WO2018215965A1 - Procédés permettant de récupérer des produits à partir d'un moût de fermentation de maïs - Google Patents

Procédés permettant de récupérer des produits à partir d'un moût de fermentation de maïs Download PDF

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Publication number
WO2018215965A1
WO2018215965A1 PCT/IB2018/053688 IB2018053688W WO2018215965A1 WO 2018215965 A1 WO2018215965 A1 WO 2018215965A1 IB 2018053688 W IB2018053688 W IB 2018053688W WO 2018215965 A1 WO2018215965 A1 WO 2018215965A1
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WO
WIPO (PCT)
Prior art keywords
product
fiber rich
μπι
ethanol
fiber
Prior art date
Application number
PCT/IB2018/053688
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English (en)
Inventor
Jason Bootsma
Original Assignee
Flint Hills Resources, Lp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US15/604,507 external-priority patent/US10059966B2/en
Application filed by Flint Hills Resources, Lp filed Critical Flint Hills Resources, Lp
Priority to US16/616,503 priority Critical patent/US11286509B2/en
Publication of WO2018215965A1 publication Critical patent/WO2018215965A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12C—BEER; PREPARATION OF BEER BY FERMENTATION; PREPARATION OF MALT FOR MAKING BEER; PREPARATION OF HOPS FOR MAKING BEER
    • C12C11/00—Fermentation processes for beer
    • C12C11/11—Post fermentation treatments, e.g. carbonation, or concentration
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • Embodiments described generally relate to processes and systems for recovering products derived from ground corn. More particularly, such embodiments relate to processes and systems for recovering products from a corn fermentation mash.
  • Corn or maize is often used as a starch source to produce ethanol by fermentation.
  • Corn is traditionally ground by a hammer mill in ethanol production facilities.
  • Hammer milled corn has a very wide range of sizes and generally includes relatively large particle sizes.
  • the fermentation process produces a corn fermentation mash that includes a mixture of ethanol and multiple corn products. Ethanol is removed from the corn fermentation mash by distillation to produce a whole stillage that contains a mixture of corn products. Many of these corn products are too time consuming and/or costly to separate from the stillage and therefore are never recovered as separate products.
  • a process for recovering products from a fermentation mash can include processing a ground corn product to produce a fermentation mash that can include ethanol. At least a portion of the ethanol can be separated from the fermentation mash to produce a whole stillage. The whole stillage can be separated to produce a fiber rich product and a filtrate. The fiber rich product can be hydrolyzed to produce a saccharification mash. The saccharification mash can be processed to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a fermentation mash can include processing a ground corn product to produce a fermentation mash that can include ethanol. At least a portion of the ethanol can be separated from the fermentation mash to produce a whole stillage. The whole stillage can be separated with a fiber filter to produce a fiber rich product and a filtrate. The fiber rich product can be hydrolyzed to produce a saccharification mash. The saccharification mash can be processed to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a fermentation mash can include processing a ground corn product to produce a fermentation mash that can include ethanol. At least a portion of the ethanol can be separated from the fermentation mash to produce a whole stillage. The whole stillage can be separated to produce a fiber rich product and a filtrate.
  • the fiber rich product can have an ethanol potential of at least 90 gallons of ethanol per 1,000 kilograms of the fiber rich product.
  • Figure 1 depicts a schematic view of an illustrative system for recovering products derived from corn fermentation mash, according to one or more embodiments described.
  • Figure 2 depicts a schematic view of an illustrative system for producing ethanol from a fiber product recovered from a whole stillage, according to one or more embodiments described.
  • Figure 3 depicts a schematic view of another illustrative system for producing ethanol from a fiber product recovered from a whole stillage, according to one or more embodiments described.
  • Figure 4 is an optical microscope image of hammer milled corn (Comparative Example 1) at a magnification of lOx.
  • Figure 5 is an optical microscope image of hammer milled corn (Comparative Example
  • Figure 6 is an optical microscope image of roller milled corn (Comparative Example
  • Figure 7 is an optical microscope image of roller milled corn (Comparative Example 2) at a magnification of 200x.
  • Figure 8 is an optical microscope image of disk pulverized corn (Example 1) at a magnification of lOx.
  • Figure 9 is an optical microscope image of disk pulverized corn (Example 1) at a magnification of 200x.
  • Figure 10 is an optical microscope image of disk pulverized corn (Example 2) at a magnification of lOx.
  • Figure 11 is an optical microscope image of disk pulverized corn (Example 2) at a magnification of lOOx.
  • Figure 12 is an optical microscope image of disk fiberized corn (Example 3) at a magnification of lOx.
  • Figure 13 is an optical microscope image of disk fiberized corn (Example 3) at a magnification of 200x.
  • Figure 14 is an optical microscope image of disk fiberized corn (Example 4) at a magnification of lOx.
  • Figure 15 is an optical microscope image of disk fiberized corn (Example 4) at a magnification of 200x.
  • Figure 1 depicts a schematic view of an illustrative separation system 100 for recovering products derived from fermented com.
  • Illustrative products derived from fermented com can include, but are not limited to, ethanol, distillers grains, protein rich products, oil, and other products.
  • a ground com product that can be produced from the com can be processed to produce the fermented com.
  • the ground com product can be milled from a plurality of corn pieces by one or more high shear mills.
  • the plurality of com pieces via line 101 can be introduced into one or more high shear mills 102.
  • the com pieces, prior to being high shear milled can be or include, but are not limited to, whole com kernels, fragmented corn kernels, size-reduced corn kernels, milled com kernels, ground corn kernels, fresh corn kernels, dried corn kernels, or any mixture thereof.
  • whole com kernels can be size- reduced via one or more non-high shear mills, such as one or more hammer mills and/or one or more roller mills using a non-shearing technique, to produce a coarse ground com.
  • the coarse ground corn can be further size-reduced, such as sheared, milled, or otherwise ground, in the high shear mill 102 to produce the ground com product.
  • the high shear mill 102 can be or include, but is not limited to, one or more disk mill fiberizers, one or more air swept pulverizers, one or more other high shear mills, or any combination thereof.
  • the ground com product can have a particle size of less than a particle size of conventional ground corn (e.g., hammer milled com or roller milled com).
  • the ground corn product can have a dso by volume percent of about 100 ⁇ to about 500 ⁇ , as measured according to ISO 13320:2009.
  • hammer milled com generally has a dso by volume percent of greater than 500 ⁇
  • roller milled com generally has a dso by volume percent of greater than 600 ⁇ .
  • greater than 25 wt% of the ground com product can have a particle size of greater than 105 ⁇ and greater than 80 wt% of the ground com product can have a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966.
  • the particle size distribution of the ground com product produced in the high shear mill is further discussed and described below.
  • one or more product yields e.g., com oil
  • one or more system efficiencies is realized as compared to conventional ethanol production processes that use a ground com in which less than 80 wt% of the ground corn has a particle size of 425 ⁇ or less or when less than 25 wt% (e.g. , less than 20 wt%) of the ground corn product has a particle size of greater than 105 ⁇ .
  • the ground corn product produced in the high shear mill 102 can be processed or otherwise treated in one or more process units to produce a fermentation mash.
  • the process units can include one or multiple vessels and/or apparatuses, such as slurry tanks and/or liquefaction tanks, for heating, mixing, separating, and/or carrying out other operations on the slurry.
  • the ground corn product via line 103 can be transferred from the high shear mill 102 to one or more slurry tanks 104.
  • Other components or products from downstream in the separation system 100 can also be mixed, blended, or otherwise combined with the ground corn product in the slurry tank 104.
  • the ground corn product can be mixed, blended, or otherwise combined with water and one or more enzymes, such as alpha-amylase, to produce a slurry tank mixture.
  • One or more optional additives and/or one or more optional recycled downstream components can also be mixed, blended, or otherwise combined with the ground corn product, water, and enzyme to produce the slurry tank mixture.
  • the slurry tank mixture can be processed to produce the fermentation mash.
  • the slurry tank mixture can be heated to produce a gelatinized starch.
  • the gelatinized starch can be hydrolyzed to produce a liquefaction mash.
  • the liquefaction mash can be subjected to saccharification and fermentation to produce the fermentation mash.
  • the slurry tank mixture can be heated in a cooker (e.g., a pressurized jet cooker) to solubilize the starch in the ground corn product to produce a solubilized mixture of gelatinized starch.
  • a cooker e.g., a pressurized jet cooker
  • the slurry tank mixture can be mixed using a paddle mixer, a ribbon blender, a dense phase slurry mixer, or any combination thereof.
  • the slurry tank mixture can be heated to a temperature that is at or above the onset of starch gelatinization where the alpha amylase can solubilize the starch. In one example, this temperature can be above the temperature where the onset of gelatinization occurs, but below the temperature needed to complete gelatinization.
  • the starch is hydrolyzed by the enzyme into maltodextrins and oligosaccharides. Given sufficiently small particle size the hydrolysis can occur without complete gelatinization. Lower temperature liquefaction offers the benefit of reduced energy use and reduced damage to starch due to undesirable side reactions, such as the Maillard reaction, as well as a reduced formation of "dough balls", which are lumps of corn flour that can form in the slurry tank mixture and can reduce or cease the production of ethanol.
  • the slurry tank mixture in the slurry tank 104 can be heated to a temperature of less than 90°C, less than 85°C, less than 80°C, less than 75°C, less than 72°C, or less than 70°C.
  • the slurry tank mixture can be heated to a temperature of greater than 50°C, greater than 55°C, greater than 60°C, greaterthan 62°C, greater than 64°C, or greaterthan 66°C to less than 90°C, less than 85°C, less than 80°C, less than 75°C, less than 72°C, or less than 70°C.
  • the solubilized mixture of gelatinized starch via line 105 can be transferred from the slurry tank 104 to one or more liquefaction tanks 106.
  • One or more enzymes such as alpha- amylase, can be added to the solubilized mixture of gelatinized starch in a liquefaction process to produce a liquefaction mash containing a hydrolyzed mixture.
  • the enzyme can hydrolyze the gelatinized starch into maltodextrins and oligosaccharides.
  • the liquefaction mash via line 107 can be transferred from the liquefaction tank 106 to one or more fermenters 108.
  • the liquefaction mash containing the hydrolyzed mixture can be further processed in one or more saccharification and fermentation processes to produce the fermentation mash.
  • the saccharification and fermentation can occur sequentially or simultaneously.
  • the liquefied mash can be cooled and one or more enzymes, such as glucoamylase, can be added to hydrolyze the maltodextrins and oligosaccharides into single glucose sugar molecules.
  • one or more strains of yeast such as Saccharomyces cerevisae, can be added to metabolize the glucose sugars into ethanol and carbon dioxide.
  • the fermentation mash can include about 15 vol% to about 25 vol% of ethanol (volume/volume basis), as well as remaining grain components.
  • the fermentation mash via line 109 can be pumped or otherwise transferred from the fermenter 108 to one or more distillers 110 where the fermentation mash can be heated to vaporize at least a portion of the ethanol.
  • the distiller 110 can be or include, but is not limited to, one or more distillation columns, one or more distillation trains, one or more condensers, or other device(s) configured to vaporize the ethanol and to condense the vaporized ethanol.
  • the ethanol can be distilled or otherwise separated from the fermentation mash within the distiller 110 to produce a whole stillage.
  • the whole stillage can include, but is not limited to, water, fibers, starches, oils, and proteins.
  • the vaporized ethanol can be condensed in a condenser within the distiller 110, and liquid alcohol (e.g., ethanol) can be recovered from the distiller 110 at about 95 vol% purity (190 proof) .
  • the 190 proof ethanol via line 111 can be transferred into one or more dehydrators 112 and dried.
  • the dehydrator 112 can be or include one or more dehydration columns, such as molecular sieve dehydration columns.
  • the 190 proof ethanol can pass through the dehydration columns in the dehydrator 1 12 that can remove residual water from the ethanol, to yield a drier product of purified ethanol, such as about 99.75 vol% of ethanol (about 199.5 proof) that can be transferred via line 1 13 to one or more ethanol storage containers 1 14.
  • the whole stillage left in the distiller 1 10 can be further processed to separate and/or recover a variety of products.
  • Illustrative products that can be derived from the whole stillage can include, but are not limited to, other alcohols, oil products (e.g., a corn oil product), distillers grains (e.g. , a wet fiber rich product, a wet fiber rich product with syrup, a dried fiber rich product, and/or a dried fiber rich product with syrup), protein products (e.g., a protein rich product), and/or other products from the whole stillage (e.g. , a syrup product).
  • oil products e.g., a corn oil product
  • distillers grains e.g. , a wet fiber rich product, a wet fiber rich product with syrup, a dried fiber rich product, and/or a dried fiber rich product with syrup
  • protein products e.g., a protein rich product
  • other products from the whole stillage e.g. , a syrup product
  • the whole stillage left in the distiller 1 10 can be transferred via line 1 15 to one or more separators 1 16.
  • the whole stillage can be contacted or otherwise processed in the separator 1 16 to separate or otherwise produce a fiber rich portion or fiber rich product via line 1 17 and a filtrate via line 1 19.
  • the fiber rich product can be filtered or otherwise removed from stillage by the separator 1 16 to produce the filtrate that passes through the separator 1 16.
  • the fiber rich product can include fibrous material, such as fibers.
  • the fiber rich product can be used alone or combined with other components to produce various types of products, as will be further discussed and described below.
  • the separator 1 16 can be or include, but is not limited to, one or more pressure screens, one or more centrifuges (e.g. , a filtration centrifuge such as those discussed and described in U.S. Patent Nos.: 8,813,973 and 8,778,433), one or more paddle screens, one or more fiber filters, one or more rotary drum screens, one or more rotary vacuum drum filters, one or more brush strainers, one or more vibratory separators, one or more centrifugal screeners, one or more linear motion screens, one or more vacu-deck screens, or any combination thereof.
  • one or more pressure screens e.g. , a filtration centrifuge such as those discussed and described in U.S. Patent Nos.: 8,813,973 and 8,778,433
  • one or more paddle screens e.g. , a filtration centrifuge such as those discussed and described in U.S. Patent Nos.: 8,813,973 and 8,778,433
  • one or more paddle screens e.g
  • the separator 1 16 can be or include a single pressure screen. In other examples, the separator 1 16 can be or include two or more pressure screens. In other examples, the separator 1 16 can be a single pressure screen or two or more pressure screens and can be free of or otherwise exclude any centrifuge. In another example, the separator 1 16 be a single pressure screen or two or more pressure screens and can be free of or otherwise exclude any centrifuge, paddle screen, fiber filter, or any combination of centrifuge, paddle screen, and filter.
  • the separator 116 can be a single pressure screen or two or more pressure screens and can be free of or otherwise exclude any centrifuge, paddle screen, fiber filter, rotary drum screen, rotary vacuum drum filter, brush strainer, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen.
  • the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more pressure screens.
  • Illustrative pressure screens can be or include outflow pressure screens, inflow pressure screens, inflow/outflow pressure screens, and/or foils on accept side of plate pressure screens.
  • outflow pressure screen the whole stillage can flow from the inside of the screen plate cylinder to the outside, with the rotor being on the inside of the screen plate.
  • the fibers can be held inside the plate until the fibers reach the reject port.
  • inflow pressure screen the whole stillage can flow from the outside of the screen cylinder to the inside with the rotor being on the outside of the screen plate.
  • the fibers can be held on the outside of the cylinder.
  • Suitable rotors can include foiled rotors, bump rotors, lobe rotors, and/or S-rotors.
  • the openings in the pressure screens can be circular, slotted, or a combination thereof.
  • the pressure screen can be made by milling slots into a single piece of metal and rolling the milled metal into a cylinder.
  • the pressure screen can also be made by banding wires together to form a cylinder, which is also referred to as wedge-wire baskets.
  • Pressure screens that include slotted openings can have a width of about 12 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , or more.
  • the pressure screen can include slotted openings having a width of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • the separator 116 can be or include one or more fiber filters. In some examples, the separator 116 can be a single fiber filter. In other examples, the separator 116 can be a single fiber filter or two or more fiber filters. In some examples, the separator 116 can be or include 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more fiber filters. In other examples, the separator 116 can be a single fiber filter or two or more fiber filters and can be free of or otherwise exclude any centrifuge, any pressure screen, any paddle screen, or any combination of a centrifuge, pressure screen, and paddle screen.
  • the separator 116 can be or include 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more fiber filters and can be free of or otherwise exclude any centrifuge, any pressure screen, any paddle screen, or any combination of a centrifuge, pressure screen, and paddle screen.
  • the separator 116 can be a single fiber filter or two or more fiber filters and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, rotary drum screen, rotary vacuum drum filter, brush strainer, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen.
  • the separator 116 can be or include 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more fiber filters and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, rotary drum screen, rotary vacuum drum filter, brush strainer, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen.
  • the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more fiber filters.
  • the whole stillage can be introduced, e.g. , pumped, into a filter sleeve of the fiber filter.
  • the filter sleeve can have hole sizes or openings of about 12.7 ⁇ , about 25.4 ⁇ , about 50.8 ⁇ , or about 76.2 ⁇ to about 101.6 ⁇ , about 127 ⁇ , about 152.4 ⁇ , about 177.8 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , or more.
  • the filter sleeve can have hole sizes or openings of about 10 ⁇ , about 12 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , or more.
  • the filter sleeve can have hole sizes or openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • the filter sleeve can be vibrated, e.g. , at high frequency.
  • vibration of the filter sleeve can be accomplished by (1) tensioning the filter sleeve with a pair of springs, (2) rotating a high speed rotor disposed inside the filter sleeve that can induce pulsed waves in the whole stillage, or (3) a combination thereof.
  • the rotor can include one or more flights that can push or otherwise urge solids toward a sludge discharge at the end of the fiber filter.
