DE112021000385T5 - PROCESS FOR EXTRACTING STARCH FROM AGRICULTURAL PRODUCTS - Google Patents

Abstract

Methods for extracting starch and/or protein from agricultural produce such as wheat, potatoes and corn are described. The processes involve the use of continuous or semi-continuous dosing of monochloramine at various stages of the process. The methods may result in an increase in the amount of starch and/or protein extracted, as well as one or more other benefits.

Description

BACKGROUND ART

This application claims priority under 35 USC §119(e) to prior US Provisional Patent Application No. 62/966,700 , filed January 28, 2020, which is incorporated herein by reference in its entirety.

The present invention relates to methods for extracting starch and/or protein from agricultural produce, including but not limited to bacterial control during starch and/or protein extraction process steps.

Starch is extracted from a wide range of agricultural products. These include corn, wheat, potatoes and cassava, and to a lesser extent rice, barley, sorghum, sago and plants from the legume family. Regardless of which crop the starch is to be extracted from, the manufacturing processes are essentially the same. They are all based on the decomposition (grinding) of the raw material and the subsequent mechanical separation of the various components. Grains like corn and wheat are ground by crushing, while tubers/roots like potatoes and cassava/manioc are chopped up using graters. Subsequent separation of the components occurs either on the basis of their different size - using sieves or filters - or their different weight - using gravity in centrifugal separators (decanter centrifuges, jet centrifuges or hydrocyclones) in the presence of water.

A problem faced by the industry in general is the efficiency of the separation process, the quality of the product and the yield, which generally depends on a variety of factors. In wheat, long polymers, which 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 during dough preparation to break down these polymers and lower dough viscosity to achieve optimal separation of the starch and gluten (or protein) phases, resulting in high cost with limited performance , which depends on the conditions in the mixing tank (temperature, pH value).

Another problem in the industry is the wet processing of starch. Temperatures between 30 and 40°C and the availability of dextrans and polysaccharides in an aqueous solution during such starch processes provide an ideal environment for the growth of microorganisms. The microorganisms are equipped with an enzymatic system to break down these molecules into sugars and ferment the sugars into a variety of organic acids, e.g. B. lactic acid, which causes the pH value of the process water to drop significantly above the optimal pH value for processing (about pH 4). This formation of lactic acid can be accompanied by premature breakdown of the starch by the formation of microbial amylases, which leads to reduced yields and reduced starch quality. The use of strong oxidizing agents to prevent bacterial growth often results in undesirable oxidation of the organic materials. If the dough is oxidized too much, the structure of the starch and gluten can change and the quality of the end products can deteriorate.

Another problem facing the industry is the agglomeration process used to simultaneously obtain high quality gluten and high quality starch. Intense mixing, high shear, good hydration, and operating at isoelectric point pH can be useful parameters. The pH of the gluten can be adjusted to the isoelectric point (pH 5.2-6.2) by adding a base. This increases drainage ability and yield because the gluten's water absorption is reduced. A screw press can be used to remove excess water from wet feed material in preparation for drying. The solubility of grain proteins is a function of pH. Poor drainage, high water retention and/or inhomogeneous moisture distribution due to acidification of the process can lead to reduced evaporative capacity of the dryer and high energy requirements. Accordingly, large amounts of alkalis such as caustic soda or sodium bicarbonate are usually used to stabilize the pH near the isoelectric point of the gluten and thus optimize the agglomeration of the gluten, resulting in high chemical costs and a more complicated process.

Another problem in industry is the presence of microbial cells on surfaces, leading to the formation of biofilms, which can also lead to microbiologically influenced corrosion. Biofilms accumulate on all submerged surfaces in industry and the environment. Contamination of the surfaces of pipes and tanks in a wet scrubbing plant requires frequent cleaning. This presents a significant problem as water and chemical disposal costs increase. Under pollution ver is the undesirable deposition of material on a surface and this includes protein and mineral deposits, product solidification, biofilm growth and the accumulation of material in stagnant or stagnant areas of equipment. Cleaning methods such as CIP are widely used to remove unwanted contaminants in a processing facility to maintain product safety and process efficiency. The economic disadvantages of contaminants in wet separation can be quantified in terms of maintenance costs and costs due to production losses, as well as cleaning agent and water costs.

Another problem in industry is the washing of vegetables or plants, which produces water with a high particle load and some dissolved organic matter. Annually in the European Union more than 2 million tons of juice are obtained from the starch production of potatoes. This stream consists mainly of water with a high concentration of potassium and has a high COD value (at least 20 000 mg O/1) due, among other things, to the presence of proteins, amino acids and sugars. The grain and vegetable processing food industry generates a lot of effluent and organic sugars and starches that may contain pesticide residues.

Water and energy consumption in this industry can also be very high. In the production of wheat starch, the water consumption during deglutination alone can amount to 11-15 m ³ 1 ^-1 wheat flour and is then discharged as waste water.

The inventors have therefore determined that the starch production industry needs improved processes that solve one or more of the above problems without sacrificing the quality of the starch obtained.

SUMMARY OF THE PRESENT INVENTION

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.

An additional feature of the present invention is to provide a method of 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 may have a pH of 6 or about 6, which provides optimal conditions for the extraction or separation process and may avoid or minimize the use of pH control agents or pH control steps such as the use of caustic).

It is another feature of the present invention to provide a method of using a monochloramine in a starch extraction process or protein extraction process.

Another feature of the present invention is to provide a method for increasing the amount of starch recovered and/or the amount of protein (or gluten) recovered.

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

To achieve these and other advantages, and in accordance with the objects of the present invention, as embodied and broadly described herein, the present invention relates to a method of extracting starch and/or protein from an agricultural produce. The method includes obtaining a processed product that is a starting agricultural product that is, consists essentially of, consists of, or comprises ground, ground, ground, or a combination thereof. The method further comprises performing one or more separation steps (e.g. solid-liquid separations) on the processed product or a fraction thereof to obtain at least a first wet solid comprising starch or protein or both substantially therefrom consists of, consists of or has this. The method further comprises drying the first wet solid to obtain a dried solid comprising, consisting essentially of, consisting of, or having dry starch, dry protein, or both. In the process, at a point prior to performing and/or during a first of the one or more separation steps, the method further comprises the step(s) of treating the processed product or a feed line(s) with monochloramine. Treating includes continuous or near-continuous or non-continuous dosing(s) of the monochloramine (MCA) to provide an MCA concentration in an amount between about 40 ppm and about 800 ppm (this can be done, for example, by adding from 50 g to about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural produce be achieved). Treating with MCA may also include dosing an aqueous monochloramine solution containing between about 0.1% and about 2% (such as about 0.1% to 1% by weight) monochloramine by weight ( based on the total weight of the aqueous monochloramine solution).

The present invention also relates to a method for extracting starch or protein or both from an agricultural product, which comprises processing a starting agricultural product to obtain a processed product which is ground, grated, comminuted or any combination thereof. The method then comprises wetting the processed product to obtain a wet product and thereafter subjecting the wet product or fraction thereof to one or more solid-liquid separation steps to obtain at least a first wet solid comprising starch or protein or both. The method then includes the step of drying the first wet solid to obtain a dried solid comprising starch or protein or both. In the method, during and/or after the wetting step and before performing 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 the supply line(s) with monochloramine ("MCA"). This treatment step includes or is a continuous or near-continuous or discontinuous dosing of the monochloramine to provide an MCA concentration. The treating includes or features continuous or near-continuous or discontinuous dosing(s) of the monochloramine (MCA) to provide an MCA concentration in an amount between about 40 ppm and about 800 ppm (this may be, for example, by the addition of 50 g to about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural produce can be achieved). Treating with MCA also includes dosing an aqueous monochloramine solution containing between about 0.1% and about 2% (such as about 0.1% to 1% by weight) monochloramine by weight (based on based on the total weight of the aqueous monochloramine solution).

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 performing at least two wet separation steps on the wet product and/or a fraction thereof. The wet separation steps are separations based on weight, size, or both of the wet product or a fraction thereof. A first wet separation step at least partially separates Type A starches from at least gluten (or a protein) and a non-Type A starch in the wet product, and a second wet separation step at least partially separates Type A starches from non-types - Type A starches, such as Type B starches, in at least one fraction of the wet product. The method further includes the step of drying at least the Type A starches to obtain a dried starch. Furthermore, in this method, during and/or after wetting and before performing and/or during a first of the two wet separation steps, the method further comprises treating the wet product and/or the feed line(s) with monochloramine and comprises a treating the fraction with monochloramine just before and/or during the second wet separation step. The treating preferably includes or comprises continuous or near-continuous or discontinuous dosing of the monochloramine (MCA) to provide an MCA concentration. The treating includes or features continuous or near-continuous or discontinuous dosing(s) of the monochloramine (MCA) to provide an MCA concentration in an amount between about 40 ppm and about 800 ppm (this may be, for example, by the addition of 50 g to about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural produce can be achieved). Preferably, treating with MCA also includes dosing an aqueous monochloramine solution containing between about 0.1% and about 2% (such as about 0.1% to 1% by weight) monochloramine by weight ( based on the total weight of the aqueous monochloramine solution).

The present invention further relates to an optional processing of the starch or refining of the starch to obtain glucose, sugars, 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.

The present invention further relates to products obtained from one or more of the processes of the present invention, including but not limited to starch and/or gluten (or a protein) and/or by-products from the one or more processes.

It is to be noted that both the foregoing general description and the following detailed description are exemplary and explanatory only and are intended to provide further explanation of the present invention as claimed.

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.

character list

• 1 ist ein Prozessflussdiagramm, das ein Verfahren zum Extrahieren von Stärke und/oder Protein gemäß einem Beispiel der vorliegenden Erfindung veranschaulicht.
• 2 ist ein Prozessflussdiagramm, das ein Verfahren zum Extrahieren von Stärke und/oder Protein gemäß einem Beispiel der vorliegenden Erfindung veranschaulicht.
• 3 ist ein Prozessflussdiagramm, das ein Verfahren gemäß einem Beispiel der vorliegenden Anmeldung veranschaulicht, wobei das landwirtschaftliche Erzeugnis Mais ist.
• 4 ist ein Prozessflussdiagramm, das ein Verfahren gemäß einem Beispiel der vorliegenden Anmeldung veranschaulicht, wobei das landwirtschaftliche Erzeugnis Weizen ist.
• 5 ist ein Prozessflussdiagramm, das ein Verfahren gemäß einem Beispiel der vorliegenden Anmeldung veranschaulicht, wobei das landwirtschaftliche Erzeugnis Knollen sind.
• 6 ist ein Prozessflussdiagramm, das ein Verfahren gemäß einem Beispiel der vorliegenden Anmeldung veranschaulicht.
• 7 ist ein Prozessflussdiagramm, das ein Verfahren gemäß einem Beispiel der vorliegenden Anmeldung veranschaulicht, wobei das landwirtschaftliche Erzeugnis Weizen ist.
• 8 ist ein Prozessflussdiagramm, das ein Verfahren gemäß einem weiteren Beispiel der vorliegenden Anmeldung veranschaulicht, wobei das landwirtschaftliche Erzeugnis Weizen ist.
• 9 ist ein Prozessflussdiagramm, das Optionen für weitere Schritte veranschaulicht, sobald die Stärke extrahiert wurde, wie etwa, jedoch nicht beschränkt auf eine Stärkeumwandlung und ein Erhalten von Glukose oder eine Fermentation.
• 10 ist ein Prozessflussdiagramm, das den Vorgang zur Umwandlung von Stärke in eine oder mehrere Arten von Dextrinen veranschaulicht.
• 11 ist ein Prozessflussdiagramm, das eine Ausführungsform der Herstellung einer Stärkesuspension ausführlicher veranschaulicht.
• 12 ist ein Prozessflussdiagramm, das die Herstellung von Stärkeerzeugnissen veranschaulicht.
• 13 ist ein Prozessflussdiagramm, das die Herstellung von Süßungsmitteln und Ethanol aus Stärkeerzeugnissen veranschaulicht.
• 14 ist ein Prozessflussdiagramm, das die Herstellung von Stärke aus Weizen veranschaulicht, was eine mögliche Ausführungsform darstellt.
• 15 ist ein Prozessflussdiagramm, das die Herstellung von Stärke aus Kartoffeln veranschaulicht, was eine mögliche Ausführungsform darstellt.

The present invention can be more fully understood with reference to the attached figures. The figures are intended to illustrate exemplary features of the present invention without limiting the scope of the invention.

