount of protein compared to when MCA treatment is not used.

36. The method of any preceding or following embodiment/feature/aspect, wherein fouling in said method due to at least biofilm formation is reduced due to the MCA treatment, as compared to when MCA treatment is not used.

37. The method of any preceding or following embodiment/feature/aspect, wherein said method reduces the amount or eliminates the need of adding alkaline agents to maintain a pH environment.

38. The method of any preceding or following embodiment/feature/aspect, wherein said dosage of monochloramine comprises at least 3 dosage points in said method.

39. The method of any preceding or following embodiment/feature/aspect, wherein said dosage of monochloramine comprises at least 5 dosage points in said method.

40. The method of any preceding or following embodiment/feature/aspect, wherein said dosage of monochloramine comprises at least 8 dosage points in said method.

41. The method of any preceding or following embodiment/feature/aspect, wherein said treating comprises treating said water with monochloramine prior to, during, and/or after said adding of water to the milled wheat.

42. The method of any preceding or following embodiment/feature/aspect, wherein said first wet separation step comprises at least one 3-phase decanter centrifuge and/or separation tank.

43. The method of any preceding or following embodiment/feature/aspect, wherein said method comprises at least three separate wet separations of said wet product or a fraction thereof utilizing separators (e.g., 3 -phase separators) located at three different points of the method, and said method further comprises dosing with said monochloramine immediately before and/or during each of said at least three separations.

44. The method of any preceding or following embodiment/feature/aspect, wherein said treating with monochloramine comprises multiple dosing points throughout said method such that said MCA concentration is maintained with respect to any point from said wet product to prior to obtaining said dried starch.

45. The method of any preceding or following embodiment/feature/aspect, wherein said treating with said monochloramine occurs within 20 minutes after forming said milled wheat.

46. The method of any preceding or following embodiment/feature/aspect, wherein said treating with said monochloramine occurs within 20 minutes after forming said wet product.

47. The method of any preceding or following embodiment/feature/aspect, wherein said method further comprises utilizing multiple tanks to hold liquid that comprises primarily water, wherein said liquid comprises process water, pulp press water, wash water, or any combinations thereof, and said multiple tanks include feed lines to and/or from each of said multiple tanks, and said liquid has said MCA concentration in said multiple tanks and in said feed lines.

48. The method of any preceding or following embodiment/feature/aspect, said method further comprising converting at least a portion of said starch to glucose or dextrin.

49. The method of any preceding or following embodiment/feature/aspect, said method further comprising converting at least a portion of said starch to glucose or dextrin and then conducting a fermentation of said glucose or dextrin to form one or more bioproducts.

50. The present invention, in addition or alternatively, relates to a method for extracting starch from an agricultural product, said method comprising obtaining a processed product that is a starting agricultural product that is milled, grated, pulped, diced, shredded, or any combination thereof, conducting one or more separation steps to the processed product or to a fraction thereof to obtain at least a first wet solid that comprises starch, and drying the first wet solid to obtain a dried solid that comprises dry starch, wherein at a point immediately prior to conducting and/or during a first of the one or more separation steps, the method further comprises treating the processed product with monochloramine, and wherein said method reduces the amount or eliminates the need of adding alkaline agents to maintain a pH environment.

51. The method of any preceding or following embodiment/feature/aspect, wherein the processed product or a fraction thereof has a maximum chloramine or MCA residual amount of 10 ppm until the processed product or fraction thereof is dried or subject to enzymatic or microbial treatments in one or more starch conversion processes.

[00147] The present invention can include any combination of these various features or embodiments above and/or below as set forth in sentences and/or paragraphs. Any combination of disclosed features herein is considered part of the present invention and no limitation is intended with respect to combinable features.

[00148] Applicants specifically incorporate the entire contents of all cited references in this disclosure. Further, when an amount, concentration, or other value or parameter is given as either a range, preferred range, or a list of upper preferable values and lower preferable values, this is to be understood as specifically disclosing all ranges formed from any pair of any upper range limit or preferred value and any lower range limit or preferred value, regardless of whether ranges are separately disclosed. Where a range of numerical values is recited herein, unless otherwise stated, the range is intended to include the endpoints thereof, and all integers and fractions within the range. It is not intended that the scope of the invention be limited to the specific values recited when defining a range.

[00149] Other embodiments of the present invention will be apparent to those skilled in the art from consideration of the present specification and practice of the present invention disclosed herein. It is intended that the present specification and examples be considered as exemplary only with a true scope and spirit of the invention being indicated by the following claims and equivalents thereof.

Claims

WHAT IS CLAIMED IS:

1. A method for extracting starch or protein or both from an agricultural product, said method comprising obtaining a processed product that is a starting agricultural product that is milled, grated, pulped, diced, shredded, or any combination thereof, conducting one or more separation steps to the processed product or to a fraction thereof to obtain at least a first wet solid that comprises starch or protein or both, and drying the first wet solid to obtain a dried solid that comprises dry starch or dry protein or both, wherein at a point immediately prior to conducting and/or during a first of the one or more separation steps, the method further comprises treating the processed product or a feed line or both with monochloramine.