  • the rotor can include straight paddles with ribbon flighting that can direct solids toward the discharge.
  • the pulsing and/or vibrations can also force or otherwise urge the filtered liquid through the filter sleeve.
  • the filter sleeve can be made of one or more polymer fabrics.
  • the polymer can be or include, but is not limited to, polyester, polyether ether ketone (PEEK), or other suitable polymers.
  • the polymer fabric can be a woven polymer fabric. Any type of weave can be used to produce a filter sleeve composed of a woven polymer fabric. Illustrative types of weaves can include plain weave, twill weave, satin weave, basket weave, leno weave, and mock leno weave.
  • the filter sleeve can be formed by connecting opposing edges of a filter sleeve by a lap or double hook joint.
  • One suitable fiber filter can include the fiber filter discussed and described in U.S. Patent No. 6,117,321.
  • the fiber filter can include a flltering body that includes a filter unit.
  • the filter unit can include, but is not limited to, a flexible flltering sleeve and a rotor disposed within the flexible flltering sleeve.
  • the rotor can be configured to pulse a fluid radially outwardly against the flltering sleeve.
  • the flltering sleeve can be assembled or otherwise located on the flltering body via one or more supports.
  • the one or more supports can be elastic and can permit the flltering sleeve to expand and contract along a longitudinal axis thereof.
  • the one or more supports can be adjusted and tensioned by one or more adjustment devices located outside of the flow of a filtrate.
  • Some commercially available fiber filters can include, but are not limited to, the FF 6, the FF 12, and the FF 30, available from Vincent Corporation.
  • the separator 116 can be or include one or more paddle screens. In some examples, the separator 116 can be a single paddle screen. In other examples, the separator 116 can be a single paddle screen or two or more paddle screens. In other examples, the separator 116 can be a single paddle screen or two or more paddle screens and can be free of or otherwise exclude any centrifuge, any pressure screen, and fiber filter, or any combination of a centrifuge, pressure screen, and fiber filter.
  • the separator 116 can be a single paddle screen or two or more paddle screens and can be free of or otherwise exclude any pressure screen, centrifuge, fiber filter, rotary drum screen, rotary vacuum drum filter, brush strainer, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen.
  • the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more paddle screens.
  • the paddle screen can include a screen that can include openings of about 12.7 ⁇ , about 25.4 ⁇ , about 50.8 ⁇ , or about 76.2 ⁇ ⁇ about 101.6 ⁇ , about 127 ⁇ , about 152.4 ⁇ , about 177.8 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , or more.
  • the screen can have openings of about 12 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , or more.
  • the screen can have openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available paddle screen can include, but is not limited to, the FQ- PS32 Paddle Screen available from Fluid-Quip, Inc.
  • the separator 116 can be or include one or more rotary drum screens. In some examples, the separator 116 can be or include a single rotary drum screen. In other examples, the separator 116 can be or include a single rotary drum screen or two or more rotary drum screens. In other examples, the separator 116 can be or include a single rotary drum screen or two or more rotary drum screens and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary vacuum drum filter, brush strainer, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen. As such, in at least one example, the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more rotary drum screens.
  • the rotary drum screen can include a filter element or screen having openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , about 700 ⁇ , about 900 ⁇ , about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the rotary drum screen can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available rotary drum screen can include, but is not limited to, the LIQUI- FUGE ® LFS rotary drum screen available from Vulcan.
  • the separator 116 can be or include one or more brush strainers. In some examples, the separator 116 can be or include a single brush strainer. In other examples, the separator 116 can be or include a single brush strainer or two or more brush strainers. In other examples, the separator 116 can be or include a single brush strainer or two or more brush strainers and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary drum screen, rotary vacuum drum filter, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen.
  • the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more brush strainers.
  • the brush strainer can include a casing surrounding a filter element or perforated strainer cylinder, through which the liquid can flow through. Particles suspended in the whole stillage can be held back in the cylinder and forced downward by rotating brushes mounted on a shaft.
  • the filter element or perforated strainer cylinder can have openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ m, about 380 ⁇ , about 430 ⁇ , about 500 ⁇ m, about 700 ⁇ , about 900 ⁇ m, about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the perforated strainer cylinder can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available brush strainer can include, but is not limited to, the W-SIL self-cleaning brush strainer, available from Alfa Laval.
  • the separator 116 can be or include one or more rotary vacuum drum filters. In some examples, the separator 116 can be or include a single rotary vacuum drum filter. In other examples, the separator 116 can be or include a single rotary vacuum drum filter or two or more rotary vacuum drum filters. In other examples, the separator 116 can be or include a single rotary vacuum drum filter or two or more rotary vacuum drum filters and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary drum screen, brush strainer, vibratory separator, centrifugal screener, linear motion screen, and vacuum deck screen. As such, in at least one example, the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more rotary vacuum drum filters.
  • the rotary vacuum drum filter can include a vacuum pump, a filtrate pump, and a vacuum/filtrate receiver.
  • the rotary vacuum drum filter can also include feed and/or drain pumps and pre-coat or chemical prep tanks.
  • the drum can rotate while partially submerged in the whole stillage.
  • a vacuum can draw liquid through the filter element or screen, e.g. , a cloth or fabric filter element on the drum surface which retains the solids.
  • the vacuum can pull a gas, e.g. , air, through the cake and remove moisture as the drum rotates.
  • the filter element can have openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , about 700 ⁇ , about 900 ⁇ , about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the filter medium can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available rotary vacuum drum filter can include, but is not limited to, the vacuum drum rotary filters available from Komline-Sanderson.
  • the separator 116 can be or include one or more vibratory separators. In some examples, the separator 116 can be or include a single vibratory separator.
  • the separator 116 can be or include a single vibratory separator or two or more vibratory separators. In other examples, the separator 116 can be or include a single vibratory separator or two or more vibratory separators and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary drum screen, brush strainer, rotary vacuum drum filter, centrifugal screener, linear motion screen, and vacuum deck screen. As such, in at least one example, the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more vibratory separators.
  • the vibratory separator can vibrate, e.g. , about its center of mass.
  • the vibration can be induced by eccentric weights on the upper and lower ends of a motion-generator shaft.
  • the vibratory separator can include one or more filter elements, e.g. , screen decks, e.g., 1, 2, 3, 4, or more filter elements.
  • the filter element e.g.
  • screen decks can have openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , about 700 ⁇ , about 900 ⁇ , about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the filter elements can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • Some commercially available vibratory separators can include, but are not limited to, the VIBRO- ENERGY ® Round Separators, the MX Separators, and the Super MX Separators, available from SWECO, Inc.
  • the separator 116 can be or include one or more centrifugal screeners. In some examples, the separator 116 can be or include a single centrifugal screener. In other examples, the separator 116 can be or include a single centrifugal screener or two or more centrifugal screeners. In other examples, the separator 116 can be or include a single centrifugal screener or two or more centrifugal screeners and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary drum screen, brush strainer, rotary vacuum drum filter, vibratory separator, linear motion screen, and vacuum deck screen.
  • the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more centrifugal screeners.
  • the whole stillage can be introduced to an inlet and redirected into a cylindrical sifting chamber via a feed screw.
  • Helical paddles can be rotated within the chamber to propel the whole stillage against a screen, while the resultant, centrifugal force on the particles can accelerate the particles through apertures in the screen.
  • the rotating paddles which do not contact the screen, can breakup soft agglomerates. Over-sized particles and trash can be ejected via an oversize discharge spout.
  • the screen can have openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , about 700 ⁇ , about 900 ⁇ , about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the screen can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available centrifugal screener can include, but is not limited to, the CENTRI-SIFTERTM, available from Kason Corporation.
  • the separator 116 can be or include one or more linear motion screens. In some examples, the separator 116 can be or include a single linear motion screen. In other examples, the separator 116 can be or include a single linear motion screen or two or more linear motion screens. In other examples, the separator 116 can be or include a single linear motion screen or two or more linear motion screens and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary drum screen, brush strainer, rotary vacuum drum filter, vibratory separator, centrifugal screener, and vacuum deck screen. As such, in at least one example, the whole stillage in line 115 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more linear motion screens.
  • the whole stillage can be introduced to the linear motion screener, which can include an angled filter element, e.g., screen.
  • the filter element can be at an angle of about +10° to about -15° relative to horizontal.
  • the filter element or screen can have openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , about 700 ⁇ , about 900 ⁇ , about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the filter element or screen can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available linear motion screener can include, but is not limited to, the linear motion screeners available from Tinsley Company.
  • the separator 116 can be or include one or more vacu-deck screens. In some examples, the separator 116 can be or include a single vacu-deck screen. In other examples, the separator 116 can be or include a single vacu-deck screen or two or more vacu- deck screens. In other examples, the separator 116 can be or include a single vacu-deck screen or two or more vacu-deck screens and can be free of or otherwise exclude any pressure screen, centrifuge, paddle screen, fiber filter, rotary drum screen, brush strainer, rotary vacuum drum filter, vibratory separator, centrifugal screener, and linear motion screener. As such, in at least one example, the whole stillage in line 1 15 can be separated into the fiber rich product via line 117 and the filtrate via line 119 with only one or two or more vacu-deck screens.
  • the vacu-deck screen can include one or more filter elements or screens that can have openings of about 10 ⁇ , about 25 ⁇ , about 50 ⁇ , or about 75 ⁇ to about 100 ⁇ , about 130 ⁇ , about 150 ⁇ , about 175 ⁇ , about 230 ⁇ , about 255 ⁇ , about 330 ⁇ , about 380 ⁇ , about 430 ⁇ , about 500 ⁇ , about 700 ⁇ , about 900 ⁇ , about 1 mm, about 1.5 mm, about 2 mm, or more.
  • the filter element or screen can include openings of about 10 ⁇ , about 30 ⁇ , about 50 ⁇ , about 75 ⁇ , about 100 ⁇ , about 125 ⁇ , or about 150 ⁇ to less than 250 ⁇ , less than 300 ⁇ , less than 350 ⁇ , less than 400 ⁇ , less than 450 ⁇ , or less than 500 ⁇ .
  • a commercially available vacu-deck screen can include, but is not limited to, the vacu-deck screens available from Tinsley Company.
  • the separator 116 e.g., a pressure screen and/or a fiber filter, can process or filter the whole stillage at a rate of about 94.6 liters per minute, about 379 liters per minute, about 946 liters per minute, or about 1,890 liters per minute to about 2,840 liters per minute, about 3,790 liters per minute, about 4,730 liters per minute, about 5,680 liters per minute, about 6,620 liters per minute, about 7,570 liters per minute, about 11,000 liters per minute, about 15,000 liters per minute, about 19,000 liters per minute, about 22,500 liters per minute, about 26,500 liters per minute, or about 30,500 liters per minute.
  • a pressure screen and/or a fiber filter can process or filter the whole stillage at a rate of about 94.6 liters per minute, about 379 liters per minute, about 946 liters per minute, or about 1,890 liters per minute to about 2,840
  • the separator e.g. , a pressure screen and/or a fiber filter
  • the filtrate via line 119 can contains less solids as compared to if the separator 116 includes one or more centrifuges, one or more pressure screens, one or more paddle screens, or any combination thereof.
  • the separator 116 includes only one or more fiber filters, i.e. , does not include a centrifuge, a pressure screen, a paddle screen, or other separator, the filtrate via line 119 can contain less solids as compared to if the separator includes a centrifuge, a pressure screen, a paddle screen, or other separator, but not a fiber filter.
  • the filtrate can be transferred via line 119 from the separator 116 to one or more separators 120 (e.g., a two phase separator such as a nozzle centrifuge, or a three phase separator such as a TRI CANTER ® , available from Flottweg).
  • the separator 120 can be a three phase separator and can separate or otherwise produce a protein rich product via line 122, an oil product via line 123, and a clarified stillage that can be free from or have a reduced oil content via line 121.
  • the separator 120 can be a centrifuge that can separate or otherwise produce the protein rich product via line 122 and a clarified stillage via line 121 from the filtrate in line 119.
  • the separator 120 can be provided with washing capabilities so that water, along with the filtrate, can be supplied to the separator 120. If the separator 120 includes a centrifuge, the additional water can facilitate separation of the filtrate into the protein rich product and the clarified stillage.
  • the heavier protein can separate from the lighter components and can be removed as an underflow containing the protein rich product, whereas the lighter components, which can include oil and starch, can be removed as an overflow containing the clarified stillage.
  • the separator 120 can also include or can be replaced with a cyclone separation apparatus or other device to separate the filtrate portion into the protein rich product and the clarified stillage.
  • the protein rich product can be dewatered or otherwise dried such that water can be removed from the protein rich product to produce a dried protein product.
  • the protein rich product via line 122 can be transferred from the centrifuge 120 to one or more dryers 124. In some examples, as depicted in Figure 1, the protein rich product via line 122 can be transferred to the dryer 124 to reduce the amount of water and/or otherwise dry the protein rich product to produce the dried protein product.
  • the dried protein product via line 126 can be transferred from the dryer 124 to one or more storage containers 128. In some examples, the separated water portion or filtrate from the dryer 124 can be recycled back or otherwise transferred to the fermenter 108 for liquefaction and/or fermentation.
  • the dried protein product can include less water than the protein rich product.
  • the dryer 124 can be or include one or more centrifuges (e.g. , a decanter centrifuge), one or more ring dryers (e.g. , P-ring dryers), one or more flash dryers, one or more fluid bed dryers, one or more heated air dryers, one or more heaters, one or more steam dryers (e.g. , steam ring dryers, steam flash dryers, and/or steam tube dryers), one or more rotary dryers, one or more steam and rotary dryers (e.g. , Swiss Combi's ecoDRYTM drying system), one or more superheated steam dryers, one or more spray dryers, one or more vacuum filtration dryers, one or more other drying devices, or any combination thereof to remove water and produce the dried protein product.
  • centrifuges e.g. , a decanter centrifuge
  • ring dryers e.g. , P-ring dryers
  • flash dryers e.g. , one or more flash dryers, one
  • the dried protein product in line 126 can be or include high protein corn meal.
  • the dried protein product can be used as fish feed, shrimp feed, crab feed, other aquaculture feeds, pig feed, cattle feed, chicken feed, or other livestock feed.
  • the dried protein product can include about 35 wt%, about 40 wt%, or about 45 wt% to about 50 wt%, about 55 wt%, about 60 wt%, about 70 wt%, about 80 wt%, or greater of protein on a dry matter basis.
  • the dried protein product can include about 35 wt% to about 80 wt%, about 35 wt% to about 70 wt%, about 35 wt% to about 60 wt%, about 35 wt% to about 55 wt%, about 35 wt% to about 50 wt%, about 45 wt% to about 80 wt%, about 45 wt% to about 70 wt%, about 45 wt% to about 60 wt%, about 45 wt% to about 55 wt%, or about 45 wt% to about 50 wt% of protein on a dry matter basis.
  • the clarified stillage via line 121 can be transferred via line 121 to one or more evaporators 140.
  • the clarified stillage can be dewatered, i. e. , water can be removed from the clarified stillage, to produce an evaporated clarified stillage.
  • the evaporator 140 can gasify at least a portion of the water in the clarified stillage to produce the evaporated clarified stillage.
  • the evaporated clarified stillage via line 142 can be transferred from the evaporator 140 to one or more additional evaporators 150.
  • the evaporated clarified stillage via line 142 can be introduced to the additional evaporator 150.
  • the evaporated clarified stillage via line 141 can be transferred from the evaporator 140 to one or more oil recovery centrifuges 145.
  • the evaporated clarified stillage can be introduced to the oil recovery centrifuge 145 to separate and produce an oil product and an evaporated clarified stillage with reduced oil, also referred to as a stillage with reduced oil.
  • One or more oil products via line 146 can be transferred from the oil recovery centrifuge 145 to one or more storage containers 148.
  • the oil product can include a mixture of typical fatty acids found in corn oil.
  • the final recovered oil product can be about 30 wt%, about 40 wt%, about 45 wt% to about 50 wt%, about 60 wt%, or about 70 wt% of the total corn oil in the corn (e.g., corn kernels and/or other corn pieces).
  • the oil recovery centrifuge 145 can function at a higher capacity because the evaporated clarified stillage, which can be subjected to the oil recovery centrifuge 145, can include less water and less protein than the clarified stillage.
  • the evaporated clarified stillage in line 142 when the separator 120 is or includes a three phase separator and produces the oil product via line 123, can also be introduced to the oil recovery centrifuge 145 to produce additional oil product via line 146, provided less than all of the oil in the filtrate was separated by the separator 120.
  • the stillage with reduced oil via line 143 from the oil recovery centrifuge 145 can be introduced into one or more evaporators 150.
  • the stillage with reduced oil can be further dewatered or dried in the evaporator 150 where water or other liquids can be further evaporated from the stillage with reduced oil to produce a syrup.
  • the syrup can include, but is not limited to, minerals, sugars, starches, proteins, fibers, other components contained in water, or any mixture thereof.
  • the syrup can be used alone or combined with other components or stream in the separation system 100 to produce various types of products.
  • the syrup via line 151 from the evaporator 150 can be transferred without any further processing to one or more storage containers 152 and can be used or sold as an independent product.
  • the syrup via line 153, 157, or 159 can be transferred from the evaporator 150 to one of several portions of the separation system 100 and combined with the fiber rich product, as will be further discussed and described below.
  • each evaporator 140, 150 can be one evaporator or a plurality of evaporators, such as 2, 3, 4, 5, 6, or more evaporators coupled in series and in fluid communication with one another.
  • the evaporator 140 can have three or more evaporators and the evaporator 150 can also have three or more evaporators.
  • the fiber rich product via line 1 17 from the separator 1 16 can be transferred without any further processing via line 136 to one or more storage containers 138 and referred to as a wet fiber rich product that can be used or sold as an independent product.