• 1 Figure 12 is a process flow diagram illustrating a method for extracting starch and/or protein according to an example of the present invention.
• 2 Figure 12 is a process flow diagram illustrating a method for extracting starch and/or protein according to an example of the present invention.
• 3 Figure 12 is a process flow diagram illustrating a method according to an example of the present application, wherein the agricultural product is corn.
• 4 Figure 12 is a process flow diagram illustrating a method according to an example of the present application, where the agricultural product is wheat.
• 5 Figure 12 is a process flow diagram illustrating a method according to an example of the present application, wherein the agricultural product is tubers.
• 6 Figure 12 is a process flow diagram illustrating a method according to an example of the present application.
• 7 Figure 12 is a process flow diagram illustrating a method according to an example of the present application, where the agricultural product is wheat.
• 8th Figure 12 is a process flow diagram illustrating a method according to another example of the present application, wherein the agricultural product is wheat.
• 9 Figure 12 is a process flow diagram illustrating options for further steps once the starch has been extracted, such as but not limited to starch conversion and obtaining glucose or fermentation.
• 10 Figure 12 is a process flow diagram illustrating the process of converting starch into one or more types of dextrins.
• 11 Figure 12 is a process flow diagram illustrating in more detail one embodiment of preparing a starch suspension.
• 12 Figure 12 is a process flow diagram illustrating the manufacture of starch products.
• 13 Figure 12 is a process flow diagram illustrating the manufacture of sweeteners and ethanol from starch products.
• 14 Figure 12 is a process flow diagram illustrating the production of starch from wheat, which is one possible embodiment.
• 15 Figure 12 is a process flow diagram illustrating the production of starch from potatoes, which is one possible embodiment.

DETAILED DESCRIPTION OF THE PRESENT INVENTION

According to the present invention, a method is provided to extract starch or protein or both from agricultural produce using chloramine such as monochloramine.

A key to effectively solving the above problems is proper biocide treatment and this includes using the right biocide, the right dosage, the right application site(s), stabilizing the pH, maintaining the correct residual biocide content and maintaining this treatment over a longer period of time. The biocide can be considered as an antimicrobial processing aid.

Consequently, methods for extracting starch and/or protein from agricultural sources (e.g. agricultural produce) are strategically combined at certain points in the process with one or more chloramines, e.g. monochloramine (MCA), dichloramine (DCA) or a combination thereof. Monochloramine is preferably used primarily. A majority (by weight) of the chloramine may 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 that present chloramines). The treatment can be carried out in any suitable manner. The treatment can be continuous, substantially continuous, intermittent, cyclic, batch, or a combination thereof. The treatment is performed at multiple points in a starch extraction process as further described herein.

The agricultural product may be a vegetable material containing starch. The agricultural product may be a tree material containing starch. The term "plant" is used herein botanically unless otherwise noted. Examples of agricultural products include, but are not limited to, wheat, potato, corn, cassava, tapioca, rice, sorghum, barley, sago, cassava, or any plant of the legume family, or any combination thereof, or any part thereof. The starting agricultural product may be a raw agricultural product such as, but not limited to, raw wheat, potato, corn, cassava, tapioca, rice, sorghum, barley, sago, cassava, or a plant of the legume family, or any combination thereof. The starting agricultural product may be a fraction or part of wheat, potato, corn, cassava, tapioca, rice, sorghum, barley, sago, cassava, or any plant of the legume family, or any combination thereof. The starting agricultural product may be a washed and/or peeled and/or sliced or diced or minced or pounded raw agricultural product. In general, the agricultural product is neither cooked nor exposed to high temperatures, such as above 100 degrees Celsius, before it is ground and/or grated.

A key point of the present invention and to achieve one or more benefits, such as increased starch production, is the use of chloramine treatment (hereinafter sometimes referred to as monochloramine treatment (or MCA treatment)) at appropriate dosing points in the starch and/or protein extraction process. Consequently, not only is the use of monochloramine important, but also the location of monochloramine dosing, the frequency of monochloramine dosing, and the amount (concentration) of monochloramine dosing.

A treatment that stabilizes the pH value is also important or helpful. Most other biocides or antimicrobial processing aids used in starch and/or protein extraction do not control pH as well, although they do control the microbiology. For example, with peracetic acid, despite the inhibition of lactic acid formation, the environment is still acidic, requiring the addition of caustic and close monitoring of pH. In the present invention and processes, a real differentiator from monochloramine is the stabilization of the pH around pH 6 (within 15% or within 10% of pH 6), which provides optimal conditions for separation processes without the pH control and/or over- or under-dosing of caustic or other pH agents is required.

In one aspect of the present invention, the present invention relates to a method for extracting starch or protein or both from an agricultural produce (as described herein). The method includes obtaining a processed product which is a starting agricultural product that is ground, diced, grated, minced, crushed, or a combination thereof, consists essentially of, consists of, or comprises. This processed product may take or be in the form of a flour, pulp, pulp and/or fiber and the like.

The method further comprises performing one or more separation steps (e.g. solid-liquid separations) on the processed product or a fraction thereof to obtain at least a first wet solid comprising starch or protein or both substantially therefrom consists of, consists of or has. The method further comprises drying the first wet solid to obtain a dried solid comprising, consisting essentially of, consisting of, or comprising dry starch or dry protein or both. Intermediate processing steps may occur before the one or more separating steps and one or more pre-drying processing steps may occur after one or more of the separating steps to obtain the starch and/or protein. This general process is in 1 shown showing a flow chart of the steps. In all figures, "MCA" means the dosing sites for the chloramine (e.g., MCA) at the MCA concentrations and dosages described herein. By "optional MCA" in the figures is meant optional dosing sites for the chloramine (e.g., MCA) at the MCA concentrations and dosages described herein. The "MCA or MCA” in the figures indicates that the dosing site can be in either of two or more sites or in both of the two or more sites.

In the processes of the present invention, at least at a point immediately prior to performing and/or during a first of the one or more separating steps, the method further comprises the step(s) of treating the processed product and/or the feed line(s), used in the processed product with chloramine such as monochloramine. The treating preferably includes or has discontinuous or continuous or near-continuous dosing(s) of the monochloramine (MCA) to provide an MCA concentration in an amount between about 40 ppm and about 800 ppm (this can be done, for example, by the addition from 50 g to about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural produce can be achieved). Treating with MCA also includes dosing an aqueous monochloramine solution containing between about 0.1% and about 2% (such as about 0.1% to 1% by weight) monochloramine by weight (based on based on the total weight of the aqueous monochloramine solution). The MCA concentration in an amount from about 40 ppm to about 800 ppm refers to the concentration of the material being treated (e.g., the processed produce or the water being used).

As an option, the material being treated in the present invention can also have a maximum residual level of chloramine or MCA of 10ppm, 7ppm, 5ppm, 3ppm or 2.5ppm or 2ppm or 1.5ppm or 1ppm or 0.5 ppm. This residual level can be determined based on the total chlorine detected in the material being tested for residual level. Optionally, this residual amount can be present after the first dosing of MCA in the process and either be present throughout the process until the starch or a fraction thereof (or the protein) is dried, or it can be present at a point just after the last separation step be continued to further concentrate a starch or a fraction thereof (or a protein). If a starch or a fraction thereof (or protein) is to be further processed with some type of enzymatic and/or microbial treatment (e.g. starch conversion such as hydrolysis or fermentation), the remainder can be treated with an enzyme and/or microbial treatment before further processing treatment to a value below 0.5 ppm or to about 0 ppm or to 0 ppm. This can be achieved by aborting the MCA treatment prior to this further processing.

As a more specific example, as in 2 which is 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 processing, consists essentially of, consists of, or includes processing of a starting agricultural product to obtain a processed product that is ground, grated, diced, minced, mashed, or a combination thereof. The method includes wetting the processed product to obtain a wet product. The method further comprises performing one or more separation steps (e.g. solid-liquid separations) on the wet product or a fraction thereof to obtain at least a first wet solid comprising starch or protein or both substantially therefrom consists of, consists of or has. The method further comprises drying the first wet solid to obtain a dried solid comprising, consisting essentially of, consisting of, or comprising dry starch or dry protein or both. In the process, the method further comprises, at least at a point during and/or after the wetting and before performing and/or during a first of the one or more separating steps, the step(s) of treating the wet product (and/or the Wet product feed line(s) with chloramine, such as monochloramine ("MCA"). The treating preferably includes or has discontinuous or continuous or near-continuous dosing(s) of the monochloramine (MCA) to provide an MCA concentration in an amount between about 40 ppm and about 800 ppm (this can be done, for example, by the addition of 50 g to about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural produce can be achieved). Treating with MCA also includes dosing an aqueous monochloramine solution containing between about 0.1% and about 2% (such as about 0.1% to 1% by weight) monochloramine by weight (based on based on the total weight of the aqueous monochloramine solution).

Processing of the starting agricultural product (the “Processing” step) may include, consist essentially of, consist of, or comprise milling, grating, dicing, crushing, mincing and/or otherwise reducing the size of the starting agricultural product. This can be accomplished with grinders, rotary graters, graters, and the like. This processing step and the way it is carried out is known to those skilled in the art. This processing can result in a flour, mash, pulp and/or fiber and the like. Optionally, the starting agricultural product may be subjected to a cleaning step, such as with water and/or scrubbers and/or sieves, prior to this processing step. Optionally, prior to the processing step, the starting agricultural product may be subjected to, for example, a steeping step to soften the starting agricultural product (e.g., corn). These options and a more detailed flowchart of the general process are in 6 shown. The water or liquid used for an optional cleaning or washing step can be pre- and/or post-treated with the MCA treatment as described herein.

After the processing step (milling, grating, crushing and/or reducing the size of the starting agricultural product in some other way) and for example before a separation step (e.g. a solid-liquid separation step), the processed product can optionally be one or more of the undergo the following steps, which may depend on the nature of the initial agricultural product: juice separation, the use of hydrocyclones and/or sieves 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 the material during the optional step are receiving or undergoing MCA treatment as described herein. In other words, before (or immediately before) and/or after (or immediately after) and/or during the one or more optional steps, the material or a portion of the material may receive or be subjected to an MCA treatment as described herein will. This possibility of performing an MCA treatment in one or more optional steps is partly in 6 played back.

For purposes of the present invention, it is to be understood that the "processing" step includes or may include the loading or unloading of a product that has already been processed, such as a product that has already been ground, grated, diced, or shredded. It is within the scope of the present invention for the milling, grating, dicing, crushing and/or mincing to be performed at a different location or processing facility and then moved to a location where the subsequent steps of the present invention are performed. As a more specific example, wheat flour may be formed at another site and then transferred or transported to the site where the subsequent steps of the present invention are performed, and this prior preparation of the processed product and transfer/transportation may complete the step of processing include unless otherwise noted.

Depending on the starting agricultural product, the process may include the step of wetting the processed product. The wetting step may include combining or adding at least water to the processed product to form a suspension or mixture or wetted product. It is noted that prior to the wetting step, the processed product may be in either a dry state (e.g. wheat flour) or wet state (e.g. potato pulp or corn fiber). The wetting step with water can include a dilution step or can be a dilution step. The wetting step may include a water washing step or may be a water washing step. The water can optionally contain one or more other components or ingredients. The techniques and apparatus used, as well as the amounts of water used to wet the processed product, are conventional in the art and known to those skilled in the art.

Any water or portions thereof used in the processes of the present invention (e.g. one of the streams and/or more than one stream) may be added before, during and/or after the water is combined or added to the processed product treated with chloramine such as monochloramine. The techniques and dosages can be as described herein. Thus, the treatment may optionally include treating water with monochloramine before, during and/or after adding water to the ground wheat or other processed product or fraction thereof.

The one or more separation steps may include or be one or more solid-liquid separation steps.

The one or more separation steps can be carried out by using at least one centrifuge, at least one decanter (e.g. 2-phase decanter or 3-phase decanter), at least one sieve (e.g. curved sieve), at least one separation tank, at least a grid, at least one hydrocyclone or any combination thereof can be achieved. The one or more separation steps may be viewed as, or result in, a concentration of one or more particular components or fractions of the processed product. Ultimately, at least one or more of the separation steps lead to the isolation or concentration of starch or a type of starch and/or to the isolation or concentration of protein or a type of protein.

More specific examples of a centrifuge include a jet centrifuge, a decanter centrifuge, and a three-phase decanter centrifuge, among others. Depending on the product to be processed, certain centrifuges are considered more advantageous. For example, a jet centrifuge is more common in corn separation. Decanter centrifuges are mainly used to separate wheat and potatoes. The separation step, particularly that using one or more centrifuges, is known to those skilled in the art and centrifuges are commercially available, for example from manufacturers such as Alfa Laval (e.g. the Alfa Laval Merco centrifuge and the Alfa Laval STNX 944 centrifuge) or a Hiller DecaPress decanter centrifuge or a Centri-Force or Flottweg decanter centrifuge (2- or 3-phase decanters, centrifuges and the like).

The one or more separating steps may include or include at least a first separating step and a second separating step, wherein at least a portion of the product separated in the first separating step is processed by the second separating step, and wherein treating (as described herein) the processed product or a fraction thereof with monochloramine prior to (and preferably immediately prior to) and/or during both the first and second separation steps.

As a more specific example, the plurality of separation steps may be one or more separation steps that may include or have 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 separating step, being processed by the second solid-liquid separating step, and prior to and/or during both the first solid-liquid separating step and the second solid-liquid separating step, treating (as described herein) the processed product or fraction of which takes place with monochloramine.