2. The method of claim 1, wherein the method further comprises at a point immediately prior to conducting and/or during a second of the one or more separation steps, the method further comprises treating the processed product or a feed line with monochloramine.

3. A method for extracting starch or protein or both from an agricultural product, said method comprising processing a starting agricultural product to obtain a processed product that is milled, grated, shredded, or any combination thereof, wetting the processed product to obtain a wet product, conducting one or more separation steps to the wet product or a fraction thereof, to obtain at least a first wet solid that comprises starch or protein or both; and drying said first wet solid to obtain a dried solid that comprises starch or protein or both, and wherein after said wetting, and prior to conducting and/or during a first of said one or more separation steps, said method further comprises treating said wet product with monochloramine, wherein said treating comprises a non-continuous, continuous or nearly continuous dosage of said monochloramine (MCA) to provide a MCA concentration in an amount of from about 50 g to about 800 g MCA per 1 ton (2,000 lb) of starting agricultural product; and wherein said treating comprises an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% monochloramine.

4. The method of any preceding claim, wherein said agricultural product is wheat, potatoes, maize, cassava, tapioca, rice, sorghum, barley, sago, manioc or a plant from the legume family, or any combinations thereof.

5. The method of any preceding claim, wherein said wetting comprising adding at least water to the processed product to form a slurry.

6. The method of claim 5, wherein said wetting comprises treating said water with monochloramine prior to, during, or after said adding of water to the processed product.

7. The method of any preceding claim, wherein said one or more separation steps comprises utilizing at least one centrifuge, at least one decanter, at least one separation tank, at least one sieve, at least one screen, or at least one hydrocyclone, or any combinations thereof.

8. The method of any preceding claim, wherein said one or more separation steps comprises at least a first solid-liquid separation step and a second solid-liquid separation step, wherein at least a portion of the liquid separated in said first solid-liquid separation step is processed through said second solid-liquid separation step, and prior to and/or during each of said first solid-liquid separation step and said second solid-liquid separation step, said treating with monochloramine occurs.

9. The method of any preceding claim, wherein said method results in a reduced chemical oxygen demand in an effluent stream not containing starch or a fraction thereof.

10. The method of any preceding claim, wherein starch yields or protein yields or both are increased compared to the same method except in the absence of monochloramine.

11. The method of any preceding claim, wherein said treating with monochloramine comprises multiple dosing points throughout said method such that said MCA concentration is maintained with respect to any point from said wet product to prior to obtaining said dried solid.

12. The method of any preceding claim, wherein said method further comprises utilizing multiple tanks to hold liquid that comprises primarily water, wherein said liquid comprises process water, pulp press water, wash water, or any combinations thereof, and said multiple tanks include feed lines to and/or from each of said multiple tanks, and said liquid has said MCA concentration in said multiple tanks and in said feed lines.

13. The method of any preceding claim, wherein said treating with said monochloramine occurs within 20 minutes after forming said processed product.

14. The method of any preceding claim, wherein said treating with said monochloramine occurs within 1 minute after forming said processed product.

15. A method for extracting starch from wheat, said method comprising milling said wheat to obtain milled wheat, wetting the milled wheat to obtain a wet product, conducting at least two wet separation steps to the wet product or to a fraction thereof, based on weight, size, or both, wherein a first wet separation step at least partially separates A-type starches from at least gluten or protein and some non-type A starches in said wet product, and a second wet separation step at least partially separates said A-type starches from non- A-type starch components in at least one fraction from said wet product, drying at least said A-type starches to obtain a dried starch, wherein after said wetting, and prior to conducting and/or during a first of said two wet separation steps, said method further comprises treating said wet product with monochloramine, and immediately prior to and/or during said second wet separation step, treating said fraction with monochloramine, wherein said treating comprises a non-continuous, continuous or nearly continuous dosage of said monochloramine (MCA) to provide a MCA concentration in an amount of from about 50 g to about 800 g MCA per 1 ton (2,000 lb) of wheat; and wherein said treating comprises an aqueous monochloramine solution containing from about 0.1 wt% to about 2 wt% monochloramine.

16. The method of claim 15, wherein said first wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter, at least one sieve, at least one screen, or at least one hydrocyclone, or any combinations thereof.

17. The method of claim 15, wherein said second wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter, at least one sieve, at least one screen, or at least one hydrocyclone, or any combinations thereof.

18. The method of claim 15, wherein said wetting comprising forming a slurry of milled wheat and water.

19. The method of claim 1, said method further comprising a fiber screening prior to said second wet separation step, and said treating occurs after said fiber screening and prior to and/or during said second wet separation step.