  • the fiber rich product via lines 1 17 and 154 can be transferred to one or more dryers 160.
  • the fiber rich product can be further dried or dewatered by the dryer 160 to provide a dried fiber rich product that can be transferred via line 162 to one or more storage containers 164.
  • the dryer 160 can be or include one or more centrifuges (e.g., a decanter centrifuge), one or more ring dryers (e.g., P-ring dryers), one or more flash dryers, one or more fluid bed dryers, one or more heated air dryers, one or more heaters, one or more steam dryers (e.g., steam ring dryers, steam flash dryers, and/or steam tube dryers), one or more rotary dryers, one or more steam and rotary dryers (e.g., Swiss Combi's ecoDRY drying system), one or more superheated steam dryers, one or more spray dryers, one or more vacuum filtration dryers, one or more other drying devices, or any combination thereof to remove water and produce the dried protein product.
  • centrifuges e.g., a decanter centrifuge
  • ring dryers e.g., P-ring dryers
  • flash dryers e.g., one or more flash dryers
  • fluid bed dryers e.g.
  • the fiber rich product and the syrup can be combined together.
  • the fiber rich product via line 117 and the syrup via line 153 from the evaporator 150 can be combined and mixed in line 154 or other processing unit to produce a wet fiber rich product with syrup that can be transferred via line 155 to one or more storage containers 156.
  • the wet fiber rich product with syrup via line 154 can be transferred to the dryer 160.
  • the wet fiber rich product with syrup can be further dried or dewatered by dryer 160 to provide a dried fiber rich product with syrup that can be transferred via line 165 to one or more storage containers 168.
  • the dried fiber rich product with syrup can be used or sold as an independent product.
  • the fiber rich product and the syrup can be combined together in the dryer 160.
  • the fiber rich product via lines 1 17 and 154 and the syrup via line 157 from the evaporator 150 can be combined and mixed in dryer 160 to produce the wet fiber rich product with syrup that can be dried in the dryer 160 to produce the dried fiber rich product with syrup.
  • the dried fiber rich product with syrup can be transferred from the dryer 160 via line 165 to the storage container 168.
  • the dried fiber rich product via line 162 from the dryer 160 and the syrup via line 159 from the evaporator 150 can be combined and mixed in line 167 or other processing unit to produce the dried fiber rich product with syrup that can be transferred via line 167 to the storage container 168.
  • Figure 2 depicts a schematic view of an illustrative system 200 for producing ethanol from a fiber product recovered from a whole stillage, according to one or more embodiments.
  • a whole stillage via line 215 can be introduced to one or more separators 216.
  • the whole stillage can be produced in the same or substantially the same way as the whole stillage in line 1 15 discussed and described above with reference to Figure 1.
  • the ground corn that can be processed to produce a fermentation mash that the whole stillage can be separated from can be ground with one or more disk mill fiberizers.
  • the whole stillage can be contacted or otherwise processed in the separator 216 to separate or otherwise produce a fiber rich product via line 217 and a filtrate via line 219.
  • the separator 216 can be or include any one or more of the separators 1 16 discussed and described above with reference to Figure 1.
  • the separator 216 can be or include, but is not limited to, one or more pressure screens, one or more centrifuges (e.g., a filtration centrifuge such as those discussed and described in U.S. Patent Nos.: 8,813,973 and 8,778,433), one or more paddle screens, one or more fiber filters, one or more rotary drum screens, one or more rotary vacuum drum filters, one or more brush strainers, one or more vibratory separators, one or more centrifugal screeners, one or more linear motion screens, one or more vacu-deck screens, or any combination thereof.
  • the separator 216 can be or include one or more fiber filters.
  • the separator 216 can be or include one or more paddle screens.
  • the filtrate in line 219 can be processed in the same or substantially the same manner as the filtrate in line 119 discussed and described above with reference to Figure 1.
  • the fiber rich product via line 217 can be introduced to one or more pretreatment vessels 224 to produce a pretreated fiber rich product via line 226.
  • the pretreatment vessel 224 can be or include, for example, a slurry tank or a pressure vessel.
  • the pretreatment vessel 224 can disrupt the structure of the fiber rich product to produce a fiber rich product that can be more readily accessible and digestible to hydrolysis with an enzyme, e.g., a cellulose enzyme.
  • hemicellulose can be converted to oligomers, xylose, and/or arabinose and the cellulose and/or hemicellulosic oligomers can be made more accessible and digestible to the cellulase enzyme.
  • one or more acids and/or one or more bases via line 222 can be mixed, blended, combined, or otherwise contacted with the fiber rich product within the pretreatment vessel 224.
  • the fiber rich product and the acid and/or base can be heated to a temperature of about 50°C, about 75°C, or about 100°C to about 1 15°C, about 125°C, about 150°C, about 175°C, about 200°C, or about 225 °C.
  • the fiber rich product and the acid and/or base can be heated for a time of about 10 minutes, about 30 minutes, or about 1 hour to about 2 hours, about 5 hours, or about 10 hours.
  • Illustrative acids that can be contacted with the fiber rich product can include, but are not limited to, sulfuric acid, nitric acid, hydrochloric acid, phosphoric acid, strong acid resins, acetic acid, citric acid, trichloroacetic acid, or any mixture thereof.
  • Illustrative bases that can be contacted with the fiber rich product can include, but are not limited to, ammonium hydroxide, potassium hydroxide, sodium hydroxide, calcium hydroxide, magnesium hydroxide, strong base resins, sodium carbonate, potassium carbonate, lime, or any mixture thereof.
  • the fiber rich product contacted with the acid and/or base can also be irradiated, e.g., microwaves and/or radio waves.
  • the fiber rich product without being contacted with an acid or a base, can be irradiated, e.g. , microwaves and/or radio waves.
  • the fiber rich product can be subjected to steam explosion, e.g. , contact with steam at a temperature of about 160°C to about 260°C, under a pressure of about 0.7 Mpa to about 5 Mpa, for a time of about 1 minute to about 20 minutes.
  • Other processes that can be used to produce the pretreated fiber rich product in lieu of or in addition to an acid and/or a base can include, but are not limited to, ionic liquid pretreatment; liquid hot water (LHW) pre-treatment; supercritical water; steam explosion; ammonia fiber explosion (AFEX); carbon dioxide explosion; contact with heteropolyacids, e.g., H5BW12O40; ozonolysis; organosolvation treatment with an organic solvent such as acetone, methanol, ethanol, phenol, ethylene glycol, tetrahydrofuran, and/or tetrahydrofurfuryl; or any combination thereof.
  • ionic liquid pretreatment liquid hot water (LHW) pre-treatment
  • supercritical water steam explosion
  • AFEX ammonia fiber explosion
  • carbon dioxide explosion contact with heteropolyacids, e.g., H5BW12O40
  • ozonolysis organosolvation treatment with an organic solvent such as acetone, methanol,
  • the pretreated fiber rich product via line 226 can be introduced to one or more saccharification vessels 232.
  • One or more enzymes via line 228 can also be introduced to the saccharification vessel 232.
  • the pretreated fiber rich product can be contacted under conditions sufficient to produce a saccharification mash that can be recovered via line 236.
  • the pretreated fiber rich product can be cooled and one or more enzymes, e.g. , glucoamylase, can be added to hydrolyze maltodextrins and oligosaccharides into single glucose sugar molecules.
  • Illustrative enzymes can include, but are not limited to, one or more cellulases, one or more hemicellulases, or a mixture thereof.
  • a cellulase and a hemicellulase can be used.
  • the cellulase can include, but is not limited to, exo-glucanases, endo-gluconases, beta-glucosidase, and potentially some xylanase activity.
  • the hemicellulase can include a number of different activities such as exo-xylanase, endo-xylanase, arabinose, esterase, and proteases.
  • enzyme mixtures are available commercially from Novozymes (Franklinton NC) and DuPont (Wilmington DE).
  • Commercially available enzymes that can be used can include, but are not limited to, ACCELLERASE ® Trio; ACCELLERASE ® 1500; ACCELLERASE ® BG, OPTIMASH ® , and SPEZYME ® CP (available from Dupont); CELLUCLAST ® 1.5L; CELLIC ® CTec2; CELLIC ® CTec3, CELLIC ® CTec4, HTecl, HTec2, HTec3 (available from Novozymes); ROHAMENT ® CL, ROHAMENT ® CEP, ROHALASE ® BXL, ROHALASE ® SEP (available from AB Enzymes); SZM XC-150 (available from CTE- Global), and CODEXYME ® 4 (available from Codexis).
  • the saccharification mash via line 236 can be introduced to one or more fermenters 242.
  • One or more strains of yeast e.g., Saccharomyces cerevisae, Pichia Stipitis, and/or Candida utilis, can be introduced via line 238 to the fermenter 242 to initiate fermentation of the saccharification mash and produce a fermented product that can include ethanol and a stillage protein product that can be recovered via line 246.
  • the yeast can ferment, metabolize, digest, or otherwise convert the sugars in the saccharification mash with yeast into ethanol and carbon dioxide.
  • the saccharification mash can be heated or otherwise maintained at a temperature of about 28°C to about 55°C during the fermentation.
  • the fermented product via line 246 can be introduced to one or more distillers 252 where the fermented product can be heated to vaporize at least a portion of the ethanol.
  • the distiller 252 can be or include, but is not limited to, one or more distillation columns, distillation trains, one or more condensers, or other devices configured to vaporize the ethanol and to condense the vaporized ethanol.
  • the ethanol can be distilled or otherwise separated from the fermented product within the distiller 252 and recovered via line 254.
  • the stillage protein product can be recovered via line 256.
  • Figure 3 depicts a schematic view of another illustrative system 300 for producing ethanol from a fiber product recovered from a whole stillage, according to one or more embodiments.
  • a whole stillage via line 315 can be introduced to one or more separators 316.
  • the whole stillage can be produced in the same or substantially the same way as the whole stillage in line 315 discussed and described above with reference to Figure 1.
  • the whole stillage can be contacted or otherwise processed in the separator 316 to separate or otherwise produce a fiber rich product via line 317 and a filtrate via line 319.
  • the filtrate in line 319 can be processed in the same or substantially the same manner as the filtrate in line 119 discussed and described above with reference to Figure 1.
  • the fiber rich product via line 317 can be introduced to one or more pretreatment vessels 324 to produce a pretreated fiber rich product via line 326.
  • the pretreatment vessel 324 can be or include, for example, a slurry tank or a pressure vessel.
  • the pretreatment vessel 324 can disrupt the structure of the fiber rich product to produce a fiber rich product that can be more readily accessible and digestible to hydrolysis with an enzyme, e.g., a cellulose enzyme.
  • hemicellulose can be converted to oligomers, xylose, and/or arabinose and the cellulose and/or hemicellulosic oligomers can be made more accessible and digestible to the cellulase enzyme.
  • one or more acids and/or one or more bases via line 322 can be mixed, blended, combined, or otherwise contacted with the fiber rich product within the pretreatment vessel 324.
  • the fiber rich product and the acid and/or base can be heated to a temperature of about 50°C, about 75°C, or about 100°C to about 115°C, about 125°C, about 150°C, about 175°C, about 200°C, or about 225 °C.
  • the fiber rich product and the acid and/or base can be heated for a time of about 10 minutes, about 30 minutes, or about 1 hour to about 2 hours, about 5 hours, or about 10 hours.
  • Illustrative acids that can be contacted with the fiber rich product can include, but are not limited to, sulfuric acid, nitric acid, hydrochloric acid, phosphoric acid, or any mixture thereof.
  • Illustrative bases that can be contacted with the fiber rich product can include, but are not limited to, ammonium hydroxide, potassium hydroxide, sodium hydroxide, calcium hydroxide, or any mixture thereof.
  • the fiber rich product and the acid and/or base can also be irradiated, e.g. , microwaves and/or radio waves.
  • the fiber rich product can be subjected to steam explosion, e.g., contact with steam at a temperature of about 160°C to about 260°C, under a pressure of about 0.7 Mpa to about 5 Mpa, for a time of about 1 minute to about 20 minutes.
  • steam explosion e.g., contact with steam at a temperature of about 160°C to about 260°C, under a pressure of about 0.7 Mpa to about 5 Mpa, for a time of about 1 minute to about 20 minutes.
  • LHW liquid hot water
  • AFEX ammonia fiber explosion
  • carbon dioxide explosion contact with heteropolyacids, e.g., H5BW12O40; ozonolysis; organosolvation treatment with an organic solvent such as acetone, methanol, ethanol, phenol, ethylene glycol, and/or tetrahydrofurfuryl; or any combination thereof.
  • the pretreated fiber rich product via line 326 can be introduced to one or more fermenters 342.
  • the pretreated fiber rich product can be subjected to simultaneous saccharification and fermentation (SSF) within the fermenter 342.
  • SSF simultaneous saccharification and fermentation
  • one or more enzymes via line 328 and one or more yeasts rains of yeast e.g. , Saccharomyces cerevisae, Pichia Stipitis, and/or Candida utilis
  • yeast e.g. , Saccharomyces cerevisae, Pichia Stipitis, and/or Candida utilis
  • the enzyme via line 328 and the yeast via line 338 can be introduced to the fermenter 342 at the same time.
  • Illustrative enzymes can include, but are not limited to, one or more cellulases, one or more hemicellulases, or a mixture thereof.
  • a cellulase and a hemicellulase can be used.
  • the cellulase can include, but is not limited to, exo-glucanases, endo-gluconases, beta-glucosidase, and potentially some xylanase activity.
  • the hemicellulase can include a number of different activities such as exo-xylanase, endo-xylanase, arabinose, esterase, and proteases. These enzyme mixtures are available commercially from Novozymes (Franklinton NC) and DuPont (Wilmington DE).
  • the enzyme via line 328 can be introduced to the fermenter 342 before the yeast via line 338.
  • the saccharification of the pretreated fiber rich product can hydrolyze maltodextrins and oligosaccharides into single glucose sugar molecules.
  • the fermentation of the fiber rich product and/or the saccharification mash can produce additional ethanol and a stillage protein product that can be recovered as the fermented product via line 346 from the fermenter 342.
  • the fiber rich product and/or saccharification mash can be heated or otherwise maintained at a temperature of about 28°C to about 55°C during saccharification and fermentation.
  • the fermented product via line 346 can be introduced to one or more distillers 352 where the fermented product can be heated to vaporize at least a portion of the ethanol.
  • the distiller 352 can be or include, but is not limited to, one or more distillation columns, distillation trains, one or more condensers, or other devices configured to vaporize the ethanol and to condense the vaporized ethanol.
  • the ethanol can be distilled or otherwise separated from the fermented product within the distiller 352 and recovered via line 354.
  • the stillage protein product can be recovered via line 356.
  • the fiber rich products can include inorganic compounds (commonly referred to as ash); structural protein; extractives such as fats and glycerol; acetate; lignin; C6 polysaccharides; C5 polysaccharides; or any mixture thereof.
  • inorganic compounds commonly referred to as ash
  • structural protein such as structural protein
  • extractives such as fats and glycerol
  • acetate such as lignin
  • C6 polysaccharides such as C6 polysaccharides
  • C5 polysaccharides or any mixture thereof.