Referring to examples of agricultural products and as in 3 reproduced, in the case of corn processing, a first separation step can separate at least part of the starch from the gluten (or protein), known as primary separation, and the second separation step can separate at least part of the gluten (or product) from water. After the primary separation, the recovered starch can optionally be washed with water or subjected to a further separation step to remove at least part of the protein that is still present and/or other impurities. This can be done with one or more centrifuges and/or hydrocyclones. The second separation step may further include further processing, including but not limited to, for example, dewatering steps to remove additional water from the gluten (or a protein), for example using one or more filters, such as one or more suction filters. As indicated, the processed product or a fraction thereof is treated with the MCA treatment as described herein before and/or during the first and second separation steps, and preferably immediately before and/or during both the first and second separation steps.

With further reference to examples of agricultural products and as in 4 For example, wheat in flour or milled form can be made into a suspension with water. The suspension may then undergo a first separation step which, in the case of wheat processing, separates at least part of the Type A starch (also known as Prime A starch or A starch) from one or more other fractions in the processed product (e.g e.g. at least part of the B starch and gluten) and from one or more additional fractions in the processed product (e.g. at least part of the C starch and optionally pentosans and/or other solubles). The first separation in the case of wheat processing can therefore be a separation into at least three fractions (a first fraction consisting primarily of A starch, a second fraction consisting primarily of B starch and gluten, and a third fraction primarily consists of C-starch and/or pentosans). The second separation may be one or more of the following: a) separating the second fraction so that at least part of the B starch is separated from the gluten, b) further separating the first fraction by separating at least part of the A starch from non -A-starch components and/or water, c) separating at least part of the fibers present in the first fraction from A-starch. The second separation can be one of the following: a) or b) or c), or a) and b), or a) and c), or b) and c). As indicated, the processed product or a fraction thereof is provided and/or treated with the MCA treatment as described herein during the first and second separation steps and preferably immediately before and/or during both the first and second separation steps.

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

It is noted that the drying step, in which the starch or a component thereof or a by-product thereof is dried, is not shown in any of the figures. Other steps not shown or described may also be included. The figures are intended to show the most important steps for the purposes of the present invention along with the preferred MCA dosage points and the optional MCA dosage points.

Optionally, the process of the present invention can provide at least three separate separations of the wet product and/or a fraction thereof using separators (e.g. centrifuges of the same or a different type, such as nozzle centrifuges and/or decanter centrifuges and/or decanters and/or or 3-phase separators and/or 2-phase separators and/or grids and/or sieves and/or separation tanks and/or hydrocyclones) located at three different processing points of the process and the process further comprises a Dosing of the chloramine (e.g. monochloramine) immediately before and/or during each of the at least three separations.

In general, the 'immediate' treatment of the processed product or a fraction thereof with chloramine (e.g. monochloramine) before a separation step can mean, for example, that the MCA treatment occurs after a previous mechanical processing step that takes place before a separation step (e.g. B. after suspension formation, but before a separation step), and / or that the MCA treatment in a range of 1 second to 5 minutes before performing the / the separation step (s), for example from 5 seconds to 3 minutes or from 10 seconds to 1 minute before the separation step(s).

In general, treatment of the processed product or a fraction thereof with chloramine (e.g. monochloramine) 'during' a separation step may mean that the chloramine is fed directly to the separation device or site (e.g. dosed directly into the decanter) , and this can be done with chloramine present in water or other dosing techniques mentioned herein. The 'during' can be continuous, non-continuous, intermittent, before the start of the breakup, during the breakup, and/or after the breakup. Any combination of dosing times is possible.

When the process includes the step of forming the processed product (e.g., by milling or grating or crushing), which occurs prior to the first separation step, any MCA treatment can be performed within 20 minutes or within 10 minutes of this forming step, such as take place, for example, within 5 minutes, or within 1 minute, or within 30 seconds, or immediately after this formation step.

When the wetting step is included in the method(s) of the present invention, the MCA treatment may 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 the wetting step or within 30 seconds for this wetting step to take place or the water used to wet the processed product can be pretreated with MCA at the dosages/concentrations described herein.

Optionally, the method(s) of the present invention can include pH control such that a pH of about 5 to about 7 is maintained with respect to the wet product or wet fractions thereof.

In conventional methods for extracting starch (or protein) from agricultural Crisp produce typically has alkaline agents added to the process (e.g., the process water and/or produce or a fraction thereof) to maintain a desirable pH environment, such as a pH of from 5 to about 7. In the present invention, particularly in wheat processing but not limited to wheat, the methods of the present invention can reduce the amount (of pH control agents) required to produce a pH due to the strategic use of the MCA treatment described herein. environment, such as a pH of about 5 to about 7 to maintain. The reduction in the amount of alkaline agents may be at least 5%, at least 10% or at least 20%, for example from 1% to 20% or 5% to 20% by weight (based on the comparison described above).

Additionally, the present invention, the MCA treatment described herein may eliminate the need for the addition of caustics to the starch extraction process or parts of the process, or process stages may be performed without the addition of caustics to maintain a pH environment.

As indicated, the methods of the present invention involve the strategic dosing of MCA at multiple points of a starch and/or protein extraction process. Preferably, the dosage of monochloramine can comprise or have at least 2 dosage points or at least 3 dosage points (which are separate from each other and are in different processing phases of the starch and/or protein extraction process), or it can comprise at least 4 dosage points or at least 5 dosage points (which are separate from each other and are in different processing phases of the starch and/or protein extraction process) or it may comprise or have at least 8 dosing points (which are separate from each other and are in different processing phases of the starch and/or protein extraction process).

Optionally, the monochloramine treatment may include or have multiple dosing points throughout the starch and/or protein extraction process such that the MCA concentration (±20% or ±10% or ±5%) relative to any point from the formation of the wet product is maintained until prior to obtaining the dried starch or the dried protein or both.

The starch and/or protein extraction process may also generally involve the use of multiple tanks for holding liquid that primarily contains water (e.g. the liquid comprises at least 51% water by weight, 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 may include process water, pulp press water, wash water, or any combination thereof. The multiple tanks have supply lines to and/or from each of the multiple tanks. The liquid in the supply lines and in the multiple tanks may have the MCA concentration and/or is a dosing point for the MCA.

The term "feed line(s)" or "feed lines" is sometimes used to describe what is being treated. For example, as described herein, "at a point immediately prior to performing or during a first of the one or more separating steps, the method further comprising treating the processed product or the feed line(s) or both." The "feed line( en)" is/are a reference to the piping system or lines 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 thereby the one or more features and/or Benefits as described herein are achieved. In a sense, by treating the processed product, or a fraction thereof, as described herein, since the MCA is present with the processed product, the hardware used to transport or hold the processed product is treated equally. Similarly, by treating the hardware itself with the MCA as described herein, the processed product, or fraction thereof, that passes through the hardware is treated somewhat equally.

In the present invention, the method may comprise, consist essentially of, consist of or comprise utilizing multiple tanks for holding liquor predominantly comprising water, the liquor comprising process water, pulp press water, wash water or any combination thereof, and wherein the plurality of tanks includes supply lines to and/or from each of the plurality of tanks, and wherein the liquid has the MCA concentration (as described herein) in the plurality of tanks and in the supply lines.

As indicated, the figures which form a part of the present invention show example flow charts of the starch extraction process (and/or protein extraction process) and non-limiting example MCA dosage points. 7 and 8th show more specific examples of a starch extraction process for wheat and preferred MCA dosage points. 7 depicts "monochloramine" with arrows to show locations of preferred MCA dosing points in the process. 7 shows a preferred process scheme in which B-starch is used for ethanol processing or for animal feed and therefore the dosing of MCA for the 'medium flow' takes place after a further 3-phase separation step. 8th Figure 1 shows a preferred process scheme where B-starch is used for a refinery and therefore the dosing of MCA for the 'middle flow' can be done before this particular 3-phase separation step. It is to be understood that when "monochloramine" in 7 and 8th shown with an arrow next to the "3-phase decanter", the introduction of MCA or the dosing of MCA either before and/or during this separation step (e.g. by dosing directly into the separator or zone) before, during and/or after the separation has been performed but in the separation device or zone.

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

Once the starch is concentrated or divided into fractions, in a post-starch treatment, the starch or a fraction thereof can optionally be subjected to one or more starch conversion steps, in which the starch or a fraction thereof is converted into glucose or dextrin (used as a sweetener can), or the product converted to starch can be subjected to a conventional fermentation process to produce one or more bioproducts, such as ethanol. 9 and 10 show these general process steps in flow charts. Starch conversion can be a hydrolysis process using one or more enzymes and/or one or more acids. The enzymes are conventional enzymes such as glucose isomerase, glucoamylase, alpha-amylase, papain, trypsin and/or other food proteases. Further processing of the starch may include, but is not limited to, the steps of liquefaction, saccharification, purification (to maltose syrups, glucose syrups, blended syrups), isomerization and/or conventional refining steps to form/obtain fructose syrups.

Further details of the starch extraction process (and/or protein extraction process) are provided here (along with some optional post-starch (or post-protein) processing steps), and the description given here is one possible embodiment, with the understanding that additional steps used and others listed here may be omitted. The process described here is particularly suitable for obtaining starch from corn. The corn in the form of kernels undergoes a soaking process. During soaking, the kernels absorb water, which can more than double their moisture content, for example from 15 percent to 45 percent. In traditional processes, 0.1 percent sulfur dioxide was added to the water to prevent excessive bacterial growth in the warm environment. However, instead of this biocide, an MCA treatment as described herein can also be used. As the corn puffs up and softens, the mild acidity of the steep water begins to break the gluten bonds in the corn and release the starch. After soaking, the corn is coarsely ground to separate the germ from the other components. The steep water is condensed to recover the nutrients contained in the water for use in animal feed and as a nutrient for later fermentation processes. The ground corn flows in a water suspension to the germ separators. Then, in a process, cyclone separators throw the low-density maize germ out of the suspension. The oily germ, which contains about 85 percent of the corn oil, for example, is pumped onto grids and washed several times to remove the starch remaining in the mixture. Here, this washing step can optionally include 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 corn oil. The remains of the germs are kept as another useful component of the animal feed. The corn and water suspension then exits the germ separator for a second, more thorough grinding in an impact or impact mill to loosen the starch and gluten from the fibers of the grain. The suspension of starch, gluten and fibers flows over fixed concave grids that catch the fibers, but leave the starch and gluten let it sit. The fibers are collected, slurried and screened again to recover any residual starch or protein, and then sent to the feed industry as the main component of animal feed. The starch-gluten suspension, also known as mill starch, is fed into the starch separator. Gluten has a low density compared to starch. By running the mill starch through a centrifuge, the gluten can be easily extracted for use in animal feed. As indicated, an MCA treatment may be performed before (or just before) this centrifugation step. The starch, with only a percent or two of protein left, is diluted, washed (one or more times, e.g. eight to 14 times), diluted again and washed again in hydroclones to remove the last traces of Remove protein and produce a high-quality starch that is typically greater than 99.5 percent pure. The washing step or immediately before this washing step, an MCA treatment as described herein can be carried out. A portion of the starch can be dried and marketed as unmodified cornstarch, the starch or portion of it can be modified into specialty starches, and/or the starch or portion of it can be converted to corn syrup and glucose.

For obtaining corn-based starch or any other starch, the following processes can be used. The starch suspended in water is liquefied in the presence of acid and/or enzymes that convert the starch into a low-glucose solution. An MCA treatment can be carried out before, during and/or after this liquefaction process. Treatment with another enzyme continues the conversion process. Throughout the process, refiners can interrupt acid or enzyme action at crucial points to create the right blend of sugars, such as glucose and maltose, for syrups that meet different needs. For some syrups, the conversion of starch to sugar is stopped at an early stage to produce low to medium sweetness syrups. In others, the conversion continues until the syrup is almost entirely glucose. The syrup is refined in filters, centrifuges and ion exchange columns, and excess water is evaporated. Syrups are sold direct, crystallized into pure glucose, or further processed into high fructose corn syrup. Optionally, a fermentation process can also be used afterwards.

Glucose is one of the most fermentable types of sugar. After the conversion of starch to glucose, the glucose can be used in glucose digestion plants, where the glucose is converted into alcohol through traditional yeast fermentation, or into amino acids and other bioproducts through yeast or bacterial fermentation. After fermentation, the resulting broth is distilled to recover alcohol or concentrated by membrane separation to produce other organic products. The carbon dioxide produced during fermentation is recovered for sale, and the nutrients remaining after fermentation are used as components of feed ingredients.