20. The method of any preceding claim, wherein no biocide except for the monochloramine is added at any stage.

21. The method of any preceding claim, wherein no agent is added to potentiate the monochloramine.

22. The method of any preceding claim, wherein said wet product is a slurry that has a viscosity that is lower due to the MCA treatment.

23. The method of any preceding claim, wherein said wet product is a slurry that is oxidized less due to the MCA treatment.

24. The method of claim 15, wherein said gluten or other protein is recovered, and said method requires less alkaline additions to maintain a pH value within 10% of the isoelectric point of the gluten or the other protein due to the MCA treatment, compared to when said MCA treatment is not used.

25. The method of any preceding claim, wherein microbial activity is controlled throughout all points in the process such that the CFU/g is maintained or reduced by at least 1 log.

26. The method of any preceding claim, wherein said method results in a reduced chemical oxygen demand in an effluent stream not containing starch or a fraction thereof.

27. The method of any preceding claim, wherein in said method, microbial lactic acid formation is below 1.5 g/1.

28. The method of any preceding claim, wherein in said method, a pH of from about 5 to about 7 is maintained with respect to the wet product or wet fractions thereof.

29. The method of any preceding claim, wherein starch yields are increased compared to when said MCA treatment is not used.

30. The method of any preceding claim, wherein the addition of xylanases and/or cellulases for viscosity reduction is reduced or eliminated.

31. The method of any preceding claim, wherein mineral scale up is reduced.

32. The method of any preceding claim, wherein said MCA treatment removes biofilms or prevents biofilm formation.

33. The method of claim 15, wherein improved gluten agglomeration and dewatering is achieved compared to when said MCA treatment is not used.

34. The method of claim 15, wherein said gluten or other protein is recovered and wherein the gluten or other protein has an increased number of disulfide bonds compared to when said MCA treatment is not used.

35. The method of claim 15, wherein said gluten or other protein is recovered and wherein said gluten or other protein has an increased amount of protein compared to when MCA treatment is not used.

36. The method of any preceding claim, wherein fouling in said method due to at least biofilm formation is reduced due to the MCA treatment, as compared to when MCA treatment is not used.

37. The method of any preceding claim, wherein said method reduces the amount or eliminates the need of adding alkaline agents to maintain a pH environment.

38. The method of any preceding claim, wherein said dosage of monochloramine comprises at least 3 dosage points in said method.

39. The method of any preceding claim, wherein said dosage of monochloramine comprises at least 5 dosage points in said method.

40. The method of any preceding claim, wherein said dosage of monochloramine comprises at least 8 dosage points in said method.

41. The method of claim 15, wherein said treating comprises treating said water with monochloramine prior to, during, and/or after said adding of water to the milled wheat.

42. The method of claim 15, wherein said first wet separation step comprises at least one 3 -phase decanter centrifuge or at least one separation tank.

43. The method of claim 15, wherein said method comprises at least three separate wet separations of said wet product or a fraction thereof utilizing separators located at three different points of the method, and said method further comprises dosing with said monochloramine immediately before and/or during each of said at least three separations.

44. The method of any preceding claim, wherein said treating with monochloramine comprises multiple dosing points throughout said method such that said MCA concentration is maintained with respect to any point from said wet product to prior to obtaining said dried starch.

45. The method of claim 15, wherein said treating with said monochloramine occurs within 20 minutes after forming said milled wheat.

46. The method of claim 15, wherein said treating with said monochloramine occurs within 20 minutes after forming said wet product.

47. The method of claim 15, wherein said method further comprises utilizing multiple tanks to hold liquid that comprises primarily water, wherein said liquid comprises process water, pulp press water, wash water, or any combinations thereof, and said multiple tanks include feed lines to and/or from each of said multiple tanks, and said liquid has said MCA concentration in said multiple tanks and in said feed lines.

48. The method of any preceding claim, said method further comprising converting at least a portion of said starch to glucose or dextrin.

49. The method of any preceding claim, said method further comprising converting at least a portion of said starch to glucose or dextrin and then conducting a fermentation of said glucose or dextrin to form one or more bioproducts.

50. A method for extracting starch or protein or both from an agricultural product, said method comprising obtaining a processed product that is a starting agricultural product that is milled, grated, pulped, diced, shredded, or any combination thereof, conducting one or more separation steps to the processed product or to a fraction thereof to obtain at least a first wet solid that comprises starch or protein or both, and drying the first wet solid to obtain a dried solid that comprises dry starch or dry protein or both, wherein at a point immediately prior to conducting and/or during a first of the one or more separation steps, the method further comprises treating the processed product with monochloramine, and wherein said method reduces the amount or eliminates the need of adding alkaline agents to maintain a pH environment.

51. The method of any preceding claim, wherein the processed product or a fraction thereof has a maximum chloramine or MCA residual amount of 10 ppm until the processed product or fraction thereof is dried or subject to enzymatic or microbial treatments in one or more starch conversion processes.