  • the fiber rich products in lines 217 and 317 can include at least 20 wt%, at least 21 wt%, at least 22 wt%, at least 23 wt%, at least 24 wt%, at least 25 wt%, at least 26 wt%, at least 27 wt%, at least 28 wt%, at least 29 wt%, or at least 30 wt% of C6 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include at least 20 wt%, at least 21 wt%, at least 22 wt%, at least 23 wt%, at least 24 wt%, at least 25 wt%, at least 26 wt%, at least 27 wt%, at least 28 wt%, at least 29 wt%, at least 30 wt%, at least 31 wt%, at least 32 wt%, at least 33 wt%, at least 34 wt%, at least 35 wt%, at least 36 wt%, at least 37 wt%, at least 38 wt%, at least 39 wt%, at least 40 wt%, at least 41 wt%, or at least 42 wt% of C5 polysaccharides, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 25 wt% to about 35 wt% of C6 polysaccharides and about 23 wt% to about 45 wt% of C5 polysaccharides, based on the dried weight of the fiber rich products. In some examples, the fiber rich products in lines 217 and 317 can include about 27 wt% to about 30 wt% of C6 polysaccharides and about 24 wt% to about 28 wt% of C5 polysaccharides, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 28 wt% to about 33 wt% of C6 polysaccharides and about 38 wt% to about 45 wt% of C5 polysaccharides, based on the dried weight of the fiber rich products. In some examples, the fiber rich products in lines 217 and 317 can include at least 20 wt% to about 35 wt% of C6 polysaccharides and at least 20 wt% to about 45 wt% of C5 polysaccharides, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include at least 20 wt%, at least 21 wt%, at least 22 wt%, at least 23 wt%, at least 24 wt%, at least 25 wt%, at least 26 wt%, at least 27 wt%, at least 28 wt%, at least 29 wt%, or at least 30 wt% of a combined amount of glucan, galactan, mannan, and starch, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include at least 20 wt%, at least 21 wt%, at least 22 wt%, at least 23 wt%, at least 24 wt%, at least 25 wt%, at least 26 wt%, at least 27 wt%, at least 28 wt%, at least 29 wt%, at least 30 wt%, at least 31 wt%, at least 32 wt%, at least 33 wt%, at least 34 wt%, at least 35 wt%, at least 36 wt%, at least 37 wt%, at least 38 wt%, at least 39 wt%, at least 40 wt%, at least 41 wt%, or at least 42 wt% of a combined amount of xylan and arabinan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 25 wt% to about 35 wt% of a combined amount of glucan, galactan, mannan, and starch and about 23 wt% to about 45 wt% of a combined amount of xylan and arabinan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 27 wt% to about 30 wt% of a combined amount of glucan, galactan, mannan, and starch and about 24 wt% to about 28 wt% of a combined amount of xylan and arabinan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 28 wt% to about 33 wt% of a combined amount of glucan, galactan, mannan, and starch and about 38 wt% to about 45 wt% of a combined amount of xylan and arabinan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include at least 20 wt% to about 35 wt% of a combined amount of glucan, galactan, mannan, and starch and at least 20 wt% to about 45 wt% of a combined amount of xylan and arabinan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 12 wt%, about 13 wt%, about 14 wt%, about 15 wt%, about 16 wt%, about 17 wt%, or about 18 wt% to about 19 wt%, about 20 wt%, about 21 wt%, about 22 wt%, about 23 wt%, about 24 wt%, or about 25 wt% of glucan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 2 wt%, about 3 wt%, about 4 wt%, about 4.5 wt%, or about 5 wt% to about 6 wt%, about 6.5 wt%, about 7 wt%, about 7.5 wt%, about 8 wt%, about 8.5 wt%, about 9 wt%, about 9.5 wt%, or about 10 wt% of galactan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 1 wt%, about 1.3 wt%, about 1.5 wt%, about 1.7 wt%, about 2 wt%, about 2.3 wt%, or about 2.5 wt% to about 2.7 wt%, about 3 wt%, about 3.3 wt%, about 3.5 wt%, about 3.7 wt%, about 4 wt%, about 4.3 wt%, about 4.5 wt%, about 4.7 wt%, or about 5 wt% of starch, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 10 wt%, about 12 wt%, about 14 wt%, about 16 wt%, or about 18 wt% to about 20 wt%, about 22 wt%, about 24 wt%, about 26 wt%, or about 28 wt% of xylan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 7 wt%, about 8 wt%, about 9 wt%, or about 10 wt% to about 12 wt%, about 14 wt%, about 16 wt%, about 17 wt%, about 18 wt%, about 19 wt%, or about 20 wt% of arabinan, based on the dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 12 wt% to about 22 wt% of glucan, about 11 wt% to about 28 wt% of xylan, about 2.5 wt% to about 8 wt% of galactan, about 7 wt% to about 20 wt% of arabinan, and about 2 wt% to about 5 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich products in lines 217 and 317 can include about 16 wt% to about 22 wt% of glucan, about 14 wt% to about 28 wt% of xylan, about 5 wt% to about 8 wt% of galactan, about 8 wt% to about 20 wt% of arabinan, and about 3.7 wt% to about 5 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich products in lines 217 and 317 can include at least 16 wt% of glucan, at least 15 wt% of xylan, at least 5 wt% of galactan, at least 9 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich products in lines 217 and 317 can include at least 18 wt% of glucan, at least 16 wt% of xylan, at least 6 wt% of galactan, at least 9 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich products in lines 217 and 317 can include at least 20 wt% of glucan, at least 20 wt% of xylan, at least 6 wt% of galactan, at least 15 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich products in lines 217 and 317 can include about 10 wt%, about 13 wt%, or about 15 wt% to about 20 wt%, about 23 wt%, about 25 wt%, or about 27 wt% of structural protein based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 20 wt%, less than 19 wt%, less than 18 wt%, less than 17 wt%, less than 16 wt%, less than 15 wt%, or less than 14 wt% of structural protein, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include at least 19 wt%, at least 20 wt%, at least 21 wt%, or at least 22 wt% to about 23 wt%, about 24 wt%, about 25 wt%, or about 27 wt% of structural protein, based on a dried weight of the fiber rich product.
  • the fiber rich products in lines 217 and 317 can include less than 1.4 wt%, less than 1.3 wt%, less than 1.2 wt%, less than 1.1 wt%, less than 1 wt%, less than 0.9 wt%, less than 0.8 wt%, or less than 0.7 wt% of the inorganic compounds, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 5 wt%, less than 4.5 wt%, less than 4 wt%, less than 3.5 wt%, less than 3 wt%, less than 2.5 wt%, less than 2 wt%, or less than 1.7 wt% of the extractives.
  • the fiber rich products in lines 217 and 317 can include about 1.5 wt%, about 1.7 wt%, about 2 wt%, or about 2.3 wt% to about 2.7 wt%, about 3 wt%, about 3.5 wt%, or about 4 wt% of acetate, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include about 15 wt%, about 16 wt%, about 17 wt% or about 18 wt% to about 19 wt%, about 20 wt%, about 21 wt%, or about 22 wt% of lignin, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 1 wt% of the inorganic compounds, less than 2 wt% of the extractives, about 1.8 wt% to about 4 wt% of acetate, about 27 wt% to about 30 wt% of C6 polysaccharides, and about 24 wt% to about 28 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 1 wt% of the inorganic compounds, about 20 wt% to about 26 wt% of structural protein, less than 2 wt% of the extractives, about 2 wt% to about 4 wt% of acetate, about 27 wt% to about 30 wt% of C6 polysaccharides, and about 24 wt% to about 28 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 1 wt% of the inorganic compounds, less than 2 wt% of the extractives, about 1.8 wt% to about 4 wt% of acetate, about 20 wt% to about 25 wt% of structural protein, about 17 wt% to about 22 wt% of lignin, about 27 wt% to about 30 wt% of C6 polysaccharides, and about 24 wt% to about 28 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 1 wt% of inorganic compounds, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, about 28 wt% to about 33 wt% of C6 polysaccharides, and about 38 wt% to about 45 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 1 wt% of inorganic compounds, about 10 wt%to about 16 wt% of structural protein, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, about 28 wt% to about 33 wt% of C6 polysaccharides, and about 38 wt% to about 45 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich products in lines 217 and 317 can include less than 1 wt% of inorganic compounds, about 10 wt% to about 16 wt% of structural protein, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, about 17 wt% to about 22 wt% of lignin, about 28 wt% to about 33 wt% of C6 polysaccharides, and about 38 wt% to about 45 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the dried weight or solids weight of the fiber rich products, the stillage protein products, and other products can be determined via standard tests used in the industry.
  • the dried weight or solids weight of the fiber rich product, the stillage protein product, or other product can be determined according to the National Renewable Energy Laboratory (NREL) test, "Determination of Total Solids in Biomass and Total Dissolved Solids in Liquid Process Samples", Version 2008.
  • NREL National Renewable Energy Laboratory
  • the amount of the inorganic compounds, structural protein, extractives, acetate, lignin, C6 polysaccharides, and C5 polysaccharides in the fiber rich products can also be determined via standard tests used in the industry.
  • the amount of inorganic compounds in the fiber rich products can be determined according to the NREL Chemical Analysis and Standard Testing Procedure, "Determination of Ash in Biomass", Version 2005.
  • the amount of structural protein in the fiber rich products can be determined according to the NREL Chemical Analysis and Standard Testing Procedure, “Determination of Protein Content in Biomass", Version 2008.
  • the amount of extractives in the fiber rich products can be determined according to the NREL Chemical Analysis and Standard Testing Procedure, "Determination of Extractives in Biomass", Version 2005.
  • the amount of acetate, lignin, C6 polysaccharides, and C5 polysaccharides in the fiber rich products can be determined according to the NREL Chemical Analysis and Standard Testing Procedure, "Determination of Structural Carbohydrates and Lignin in Biomass", Version 2012.
  • the amount of starch in the fiber rich products can be determined according to the NREL Chemical Analysis and Standard Testing Procedure, "Determination of Starch in Solid Biomass Sample", Version 2005.
  • test procedure outlined in ASTM El 758-01 (2015) can be used to determine the amounts of any C6 polysaccharides and/or C5 polysaccharides in the fiber rich products in lines 217 and 317.
  • ASTM El 758-01 (2015) can be used to determine the amounts of any C6 polysaccharides and/or C5 polysaccharides in the fiber rich products in lines 217 and 317.
  • an AOAC, AACC, and/or ICC test procedure can be used. More particularly, in other examples the test procedures outlined in AOAC Method 996.11, AACC Method 76.13, and/or ICC Standard Method No. 168 can be used to determine the amount of starch in the fiber rich products in lines 217 and 317.
  • the amount of C6 polysaccharides, C5 polysaccharides, starch, and other components in the fiber rich products in lines 217 and 317 can be determined using any combination of these standardized tests or any other standardized test capable of determining the amount of any one or more of the carbohydrates or starch in the fiber rich products in lines 217 and 317.
  • the fiber rich products in lines 217 and 317 can have an ethanol potential of at least 90 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 91 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 92 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 93 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 94 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 95 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 96 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 97 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 98 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 99 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 100 gallons of ethanol per 1,000 kilograms of the fiber rich product, at least 101 gallons of ethanol per 1,000 kilograms
  • the fiber rich products in lines 217 and 317 can have an ethanol potential of about 92 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 96 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 99 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 103 gallons of ethanol per 1,000 kilograms of the fiber rich product, or about 105 gallons of ethanol per 1,000 kilograms of the fiber rich product to about 130 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 135 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 140 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 145 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 150 gallons of ethanol per 1,000 kilograms of the fiber rich product, or about 155 gallons of ethanol per 1,000 kilograms of the fiber rich product.
  • the fiber rich products in lines 217 and 317 can have an ethanol potential of about 90 gallons of ethanol per 1,000 kilograms of the fiber rich product to about 160 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 90 gallons of ethanol per 1,000 kilograms of the fiber rich product to about 145 gallons of ethanol per 1,000 kilograms of the fiber rich product, about 100 gallons of ethanol per 1,000 kilograms of the fiber rich product to about 110 gallons of ethanol per 1,000 kilograms of the fiber rich product, or about 130 gallons of ethanol per 1,000 kilograms of the fiber rich product to about 145 gallons of ethanol per 1,000 kilograms of the fiber rich product.
  • the ethanol potential of the fiber rich product is on a dry matter basis, / ' . e. , based on a dried weight of the fiber rich product.
  • the "ethanol potential" of the fiber rich product is measured in gallons of ethanol per 1,000 kilograms of the fiber rich product and is determined according to the following procedure.
  • the extractives are removed from the fiber rich product as outlined in the NREL Chemical Analysis and Standard Test Procedure, "Determination of Extractives in Bimass", Version 2005.
  • water is removed from the fiber rich product as outlined in the NREL Chemical Analysis and Standard Test Procedure, "Determination of Total Solids in Biomass", Version 2008.
  • the amounts of any glucan, any xylan, any galactan, any arabinan, and any mannan in the fiber rich product, after removing the extractives and the water, are determined as outlined in the NREL Chemical Analysis and Standard Test Procedure, "Determination of Structural Carbohydrates and Lignin in Biomass", Version 2012.
  • the amount of any starch in the fiber rich product, after removing the extractives and the water, is determined as outlined in the NREL Chemical Analysis Standard Test Procedure, "Determination of Starch in Solid Biomass Sample", Version 2005.
  • any glucan, any galactan, any mannan, and any starch are multiplied by 1,000 kg to determine the amount of any glucan, galactan, mannan, and starch in kilograms per 1,000 kg of the fiber rich product (FRP).
  • the mass (kg) of the glucan, galactan, mannan, and starch per 1,000 kg of the FRP are converted to mass (kg) monosaccharides per 1,000 kg of the FRP by multiplying the mass of the glucan, galactan, mannan, and starch by 1.11 to account for the molecule of water that adds to the polysaccharides when the sugar monomers are hydrolyzed from the polysaccharides.
  • the mass (kg) of the monosaccharides per 1,000 kg of the FRP is multiplied by 0.51 (conversion of kilograms sugar to kilograms ethanol assuming 100% of theoretical yield).
  • the kilograms of ethanol per 1,000 kg of the FRP is converted to liters (L) per 1,000 kg of the FRP by dividing the kilograms of ethanol by the density of ethanol (0.789 kg/L).
  • the liters of ethanol per 1,000 kg of the FRP is converted to gallons of ethanol per 1,000 kg of the FRP by dividing the liters of ethanol by 3.789.
  • the amounts (wt%) of any xylan and any arabinan are multiplied by 1,000 kg to determine the amount of any xylan and any arabinan in kilograms per 1,000 kg of the FRP.
  • the mass (kg) of the xylan and arabinan per 1,000 kg of the FRP are converted to mass (kg) of monosaccharides per 1,000 kg of the FRP by multiplying the mass fraction by 1.136 to account for the molecule of water that adds to the polysaccharides when the sugar monomers are hydrolyzed from the polysaccharides.
  • the mass (kg) of monosaccharides per 1,000 kg of the FRP is multiplied by 0.51 (conversion of kilograms sugar to kilograms ethanol assuming 100% of theoretical yield).
  • the kilograms of ethanol per 1,000 kg of the FRP is converted to liters (L) per 1,000 kg of the FRP by dividing the kilograms of ethanol by the density of ethanol (0.789 kg/L).
  • the liters of ethanol per 1,000 kg of the FRP is converted to gallons of ethanol per 1,000 kg of the FRP by dividing the liters of ethanol by 3.789.
  • the theoretical amount of ethanol per 1,000 kilograms of the FRP i.e. , the ethanol potential, that can potentially be produced from the glucan, galactan, mannan, and starch and the xylan and arabinan are added to provide the ethanol potential of the fiber rich products.
  • the ethanol potential of the fiber rich products in lines 217 and 317 is limited to any glucan, any galactan, any mannan, any starch, any xylan, and any arabinan present therein and does not include any additional C5 polysaccharides and any additional C6 polysaccharides.
  • the saccharification mash in line 236 and/or the saccharification mash produced within the fermenter 342 can be fermented in the fermenter 242 and 342, respectively, to produce at least 25 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 30 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 35 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 40 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 45 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 50 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 60 gallons
  • the saccharification mash in line 236 and/or the saccharification mash produced within the fermenter 342 can be fermented in the fermenter 242 and 342, respectively, to produce about 25 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 30 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 35 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 40 gallons of ethanol per 1,000 kilograms of the saccharification mash, or about 45 gallons of ethanol per 1,000 kilograms of the saccharification mash to about 50 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 55 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 60 gallons of ethanol per 1,000 kilograms of the saccharification mash, or about 65 gallons of ethanol per 1,000 kilograms of the saccharification mash
  • the saccharification mash in line 236 and/or the saccharification mash produced within the fermenter 342 can be fermented in the fermenter 242 and 342, respectively, to produce at least 25 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 30 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 35 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 40 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 45 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 50 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 55 gallons of ethanol per 1,000 kilograms of the saccharification mash, at least 60 gallons of ethanol per 1,000 kilograms of the saccharification mash, or at least
  • the saccharification mash in line 236 and/or the saccharification mash produced within the fermenter 342 can be fermented in the fermenter 242 and 342, respectively, to produce about 25 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 30 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 35 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 40 gallons of ethanol per 1,000 kilograms of the saccharification mash, or about 45 gallons of ethanol per 1,000 kilograms of the saccharification mash to about 50 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 55 gallons of ethanol per 1,000 kilograms of the saccharification mash, about 60 gallons of ethanol per 1,000 kilograms of the saccharification mash, or about 65 gallons of ethanol per 1,000 kilograms of the
  • the stillage protein products in lines 256 and/or 356 can include, but are not limited to, protein, fat, ash, neutral detergent fibers, acid detergent fibers, yeast, or any mixture thereof.
  • the stillage protein products in lines 256 and 356 can include about 40 wt%, about 45 wt%, or about 50 wt% to about 60 wt%, about 70 wt%, or about 80 wt% of protein, based on a dry weight of the stillage protein product.
  • each stillage protein products in lines 256 and 356 can include about 2 wt%, about 5 wt%, or about 8 wt% of fat to about 12 wt%, about 17 wt%, or about 20 wt% of the fat, based on the dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 0.5 wt%, about 1 wt%, or about 2 wt% to about 3 wt%, about 4 wt%, or about 5 wt% of ash, based on the dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 1 wt%, about 5 wt%, about 10 wt%, or about 15 wt% to about 20 wt%, about 25 wt%, or about 30 wt% of the neutral detergent fibers, based on the dry weight of the stillage protein product. In some examples, the stillage protein products in lines 256 and 356 can include about 1 wt%, about 2 wt%, or about 5 wt% to about 8 wt%, about 10 wt%, or about 15 wt% of acid detergent fibers, based on the dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 15 wt%, about 17 wt%, about 20 wt%, or about 23 wt% to about 25 wt%, about 27 wt%, about 30 wt%, about 33 wt%, or about 35 wt% of yeast, based on the dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include at least 15 wt%, at least 16 wt%, at least 17 wt%, at least 18 wt%, at least 19 wt%, at least 20 wt%, at least 21 wt%, at least 22 wt%, at least 23 wt%, at least 24 wt%, or at least 25 wt% to about 26 wt%, about 27 wt%, about 28 wt%, about 29 wt%, about 30 wt%, about 31 wt%, about 32 wt%, about 33 wt%, about 34 wt%, or about 35 wt% of yeast, based on the dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can also include water.