• • 70-80 % Rohprotein
• • 6-8 % Rohfette
• • 10-14 % Kohlenhydrate
• • 0,8-1,4 % Mineralien

Wheat starch granules can be divided into two groups (A starch and B starch) or three groups by size, with B starch (e.g. 15-20% by volume) having a diameter of 1-15 microns (or 1 -10 microns), the larger A-starch granules (e.g., 80-85% by volume) are 10-35 microns (or 20-35 microns) in diameter, and the C-starch can be one size , which is smaller than the B-starch size and/or a size of less than 5.3 microns. B-Starch and/or C-Starch can be so heavily contaminated with pentosans, fibres, lipids and proteins that further treatment is required. Gluten are wheat proteins. Gluten forms long molecules that are insoluble in water. This gives the dough its characteristic texture and allows breads and cakes to rise as the carbon dioxide released by the yeast is trapped in the gluten scaffold. Gluten is particularly important in the manufacture of starch from wheat as it is a very valuable by-product, accounting for half of sales. If the gluten is extracted and gently air-dried at moderate temperatures, it retains its properties. If this is the case, it is referred to as "vital gluten". Vital gluten can be added as a dry powder to the otherwise low-gluten flour and thus improve the baking properties of the flour. Commercial gluten can be dried to at least 90% dry matter and a typical composition is as follows (in percent by weight):

• • 70-80% crude protein
• • 6-8% raw fats
• • 10-14% carbohydrates
• • 0.8-1.4% minerals

Gluten is used in bread making as an ingredient that is added to the dough to improve the properties of the bread dough, e.g. B. in terms of elasticity and rising. In addition, gluten can be used as an extender in both food and feed. Gluten can be used in the fermentation industry using acid hydrolysis or enzyme hydrolysis. the gluten can be used to produce hydrolyzed vegetable protein and glutamic acid.

• Kleie 12 %
• Keim 2 %
• Endosperm 82 %

Wheat grains can be used as a raw material like corn, but usually the starch manufacturer can use already prepared flour from a flour mill. The composition of the wheat grain can be as follows (in percent by weight):

• bran 12%
• germ 2%
• endosperm 82%

The number of parts by weight of flour made from 100 parts of wheat is called the extraction rate. A flour extraction is between 73 and 77%, resulting in an average mill feed production of around 25%. It is evident that the mill feed contains, in addition to the bran, a significant proportion of the starchy endosperm.

• Feuchtigkeitsgehalt: 13,5 %
• Gesamtproteingehalt: 13 %
• Fasergehalt: 1,0 %
• Aschegehalt: 0,75 %.

A typical flour composition on a dry matter basis may look like this (in percent by weight):

• Moisture content: 13.5%
• Total protein content: 13%
• Fiber content: 1.0%
• Ash content: 0.75%.

Amounts can range from 1% to 20% of the declared value. The flour used is generally fit for human consumption and is ground to a specific grain size distribution. Suspension processes (beating processes) are more industry-friendly and enable closed, continuous handling. Several variants have been practiced over time, but the Scandinavian method is by far the most elegant and efficient.

The Scandinavian process is based on wheat flour as a raw material and is designed in such a way that even weak (soft) Scandinavian wheat, which is otherwise difficult to process, can be processed and still yield a vital gluten with excellent properties. The Scandinavian process also works well with whole fresh and unconditioned flour, minimizing the need for storage capacity. The flour is conveyed pneumatically from the intermediate silos into a storage hopper equipped with devices for separating air and flour. The control system continuously releases the flour into a stream of warm water. Water and flour are mixed in-line and the resulting suspension is homogenized in a high-speed in-line disintegrator. As indicated, MCA treatment can be carried out at this stage, in which the water and/or suspension is treated with MCA as described herein.

• • Stärke - schwere Phase
• • Gluten (oder Protein) - mittlere Phase
• • Pentosane - leichte Phase.

The homogenized suspension can then be separated immediately. As indicated, the MCA treatment can occur before this separation and/or during this separation. The suspension can be separated into the following fractions using a three-phase decanter (tricanter):

• • Strength - heavy phase
• • Gluten (or protein) - middle phase
• • Pentosans - light phase.

• • Typ-A-Stärke - schwere Phase
• • Typ-B-Stärke und Gluten (oder Protein) - mittlere Phase
• • Typ-C-Stärke und Pentosane - leichte Phase

Or the homogenized suspension can then be immediately separated into the following fractions using a three-phase decanter (tricanter):

• • Type A starch - heavy phase
• • Type B starch and gluten (or protein) - middle phase
• • Type C starch and pentosans - light phase

As already mentioned, an MCA treatment can be carried out before this separation and/or during the separation. The "starch" fraction is the heavy phase, containing most of the A starch. It is repulped and refined - similar to starches of other origins. The 'Pentosan' fraction is the light phase of the tricanter - and can contain various mucilages. It can be mixed with other by-products and used as wet food. The wet food can be dried, mixed with bran, or sold as such. The 'gluten' fraction is the complex middle phase. It contains gluten, fiber, solubles, B starch and some A starch. After the gluten has matured, these components are broken down into sub-fractions. Regarding gluten maturation, the stream is treated in a maturation reactor before separating the gluten fraction. The reactor is specially designed for the maturation of gluten. During maturation, the "gluten matrix" of the wheat flour is softened and the bound starch granules are released. Glutenin and gliadin proteins can now begin to form long molecular chains, ie gluten formation can take place. As for gluten agglomeration and recovery, the gluten maturation step is followed by a treatment in gluten agglomerators. In the agglomerators, the matured gluten is formed into lumps composed of glutenin and gliadin. The lumps of gluten are strained out and placed on curved git ter washed. This washing step can optionally include an MCA treatment as described herein. The wet gluten is dewatered and dried on screw presses. The gluten retains its vital properties through gentle drying in hot air in a ring dryer. After in-line grinding and classification, the product exits the dryer ready for packaging and sale as vital gluten.

When B starch is obtained, the residual fraction is separated in hydrocyclones after the gluten has been extracted. 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 in the overflow.

The A-starch obtained with the underflow can be concentrated and combined with the A-starch main stream. The B starch can be extracted from the overflow using special extraction cyclones and dewatered using a decanter. The B starch can be hot air dried in a ring dryer or drum dried and used as a pregelatinized starch. As for solubles, a clarifier can remove the last bit of starch from the overflow, leaving essentially solubles and water. The treated overflow leaves the factory as wastewater, which is disposed of by land application or biogas digestion. The waste water can optionally receive an MCA treatment.

In A-starch refining, the starch is purified by washing it with fresh, clean water. This washing step may include an MCA treatment as described herein. With hydrocyclones (a separation step) it is possible to reduce fibers and solubles, including soluble proteins, to a low level with a minimum of fresh water. To save water, the washing process is carried out in countercurrent, i. H. the incoming fresh water is used for the very last step and the overflow is reused for the dilution of the previous step, etc. This separation step may be MCA treated and/or the overflow may be MCA treated.

By using multi-stage hydrocyclones, soluble materials and fine cellular debris can be removed in a water-saving process. The refined starch milk contains almost 100% pure starch suspended in pure water.

When dewatering A starch, the cleaned A starch milk is fed into a peeler centrifuge for dewatering. This separation step may include an MCA treatment. The filtrate from the peeler is returned to the process. The dewatered starch is peeled off in batches and drained by gravity into the wet starch bunker.

During A-starch drying, the A-starch is conveyed from the wet starch bunker via a dosing screw into a rapid dryer and dried with hot air. The intake air temperature can be moderate. The dried starch is pneumatically conveyed into a starch silo, where it is screened and bagged. The moisture content of the starch after drying can normally be 12-13% by weight. The starch can then be sieved on a fine sieve to remove deposits that have built up in augers and the like. The strength can be optionally modified, e.g. B. using a three-stage wet modification.

Starch sweeteners are a major outlet for starches, including wheat starch, and in many plants the starch is not dried at all. Instead, the refined A starch suspension is processed into starch syrups. Glucose is particularly important in wheat starch. Basic and typical operating units are: CONDENSING. The refined A starch suspension is adjusted to a specific pH value and enzymes are added. The prepared suspension is heated with direct steam in a steam jet. Liquefaction is usually 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 through hydrolysis. A low DE hydrolyzate is formed and at this point the starch has been converted to a maltodextrin. (DE = dextrose equivalent, German: dextrose equivalent). SUGARIFICATION. The pH and temperature of the low DE hydrolyzate are readjusted and new enzymes are added to produce glucose with a higher DE. Depending on the enzymes added and the process used, glucose can be produced in different compositions - even products approaching pure dextrose. Cross-flow membrane filtration of the hydrolyzate can be performed. Diafiltration can recover glucose from the filter residue, leaving a protein-rich sludge that can be disposed of as animal feed. The glucose hydrolyzate is heated and treated with activated charcoal to remove impurities and color bodies, and then filtered. The glucose hydrolyzate is demineralized with ion exchange resins in a "carousel" arrangement. Cation resins remove various ions such as sodium, calcium, trace amounts of iron and some amino acids. Anion resins remove ions such as chloride, sulfate, 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 to be filled into drums or transported in tankers. By varying the processes, a number of commercial products can be made, and the pure dextrose syrups can even form the basis for further processing into high fructose syrups, using sophisticated techniques such as enzymatic isomerization and chromatography.

11 Figure 12 shows another example of the process in flow chart form showing the preparation of a starch suspension, wherein an MCA treatment (as described herein) can be used in each of these process steps and in particular immediately before and/or during the separation step(s).

12 Figure 12 shows another example of the process in flow chart form showing the further processing of the starch, where an MCA treatment (as described herein) can be used in any of these process steps and in particular immediately before, during or after the starch suspension step.

13 Figure 12 shows another example of a process in flow chart form showing the manufacture of sweeteners from starch using MCA treatment (as described herein) in each of these process steps and particularly immediately before and/or during the separation step(s). can.

14 Figure 12 shows another example of a process in flow chart form showing the production of wheat starch, wherein an MCA treatment (as described herein) is included in each of these process steps and in particular immediately before and/or during the dough mixing step, the washing and sieving step, the gluten (or protein) washing step, sieving and/or centrifugation and cyclone separation step(s).

15 shows another example of a process in the form of a flow chart showing the production of potato starch, with an MCA treatment (as described herein) in each of these process steps and in particular immediately before and / or during the step (steps) of potato washing, sieving , the filtration and redispersion in water and/or the dewatering step of the dewatering steps).

The methods of the present invention may provide one or more beneficial results. These one or more beneficial results will be more apparent when the process of the present invention is compared to a process that is otherwise identical except that the MCA treatment is omitted entirely (and no other biocide is used) or the MCA - treatment (as described herein) before and during the first and second separation step is omitted as described herein. This comparison described here is sometimes referred to as "without monochloramine" or "without MCA" or "due to MCA treatment".

An example of a potential benefit is that the process results in reduced chemical oxygen demand (COD) in a wastewater stream that does not contain starch or a fraction thereof. The effluent stream may refer to the by-product after performing one or more stages of the process of the present invention, and while this effluent stream may be recycled, at least a portion may ultimately be removed or diverted. The effluent stream, which is a by-product, originates from any washing and/or cleaning steps and/or from the formation of the wetting of the processed produce and/or from water or juice from the starting agricultural produce. The COD reduction may be at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a potential advantage of the present invention is that the wet product (e.g., a suspension of ground wheat and water) is a suspension that has a lower viscosity due to the MCA treatment. The viscosity can be reduced by at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. by 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a possible benefit of the present invention is that the wet product (e.g., a suspension of ground wheat and water) is a suspension that is oxidized due to the MCA treatment. The reduction can be at least 1%, at least 5%, at least 10% or at least 20% amount, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a potential benefit of the present invention is when the gluten (or protein) is optionally recovered and the process requires fewer alkaline additions to maintain a pH within 10% of the gluten isoelectric point due to the MCA treatment . The reduction may additionally be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a potential benefit of the present invention is that starch yield is increased compared to when no MCA treatment is used. The increase (by weight) may be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another possible advantage of the present invention is that the addition of xylanases and/or cellulases for viscosity reduction is reduced or avoided altogether. The reduction may additionally be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a potential benefit of the present invention is the reduction in mineral deposits. This reduction can be observed especially when mineral deposits occur together with the formation of a biofilm. The reduction may be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a possible benefit of the present invention is that the MCA treatment removes biofilms or prevents the formation of biofilms. The improvement in biofilm removal may be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a potential benefit of the present invention is an improvement in gluten agglomeration and improved drainage compared to when no MCA treatment is used. Wet vital gluten can enter a dewatering funnel of a press. The shaking allows free moisture to drain from the screen sides and bottom of the hopper. A conical auger can then press the gluten against a perforated grate, forcing the water out of the gluten and through the grate before being discharged onto an angled drainage grate. This drainage grid removes excess surface water before the gluten is directed into the dryer feed system. With faster dewatering, less or no washing water is required at this stage, and the pressure in the nozzles increases before the gluten enters the dryer. Ultimately, it is a gain in gluten yield. The increase in gluten agglomeration may be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above). The increase in drainage may be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a possible advantage of the present invention is that the gluten with the optional recovery has a higher number of disulfide bonds than when no MCA treatment is used. The increased number can be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a possible advantage of the present invention is that when the gluten is optionally recovered, the gluten has a higher protein content than when no MCA treatment is used. The increased content can be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on quantity described comparison).