  • the stillage protein products in lines 256 and 356 can include about 4 wt%, about 5 wt%, about 6 wt%, or about 7 wt% to about 8 wt%, about 10 wt%, about 12 wt% of water, or about 15 wt% of water, based on a total weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, about 1 wt% to about 15 wt% of acid detergent fibers, and about 15 wt% to about 35 wt% of yeast, based on dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, about 2 wt% to about 12 wt% of acid detergent fibers, and about 18 wt% to about 32 wt% of yeast, based on dry weight of the stillage protein product, and about 4 wt% to about 15 wt% of water, based on a total weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 45 wt% to about 60 wt% of protein, about 2 wt% to about 8 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 12 wt% of neutral detergent fibers, about 5 wt% to about 8 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 45 wt% to about 60 wt% of protein, about 2 wt% to about 8 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 12 wt% of neutral detergent fibers, about 1 wt% to about 15 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on dry weight of the stillage protein product, and about 5 wt% to about 12 wt% of water, based on a total weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 50 wt% to about 54 wt% of protein, about 3 wt% to about 6 wt% of fat, about 1 wt% to about 4 wt% of ash, about 4 wt% to about 10 wt% of neutral detergent fibers, about 3 wt% to about 12 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 50 wt% to about 54 wt% of protein, about 3 wt% to about 6 wt% of fat, about 1 wt% to about 4 wt% of ash, about 4 wt% to about 10 wt% of neutral detergent fibers, about 5 wt% to about 15 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on dry weight of the stillage protein product, and about 5 wt% to about 12 wt% of water, based on a total weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 50 wt% to about 54 wt% of protein, about 3 wt% to about 5 wt% of fat, about 1 wt% to about 3 wt% of ash, about 6 wt% to about 7 wt% of neutral detergent fibers, about 5 wt% to about 8 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on dry weight of the stillage protein product.
  • the stillage protein products in lines 256 and 356 can include about 50 wt% to about 54 wt% of protein, about 3 wt% to about 5 wt% of fat, about 1 wt% to about 3 wt% of ash, and about 6 wt% to about 7 wt% of neutral detergent fibers, based on dry weight of the stillage protein product, and about 6 wt% to about 10 wt% of water, based on a total weight of the stillage protein product.
  • the protein in the stillage protein products can be determined according to the AOAC 990.03 (2000) test method.
  • the fat in the stillage protein products can be determined according to the AOAC 920.39 (2000) test method.
  • Ash is the inorganic residue (minerals) remaining after any water and organic matter have been removed by heating in a furnace.
  • the amount of ash in the stillage protein products can be determined according to test method AOAC 945.02 (2000).
  • the neutral detergent fiber (NDF) in the stillage protein products can be measured according to the Neutral Detergent Fiber in Feeds - Filter Bag Technique (for A200 and A2001), as developed and defined by Ankom Technology, and referred to as (NDF Method, Method 13, last revised on September 21, 2016).
  • the NDF is the residue remaining after digesting in a detergent solution.
  • the fiber residues are predominantly hemicellulose, cellulose, and lignin.
  • the acid detergent fiber (ADF) in the stillage protein products can be measured according to the Acid Detergent Fiber in Feeds - Filter Bag Technique (for A200 and A2001), as developed and defined by Ankom Technology, and referred to as (ADF Method, Method 12 last revised on September 21, 2016).
  • the ADF is the residue remaining after digesting with sulfuric acid and detergent solution.
  • the fiber residues are predominantly cellulose and lignin. Any water or moisture in the stillage protein products can be determined according to test method AOAC 934.01 (2000) test method.
  • the ground corn product can be quantified by having a particle size distribution, such as by weight percent (wt%) and/or volume percent (vol%), for specified particle sizes.
  • the particle size and the particle size distribution of the ground com product can be analyzed or otherwise determined by various particle size analyzers, such as laser diffraction analyzers, static and/or dynamic light scattering analyzers, zeta potential analyzers, sieve shaker with graduation test, and others.
  • particle size distribution of the ground com product by weight can be measured using sieves and the particle size distribution of the ground com product by volume can be measured by laser diffraction, as further discussed and described below.
  • the particle size and the particle size distribution of the ground com product by weight can be measured or otherwise determined with a sieve shaker, such as the RO-TAP ® RX-29 sieve shaker, commercially available from W. S. Tyler Industrial Group.
  • the sieves analysis can be performed according to the AOAC Official Method 965.22-1966, "Sorting Com Grits - Sieving Method," available from AOAC International.
  • Sieve sizes of 850 ⁇ , 425 ⁇ , 250 ⁇ , 180 ⁇ , 150 ⁇ , and 105 ⁇ can be used to categorize the particle size distribution of the ground com product by weight.
  • the amount of the ground corn product that can have a particle size of less than 100 ⁇ can be about 10 wt%, about 15 wt%, about 20 wt%, about 25 wt%, about 30 wt%, about 35 wt%, or about 40 wt% to about 45 wt%, about 50 wt%, about 55 wt%, about 60 wt%, about 65 wt%, about 70 wt%, about 75 wt%, or greater, as measured according to AOAC 965.22- 1966.
  • about 10 wt% to about 68 wt%, about 32 wt% to about 68 wt%, about 41 wt% to about 66 wt%, about 32 wt% to about 62 wt%, or about 35 wt% to about 58 wt% of the ground com product can have a particle size of less than 100 ⁇ , as measured according to AOAC 965.22-1966.
  • greater than 10 wt%, greater than 15 wt%, greater than 20 wt%, greater than 25 wt%, greater than 30 wt%, greater than 35 wt%, greater than 40 wt%, greater than 45 wt%, greater than 50 wt%, greater than 55 wt%, greater than 60 wt%, greater than 65 wt%, or greater than 70 wt% of the ground corn product can have a particle size of less than 100 ⁇ , as measured according to AOAC 965.22-1966.
  • greater than 10 wt%, greater than 15 wt%, greater than 20 wt%, greater than 25 wt%, greater than 30 wt%, greater than 35 wt%, greater than 40 wt%, greater than 45 wt%, or greater than 50 wt% to about 55 wt%, about 60 wt%, about 65 wt%, or about 70 wt% of the ground corn product can have a particle size of less than 100 ⁇ , as measured according to AOAC 965.22-1966.
  • the amount of the ground corn product that can have a particle size of 105 ⁇ or less can be about 30 wt%, about 35 wt%, or about 40 wt% to about 45 wt%, about 50 wt%, about 55 wt%, about 60 wt%, about 65 wt%, about 70 wt%, about 75 wt%, or greater, as measured according to AOAC 965.22-1966.
  • about 32 wt% to about 68 wt%, about 41 wt% to about 66 wt%, about 32 wt% to about 62 wt%, or about 35 wt% to about 58 wt% of the ground corn product can have a particle size of 105 ⁇ or less, as measured according to AOAC 965.22-1966.
  • greater than 30 wt%, greater than 35 wt%, greater than 40 wt%, greater than 45 wt%, greater than 50 wt%, greater than 55 wt%, greater than 60 wt%, greater than 65 wt%, or greater than 70 wt% of the ground corn product can have a particle size of 105 ⁇ or less, as measured according to AOAC 965.22-1966.
  • greater than 25 wt%, greater than 30 wt%, greater than 35 wt%, greater than 40 wt%, greater than 45 wt%, or greater than 50 wt% to about 55 wt%, about 60 wt%, about 65 wt%, or about 70 wt% of the ground corn product can have a particle size of greater than 105 ⁇ , as measured according to AOAC 965.22-1966.
  • the amount of the ground corn product that can have a particle size of 150 ⁇ or less can be about 41 wt% to about 79 wt%, about 57 wt% to about 90 wt%, about 57 wt% to about 78 wt%, or about 57 wt% to about 75 wt%, as measured according to AOAC 965.22-1966. In some examples, greater than 40 wt%, greater than 50 wt%, greater than 60 wt%, greater than 70 wt%, greater than 75 wt%, or greater than 80 wt% of the ground corn product can have a particle size of 150 ⁇ or less, as measured according to AOAC 965.22-1966.
  • the amount of the ground corn product that can have a particle size of 180 ⁇ or less can be about 52 wt% to about 97 wt%, about 58 wt% to about 90 wt%, about 56 wt% to about 81 wt%, or about 62 wt% to about 97 wt%, as measured according to AOAC 965.22-1966.
  • greater than 50 wt%, greater than 60 wt%, greater than 70 wt%, greater than 80 wt%, greater than 90 wt%, greater than 93 wt%, greater than 95 wt%, or greater than 97 wt% of the ground corn product can have a particle size of 180 ⁇ or less, as measured according to AOAC 965.22-1966.
  • the amount of the ground corn product that can have a particle size of 250 ⁇ or less can be about 71 wt% to about 98 wt%, about 81 wt% to about 98 wt%, about 91 wt% to about 98 wt%, or about 71 wt% to about 92 wt%, as measured according to AOAC 965.22-1966.
  • greater than 70 wt%, greater than 80 wt%, greater than 85 wt%, greater than 90 wt%, greater than 93 wt%, greater than 95 wt%, greater than 96 wt%, greater than 97 wt%, or greater than 98 wt% of the ground corn product can have a particle size of 250 ⁇ or less, as measured according to AOAC 965.22-1966.
  • the amount of the ground corn product that can have a particle size of 425 ⁇ or less can be about 87 wt% to about 96 wt%, about 87 wt% to about 95 wt%, about 87 wt% to about 99.9 wt%, or about 96 wt% to about 99.9 wt%, as measured according to AOAC 965.22-1966.
  • greater than 85 wt%, greater than 86 wt%, greater than 87 wt%, greater than 88 wt%, greater than 89 wt%, greater than 90 wt%, greater than 91 wt%, greater than 92 wt%, greater than 93 wt%, greater than 94 wt%, greater than 95 wt%, greater than 96 wt%, greater than 97 wt%, greater than 98 wt%, greater than 99 wt%, greater than 99.5 wt%, greater than 99.7 wt%, or greater than 99.9 wt% of the ground corn product can have a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966.
  • greater than 80 wt%, greater than 83 wt%, greater than 85 wt%, greater than 87 wt%, greater than 90 wt%, greater than 93 wt%, or greater than 95 wt% of the ground corn product can have a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966. In some examples 100% of the ground corn product can have a particle size of 425 ⁇ or less.
  • the amount of the ground corn product that can have a particle size of 850 ⁇ or less can be about 98 wt% to about 99.95 wt%, about 99.2 wt% to about 99.9 wt%, about 99.2 wt% to about 99.95 wt%, or about 99.9 wt% to about 99.95 wt%, as measured according to AOAC 965.22-1966.
  • greater than 97 wt%, greater than 98 wt%, greater than 99 wt%, greater than 99.3 wt%, greater than 99.5 wt%, greater than 99.7 wt%, greater than 99.9 wt%, greater than 99.91 wt%, greater than 99.93 wt%, or greater than 99.95 wt% of the ground corn product can have a particle size of 850 ⁇ or less, as measured according to AOAC 965.22-1966.
  • about 30 wt% to about 65 wt% of the ground corn product can have a particle size of 105 ⁇ or less; about 40 wt% to about 80 wt% of the ground corn product can have a particle size of 150 ⁇ or less; about 50 wt% to about 97 wt% of the ground corn product can have a particle size of 180 ⁇ or less; about 70 wt% to about 98 wt% of the ground corn product can have a particle size of 250 ⁇ or less; about 85 wt% to about 99.9 wt% of the ground corn product can have a particle size of 425 ⁇ or less; and about 98 wt% to about 99.95 wt% of the ground corn product can have a particle size of 850 ⁇ or less, as measured according to AOAC 965.22-1966.
  • greater than 30 wt%, greater than 40 wt%, greater than 50 wt%, or greater than 60 wt% of the ground com product can have a particle size of 105 ⁇ or less; greaterthan 40 wt%, greater than 50 wt%, greater than 60 wt%, or greater than 70 wt% of the ground com product can have a particle size of 150 ⁇ or less; greater than 50 wt%, greater than 60 wt%, greater than 70 wt%, or greater than 80 wt% of the ground com product can have a particle size of 180 ⁇ or less; greater than 70 wt%, greater than 80 wt%, greater than 90 wt%, or greater than 95 wt% of the ground com product for a particle size of 250 ⁇ or less; greaterthan 85 wt%, greater than 90 wt%, greaterthan 95 wt%, greater than 97 wt%, greater than 99 wt%, greater than 99.5 w
  • greater than 25 wt%, greater than 30 wt%, greater than 35 wt%, greater than 40 wt%, or greater than 45 wt% of the ground com product can have a particle size of greater than 105 ⁇ , and greater than 80 wt%, greater than 85 wt%, greater than 90 wt%, or greater than 95 wt% of the ground com product can have a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966.
  • the particle size and the particle size distribution of the ground com product by volume can be analyzed on a LSTM 13-320 laser diffraction particle size analyzer with a Tornado dry sample module attachment, both commercially available from Beckman Coulter Life Sciences.
  • the laser diffraction particle analysis can be conducted according to the ISO 13320:2009, "Particle Size Analysis - Laser Diffraction Methods," available from International Organization for Standardization.
  • the amount of the ground com product that can have a particle size of 25 ⁇ or less can be about 2 vol% to about 10 vol%, about 2 vol% to about 9 vol%, about 2 vol% to about 8 vol%, or about 3 vol% to about 10 vol%, as measured according to ISO 13320:2009. In some examples, greater than 2 vol%, greater than 4 vol%, greater than 6 vol%, greater than 8 vol%, or greater than 9 vol% of the ground corn product can have a particle size of 25 ⁇ or less, as measured according to ISO 13320:2009.
  • the amount of the ground corn product that can have a particle size of 60 ⁇ or less can be about 16 vol% to about 24 vol%, about 19 vol% to about 25 vol%, about 16 vol% to about 26 vol%, or about 19 vol% to about 28 vol%, as measured according to ISO 13320:2009.
  • greater than 10 vol%, greater than 13 vol%, greater than 15 vol%, greater than 17 vol%, greater than 18 vol%, greater than 20 vol%, greater than 22 vol%, greater than 23 vol%, greater than 25 vol%, greater than 28 vol%, greater than t 30 vol%, greater than 35 vol% of the ground corn product can have a particle size of 60 ⁇ or less, as measured according to ISO 13320:2009.
  • the amount of the ground corn product that can have a particle size of 400 ⁇ or less can be about 42 vol% to about 74 vol%, about 42 vol% to about 71 vol%, about 59 vol% to about 71 vol%, or about 54 vol% to about 71 vol% of the ground corn product can have a particle size of 400 ⁇ or less, as measured according to ISO 13320:2009.
  • greater than 40 vol%, greater than 45 vol%, greater than 50 vol%, greater than 55 vol%, greater than 60 vol%, greater than 65 vol%, or greater than 70 vol% of the ground corn product can have a particle size of 400 ⁇ or less, as measured according to ISO 13320:2009.
  • the amount of the ground corn product that can have a particle size of 800 ⁇ or less can be about 86 vol% to about 90 vol%, about 86 vol% to about 96 vol%, about 87 vol% to about 95 vol%, or about 87 vol% to about 96 vol%, as measured according to ISO 13320:2009. In some examples, greater than 85 vol%, greater than 87 vol%, greater than 89 vol%, greater than 90 vol%, greater than 93 vol%, greater than 94 vol%, or greater than 95 vol% of the ground corn product can have a particle size of 800 ⁇ or less, as measured according to ISO 13320:2009.
  • about 10 vol% to about 30 vol% of the ground corn product can have a particle size of 60 ⁇ or less; about 40 vol% to about 70 vol% of the ground corn product can have a particle size of 400 ⁇ or less; and about 85 vol% to about 95 vol% of the ground corn product can have a particle size of 800 ⁇ or less.
  • greater than 10 vol%, greater than 15 vol%, greater than 18 vol%, greater than 20 vol%, greater than 25 vol%, greater than 28 vol%, or greater than 30 vol% of the ground corn product can have a particle size of 60 ⁇ or less; greater than 40 vol%, greaterthan 50 vol%, greater than 55 vol%, greater than 60 vol%, or greater than 70 vol% of the ground corn product can have a particle size of 400 ⁇ or less; and greater than 85 vol%, greater than 90 vol%, or greater than 95 vol% of the ground corn product can have a particle size of 800 ⁇ or less.
  • greater than 18 vol% of the ground corn product can have a particle size of 60 ⁇ or less and greater than 50 vol% of the ground corn product can have a particle size of 400 ⁇ or less, as measured according to ISO 13320:2009.
  • greater than 20 vol% of the ground corn product can have a particle size of 60 ⁇ or less and greater than 60 vol% of the ground corn product can have a particle size of 400 ⁇ or less, as measured according to ISO 13320:2009.
  • greater than 18 vol% of the ground corn product can have a particle size of 60 ⁇ or less and greater than 85 vol% of the ground corn product can have a particle size of 800 ⁇ or less, as measured according to ISO 13320:2009.
  • greater than 50 vol% of the ground corn product can have a particle size of 400 ⁇ or less and greater than 85 vol% of the ground corn product can have a particle size of 800 ⁇ or less, as measured according to ISO 13320:2009.
  • greater than 22 vol% of the ground corn product can have a particle size of 60 ⁇ or less, greater than 60 vol% of the ground corn product having a particle size of 400 ⁇ or less, and greater than 90 vol% of the ground corn product can have a particle size of 800 ⁇ or less, as measured according to ISO 13320:2009.
  • the volumetric particle size distribution of the ground corn product can be provided by particle size, dv, where v is the volume percent of the ground corn product that has a particle size smaller than the specified value. For example, if the ground corn product has a dio by volume percent of 18 ⁇ , then 10 vol% of the ground corn product has a particle size of less than 18 ⁇ and 90 vol% of the ground corn product has a particle size of 18 ⁇ and larger. In another example, if the ground corn product has a dso by volume percent of 170 ⁇ , then 50 vol% of the ground corn product has a particle size of less than 170 ⁇ and 50 vol% of the ground corn product has a particle size of 170 ⁇ and larger.
  • the ground corn product has a ds>o by volume percent of 800 ⁇
  • 90 vol% of the ground corn product has a particle size of less than 800 ⁇
  • 10 vol% of the ground corn product has a particle size of 800 ⁇ and larger.
  • the ground corn product can have a dio by volume percent of 5 ⁇ , 10 ⁇ , 12 ⁇ , or 15 ⁇ to 20 ⁇ , 25 ⁇ , 30 ⁇ , 40 ⁇ , or 50 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a dio by volume percent of 10 ⁇ to 30 ⁇ , 10 ⁇ to 25 ⁇ , 10 ⁇ to 20 ⁇ , 12 ⁇ to 30 ⁇ , 12 ⁇ to 25 ⁇ , 12 ⁇ to 20 ⁇ , 14 ⁇ to 30 ⁇ , 14 ⁇ to 25 ⁇ , 14 ⁇ to 20 ⁇ , 15 ⁇ to 25 ⁇ , 16 ⁇ to 30 ⁇ , or 16 ⁇ to 25 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a d25 by volume percent of 30 ⁇ , 40 ⁇ , or 50 ⁇ to 55 ⁇ , 60 ⁇ , 70 ⁇ , 80 ⁇ , 90 ⁇ , 100 ⁇ , 110 ⁇ , 120 ⁇ , 130 ⁇ , 140 ⁇ , or 150 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a d25 by volume percent of 30 ⁇ to 120 ⁇ , 30 ⁇ to 110 ⁇ , 30 ⁇ to 101 ⁇ , 30 ⁇ to 93 ⁇ , 30 ⁇ to 88 ⁇ , 30 ⁇ to 75 ⁇ , 30 ⁇ to 66 ⁇ , 30 ⁇ to 55 ⁇ , 40 ⁇ to 120 ⁇ , 40 ⁇ to 101 ⁇ , 40 ⁇ to 93 ⁇ , 40 ⁇ to 88 ⁇ , 40 ⁇ to 75 ⁇ , 40 ⁇ to 66 ⁇ , 40 ⁇ to 55 ⁇ , 40 ⁇ to 48 ⁇ , 50 ⁇ to 120 ⁇ , 50 ⁇ to 110 ⁇ , 50 ⁇ to 101 ⁇ , 50 ⁇ to 97 ⁇ , 50 ⁇ to 93 ⁇ , 50 ⁇ to 75 ⁇ , or 50 ⁇ to 66 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a dso by volume percent of 100 ⁇ , 110 ⁇ , 125 ⁇ , or 150 ⁇ to 200 ⁇ , 250 ⁇ , 300 ⁇ , 350 ⁇ , 400 ⁇ , 450 ⁇ m, or 500 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a dso by volume percent of 100 ⁇ to 500 ⁇ , 100 ⁇ to 450 urn, 100 ⁇ to 400 ⁇ , 100 ⁇ to 350 urn, 100 ⁇ to 300 ⁇ , 100 ⁇ m to 250 ⁇ , 100 ⁇ m to 200 ⁇ , 100 ⁇ m to 150 ⁇ , 110 ⁇ m to 500 ⁇ , 110 ⁇ m to 400 ⁇ , 110 ⁇ to 300 ⁇ , 110 ⁇ to 250 ⁇ , 110 ⁇ to 200 ⁇ , 110 ⁇ to 150 ⁇ , 150 ⁇ to 500 ⁇ , 150 ⁇ to 450 ⁇ , 150 ⁇ to 400 ⁇ , 150 ⁇ to 350 ⁇ , 150 ⁇ to 300 ⁇ , 150 ⁇ to 250 ⁇ , 150 ⁇ to 200 ⁇ , or 150 ⁇ to 175 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a d75 by volume percent of 350 ⁇ , 375 ⁇ , 400 ⁇ , or 425 ⁇ to 450 ⁇ , 500 ⁇ , 550 ⁇ , 600 ⁇ , 650 ⁇ , or 700 ⁇ m, as measured according to ISO 13320:2009.
  • the ground corn product can have a d75 by volume percent of 350 ⁇ to 700 ⁇ , 350 ⁇ to 650 ⁇ , 350 ⁇ to 600 ⁇ , 350 ⁇ to 550 ⁇ , 350 ⁇ to 500 ⁇ , 350 ⁇ to 450 ⁇ , 350 ⁇ to 400 ⁇ , 375 ⁇ to 700 ⁇ , 375 ⁇ to 600 ⁇ , 375 ⁇ to 500 ⁇ , 375 ⁇ to 450 ⁇ , 375 ⁇ m to 400 ⁇ , 400 ⁇ m to 700 ⁇ , 400 ⁇ m to 600 ⁇ , 400 ⁇ m to 500 ⁇ , 425 ⁇ m to 700 ⁇ , 425 ⁇ m to 650 ⁇ , 425 ⁇ m to 600 ⁇ , 425 ⁇ m to 550 ⁇ , or 425 ⁇ to 500 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a ds>o by volume percent of 650 ⁇ , 700 ⁇ , 750 ⁇ , or 800 ⁇ to 850 ⁇ , 900 ⁇ , 950 ⁇ , 1,000 ⁇ , 1,050 ⁇ m, or 1,100 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product can have a ds>o by volume percent of 650 ⁇ ⁇ 1, 100 ⁇ , 675 ⁇ to 1,100 ⁇ , 700 ⁇ m to 1, 100 ⁇ , 725 ⁇ m to 1,100 ⁇ , 750 ⁇ to 1, 100 ⁇ , 800 ⁇ to 1, 100 ⁇ , 850 ⁇ to 1, 100 ⁇ , 650 ⁇ to 1,000 ⁇ , 675 ⁇ ⁇ 1,000 ⁇ , 700 ⁇ ⁇ 1,000 ⁇ , 725 ⁇ ⁇ 1,000 ⁇ , 750 ⁇ ⁇ 1,000 ⁇ , 800 ⁇ to 1,000 ⁇ , 850 ⁇ to 1,000 ⁇ , 650 ⁇ to 950 ⁇ , 700 ⁇ to 950 ⁇ , 725 ⁇ to 950 ⁇ , 750 ⁇ to 950 ⁇ , 800 ⁇ to 950 ⁇ , 850 ⁇ to 950 ⁇ , 650 ⁇ to 950 ⁇ , 850 ⁇ to 950 ⁇ , 650 ⁇ to 900 ⁇ , 650 ⁇ to 900 ⁇ , 675
  • the ground corn product can include, but is not limited to, pericarp particles, floury endosperm particles, germ particles, starch particles, and fiber particles.
  • the starch portions and the germ portions of the corn kernels can be size-reduced to smaller sizes than the fibrous portions of the corn kernels. It is believed that this difference in sizes of the corn portions is a result of the shearing action of the milling device (e.g., air swept pulverizer or disk mill fiberizer).
  • the ground corn product therefore, can include fiber particles with different particle size distributions than the total particles of the ground corn product.
  • the fiber particles of the ground corn product can have a dso by volume percent of 125 ⁇ , 150 ⁇ , or 250 ⁇ to 300 ⁇ , 350 ⁇ , 400 ⁇ , or 500 ⁇ and the total particles of the ground corn product can have a dso by volume percent of 100 ⁇ , 125 ⁇ , or 150 ⁇ to 200 ⁇ , 300 ⁇ , 400 ⁇ , or 500 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a dso by volume percent of 125 ⁇ to 450 ⁇ , 150 ⁇ to 450 ⁇ , or 175 ⁇ to 400 ⁇ and the total particles of the ground corn product can have a dso by volume percent of 100 ⁇ to 400 ⁇ , 100 ⁇ to 350 ⁇ , or 125 ⁇ to 300 ⁇ , as measured according to ISO 13320:2009.
  • a plurality of total particles of the ground corn product can include a plurality of fiber particles.
  • the fiber particles in the ground corn product can have a dio by volume percent of greater than 160 ⁇ , greater than 180 ⁇ , greater than 200 ⁇ , greater than 250 ⁇ , greater than 300 ⁇ , or greater than 350 ⁇ to 500 ⁇ and the total particles of the ground corn product can have a dso by volume percent of 100 ⁇ to less than 300 ⁇ , less than 350 ⁇ , less than 450 ⁇ , or less than 500 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a dso by volume percent of greater than 200 ⁇ and the total particles of the ground corn product can have a dso by volume percent of less than 500 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a dso by volume percent of greater than 250 ⁇ and the total particles of the ground corn product can have a dso by volume percent of less than 450 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a dso by volume percent of greater than 300 ⁇ and the total particles of the ground corn product can have a dso by volume percent of less than 400 ⁇ , as measured according to ISO 13320:2009. In other examples, the fiber particles of the ground corn product can have a dso by volume percent of greater than 350 ⁇ and the total particles of the ground corn product can have a dso by volume percent of less than 350 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a dso by volume percent of greater than 200 ⁇ to 500 ⁇ and the total particles of the ground corn product can have a dso by volume percent of 100 ⁇ to less than 500 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a d75 by volume percent of 375 ⁇ , 400 ⁇ , or 450 ⁇ to 500 ⁇ , 600 ⁇ , or 700 ⁇ and the total particles of the ground corn product can have a d75 by volume percent of 350 ⁇ , 400 ⁇ , or 425 ⁇ to 450 ⁇ , 500 ⁇ , 600 ⁇ , or 700 ⁇ , as measured according to ISO 13320:2009.
  • the fiber particles of the ground corn product can have a d75 by volume percent of 375 ⁇ to 700 ⁇ , 400 ⁇ to 600 ⁇ , or 450 ⁇ to 700 ⁇ and the total particles of the ground corn product can have a d75 by volume percent of 350 ⁇ to 600 ⁇ , 350 ⁇ to 500 ⁇ , or 325 ⁇ to 550 ⁇ , as measured according to ISO 13320:2009.
  • the ground corn product or any portion thereof can have a combination of any two or more properties discussed and described above or elsewhere herein.
  • the ground corn product can have a combination of any two, any three, any four, or more, of the following properties: the particle size by weight, the particle size by volume, the particle size distribution by weight, the particle size distribution by volume, the dio value, the d25 value, the dso value, the d75 value, the ds>o value, and the crystallinity, which are discussed and described above or elsewhere herein.
  • the ground corn product and the corn pieces (e.g. , corn kernels) from which the ground corn product is ground can have the same composition or substantially the same composition.
  • the corn pieces and the ground corn product can contain, but are not limited to, water, one or more starches (e.g., saccharides and oligosaccharides), one or more proteins, cellulose, one or more oils and/or greases (e.g., saturated and unsaturated fatty acids), one or more volatile organic compounds, other components, or any combination thereof.
  • the corn pieces and the ground corn product can each include about 5 wt% to about 40 wt% of water, about 15 wt% to about 25 wt% of oligosaccharides, and about 0.5 wt% to about 5 wt% of corn oil.
  • the corn oil can be or include one or more oils and/or one or more greases which can include one or more saturated fatty acids and/or one or more unsaturated fatty acids.
  • Illustrative saturated fatty acids and unsaturated fatty acids that can be contained in the corn pieces and the ground corn product can be or include caprylic acid, capric acid, myristic acid, palmitic acid, stearic acid, arachidic acid, oleic acid, linoleic acid, linolenic acid, isomers thereof, or any mixture thereof.
  • the corn oil can include about 10 wt% to about 15 wt% of palmitic acid, about 1 wt% to about 2 wt% of stearic acid, about 0.5 wt% to about 2 wt% of arachidic acid, about 20 wt% to about 40 wt% of oleic acid, about 45 wt% to about 65 wt% of linoleic acid, and about 0.5 wt% to about 2 wt% of linolenic acid.
  • the corn pieces and the ground corn product can include about 0.5 wt%, about 0.8 wt%, about 1 wt%, about 1.5 wt%, or about 1.8 wt% to about 2 wt%, about 2.2 wt%, about 2.5 wt%, about 2.7 wt%, about 3 wt%, about 3.2 wt%, about 3.5 wt%, about 3.7 wt%, about 4 wt%, about 4.5 wt%, or more of corn oil, based on a solids weight of the corn pieces or the ground corn product.
  • the corn pieces and the ground corn product can include about 0.5 wt% to about 4.5 wt%, about 0.5 wt% to about 4 wt%, about 0.5 wt% to about 3.5 wt%, about 0.5 wt% to about 3 wt%, about 0.5 wt% to about 2.5 wt%, about 0.5 wt% to about 2 wt%, about 0.5 wt% to about 1.5 wt%, about 0.5 wt% to about 1 wt%, about 1 wt% to about 4.5 wt%, about 1 wt% to about 4 wt%, about 1 wt% to about 3.5 wt%, about 1 wt% to about 3 wt%, about 1 wt% to about 2.5 wt%, about 1 wt% to about 2 wt%, about 1 wt% to about 1.5 wt%, about 1 wt% to about 1.3 wt%, about 2 wt%,
  • the corn pieces and the ground corn product can include about 5 wt% to about 40 wt% of water, about 15 wt% to about 25 wt% of soluble starches, about 5 wt% to about 15 wt% of cellulose, and about 0.5 wt% to about 4 wt% of corn oil, based on a solids weight of the corn pieces or the ground corn product.
  • the corn pieces and the ground corn product can include about 10 wt% to about 35 wt% of water, about 17 wt% to about 28 wt% of soluble starches, about 10 wt% to about 15 wt% of cellulose, and about 2 wt% to about 4 wt% of corn oil, based on a solids weight of the corn pieces or the ground corn product.
  • Corn pieces e.g., corn kernels
  • the corn pieces can be milled, ground, pulverized, fiberized, or otherwise size-reduced to produce the ground corn product.
  • the corn pieces can also be milled, ground, pulverized, fiberized, or otherwise size-reduced two, three, or more times to produce the ground corn product.
  • the plurality of corn pieces therefore, can be or include size-reduced corn that is further size-reduced to produce the ground corn product.
  • Illustrative corn pieces that are suitable to be size-reduced can be or include, but are not limited to, whole corn kernels, milled corn kernels, pulverized corn kernels, fiberized corn kernels, ground corn kernels, fragmented corn kernels, crushed corn kernels, smashed corn kernels, shredded corn kernels, other size-reduced corn kernels, fresh corn kernels, dried corn kernels, or any mixture thereof.
  • the corn pieces can be size-reduced one or more times with a hammer mill, a roller mill, or other type of mill to produce the plurality of corn pieces that can be further size-reduced one or more times with a high shear mill to produce the ground corn product.
  • the corn pieces can be passed through one or more hammer mills to produce size-reduced corn that subsequently can be passed through a disk mill fiberizer, an air swept pulverizer, and/or any other high shear mills to produce the ground corn product.
  • the ground corn product can be or include fiberized corn, pulverized corn, disk milled corn, other high shear milled corn, or any mixtures thereof.
  • the corn pieces can be introduced to a high shear mill that can have two rotating surfaces, such as a first rotatable disk and a second rotatable disk.
  • the corn pieces can be introduced to a high shear mill that can have one rotating surface and one stationary surface, such as one rotatable disk and one stationary disk, plate, or other surface.
  • the corn pieces can make contact to the two rotating surfaces or can make contact to the one rotating surface and the one stationary surface to mill, shear, grind, fiberize, pulverize, or otherwise size-reduce the corn pieces between the two rotating surfaces or between the one rotating surface and the one stationary surface to produce the ground corn product.
  • the high shear mill can be a disk attrition mill and the corn pieces can be milled or otherwise side-reduced between: a rotatable disk and a stationary disk; a rotatable disk and a stationary surface; or two rotatable disks to produce the ground corn product.
  • the corn pieces can be fiberized between two sets of triangular teeth, relatively sharp teeth, or fiberizing teeth of the disk attrition mill to produce fiberized corn product.
  • the corn pieces can be pulverized between two sets of rectangular teeth, relatively dull teeth, or pulverizing teeth of the disk attrition mill to produce pulverized corn product.
  • at least one disk can have grinding teeth for fiberizing the corn pieces into the ground corn product.
  • Disk attrition mills can be used to fiberize and/or pulverize. Some disk attrition mills can have a fiberizing side and a pulverizing side which are independent from each other. Disk attrition mills that can be used to mill, grind, or otherwise size-reduce corn can include, for example, the 167.64 cm (66 inch) fiberizer, commercially available from Reynolds Engineering and Equipment, Inc.
  • the corn pieces can be introduced into a disk attrition mill, such as a high shear fiberizer or a high shear pulverizer.
  • the disk attrition mill can include a first rotatable disk and either a second rotatable disk or a stationary surface.
  • the disk attrition mill can have at least one set of grinding teeth disposed on each of the first rotatable disk, the second rotatable disk, and the stationary surface. In some configurations, any of the first rotatable disk, the second rotatable disk, or the stationary surface can be free of grinding teeth.
  • the first rotatable disk can have a first set of grinding teeth and either the second rotatable disk or the stationary surface is free of grinding teeth. In other examples of the disk attrition mill, the first rotatable disk can have a first set of grinding teeth and either the second rotatable disk or the stationary surface can have a second set of grinding teeth.
  • the first rotatable disk and either the second rotatable disk or the stationary surface can be separated by a predetermined distance from each other to provide a shearing gap therebetween.
  • the predetermined distance can be fixed or adjustable. If the first rotatable disk and/or either the second rotatable disk or the stationary surface have one or more sets of grinding teeth, then the shearing gap can be measured by the distance between two sets of grinding teeth or between one set of grinding teeth and either the rotatable disk or the stationary surface. For example, the shearing gap can be measured by the distance between the first set of grinding teeth on the first rotatable disk and the second set of grinding teeth on either the second rotatable disk or the stationary surface.
  • the shearing gap can be measured by the distance between the first set of grinding teeth on the first rotatable disk and either the second rotatable disk or the stationary surface absent of grinding teeth.
  • the shearing gap can be adjusted and/or can be maintained before and/or during the milling of the corn pieces to produce the ground corn product.
  • the shearing gap can be adjusted to produce the ground corn product having the particle size of the ground corn product and a desired distribution of the particle size of the ground corn product. Once the ground corn product is produced within the shearing gap, the ground corm product can pass through the shearing gap to exit the disk mill.
  • the shearing gap or the distance between the first rotatable disk and/or eitherthe second rotatable disk or the stationary surface can be less than 3,000 ⁇ , less than 2,600 ⁇ , less than 2,000 ⁇ , less than 1,500 ⁇ , less than 1,000 ⁇ , less than 800 ⁇ , less than 500 ⁇ , or less than 250 ⁇ .