Another example of a potential benefit of the present invention is that any contamination in the process, at least due to the formation of a biofilm, is reduced by the MCA treatment compared to when no MCA treatment is used. This reduction may be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on the comparison described above).

Another example of a possible benefit of the present invention is that the yield of fermentables (starch, fibers and preferably non-type A starches) compared to when MCA treatment is used is increased. The increase can be at least 1%, at least 5%, at least 10% or at least 20%, e.g. B. 1% to 20% or 5% to 20% (based on described comparison).

Optionally, in the methods of the present invention, microbial activity can be controlled at all points in the process so that CFU/g is maintained (i.e., microbial activity does not increase) or reduced by at least 1 log, or at least 2 logs (e.g., .a 1 to 2 log reduction in microbial activity). The reduction may be based on a comparison between the use of MCA treatments according to the present invention and no MCA treatment as described herein.

In the present invention, the microbial lactic acid production can be below 1.5 g/l. This amount can be an average value (over a wet separation phase or several or all together and averaged) and determined after each wet separation phase if desired. This amount of microbial lactic acid is based on one or more measurements of the processed agricultural product, for example after a separation step. This amount of microbial lactic acid formation may be of particular importance in relation to the extraction of starch from wheat.

The monochloramine treatments of the present invention can reduce or prevent pH decreases, increases in lactic acid concentration, or both, which can adversely affect wet product separation and/or pressability or cause other problems if uncontrolled.

A 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.

In addition, as a potable, approved material, the monochloramine can be dosed non-topically or topically, or both, expanding the possible points of addition of the treating agent within the starch extraction system.

The monochloramine may 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 combination thereof and/or it may be used to treat any process water , during and/or after contact with the starting agricultural product or a fraction thereof.

Monochloramine can be added in the form of water dilution, which can facilitate its introduction into a variety of aqueous process streams, masses and materials at various points in a starch extraction system.

In addition, chloramine does not have a distinct chlorine odor and therefore does not adversely affect taste or other sensory properties (unlike e.g. chlorine treatments) and is therefore more suitable for food processing.

The method for extracting starch and/or protein from a starting agricultural product can include a dosage of a starch extraction system (or protein extraction process) with a total dosage (combined dosages, all addition points) of from about 1 g to about 1000 g of 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 10g to about 300g monochloramine, or from about 20g to about 300g monochloramine, or from about 30g to about 300g monochloramine, or from about 40g to about 300g monochloramine, or from sth a 50g to about 300g of monochloramine, or other amounts, per tonne (2000 pounds) of starting agricultural product processed in the starch and/or protein extraction processes. The dosage can be constant or vary within these ranges during production. The amount of monochloramine (and/or the desired MCA level) may be an average amount of monochloramine based on a 24-hour period or some other time period. Treatment ranges given are monochloramine based. Other chloramines besides monochloramine can also be used.

The monochloramine can be in 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 ppm 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 in other ranges.

For purposes of the present invention, the MCA treatment can optionally be a chloramine treatment agent that can be used and that comprises, consists essentially of, or consists of at least one chloramine. The / chloramine (s) can be z. B. be monochloramine (MCA) (NH ₂ Cl), dichloramine (DCA) or a combination thereof. A majority (by weight) of the chloramine may 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 chloramine present). For purposes of the present invention, unless otherwise specified, the term "MCA" treatment includes chloramine(s) as specified herein.

The monochloramine treatment can be carried out in any suitable manner at any addition point of the starch extraction process that is used. The treatment can be continuous, substantially continuous, intermittent, cyclic, batch, or a combination thereof. For purposes of the present invention, 'nearly continuously' means that the dosing of MCA into the produce, or part or fraction thereof, occurs at least 75% of the time that the material is being processed through the treatment dosing point. For example, if the process is run for one hour, MCA will be dosed for at least 45 minutes during that hour. For purposes of the present invention, 'non-continuous' means that the dosing of MCA into the produce, or a portion or fraction thereof, is not continuous on a time basis. For example, if the process is run for an hour, the dosing of MCA will not occur during 60 minutes, but in less than 60 minutes of that run. Discontinuous dosing may involve one or more dosing of the material at intermittent times. Thus, the MCA treatment can be interrupted one or more times during the performance of the process in order to extract starch or a fraction thereof.

The MCA treatment and dosing may be the same concentration and/or dosing level, or different if there is more than one dosing point in the process.

The treatment can be performed at one or more stages or at multiple points in a starch and/or protein extraction process. In a processing plant, the treatment can be carried out in a vessel through which the processed material flows. The monochloramine can be added directly to the vessel or introduced indirectly via a process stream which is then sent to the vessel, or combinations thereof. The treatment can be applied in-line to a flowing process stream or mass without the need for an attendant residence time in a process vessel. A process vessel in a starch and/or protein extraction process in which the treatment may be applied is a holding tank, washer, grater, slicer, feed line, mixer, storage vessel and/or other process vessel or any combination from it.

The monochloramine treatment(s) can be applied directly to the external surfaces of the raw produce, such as by topical application of a treatment solution containing monochloramine. The treatment(s) can be carried out by pretreating process water or other process fluid with the monochloramine before it is mixed with at least one raw agricultural product, a component thereof, a fraction thereof or another medium in which the raw agricultural product and/or or the component thereof contained, dispersed or mixed is combined.

The controlled microorganisms can be bacteria, fungi, yeast 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 monochloramine treatment can be predominantly, essentially or entirely bacterial. The bacteria that can be controlled can be classical aerobic bacteria such as Leuconostoc mesenteroides, Lactobalillus, Coccus or other types of bacteria, or any combination thereof. Thermophilic microorganisms can be controlled with monochloramine treatment. The thermophilic microorganisms that can be controlled are Bacillus, Thermos and Clostridia species or other species or any combination thereof.

In the present invention, the starch, gluten, treated process water, fluid, juice, syrup, fiber, pulp, feed lines and/or other materials have very low bacterial counts. The bacteria can be controlled so that the bacterial count does not increase or the bacterial count is increased. Compared to a process that does not use MCA treatment in the manner described herein, or does not use it at all, or does not use a biocide, the bacterial count may actually decrease, for example by at least one log or at least two logs (e.g .a decrease of 1 log to 2 log).

The monochloramine or other chloramine can be obtained from any suitable source. The monochloramine can be used as a stock solution, e.g. in aqueous, dilute form, which can be introduced into process water and/or an aqueous medium containing sugary plant material or sugary 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, OXAMIN 6150, BUSPERSE 2454, BUSAN 1215 and BUCKMAN 1250 available from Buckman Laboratories International, Inc. of Memphis, Tennessee can be used as precursors for the formation of monochloramine. The monochloramine can be prepared by any suitable method. For example, monochloramine can be prepared by any of the methods described in U.S. Patent Nos. 4,038,372, 4,789,539, 6,222,071, 7,045,659 and 7,070,751 are described, which are incorporated herein in their entirety. 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 oxidizing agent. The monochloramine can be formed by reacting a dilute ammonia solution with sodium hypochlorite, calcium hypochlorite, or another source of hypochlorite, or any combination thereof. Monochloramine can be prepared by adding a solution of ammonia and sodium hypochlorite to dilution water to achieve a 1 to 1 molar ratio between ammonia and sodium hypochlorite. For example, monochloramine can be made by mixing about 1 fluid volume of OXAMIN 6150 with about 2.3 to 3 fluid volumes of bleach. Commercial bleaches may contain concentrations of sodium hypochlorite as high as 18.0% by weight sodium hypochlorite, e.g. about 14-18% by weight NaOCl, or other concentrations. The monochloramine can be formed by reacting at least one ammonium salt with sodium hypochlorite or another source of hypochlorite. The ammonium salt can be, for example, ammonium bromide, ammonium sulfate, ammonium hydroxide, ammonium chloride, or a combination thereof. Monochloramine can be prepared by reacting the ammonium salt with chlorine in a 1 to 1 molar ratio. Monochloramine can be produced on-site at a sugar factory by such reactions and used immediately or stored prior to use. Monochloramine can be manufactured off-site and transported for on-site use.

For the on-site production of monochloramine, a method and apparatus can be used to mix at least two reactants or components, such as dilute ammonia solution and sodium hypochlorite, to form the desired reaction product. The apparatus may include preparatory equipment for a conditioning unit. The apparatus may comprise a reactor, reactor system, generator, small scale generator, vessel, in-line mixer or the like. The method and device can be useful in controlling reactions that may be inherently hazardous, for example when mixing the components has the potential to create hazardous compounds or components. Precautions can be taken to ensure that the molar ratio of each reactant is accurately metered, as well as the addition of make-up water if used for the reaction. For example, the method and apparatus can be used to mix an ammonia-containing chemical (e.g., ammonia) and a hypochlorite-containing chemical (e.g., hypochlorite), which is inherently hazardous. The mixing of a chemical containing ammonia and a chemical containing hypochlorite can be carefully controlled to avoid the formation of hazardous compounds such as dichloramine, trichloramine and chlorine gas.

The equipment used to mix the at least two reactants or components, such as dilute ammonia solution and sodium hypochlorite, to form monochloramine may optionally include an automatic control mechanism. The control mechanism may relate one or more process control parameters to a monitored reaction condition, such as temperature. Optionally, a differential temperature method can be used to control an exothermic or endothermic chemical reaction. The chemical reaction can be an exothermic reaction and the temperature difference can be a temperature rise. The chemical reaction can be an endothermic reaction, and the temperature difference is a drop in temperature. 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. include. 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 depending on the temperature difference. The second reactant can be flowed 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 taken just as the reactants are combined, or at another time, if desired. The second reading used to determine the temperature difference may be the time at which the maximum increase or decrease in temperature from the reaction occurs (e.g., the maximum increase from the exothermic reaction or the maximum decrease from the endothermic reaction, depending on the case). This temperature difference can be used to determine and control the reaction, to ensure that the reaction and reaction product are the desired reaction product (e.g., monochloramine) and/or to ensure that the reaction is taking place in an efficient or correct manner expires. The device can be set up to produce any amount of monochloramine, including but not limited to 20 pounds or more monochloramine per day or less than that amount.

As indicated, treatment with monochloramine can be performed in the indicated process flow, as in 1 illustrated but not limited to occur at one or more points of addition within the system, e.g. B. at the points or in the phases that are marked with "MCA" in the figures and/or immediately before these points and/or immediately after these points. Preferred points of addition are those which allow monochloramine to be added in a liquid medium such as in aqueous form, e.g. B. in the form of a water dilution, is added to the agricultural product or a fraction thereof, a medium containing the agricultural product or an extract and / or one or more other parts thereof, or with other process materials or equipment or with any combination of these, and/or other addition points.

The treatment of the agricultural produce or the corresponding process waters with monochloramine can be carried out continuously, substantially continuously, intermittently, cyclically, in batches or in any combination thereof. A treatment can be repeated any number of times, and treatments can be separated by constant or variable periods of time. The rate of addition of monochloramine and/or precursors can be constant or variable. Monochloramine can be applied topically, nontopically, or both to provide microbiological control. Monochloramine can be added to the starchy materials (or proteinaceous materials) or the process water in any way, e.g. by pouring, by nozzle, by spray, by nebulization, by curtain, by weir, by fountain, by percolation, by mixing, by injection, or any combination thereof. For topical treatment, monochloramine in aqueous form can be sprayed onto the raw material of the produce. The monochloramine can be added in aqueous, diluted form to the process water used in the production process, which comes into contact or is brought into contact with the agricultural product and/or the component made from it.

The agricultural produce or the process water can be treated for any period of time. For example, 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 can be varied depending on one or a combination of various process factors.

Optionally, one or more other non-MCA or non-chloramine biocides may be used in addition to the MCA treatment described herein.

Optionally, in any of the methods of the present invention, no biocide other than the chloramine (e.g., monochloramine) may be used at any stage.

When another biocide is used in addition to a chloramine in any of the methods of the present invention, the chloramine (e.g., monochloramine) is the predominant biocide in terms of dosage level (e.g., at least 60% by weight, 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 in each phase chloramine or MCA).

Optionally, no agent (e.g., a chemical compound or agent) to potentiate the chloramine or monochloramine can be added in any of the methods of the present invention.