  • the shearing gap or the distance between the first rotatable disk and/or either the second rotatable disk or the stationary surface can be about 50 ⁇ , about 100 ⁇ , about 150 ⁇ , or about 250 ⁇ to about 300 ⁇ , about 500 ⁇ , about 700 ⁇ , about 800 ⁇ , about 1,000 ⁇ , about 1,500 ⁇ , about 2,000 ⁇ , about 2,500 ⁇ , or about 2,750 ⁇ .
  • the shearing gap or the distance between the first rotatable disk and/or either the second rotatable disk or the stationary surface can be about 250 ⁇ to about 3,000 ⁇ , about 400 ⁇ to about 2,000 ⁇ , about 500 ⁇ to about 1,000 ⁇ , about 700 ⁇ to about 800 ⁇ , about 700 ⁇ to about 2,800 ⁇ , or about 600 ⁇ to about 2,600 ⁇ .
  • the corn pieces can be ground, milled, fiberized, pulverized, or otherwise size-reduced to produce the ground corn product that maintains at least a substantial amount of the crystallinity relative to the corn pieces ground to produce the ground corn product.
  • the ground corn product can have a crystallinity that is greater than 75%, about 80%, about 85%, or about 90% to about 92%, about 94%, about 95%, about 96%, about 97%, about 98%, about 99%, about 99.2%, about 99.5%, about 99.7%, about 99.8%, about 99.9%, about 99.95%, about 99.97%, about 99.98%, about 99.99%, or 100%, as compared to the crystallinity of the corn pieces ground to produce the ground corn product.
  • the ground corn product can have a crystallinity that is greater than 75%, greater than 80%, greater than 85%, greater than 90%, greater than 92%, greater than 94%, greater than 95%, greater than 96%, greater than 97%, greater than 98%, greater than 99%, greater than 99.2%, greater than 99.5%, greater than 99.7%, greater than 99.8%, greater than 99.9%, greater than 99.95%, greater than 99.97%, greater than 99.98%, greater than 99.99%, or 100%, as compared to the crystallinity of the corn pieces ground to produce the ground corn product.
  • the ground corn product can have a crystallinity that is about 80% to 100%, about 85% to 100%, about 90% to 100%, about 95% to 100%, about 97% to 100%, about 98% to 100%, about 99% to 100%, about 99.5% to 100%, about 99.9% to 100%, about 99.95% to 100%, about 75% to about 99%, about 80% to about 99%, about 85% to about 99%, about 90% to about 99%, about 95% to about 99%, about 97% to about 99%, about 98% to about 99%, or about 98.5% to about 99%, as compared to the crystallinity of the corn pieces ground to produce the ground corn product.
  • the ground corn product can have a crystallinity that is greater than 75% to 100%, greater than 80% to 100%, greater than 85%to 100%, greaterthan 90% to 100%, greater than 95% to 100%, greater than 97% to 100%, greater than 98% to 100%, greater than 99% to 100%, greater than 99.5% to 100%, greater than 99.9% to 100%, greater than 99.95% to 100%, greater than 75% to about 99%, greater than 80% to about 99%, greaterthan 85% to about 99%, greaterthan 90% to about 99%, greater than 95% to about 99%, greater than 97% to about 99%, greater than 98% to about 99%, or greater than 98.5% to about 99%, as compared to the crystallinity of the corn pieces ground to produce the ground corn product.
  • the ground corn product can have a crystallinity that is reduced by less than 25%, less than 23%, less than 20%, less than 17%, less than 15%, less than 12%, less than 10%, less than 8%, less than 6%, less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.5%, less than 0.3%, less than 0.2%, less than 0.1%, less than 0.05%, less than 0.03%, or less than 0.01%, as compared to the crystallinity of the corn pieces ground to produce the ground corn product.
  • the ground corn product can have a crystallinity that is reduced by less than 25% to about 0.001%, less than 25% to about 0.01%, less than 25% to about 0.05%, less than 25% to about 0.1%, less than 10% to about 0.001%, less than 10% to about 0.05%, less than 10% to about 0.1%, less than 5% to about 0.001%, less than 5% to about 0.01%, less than 5% to about 0.05%, less than 5% to about 0.1%, less than 1% to about 0.001%, less than 1% to about 0.01%, less than 1% to about 0.05%, less than 1% to about 0.1%, less than 0.1% to about 0.001%, less than 0.1% to about 0.01%, less than 1% to about 0.05%, less than 1% to about 0.1%, less than 0.1% to about 0.001%, less than 0.1% to about 0.01%, less than 0.1% to about 0.08%, or less than 0.1% to about 0.04%, as compared to the crystallinity of the corn pieces ground to produce the ground corn
  • crystallinity refers to a volume ratio of the crystalline portion of cellulose to the total volume of cellulose that includes both the amorphous portion and the crystalline portion.
  • the degree of crystallinity of the ground corn product can be calculated from X-ray diffraction (XRD) data by using a crystalline area integration method based on Cheetham and Leping (Carbohydrate Polymers 36:277-284 (1998)); Nara et al. (Starch 35,12:407-410 (1983)); and Benedetti et al. (Journal of Material Science 18.4: 1039-1048 (1983)).
  • the intensities are first normalized over a limited range of data (e.g., 10° to 30° 2- theta).
  • the normalization is determined by a baseline connecting the upper and lower bounds of 10° and 30° 2-theta and then dividing the intensities by the integrated area below the intensities curve and above the baseline.
  • a Savitzky-Golay filter is used to smooth the data.
  • the crystalline and amorphous regions can be separated by a function that connects peak baselines.
  • the crystalline portion is the upper region and the amorphous portion is the lower region.
  • the crystalline portion area and the total diffraction area are integrated.
  • the degree of crystallinity is defined as the ratio of the crystalline area over the total diffraction area.
  • At least a portion of the corn oil can be extracted or otherwise removed from the ground corn product, the slurry tank mixture containing the ground corn product, the liquefaction mash derived from the ground corn product, the fermentation mash, and/or the stillage.
  • the portion of the corn oil that is extracted from the ground corn product is the oil liberated from the corn cellular matrix within the ground corn product and any other oil that is bound by the corn cellular matrix remains in the ground corn product.
  • the corn oil extraction and the corn oil testing can be performed on the SPE-DEX ® 3000XL Automated Extractor System and the SPEED-VAPTM Solvent Evaporation System, both commercially available from the Horizon Technology Company, using EPA Method 1664A.
  • the corn oil removed from the ground corn product can be greater than 0.6 wt%, greater than 0.7 wt%, or greater than 0.75 wt% to about 0.9 wt%, about 1 wt%, about 1.2 wt%, or greater of the total weight of the ground corn product.
  • the corn oil removed from the ground corn product can be greater than 0.6 wt% to about 1.2 wt%, greater than 0.65 wt% to about 1.1 wt%, or greater than 0.7 wt% to about 1.05 wt% of the total weight of the ground corn product.
  • the corn oil removed from the ground corn product can be greater than 0.6 wt%, greater than 0.7 wt%, greater than 0.75 wt%, greater than 0.8 wt%, or greater than 0.85 wt% to about 0.9 wt%, about 1 wt%, about 1.2 wt%, about 1.3 wt%, about 1.4 wt%, about 1.5 wt%, about 1.6 wt%, about 1.7 wt%, about 1.8 wt%, about 1.9 wt%, about 2 wt%, about 2.3 wt%, about 2.5 wt%, about 2.7 wt%, about 3 wt%, about 3.3 wt%, about 3.5 wt%, about 3.7 wt%, about 4 wt%, or greater of the total weight of the ground corn product.
  • Examples 1-4 the following mill or mills were used as specified in each example.
  • the hammer mill was a Model MG mill, manufactured by Kelly Duplex Mill and Manufacturing Company in Springfield, Ohio.
  • the pulverizer was a Model 16-H air swept pulverizer manufactured by Schutz-O'Neill Company in Minneapolis, Minnesota.
  • the disk mill fiberizer was a Model TOQ-18 fiberizer, manufactured by Reynolds Engineering & Equipment, Inc. in Muscatine, Iowa.
  • Ex. 1 was corn that was passed through the hammer mill and through the air swept pulverizer.
  • Raw whole corn kernels were milled to produce hammermilled corn pieces.
  • the hammer mill was operated at about 90 Hz with a tip speed of about 124 meters per second (about 24,500 fpm) using a number 8 screen (3.175 mm) or (8/64", or 0.125") at a feed rate of about 925 kg/hr (about 2,040 lbs/hr).
  • the hammermilled corn pieces were pulverized in the air swept pulverizer to produce the ground corn product.
  • the air swept pulverizer was operated at about 80 Hz with a tip speed of about 157 meters per second (about 30,840 fpm) using three 43.18 cm (about 17-inch) diameter CCD beater plates and a CLP liner at a feed rate of about 599 kg/hr (about 1,320 lbs/hr).
  • Ex. 2 was the same as Ex. 1, but the speed of the air swept pulverizer was reduced as compared to the air swept pulverizer in Ex. 1.
  • Raw whole corn kernels were milled to produce hammermilled corn pieces.
  • the hammer mill was operated at about 90 Hz with a tip speed of about 124 meters per second (about 24,500 fpm) using a number 8 screen (3.175 mm) or (8/64", or 0.125") at a feed rate of about 925 kg/hr (about 2,040 lbs/hr).
  • the hammermilled corn pieces were pulverized in the air swept pulverizer to produce the ground corn product.
  • the air swept pulverizer was operated at about 50 Hz with a tip speed of about 97.9 meters per second (about 19,270 fpm) using three 43.18 cm (about 17-inch) diameter CCD beater plates and a CLP liner at a feed rate of about 599 kg/hr (about 1,320 lbs/hr).
  • Ex. 3 was whole corn that was only run through a disk mill fiberizer.
  • Raw whole corn kernels were milled in the disk mill fiberizer to produce the ground corn product.
  • the disk mill fiberizer used a 45.72 cm ( 18-inch) diameter TQ 18-016 fine tooth plates set with a gap of about 762 ⁇ (about 0.030 inches) and was operated at about 60 Hz with a tip speed of about 124 meters per second (about 24,500 fpm) at a feed rate of about 413 kg/hr (about 910 lbs/hr).
  • Ex. 4 was corn that was passed through a hammer mill and a disk mill fiberizer.
  • Raw whole corn kernels were milled to produce hammermilled corn pieces.
  • the hammer mill was operated at about 90 Hz with a tip speed of about 124 meters per second (about 24,500 fpm) using a number 8 screen (3.175 mm) or (8/64", or 0.125") at a feed rate of about 925 kg/hr (about 2,040 lbs/hr).
  • the hammermilled corn pieces were milled in the disk mill fiberizer to produce the ground corn product.
  • the disk mill fiberizer used 45.72 cm (about 18-inch) diameter TQ18-016 fine tooth plates set with a gap of about 2.54 mm (about 0.100 inches) and was operated at about 60 Hz with a tip speed of about 124 meters per second (about 24,500 fpm) at a feed rate of about 1,890 kg/hr (about 4, 170 lbs/hr).
  • CEx. 1 was corn that was passed through a hammer mill.
  • CEx. 2 was corn that was run through a quad pair set up (a stack of 4 pairs of rolls) roller mill.
  • the corn used in Exs. 1-4 were sourced locally in Muscatine, Iowa; the corn used in CEx. 1 was sourced from a Flint Hills Resources Fairbank facility; and the corn used in CEx. 2 was sourced from RMS in Tea, South Dakota.
  • Table 1 shows the particle size by weight of the ground corn products as measured with sieves for Exs. 1-4 and CExs. 1-2.
  • the sieves analysis was conducted according to the AOAC Official Method 965.22 "Sorting Corn Grits - Sieving Method," available from the AOAC International.
  • the weight percent of the sample that was left on the specified sieve size had a particle size larger than the respective sieve size.
  • Table 1 the sample particles in Ex.
  • wt% particles had the following weight percent (wt%) particles for the respective particle sizes: 0.10 wt% larger than 850 ⁇ , 3.60 wt% larger than 425 ⁇ to 850 ⁇ , 4.80 wt% larger than 250 ⁇ to 425 ⁇ , 1.50 wt% larger than 180 ⁇ to 250 ⁇ , 14.90 wt% larger than 150 ⁇ to 180 ⁇ , 9.75 wt% larger than 105 ⁇ to 150 ⁇ , and 65.35 wt% 105 ⁇ or less in the pan.
  • Table 2 shows the particle size by volume of the ground corn products and Table 3 shows the particle size distribution by volume of the ground corn products that were analyzed on a LSTM 13-320 laser diffraction particle size analyzer with a Tornado dry sample module attachment, both commercially available from Beckman Coulter Life Sciences.
  • the laser diffraction particle analysis was conducted according to the ISO 13320:2009 "Particle Size Analysis - Laser Diffraction Methods" .
  • the particle size by volume of the ground corn products shown in Table 2 is smaller than the particle size listed.
  • 10 vol% of the particles in the Ex. 3 sample had a particle size smaller than 17.68 ⁇ .
  • Table 3 gives the complete distribution of particles within each of the listed size ranges. For example: 28.3 vol% of the particles in the Ex. 3 sample had a particle size of greater than 4 ⁇ (e.g., about 4.01 um) to about 60 ⁇ .
  • each ground corn sample was combined with about 200 mL of water having a temperature of about 80°C to provide a slurry of about 35 wt% of ground corn.
  • About 1 mL of alpha amylase was added to the slurry.
  • Enough 1.2 M HC1 was added to each slurry to adjust the pH of the slurry to about 4.
  • Each slurry sample was then placed in a shaker water bath at about 85°C for about 60 min. After removing slurry sample from the shaker bath, about 0.3 mL of 12 M HC1 was added to lower the slurry pH and arrest the amylase activity. The time needed to complete each process of liquefaction for each sample slurry was kept constant to limit sample to sample variability.
  • the first sample (Comparative Example 3 (CEx. 3) was a wet cake produced by separating ethanol from a fermentation mash to provide the wet cake.
  • the ground corn that was subjected to the first or primary fermentation that produced the fermentation mash was ground with a hammermill (Roskamp Champion Champion Series 48 x 38).
  • the particle size distribution of the ground corn is similar to the CEx. 1 distribution given above. The whole stillage was not subjected to a fiber/protein separation process.
  • the second sample (Example 5 (Ex. 5) was a fiber product produced by separating a whole stillage into a fiber rich product and a protein product.
  • the ground corn that was subjected to the first or primary fermentation that produced the fermentation mash from which the whole stillage was separated was ground with a hammermill (Roskamp Champion Champion Series 48 x 38).
  • the particle size distribution of the ground corn was similar to the CEx. 1 distribution given above.
  • the third sample (Example 6 (Ex. 6) was a fiber product produced by separating a whole stillage into a fiber rich product and a protein product.
  • the ground corn that was subjected to the first or primary fermentation that produced the fermentation mash from which the whole stillage was separated was ground with the disk mill fiberizer, i.e. , Model TOQ-18 fiberizer, manufactured by Reynolds Engineering & Equipment, Inc. in Muscatine, Iowa.
  • the fourth sample was a fiber product produced by separating a whole stillage into a fiber rich product and a protein product.
  • the ground corn that was subjected to the first or primary fermentation that produced the fermentation mash from which the whole stillage was separated was ground with the disk mill fiberizer, i.e. , Model TOQ-18 fiberizer, manufactured by Reynolds Engineering & Equipment, Inc. in Muscatine, Iowa. This ground corn had a similar particle size distribution as Example 3 above.
  • Ex 6 and Ex 7 were separate fermentation batches of different lots of corn that were milled to the same specification.
  • the only difference in the separation process that was used between Ex. 6 and Ex. 7 is that a smaller screen size was used to separate the fibers from the protein in the whole stillage. More particularly, a fiber screen size of about 45 ⁇ was used to separate the fiber product of Ex. 6, whereas a fiber screen size of about 20 ⁇ was used to separate the fiber product of Ex. 7.
  • the filter used was an FF6 Fiber Filter from Vincent Corporation, Tampa Florida.
  • the ethanol potential per 1,000 kg of each fiber containing sample was calculated and the results are shown in Table 7 below.
  • the ethanol potential was determined according to the procedure discussed and described above.
  • the determination of the ethanol potential of Ex. 6, a fiber rich product (FRP) was calculated as follows.
  • glucan, galactan, mannan and starch (20.71 wt% of glucan, 6.93 wt% of galactan, 0 wt% of mannan, and 2.84 wt% of starch) were added together and equaled a total of 30.48 wt% of glucan, galactan, mannan and starch.
  • the amount (wt%) of the combined amount of glucan, galactan, mannan and starch was multiplied by 1,000 kg (0.3048 x 1,000) to determine the amount of any glucan, galactan, mannan, and starch in kilograms per 1,000 kg of the FRP, which was equal to 304.8 kg of glucan, galactan, mannan and starch per 1,000 kg of the FHP.
  • the mass (kg) of glucan, galactan, mannan and starch per 1,000 kg of the FRP was converted to mass (kg) of monosaccharides per 1,000 kg of the FRP by multiplying the mass of the glucan, galactan, mannan, and starch (304.8 kg) by 1.11 to account for the molecule of water that adds to the polysaccharides when the sugar monomers are hydrolyzed from the polysaccharides, which was equal to 338.3 kg of monosaccharides per 1,000 kg of the FRP.
  • the mass (kg) of the monosaccharides per 1,000 kg of the FRP was multiplied by 0.51 to convert the kilograms of monosaccharides per 1,000 kg of the FRP to kilograms ethanol per 1,000 kg of the FRP while assuming 100% of the theoretical yield, which was equal to 172.5 kg of ethanol per 1,000 kg of the FRP.