1. 1. Die vorliegende Erfindung betrifft ein Verfahren zum Extrahieren von Stärke oder Protein oder beidem aus einem landwirtschaftlichen Erzeugnis, wobei das Verfahren umfasst: Erhalten eines verarbeiteten Erzeugnisses, welches ein landwirtschaftliches Anfangserzeugnis ist, das gemahlen, gerieben, zerdrückt, gewürfelt, zerkleinert oder eine beliebige Kombination daraus wird, Durchführen eines oder mehrerer Trennschritte an dem verarbeiteten Erzeugnis oder einer Fraktion davon, um mindestens einen ersten nassen Feststoff zu erhalten, der Stärke oder Protein oder beides umfasst, und Trocknen des ersten nassen Feststoffs, um einen getrockneten Feststoff zu erhalten, der trockene Stärke oder trockenes Protein oder beides umfasst, wobei das Verfahren an einem Punkt unmittelbar vor dem Durchführen und/oder während eines ersten des einen oder der mehreren Trennschritte ferner ein Behandeln des verarbeiteten Erzeugnisses oder einer Zufuhrleitung (von Zufuhrleitungen) oder von beidem mit Monochloramin umfasst.
2. 2. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren an einem Punkt unmittelbar vor dem Durchführen und/oder während eines zweiten des einen oder der mehreren Trennschritte ferner ein Behandeln des verarbeiteten Erzeugnisses oder der Zufuhrleitung(en) oder von beidem mit Monochloramin umfasst.
3. 3. Die vorliegende Erfindung betrifft zudem oder alternativ ein Verfahren zum Extrahieren von Stärke oder Protein oder beidem aus einem landwirtschaftlichen Erzeugnis, wobei das Verfahren umfasst:
   • Verarbeiten eines landwirtschaftlichen Anfangserzeugnisses, um ein verarbeitetes Erzeugnis zu erhalten, das gemahlen, gerieben, zerkleinert oder eine beliebige Kombination daraus wird,
   • Benetzen des verarbeiteten Erzeugnisses, um ein nasses Erzeugnis zu erhalten,
   • Durchführen eines oder mehrerer Trennschritte an dem nassen Erzeugnis oder einer Fraktion davon, um mindestens einen ersten nassen Feststoff zu erhalten, der Stärke oder Protein oder beides umfasst; und
   • Trocknen des ersten nassen Feststoffs, um einen getrockneten Feststoff zu erhalten, der Stärke oder Protein oder beides umfasst, und
   • wobei das Verfahren nach dem Benetzen und vor dem Durchführen und/oder während eines ersten des einen oder der mehreren Trennschritte ferner ein Behandeln des nassen Erzeugnisses (und/oder der Zufuhrleitung(en)) mit Monochloramin umfasst,
   • wobei das Behandeln eine nicht kontinuierliche, kontinuierliche oder nahezu kontinuierliche Dosierung des Monochloramins (MCA) umfasst, um eine MCA-Konzentration in einer Menge zwischen etwa 50 g und etwa 800 g MCA pro 1 Tonne (2.000Pfund) landwirtschaftlichen Anfangserzeugnisses bereitzustellen; und wobei das Behandeln eine wässrige Monochloraminlösung umfasst, die zwischen etwa 0,1 Gew.-% und etwa 2 Gew.-% Monochloramin enthält.
4. 4. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das landwirtschaftliche Erzeugnis Weizen, Kartoffeln, Mais, Cassava, Tapioka, Reis, Sorghum, Gerste, Sago oder Maniok oder eine Pflanze aus der Familie der Hülsenfrüchte oder eine beliebige Kombination daraus ist.
5. 5. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Benetzen ein Zugeben von zumindest Wasser zu dem verarbeiteten Erzeugnis umfasst, um eine Suspension zu bilden.
6. 6. Verfahren einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Benetzen ein Behandeln des Wassers mit Monochloramin vor, während und/oder nach dem Zugeben von Wasser zu dem verarbeiteten Erzeugnis umfasst.
7. 7. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei der eine oder die mehreren Trennschritte ein Nutzen mindestens einer Zentrifuge, mindestens eines Dekanters (z. B. eines 2-Phasen-Dekanters oder 3-Phasen-Dekanters), mindestens eines Trenntanks, mindestens eines Siebs (z. B. eines Bogensiebs), mindestens eines Gitters oder mindestens eines Hydrozyklons oder einer beliebigen Kombination daraus umfasst.
8. 8. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei der eine oder die mehreren Trennschritte mindestens einen ersten Fest-flüssig-Trennschritt und einen zweiten Fest-flüssig-Trennschritt umfassen, wobei mindestens ein Teil der Flüssigkeit, die in dem ersten Fest-flüssig-Trennschritt getrennt wird, durch den zweiten Fest-flüssig-Trennschritt verarbeitet wird und vor und/oder während sowohl des ersten Fest-flüssig-Trennschritts als auch des zweiten Fest-flüssig-Trennschritts das Behandeln mit Monochloramin stattfindet.
9. 9. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren zu einem reduzierten chemischen Sauerstoffbedarf in dem Prozesswasser führt, das sich aus dem Verfahren ergibt (z. B. ein oder mehrere Abflussströme, die keine Fraktionen von Erzeugnissen enthalten, wie etwa Stärke, Protein und/oder Fasern).
10. 10. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei der Stärkeertrag oder Proteinertrag oder beides im Vergleich zu dem gleichen Verfahren ohne Monochloramin erhöht ist.
11. 11. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln mit Monochloramin mehrere Dosierungspunkte im Verlauf des gesamten Verfahrens umfasst, sodass die MCA-Konzentration in Bezug auf einen beliebigen Punkt von dem nassen Erzeugnis bis vor dem Erhalt des getrockneten Feststoffs aufrechterhalten wird.
12. 12. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren ferner ein Nutzen mehrerer Tanks zum Halten von Flüssigkeit umfasst, die vorwiegend Wasser aufweist, wobei die Flüssigkeit Prozesswasser, Pulpepresswasser, Waschwasser oder eine beliebige Kombination daraus umfasst, und wobei die mehreren Tanks Zufuhrleitungen zu und/oder von jedem der mehreren Tanks umfassen, und wobei die Flüssigkeit die MCA-Konzentration in den mehreren Tanks und in den Zufuhrleitungen aufweist.
13. 13. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln mit dem Monochloramin innerhalb von 20 Minuten nach Bilden des verarbeiteten Erzeugnisses stattfindet.
14. 14. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln mit dem Monochloramin innerhalb von 1 Minute nach Bilden des verarbeiteten Erzeugnisses stattfindet.
15. 15. Die vorliegende Erfindung betrifft zudem oder alternativ ein Verfahren zum Extrahieren von Stärke aus Weizen, wobei das Verfahren umfasst:
    • Mahlen des Weizens, um gemahlenen Weizen zu erhalten,
    • Benetzen des gemahlenen Weizens, um ein nasses Erzeugnis zu erhalten,
    • Durchführen von mindestens zwei Nass-Trennschritten an dem nassen Erzeugnis oder an einer Fraktion davon basierend auf Gewicht, Größe oder beidem, wobei ein erster Nass-Trennschritt Typ-A-Stärken von mindestens Gluten (oder einem Protein) und einigen Nicht-Typ-A-Stärken in dem nassen Erzeugnis zumindest teilweise trennt und ein zweiter Nass-Trennschritt die Typ-A-Stärken von Komponenten von Nicht-Typ-A-Stärken in mindestens einer Fraktion des nassen Erzeugnisses zumindest teilweise trennt,
    • Trocknen mindestens der Typ-A-Stärken, um eine getrocknete Stärke zu erhalten, wobei das Verfahren nach dem Benetzen und vor dem Durchführen und/oder während eines ersten der zwei Nass-Trennschritte ferner ein Behandeln des nassen Erzeugnisses mit Monochloramin und unmittelbar vor und/oder während des zweiten Nass-Trennschrittes ein Behandeln der Fraktion mit Monochloramin umfasst,
    • wobei das Behandeln eine nicht kontinuierliche, kontinuierliche oder nahezu kontinuierliche Dosierung des Monochloramins (MCA) umfasst, um eine MCA-Konzentration in einer Menge zwischen etwa 50 g und etwa 800 g MCA pro 1 Tonne (2.000 Pfund) Weizen bereitzustellen; und wobei das Behandeln eine wässrige Monochloraminlösung umfasst, die zwischen etwa 0,1 Gew.-% und etwa 2 Gew.-% Monochloramin enthält.
16. 16. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei der erste Nass-Trennschritt mindestens eine Zentrifuge, mindestens einen Trenntank, mindestens einen Dekanter (z. B. einen 2-Phasen-Dekanter oder 3-Phasen-Dekanter), mindestens ein Sieb (z. B. ein Bogensieb), mindestens ein Gitter oder mindestens einen Hydrozyklon oder eine beliebige Kombination daraus umfasst.
17. 17. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei der zweite Nass-Trennschritt mindestens eine Zentrifuge, mindestens einen Trenntank, mindestens einen Dekanter (z. B. einen 2-Phasen-Dekanter oder 3-Phasen-Dekanter), mindestens ein Sieb (z. B. ein Bogensieb), mindestens ein Gitter oder mindestens einen Hydrozyklon oder eine beliebige Kombination daraus umfasst.
18. 18. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Benetzen ein Bilden einer Suspension aus gemahlenem Weizen und Wasser umfasst.
19. 19. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren ferner ein Fasersieben vor dem zweiten Nass-Trennschritt umfasst und das Behandeln nach dem Fasersieben und vor und/oder während des zweiten Nass-Trennschritts stattfindet.
20. 20. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei in keiner Phase ein Biozid außer dem Monochloramin zugegeben wird.
21. 21. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei kein Mittel zugegeben wird, um das Monochloramin zu verstärken.
22. 22. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das nasse Erzeugnis eine Suspension ist, die eine Viskosität hat, die aufgrund der MCA-Behandlung niedriger ist.
23. 23. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das nasse Erzeugnis eine Suspension ist, die aufgrund der MCA-Behandlung weniger oxidiert ist.
24. 24. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Gluten (oder ein Protein) gewonnen wird und wobei das Verfahren aufgrund der MCA-Behandlung (im Vergleich dazu, wenn keine MCA-Behandlung verwendet wird,) weniger alkalische Zusätze erfordert, um einen pH-Wert innerhalb von 10 % des isoelektrischen Punkts des Glutens (oder Proteins) aufrechtzuerhalten.
25. 25. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei eine mikrobielle Aktivität an allen Punkten in dem Prozess kontrolliert wird, sodass die KBE/g aufrechterhalten oder um mindestens 1 log reduziert wird.
26. 26. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren zu einem verringerten chemischen Sauerstoffbedarf in einem Abflussstrom führt, der keine Stärke, kein Protein oder keine Faser oder eine Fraktion davon enthält.
27. 27. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei in dem Verfahren eine mikrobielle Milchsäurebildung unter 1,5 g/l liegt.
28. 28. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei in dem Verfahren ein pH von etwa 5 bis etwa 7 in Bezug auf das nasse Erzeugnis oder nasse Fraktionen davon aufrechterhalten wird.
29. 29. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei ein Stärkeertrag (und/oder Proteinertrag) im Vergleich dazu, wenn keine MCA-Behandlung verwendet wird, erhöht ist.
30. 30. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei die Zugabe von Xylanasen und/oder Cellulasen zur Viskositätsreduzierung reduziert oder eliminiert wird.
31. 31. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei die Mineralienablagerung reduziert wird.
32. 32. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei die MCA-Behandlung Biofilme entfernt oder eine Biofilmbildung verhindert.
33. 33. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei eine verbesserte Glutenagglomeration und Entwässerung im Vergleich dazu, wenn keine MCA-Behandlung verwendet wird, erreicht wird.
34. 34. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Gluten gewonnen wird und wobei das Gluten im Vergleich dazu, wenn keine MCA-Behandlung verwendet wird, eine erhöhte Anzahl von Disulfidbindungen aufweist.
35. 35. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Gluten gewonnen wird und wobei das Gluten im Vergleich dazu, wenn keine MCA-Behandlung verwendet wird, eine erhöhte Menge Protein aufweist.
36. 36. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei eine Verunreinigung in dem Verfahren aufgrund von zumindest Biofilmbildung aufgrund der MCA-Behandlung Vergleich dazu, wenn keine MCA-Behandlung verwendet wird, reduziert wird.
37. 37. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren die Menge oder den Bedarf einer Zugabe alkalischer Mittel zur Aufrechterhaltung einer pH-Umgebung reduziert oder eliminiert.
38. 38. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei die Dosierung von Monochloramin in dem Verfahren mindestens 3 Dosierungspunkte umfasst.
39. 39. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei die Dosierung von Monochloramin in dem Verfahren mindestens 5 Dosierungspunkte umfasst.
40. 40. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei die Dosierung von Monochloramin in dem Verfahren mindestens 8 Dosierungspunkte umfasst.
41. 41. Verfahren einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln ein Behandeln des Wassers mit Monochloramin vor, während und/oder nach dem Zugeben von Wasser zu dem gemahlenen Weizen umfasst.
42. 42. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei der erste Nass-Trennschritt mindestens eine 3-Phasen-Dekanterzentrifuge und/oder einen Trenntank umfasst.
43. 43. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren mindestens drei separate Nass-Trennungen des nassen Erzeugnisses oder einer Fraktion davon unter Nutzung von Separatoren (z. B. 3-Phasen-Separatoren) umfasst, die sich an drei unterschiedlichen Punkten des Verfahrens befinden, und wobei das Verfahren ferner eine Dosierung des Monochloramins unmittelbar vor und/oder während jeder der mindestens drei Trennungen umfasst.
44. 44. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln mit Monochloramin mehrere Dosierungspunkte im Verlauf des gesamten Verfahrens umfasst, sodass die MCA-Konzentration in Bezug auf einen beliebigen Punkt von dem nassen Erzeugnis bis vor dem Erhalt der getrockneten Stärke aufrechterhalten wird.
45. 45. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln mit dem Monochloramin innerhalb von 20 Minuten nach Bilden des gemahlenen Weizens stattfindet.
46. 46. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Behandeln mit dem Monochloramin innerhalb von 20 Minuten nach Bilden des nassen Erzeugnisses stattfindet.
47. 47. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren ferner ein Nutzen mehrerer Tanks zum Halten von Flüssigkeit umfasst, die vorwiegend Wasser aufweist, wobei die Flüssigkeit Prozesswasser, Pulpepresswasser, Waschwasser oder eine beliebige Kombination daraus umfasst, und wobei die mehreren Tanks Zufuhrleitungen zu und/oder von jedem der mehreren Tanks umfassen, und wobei die Flüssigkeit die MCA-Konzentration in den mehreren Tanks und in den Zufuhrleitungen aufweist.
48. 48. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren ferner ein Umwandeln mindestens eines Teils der Stärke in Glukose oder Dextrin umfasst.
49. 49. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das Verfahren ferner ein Umwandeln mindestens eines Teils der Stärke in Glukose oder Dextrin und anschließend Durchführen einer Fermentation der Glukose oder des Dextrins zur Bildung eines oder mehrerer Bioerzeugnisse umfasst.
50. 50. Die vorliegende Erfindung betrifft zudem oder alternativ ein Verfahren zum Extrahieren von Stärke aus einem landwirtschaftlichen Erzeugnis, wobei das Verfahren umfasst: Erhalten eines verarbeiteten Erzeugnisses, welches ein landwirtschaftliches Anfangserzeugnis ist, das gemahlen, gerieben, zerdrückt, gewürfelt, zerkleinert oder eine beliebige Kombination daraus wird, Durchführen eines oder mehrerer Trennschritte an dem verarbeiteten Erzeugnis oder einer Fraktion davon, um mindestens einen ersten nassen Feststoff zu erhalten, der Stärke umfasst, und Trocknen des ersten nassen Feststoffs, um einen getrockneten Feststoff zu erhalten, der trockene Stärke umfasst, wobei das Verfahren an einem Punkt unmittelbar vor dem Durchführen und/oder während eines ersten des einen oder der mehreren Trennschritte ferner ein Behandeln des verarbeiteten Erzeugnisses mit Monochloramin umfasst und wobei das Verfahren die Menge oder den Bedarf einer Zugabe alkalischer Mittel zur Aufrechterhaltung einer pH-Umgebung reduziert oder eliminiert.
51. 51. Verfahren nach einer/m vorhergehenden oder folgenden Ausführungsform/Merkmal/Aspekt, wobei das verarbeitete Erzeugnis oder eine Fraktion davon einen maximalen Chloramin- oder MCA-Restgehalt von 10 ppm aufweist, bis das verarbeitete Erzeugnis oder eine Fraktion davon getrocknet oder enzymatischen oder mikrobiellen Behandlungen in einem oder mehreren Stärkeumwandlungsvorgängen unterzogen wird.

The present invention includes the following aspects/embodiments/features in any order and/or in any combination:

1. 1. The present invention relates to a method for extracting starch or protein or both from an agricultural product, the method comprising: obtaining a processed product which is a starting agricultural product which is ground, grated, crushed, diced, minced or any Combination thereof is, performing one or more separation steps on the processed product or a fraction thereof to obtain at least a first wet solid comprising starch or protein or both, and drying the first wet solid to obtain a dried solid which dry starch or dry protein or both, the method further comprising, at a point just prior to performing and/or during a first of the one or more separation steps, treating the processed product or a feed line(s) or both with monochlo includes ramin.
2. 2. The method of any preceding or following embodiment/feature/aspect, wherein the method further comprises, at a point immediately prior to performing and/or during a second of the one or more separating steps, treating the processed product or the feed line(s) or both with monochloramine.
3. 3. The present invention also or alternatively relates to a method for extracting starch or protein or both from an agricultural product, the method comprising:
   • Processing of an initial agricultural product to obtain a processed product that is ground, grated, crushed or any combination thereof,
   • wetting the processed product to obtain a wet product,
   • subjecting the wet product or a fraction thereof to one or more separation steps to obtain at least a first wet solid comprising starch or protein or both; and
   • drying the first wet solid to obtain a dried solid comprising starch or protein or both, and
   • the method further comprising, after wetting and before performing and/or during a first of the one or more separating steps, treating the wet product (and/or the feed line(s)) with monochloramine,
   • wherein the treating comprises intermittent, continuous, or near-continuous dosing of the monochloramine (MCA) to provide an MCA concentration in an amount between about 50 g and about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural product; and wherein the treating comprises an aqueous monochloramine solution containing between about 0.1% and about 2% by weight monochloramine.
4. 4. The method of any preceding or following embodiment/feature/aspect, wherein the agricultural product is wheat, potato, corn, cassava, tapioca, rice, sorghum, barley, sago or cassava, or a plant of the legume family, or any combination of it is.
5. 5. The method of any preceding or following embodiment/feature/aspect, wherein the wetting comprises adding at least water to the processed product to form a suspension.
6. 6. The method of any preceding or following embodiment/feature/aspect, wherein the wetting comprises treating the water with monochloramine before, during and/or after adding water to the processed product.
7. 7. The method of any preceding or following embodiment/feature/aspect, wherein the one or more separation steps include using at least one centrifuge, at least one decanter (e.g., a 2-phase decanter or 3-phase decanter) , minimum at least one separation tank, at least one screen (e.g. a curved screen), at least one grid or at least one hydrocyclone or any combination thereof.
8. 8. The method of any preceding or following embodiment/feature/aspect, wherein the one or more separation steps comprise at least a first solid-liquid separation step and a second solid-liquid separation step, wherein at least a portion of the liquid contained in is separated by the first solid-liquid separation step, is processed by the second solid-liquid separation step and treating with monochloramine takes place before and/or during both the first solid-liquid separation step and the second solid-liquid separation step.
9. 9. The method of any preceding or following embodiment/feature/aspect, wherein the method results in reduced chemical oxygen demand in the process water resulting from the method (e.g., one or more effluent streams that are not fractions of produce contain such as starch, protein and/or fiber).
10. 10. The method of any preceding or following embodiment/feature/aspect, wherein starch yield or protein yield or both is increased compared to the same method without monochloramine.
11. 11. The method of any preceding or following embodiment/feature/aspect, wherein the treating with monochloramine comprises multiple dosing points throughout the method such that the MCA concentration is relative to any point from the wet article to prior to obtaining the dried solid is maintained.
12. 12. The method of any preceding or following embodiment/feature/aspect, the method further comprising utilizing multiple tanks for holding liquor predominantly comprising water, the liquor comprising process water, pulp press water, wash water, or any combination thereof, and wherein the plurality of tanks includes supply lines to and/or from each of the plurality of tanks, and wherein the liquid has the MCA concentration in the plurality of tanks and in the supply lines.
13. 13. The method of any preceding or following embodiment/feature/aspect, wherein the treating with the monochloramine occurs within 20 minutes of forming the processed article.
14. 14. The method of any preceding or following embodiment/feature/aspect, wherein the treating with the monochloramine occurs within 1 minute of forming the processed article.
15. 15. The present invention also or alternatively relates to a method for extracting starch from wheat, the method comprising:
    • grinding the wheat to get milled wheat,
    • wetting the milled wheat to obtain a wet product,
    • performing at least two wet separation steps on the wet product or a fraction thereof based on weight, size, or both, wherein a first wet separation step removes Type A starches from at least gluten (or a protein) and some non-Type A starches - at least partially separating starches in the wet product and a second wet-separating step at least partially separating the type A starches from components of non-type A starches in at least a fraction of the wet product,
    • drying at least the Type A starches to obtain a dried starch, the method further comprising, after wetting and before performing and/or during a first of the two wet separation steps, treating the wet product with monochloramine and immediately before and/or or during the second wet separation step comprising treating the fraction with monochloramine,
    • wherein the treating comprises intermittent, continuous, or near-continuous dosing of the monochloramine (MCA) to provide an MCA concentration in an amount between about 50 grams and about 800 grams of MCA per 1 ton (2,000 pounds) of wheat; and wherein the treating comprises an aqueous monochloramine solution containing between about 0.1% and about 2% by weight monochloramine.
16. 16. The method of any preceding or following embodiment/feature/aspect, wherein the first wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter (e.g., a 2-phase decanter or 3-phase decanter ), at least one screen (e.g. a curved screen), at least one grid or at least one hydrocyclone or any combination thereof.
17. 17. The method of any preceding or following embodiment/feature/aspect, wherein the second wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter (e.g., a 2-phase decanter or 3-phase decanter ), at least one screen (e.g. a curved screen), at least one grid or at least one hydrocyclone or any combination thereof.
18. 18. The method of any preceding or following embodiment/feature/aspect, wherein the wetting comprises forming a suspension of ground wheat and water.
19. 19. The method of any preceding or following embodiment/feature/aspect, the method further comprising fiber screening prior to the second wet separation step, and the treating occurs after the fiber screening and before and/or during the second wet separation step.
20. 20. The method of any preceding or following embodiment/feature/aspect wherein no biocide other than the monochloramine is added at any stage.
21. 21. The method of any preceding or following embodiment/feature/aspect wherein no agent is added to enhance the monochloramine.
22. 22. The method of any preceding or following embodiment/feature/aspect, wherein the wet product is a suspension having a viscosity that is lower due to the MCA treatment.
23. 23. The method of any preceding or following embodiment/feature/aspect, wherein the wet product is a suspension that is less oxidized due to the MCA treatment.
24. 24. The method of any preceding or following embodiment/feature/aspect, wherein the gluten (or a protein) is recovered and wherein the method reduces due to the MCA treatment (compared to when no MCA treatment is used). alkaline additives are required to maintain a pH within 10% of the gluten (or protein) isoelectric point.
25. 25. The method of any preceding or following embodiment/feature/aspect, wherein microbial activity is controlled at all points in the process such that the CFU/g is maintained or reduced by at least 1 log.
26. 26. The method of any preceding or following embodiment/feature/aspect, wherein the method results in reduced chemical oxygen demand in an effluent stream that does not contain starch, protein or fiber or a fraction thereof.
27. 27. The method of any preceding or following embodiment/feature/aspect, wherein in the method a microbial lactic acid formation is below 1.5 g/l.
28. 28. The method of any preceding or following embodiment/feature/aspect, wherein the method maintains a pH of from about 5 to about 7 with respect to the wet product or wet fractions thereof.
29. 29. The method of any preceding or following embodiment/feature/aspect, wherein a starch yield (and/or protein yield) is increased compared to when no MCA treatment is used.
30. 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. 31. The method of any preceding or following embodiment/feature/aspect, wherein mineral deposition is reduced.
32. 32. The method of any preceding or following embodiment/feature/aspect, wherein the MCA treatment removes biofilms or prevents biofilm formation.
33. 33. The method of any preceding or following embodiment/feature/aspect, wherein improved gluten agglomeration and dewatering is achieved compared to when no MCA treatment is used.
34. 34. The method of any preceding or following embodiment/feature/aspect, wherein the gluten is recovered and wherein the gluten has an increased number of disulfide bonds compared to when no MCA treatment is used.
35. 35. The method of any preceding or following embodiment/feature/aspect, wherein the gluten is recovered and wherein the gluten has an increased amount of protein compared to when no MCA treatment is used.
36. 36. The method of any preceding or following embodiment/feature/as spect, whereby contamination in the process due to at least biofilm formation due to the MCA treatment is reduced compared to when no MCA treatment is used.
37. 37. The method of any preceding or following embodiment/feature/aspect, wherein the method reduces or eliminates the amount or need for addition of alkaline agents to maintain a pH environment.
38. 38. The method of any preceding or following embodiment/feature/aspect, wherein the dosing of monochloramine in the method comprises at least 3 dosing points.
39. 39. The method of any preceding or following embodiment/feature/aspect, wherein the dosing of monochloramine in the method comprises at least 5 dosing points.
40. 40. The method of any preceding or following embodiment/feature/aspect, wherein the dosing of monochloramine in the method comprises at least 8 dosing points.
41. 41. The method of any preceding or following embodiment/feature/aspect, wherein the treating comprises treating the water with monochloramine before, during and/or after adding water to the ground wheat.
42. 42. The method of any preceding or following embodiment/feature/aspect, wherein the first wet separation step comprises at least one 3-phase decanter centrifuge and/or a separation tank.
43. 43. The method of any preceding or following embodiment/feature/aspect, wherein the method comprises at least three separate wet separations of the wet product or a fraction thereof utilizing separators (e.g. 3-phase separators) which are at three different points in the process, and the process further comprises dosing the monochloramine just before and/or during each of the at least three separations.
44. 44. The method of any preceding or following embodiment/feature/aspect, wherein the treating with monochloramine comprises multiple dosing points throughout the method such that the MCA concentration is relative to any point from the wet article to prior to obtaining the dried starch is maintained.
45. 45. The method of any preceding or following embodiment/feature/aspect, wherein the treating with the monochloramine occurs within 20 minutes of forming the ground wheat.
46. 46. The method of any preceding or following embodiment/feature/aspect, wherein the treating with the monochloramine occurs within 20 minutes of forming the wet article.
47. 47. The method of any preceding or following embodiment/feature/aspect, the method further comprising utilizing multiple tanks for holding liquor predominantly comprising water, the liquor comprising process water, pulp press water, wash water, or any combination thereof, and wherein the plurality of tanks includes supply lines to and/or from each of the plurality of tanks, and wherein the liquid has the MCA concentration in the plurality of tanks and in the supply lines.
48. 48. The method of any preceding or following embodiment/feature/aspect, the method further comprising converting at least a portion of the starch to glucose or dextrin.
49. 49. The method of any preceding or following embodiment/feature/aspect, the method further comprising converting at least a portion of the starch to glucose or dextrin and then subjecting the glucose or dextrin to fermentation to form one or more bioproducts.
50. 50. The present invention also or alternatively relates to a method for extracting starch from an agricultural product, the method comprising: obtaining a processed product which is a starting agricultural product which is ground, grated, crushed, diced, minced or any combination therefrom, performing one or more separation steps on the processed product or a fraction thereof to obtain at least a first wet solid comprising starch and drying the first wet solid to obtain a dried solid comprising dry starch, wherein the procedure at a point immediately prior to and/or during performance a first of the one or more separating steps further comprises treating the processed product with monochloramine and wherein the method reduces or eliminates the amount or need for addition of alkaline agents to maintain a pH environment.
51. 51. The method of any preceding or following embodiment/feature/aspect, wherein the processed product or fraction thereof has a maximum residual chloramine or MCA content of 10 ppm until the processed product or fraction thereof is dried or enzymatic or microbial undergoes treatments in one or more starch conversion operations.

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

Applicants expressly incorporate the entire contents of all cited references into this disclosure. In addition, when an amount, concentration or other value or parameter is given as either a range, a preferred range, or a list of upper preferred values and lower preferred values, it is to be understood as specifically disclosing all ranges resulting from a any pair of an upper range limit or preferred value and a lower range limit or preferred value, whether or not the ranges are disclosed separately. Where a range of numerical values is specified herein, unless otherwise specified, it includes the endpoints thereof and all integers and fractions within the range. It is not intended to limit the scope of the invention to the specific values given when defining a range.

Other embodiments of the present invention will be apparent to those skilled in the art upon review of the present specification and the practice of the present invention disclosed herein. It is intended that the present specification and examples be considered as exemplary only, with the true scope and spirit of the invention being indicated by the following claims and their equivalents.

QUOTES INCLUDED IN DESCRIPTION

This list of documents cited by the applicant was generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Patent Literature Cited

• US62/966700 [0001]
• US4038372 [0121]
• US4789539 [0121]
• US6222071 [0121]
• US7045659 [0121]
• US Pat. No. 7,070,751 [0121]

Claims (51)

A method of extracting starch or protein or both from an agricultural product, the method comprising: obtaining a processed product which is a starting agricultural product which is ground, grated, mashed, diced, minced or any combination thereof, subjecting the processed product or a fraction thereof to one or more separation steps to obtain at least a first wet solid comprising starch or protein or both, and drying the first wet solid to obtain a dried solid comprising dry starch or dry protein or both, the method further comprising, at a point immediately prior to performing and/or during a first of the one or more separation steps, treating the processed product or a feed line or both with monochloramine. procedure after claim 1 , the method further comprising, at a point just prior to performing and/or during a second of the one or more separation steps, treating the processed product or a feed line with monochloramine. A method of extracting starch or protein or both from an agricultural product, the method comprising: Processing of an initial agricultural product to obtain a processed product that is ground, grated, crushed or any combination thereof, wetting the processed product to obtain a wet product, subjecting the wet product or a fraction thereof to one or more separation steps to obtain at least a first wet solid comprising starch or protein or both; and drying the first wet solid to obtain a dried solid comprising starch or protein or both, and the method further comprising, after wetting and prior to performing and/or during a first of the one or more separating steps, treating the wet product with monochloramine, wherein the treating comprises intermittent, continuous, or near-continuous dosing of the monochloramine (MCA) to provide an MCA concentration in an amount between about 50 g and about 800 g MCA per 1 ton (2,000 pounds) of starting agricultural product; and wherein the treating comprises an aqueous monochloramine solution containing between about 0.1% and about 2% by weight monochloramine. A method according to any preceding claim, wherein the agricultural product is wheat, potato, corn, cassava, tapioca, rice, sorghum, barley, sago, cassava or a plant of the legume family, or any combination thereof. A method according to any preceding claim, wherein the wetting comprises adding at least water to the processed product to form a suspension. procedure after claim 5 wherein the wetting comprises treating the water with monochloramine before, during or after adding water to the processed product. The method of any preceding claim, wherein the one or more separating steps comprises utilizing at least one centrifuge, at least one decanter, at least one separation tank, at least one screen, at least one grid, or at least one hydrocyclone, or any combination thereof. A method according to any preceding claim, wherein the one or more separating steps comprise at least a first solid-liquid separating step and a second solid-liquid separating step, wherein at least a portion of the liquid separated in the first solid-liquid separating step is processed by the second solid-liquid separation step and treating with monochloramine takes place before and/or during both the first solid-liquid separation step and the second solid-liquid separation step. A method according to any preceding claim, wherein the method results in reduced chemical oxygen demand in an effluent stream which does not contain starch or a fraction thereof. A method according to any preceding claim wherein starch yield or protein yield or both is increased compared to the same method without monochloramine. A method according to any preceding claim, wherein the treatment with monochloramine comprises multiple dosing points throughout the process such that the MCA concentration is maintained at any point from the wet product to prior to receipt of the dried solid. A method according to any preceding claim, wherein the method further comprises utilizing a plurality of tanks for holding liquid predominantly comprising water, the liquid comprising process water, pulp press water, wash water or any combination thereof, and the plurality of tanks having supply lines to and/or from each of the plurality of tanks, and wherein the liquid comprises the MCA concentration in the plurality of tanks and in the supply lines. A method according to any preceding claim, wherein the treatment with the monochloramine occurs within 20 minutes of forming the processed article. A method according to any preceding claim, wherein the treatment with the monochloramine occurs within 1 minute of forming the processed article. A method of extracting starch from wheat, the method comprising: grinding the wheat to get milled wheat, wetting the milled wheat to obtain a wet product, performing at least two wet separation steps on the wet product or on a fraction thereof based on weight, size or both, wherein a first wet separation step includes Type A starches of at least gluten or protein and some non-Type A starches in at least partially separating the wet product and a second wet-separation step at least partially separating the Type A starches from components of non-Type A starches in at least a fraction of the wet product, drying at least type A starches to obtain a dried starch, wherein after wetting and before performing and/or during a first of the two wet separation steps, the method further comprises treating the wet product with monochloramine and immediately before and/or during the second wet separation step treating the fraction with monochloramine, wherein the treating comprises intermittent, continuous, or near-continuous dosing of the monochloramine (MCA) to provide an MCA concentration in an amount between about 50 grams and about 800 grams of MCA per 1 ton (2,000 pounds) of wheat; and wherein the treating comprises an aqueous monochloramine solution containing between about 0.1% and about 2% by weight monochloramine. procedure after claim 15 wherein the first wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter, at least one screen, at least one grid, or at least one hydrocyclone, or any combination thereof. procedure after claim 15 wherein the second wet separation step comprises at least one centrifuge, at least one separation tank, at least one decanter, at least one screen, at least one grid, or at least one hydrocyclone, or any combination thereof. procedure after claim 15 wherein the wetting comprises forming a suspension of ground wheat and water. procedure after claim 1 wherein the method further comprises fiber screening prior to the second wet separation step, and the treating occurs after the fiber screening and before and/or during the second wet separation step. A method according to any preceding claim wherein no biocide other than the monochloramine is added at any stage. A method according to any preceding claim wherein no agent is added to enhance the monochloramine. A method according to any preceding claim in which the wet product is a suspension which has a viscosity which is lower due to the MCA treatment. A method according to any preceding claim, wherein the wet product is a suspension which is less oxidized due to the MCA treatment. procedure after claim 15 wherein the gluten or other protein is recovered and wherein the process requires fewer alkaline additives to achieve a pH within 10% of the isoelectric point of the gluten or of the other protein. A method according to any preceding claim, wherein microbial activity is controlled at all points in the process such that the CFU/g is maintained or reduced by at least 1 log. A method according to any preceding claim, wherein the method results in reduced chemical oxygen demand in an effluent stream which does not contain starch or a fraction thereof. A method according to any preceding claim, wherein in the method a microbial lactic acid formation is below 1.5 g/l. A process according to any preceding claim, wherein a pH of from about 5 to about 7 is maintained in the process with respect to the wet product or wet fractions thereof. A method according to any preceding claim, wherein starch yield is increased compared to when no MCA treatment is used. A method according to any preceding claim wherein the addition of xylanases and/or cellulases for viscosity reduction is reduced or eliminated. A method according to any preceding claim, wherein the mineral deposit is reduced. A method according to any preceding claim, wherein the MCA treatment removes biofilms or prevents biofilm formation. procedure after claim 15 , achieving improved gluten agglomeration and drainage compared to when no MCA treatment is used. procedure after claim 15 wherein the gluten or other protein is recovered and wherein the gluten or other protein has an increased number of disulfide bonds compared to when no MCA treatment is used. procedure after claim 15 wherein the gluten or other protein is recovered and wherein the gluten or other protein has an increased amount of protein compared to when no MCA treatment is used. A method according to any preceding claim, wherein contamination in the method due to at least biofilm formation due to the MCA treatment is reduced compared to when no MCA treatment is used. A method according to any preceding claim, wherein the method reduces or eliminates the amount or need for addition of alkaline agents to maintain a pH environment. A method according to any preceding claim, wherein the dosing of monochloramine in the method comprises at least 3 dosing points. A method according to any preceding claim, wherein the dosing of monochloramine in the method comprises at least 5 dosing points. A method according to any preceding claim, wherein the dosing of monochloramine in the method comprises at least 8 dosing points. procedure after claim 15 wherein the treating comprises treating the water with monochloramine before, during and/or after adding water to the ground wheat. procedure after claim 15 wherein the first wet separation step comprises at least one 3-phase decanter centrifuge or at least one separation tank. procedure after claim 15 , the process comprising at least three separate wet separations of the wet product or a fraction thereof utilizing separators located at three different points in the process, and the process further comprising dosing the monochloramine immediately before and/or during each of the at least three separations. A method according to any preceding claim, wherein the treatment with monochloramine comprises multiple dosing points throughout the process such that the MCA concentration is maintained at any point from the wet product to prior to obtaining the dried starch. procedure after a claim 15 wherein the treatment with the monochloramine occurs within 20 minutes of forming the milled wheat. procedure after a claim 15 wherein the treatment with the monochloramine occurs within 20 minutes of forming the wet article. procedure after claim 15 , the method further comprising utilizing a plurality of tanks for holding liquid primarily comprising water, the liquid comprising process water, pulp press water, wash water or any combination thereof, and wherein the plurality of tanks have supply lines to and/or from each of the plurality of tanks include, and where the liq fluid has the MCA concentration in the multiple tanks and in the supply lines. A method according to any preceding claim, wherein the method further comprises converting at least a portion of the starch to glucose or dextrin. A method according to any preceding claim, wherein the method further comprises converting at least a portion of the starch to glucose or dextrin and then subjecting the glucose or dextrin to fermentation to form one or more bioproducts. A method of extracting starch or protein or both from an agricultural product, the method comprising: obtaining a processed product which is a starting agricultural product which is ground, grated, mashed, diced, minced or any combination thereof, subjecting the processed product or a fraction thereof to one or more separation steps to obtain at least a first wet solid comprising starch or protein or both, and drying the first wet solid to obtain a dried solid comprising dry starch or dry protein or both, the method further comprising, at a point just prior to performing and/or during a first of the one or more separating steps, treating the processed product with monochloramine and wherein the method controls the amount or need for addition of alkaline agents to maintain a pH environment reduced or eliminated. A process according to any preceding claim, wherein the processed product or a fraction thereof has a maximum residual chloramine or MCA content of 10ppm until the processed product or a fraction thereof is dried or subjected to enzymatic or microbial treatments in one or more starch conversion operations.

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