  • the 172.5 kg of ethanol per 1,000 kg of the FRP was converted to liters (L) per 1,000 kg of the FRP by dividing the 172.5 kg of ethanol per 1,000 kg of the FRP by 0.789 kg/liter, which was equal to 218.7 liters of ethanol per 1,000 kg of the FRP.
  • the 218.7 liters of ethanol per 1,000 kg of the FRP was divided by 3.789 to convert the amount of ethanol per 1,000 kg of the FRP to gallons of ethanol per 1,000 kg of the FRP, which was equal to 57.7 gallons of ethanol per 1,000 kg of the FRP.
  • the mass (kg) of xylan and arabinan per 1,000 kg of the FRP was then converted to the mass (kg) of monosaccharides per 1,000 kg of the FRP by multiplying the mass of the xylan and arabinan (425.6 kg) by 1.136 to account for the molecule of water that adds to the polysaccharides when the sugar monomers are hydrolyzed from the polysaccharides, which was equal to 483.5 kg of monosaccharides per 1,000 kg of the FRP.
  • the mass (kg) of the monosaccharides per 1,000 kg of the FRP was multiplied by 0.51 to convert the kilograms of monosaccharides per 1,000 kg of the FRP to kilograms of ethanol per 1,000 kg of the FRP while assuming 100% of the theoretical yield, which was equal to 246.6 kg of ethanol per 1,000 kg of the FRP.
  • the 246.6 kg of ethanol per 1,000 kg of the FRP was converted to liters (L) per 1,000 kg of the FRP by dividing the 246.6 kg of ethanol per 1,000 kg of the FRP by 0.789 kg/liter, which was equal to 312.5 liters of ethanol per 1,000 kg of the FRP.
  • the 312.5 liters of ethanol per 1,000 kg of the FRP was divided by 3.789 to convert the amount of ethanol per 1,000 kg of the FRP to gallons of ethanol per 1,000 kg of the FRP, which was equal to 82.5 gallons of ethanol per 1,000 kg of the FRP.
  • the ethanol potential of the fiber rich product of Ex. 6 was equal to the combined amount of ethanol derived from the glucan, galactan, mannan, and starch (57.7 gallons of ethanol per 1,000 kg of the FRP) and the amount of ethanol derived from xylan and arabinan (82.5 gallons of ethanol per 1,000 kg of the FRP), which was equal to 140.2 gallons of ethanol per 1,000 kg of fiber rich product.
  • the fiber product recovered from the whole stillage that was produced with corn ground in the disk mill fiberizer had a significantly greater ethanol potential than CEx. 3. More particularly, Ex. 6 had the potential to make about 1.90 times the amount of ethanol as CEx. 3 and Ex. 7 had the potential to make about 1.42 times the amount of ethanol as CEx. 3.
  • the fiber samples (CEx. 3 and Exs. 5-7) were subjected to an acid pretreatment process to produce pre-treated fiber containing samples. All supplies were purchased from ThermoFisher and Sigma Aldrich and used as received. The moisture level of each substrate was determined by the moisture balance and following the manufacturer's suggested usage.
  • the fiber containing samples were all pretreated to convert the hemicellulose to oligomers, xylose, and arabinose and to make the cellulose and hemicellulosic oligomers more accessible and digestible to cellulase enzymes.
  • the acid used in these experiments was about 93% sulfuric acid containing about 7% water.
  • the pretreatments were all setup with a set amount of sample, water, and acid which were mixed together and placed in an autoclavable vessel or jar with a lid. The lid was sealed. The full jar was placed into an autoclave and heated to about 120°C for about 2 hours.
  • the acid pretreated solids were hydrolyzed, which as discussed and described above can be accomplished with two enzyme systems.
  • the first system was a cocktail of enzymes that is termed by the industry as a cellulase, but contains exo-glucanases, endo-gluconases, beta-glucosidase, and potentially some xylanase activity.
  • the second enzyme system was a hemicellulase and may contain a number of different activities including exo-xylanase, endo-xylanase, arabinose, esterase, and proteases. These enzyme cocktails are available commercially from Novozymes (Franklinton NC) and DuPont (Wilmington DE).
  • the specific process variables for the enzyme hydrolysis of the acid pretreated fiber containing samples is shown in Table 9 below.
  • the moisture or solids content of each acid pretreated fiber containing sample was used to determine the amount of wet material to use in order to obtain 15 g of the acid pretreated fiber containing sample on a dry weight basis. This amount was weighed into an appropriately sized plastic container (about 250 mL container) to hold 100 g of enzyme hydrolysis solids and liquid) with a screw on lid (to provide a water tight seal), followed by the addition of water, the pH of each sample was adjusted to about 5 to about 5.2, the enzyme was added, and the lid was closed.
  • the 250 mL containers were placed in a heated mechanical shaker set to about 50°C and a shake rpm of about 150.
  • the hydrolysis was allowed to proceed for a time of about 72 hours with the pH adjusted back to about 5 to about 5.2 at each 24 hour period.
  • the containers were removed from the shaker and the contents of each container was centrifuged to separate the residual solids from the liquid sugar solution.
  • the separated sugar solution was filtered through a 0.20 ⁇ syringe filter into HPLC vials or into a 96 well plate for analysis to determine the amount of sugar released by pretreatment and enzyme hydrolysis.
  • the structure of the fibers can also be disrupted with a base instead of an acid. Accordingly, the fiber samples (CEx. 3 and Exs. 5-7) were also subjected to a base pretreatment process to produce pre-treated fiber containing samples. Pretreatment with a base induces very little hydrolysis compared to when an acid is used. The base partially solubilizes or swells the cellulose and hemicellulose.
  • the base used in these experiments was an aqueous ammonium hydroxide solution containing about 30% ammonium hydroxide and about 70% water.
  • the water in the base solution as well as the water in the substrate were accounted for in the calculations to maintain the solids and base loadings required.
  • the added water was tap water (City of Wichita KS).
  • the material was allowed to cool upon removal from the autoclave followed a new moisture determination and a weighing to calculate a recovery of pretreated fiber substrate.
  • the base loading is calculated for ammonia (NH3).
  • the base pretreatment was setup with a set amount of the fiber containing material, water, and base that were mixed together and placed in an autoclavable vessel and the vessel was sealed with a lid.
  • the vessels were placed into an autoclave and heated to 120°C for about 2 hours. Table 12 provides the setup for these examples.
  • the base pretreated solids were hydrolyzed, which, as discussed above, can be accomplished with two enzyme systems.
  • the first system was a cocktail of enzymes that is termed by the industry as a cellulase, but contains exo-glucanases, endo-gluconases, beta-glucosidase, and potentially some xylanase activity.
  • the second enzyme system was as a hemicellulase and may contain a number of different activities including exo-xylanase, endo-xylanase, arabinose, esterase, and proteases. These enzyme cocktails were acquired from Novozymes (Franklinton NC) and DuPont (Wilmington DE).
  • each base pretreated fiber containing sample was used to determine the amount of wet material to use in order to obtain 15 g of the base pretreated fiber containing sample on a dry weight basis. This amount was weighed into an appropriately sized plastic container (about 250 mL container) to hold 100 g of enzyme hydrolysis solids and liquid) with a screw on lid (to provide a water tight seal), followed by the addition of water, the pH of each sample was adjusted to about 5 to about 5.2, the enzyme was added, and the lid was closed. The 250 mL containers were placed in a heated mechanical shaker set to about 50°C and a shake rpm of about 150.
  • the hydrolysis was allowed to proceed for atime of about 72 hours with the pH adjusted back to about 5 to about 5.2 at each 24 hour period.
  • the containers were removed from the shaker and the contents of each container was centrifuged to separate the residual solids from the liquid sugar solution.
  • the separated sugar solution was filtered through a 0.20 ⁇ syringe filter into HPLC vials or into a 96 well plate for analysis to determine the amount of sugar released by pretreatment and enzyme hydrolysis.
  • the specific process variables for the enzyme hydrolysis of the base pretreated fiber containing samples is shown in Table 13 below.
  • Embodiments of the present disclosure further relate to any one or more of the following paragraphs:
  • a process for making ethanol comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; and separating the whole stillage to produce a fiber rich product and a filtrate, wherein the fiber rich product has an ethanol potential of at least 90 gallons of ethanol per 1,000 kilograms of the fiber rich product.
  • a process for making ethanol comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage to produce a fiber rich product and a filtrate; hydrolyzing the fiber rich product to produce a saccharification mash; and processing the saccharification mash to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage with a fiber filter to produce a fiber rich product and a filtrate; hydrolyzing the fiber rich product to produce a saccharification mash; processing the saccharification mash to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: separating ethanol from a fermentation mash to produce a whole stillage, wherein the fermentation mash is derived from a ground corn product milled from a plurality of corn pieces, wherein the plurality of corn pieces comprises whole corn kernels, fragmented corn kernels, size-reduced corn kernels, milled corn kernels, or any mixture thereof, wherein greater than 80 wt% of the ground corn product has a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966; separating the whole stillage to produce a fiber rich product and a filtrate; hydrolyzing the fiber rich product to produce a saccharification mash; and processing the saccharification mash to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; and separating the whole stillage with a separator to produce a fiber rich product and a filtrate, wherein the separator comprises a rotary drum screen, a rotary vacuum drum filter, a brush strainer, a vibratory separator, a linear motion screen, a vacu-deck screen, or a combination thereof; hydrolyzing the fiber rich product to produce a saccharification mash; and processing the saccharification mash to produce additional ethanol and a stillage protein product.
  • a process for making ethanol comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage to produce a fiber rich product and a filtrate; processing the fiber rich product to produce additional ethanol and a stillage protein product comprising about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, about 1 wt% to about 15 wt% of acid detergent fibers, and about 15 wt% to about 35 wt% of yeast, based on a dry weight of the stillage protein product.
  • a process for making ethanol comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage to produce a fiber rich product and a filtrate; processing the fiber rich product to produce additional ethanol and a stillage protein product comprising about 15 wt% to about 35 wt% of yeast, based on a dry weight of the stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash comprising ethanol, wherein the ground corn product has a dso by volume percent of 100 ⁇ to 400 ⁇ , as measured according to ISO 13320:2009; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage with a single pressure screen to produce a fiber rich product and a filtrate; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash, wherein the ground corn product has a dso by volume percent of 100 ⁇ to 400 ⁇ , as measured according to ISO 13320:2009; separating ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage with a fiber filter to produce a fiber rich product and a filtrate; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash, wherein greater than 25 wt% of the ground corn product has a particle size of greater than 105 ⁇ , and wherein greater than 80 wt% of the ground corn product has a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966; separating ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage to produce a fiber rich product and a filtrate; hydrolyzing the fiber rich product to produce a saccharification mash; and processing the saccharification mash to produce additional ethanol and a stillage protein product.
  • a process for making ethanol comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage to produce a fiber rich product and a filtrate; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage with a fiber filter to produce a fiber rich product and a filtrate; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: separating ethanol from a fermentation mash to produce a whole stillage, wherein the fermentation mash is derived from a ground corn product milled from a plurality of corn pieces, wherein the plurality of corn pieces comprises whole corn kernels, fragmented corn kernels, size-reduced corn kernels, milled corn kernels, or any mixture thereof, wherein greater than 80 wt% of the ground corn product has a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966; separating the whole stillage to produce a fiber rich product and a filtrate; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash comprising ethanol; separating at least a portion of the ethanol from the fermentation mash to produce a whole stillage; and separating the whole stillage with a separator to produce a fiber rich product and a filtrate, wherein the separator comprises a rotary drum screen, a rotary vacuum drum filter, a brush strainer, a vibratory separator, a linear motion screen, a vacu-deck screen, or a combination thereof; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • a process for recovering products from a corn fermentation mash comprising: processing a ground corn product to produce a fermentation mash, wherein greater than 25 wt% of the ground corn product has a particle size of greater than 105 ⁇ , and wherein greater than 80 wt% of the ground corn product has a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966; separating ethanol from the fermentation mash to produce a whole stillage; separating the whole stillage to produce a fiber rich product and a filtrate; and processing the fiber rich product to produce additional ethanol and a stillage protein product.
  • the stillage protein product comprises about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, about 1 wt% to about 15 wt% of acid detergent fibers, and about 15 wt% to about 35 wt% of yeast, based on a dry weight of the stillage protein product.
  • the stillage protein product comprises about 47 wt% to about 57 wt% of protein, about 3 wt% to about 5 wt% of fat, about 1 wt% to about 3 wt% of ash, about 4 wt% to about 10 wt% of neutral detergent fibers, about 5 wt% to about 10 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on a dry weight of the stillage protein product.
  • the fiber rich product comprises about at least 20 wt% of C5 polysaccharides and at least 20 wt% of C6 polysaccharides, based on a dried weight of the fiber rich product.
  • the fiber rich product comprises at least 23 wt% of C5 polysaccharides and at least 24 wt% of C6 polysaccharides, based on a dried weight of the fiber rich product.
  • the fiber rich product comprises about 12 wt% to about 22 wt% of glucan, about 11 wt% to about 28 wt% of xylan, about 2.5 wt% to about 8 wt% of galactan, about 7 wt% to about 20 wt% of arabinan, and about 2 wt% to about 5 wt% of starch, based on the dried weight of the fiber product.
  • the fiber rich product comprises about 16 wt% to about 22 wt% of glucan, about 14 wt% to about 28 wt% of xylan, about 5 wt% to about 8 wt% of galactan, about 8 wt% to about 20 wt% of arabinan, and about 3.7 wt% to about 5 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises at least 16 wt% of glucan, at least 15 wt% of xylan, at least 5 wt% of galactan, at least 9 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises at least 18 wt% of glucan, at least 16 wt% of xylan, at least 6 wt% of galactan, at least 9 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises at least 20 wt% of glucan, at least 20 wt% of xylan, at least 6 wt% of galactan, at least 15 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises less than 1 wt% of inorganic compounds, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, about 28 wt% to about 33 wt% of C6 polysaccharides, and about 38 wt% to about 45 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich product comprises less than 1 wt% of inorganic compounds, about 10 wt% to about 16 wt% of structural protein, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, about 28 wt% to about 33 wt% of C6 polysaccharides, and about 38 wt% to about 45 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich product comprises less than 1 wt% of inorganic compounds, about 10 wt% to about 16 wt% of structural protein, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, about 17 wt%to about 22 wt% of lignin, about 28 wt% to about 33 wt% of C6 polysaccharides, and about 38 wt% to about 45 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich product comprises less than 1 wt% of the inorganic compounds, less than 2 wt% of the extractives, about 1.8 wt% to about 4 wt% of acetate, about 27 wt% to about 30 wt% of C6 polysaccharides, and about 24 wt% to about 28 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich product comprises less than 1 wt% of the inorganic compounds, about 20 wt% to about 26 wt% of structural protein, less than 2 wt% of the extractives, about 2 wt% to about 4 wt% of acetate, about 27 wt% to about 30 wt% of C6 polysaccharides, and about 24 wt% to about 28 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • the fiber rich product comprises less than 1 wt% of the inorganic compounds, less than 2 wt% of the extractives, about 1.8 wt% to about 4 wt% of acetate, about 20 wt% to about 25 wt% of structural protein, about 17 wt% to about 22 wt% of lignin, about 27 wt% to about 30 wt% of C6 polysaccharides, and about 24 wt% to about 28 wt% of C5 polysaccharides, based on a dried weight of the fiber rich products.
  • a fiber rich product comprising at least 20 wt% of C5 polysaccharides and at least 20 wt% of C6 polysaccharides, based on a dried weight of the fiber rich product, wherein the fiber rich product is separated from a fermentation mash produced by fermenting a ground corn product.
  • a fiber rich product comprising about 12 wt% to about 22 wt% of glucan, about 11 wt% to about 28 wt% of xylan, about 2.5 wt% to about 8 wt% of galactan, about 7 wt% to about 20 wt% of arabinan, and about 2 wt% to about 5 wt% of starch, based on a dried weight of the fiber rich product, wherein the fiber rich product is separated from a fermentation mash produced by fermenting a ground corn product.
  • the fiber rich product comprises about 16 wt% to about 22 wt% of glucan, about 14 wt% to about 28 wt% of xylan, about 5 wt% to about 8 wt% of galactan, about 8 wt% to about 20 wt% of arabinan, and about 3.7 wt% to about 5 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises at least 16 wt% of glucan, at least 15 wt% of xylan, at least 5 wt% of galactan, at least 9 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises at least 18 wt% of glucan, at least 16 wt% of xylan, at least 6 wt% of galactan, at least 9 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises at least 20 wt% of glucan, at least 20 wt% of xylan, at least 6 wt% of galactan, at least 15 wt% of arabinan, and at least 2 wt% of starch, based on the dried weight of the fiber products.
  • the fiber rich product comprises less than 1 wt% of inorganic compounds, about 10 wt% to about 16 wt% of structural protein, less than 1 wt% of extractives, about 1.5 wt% to about 3 wt% of acetate, and about 17 wt% to about 22 wt% of lignin, based on a dried weight of the fiber rich products.
  • the fiber rich product according to any one of paragraphs 111 to 120, wherein the fiber rich product comprises less than 1 wt% of the inorganic compounds, about 20 wt% to about 26 wt% of structural protein, less than 2 wt% of the extractives, and about 2 wt% to about 4 wt% of acetate, based on a dried weight of the fiber rich products.
  • the fiber rich product according to any one of paragraphs 111 to 120, wherein the fiber rich product comprises less than 1 wt% of the inorganic compounds, less than 2 wt% of the extractives, about 1.8 wt% to about 4 wt% of acetate, about 20 wt% to about 25 wt% of structural protein, and about 17 wt% to about 22 wt% of lignin, based on a dried weight of the fiber rich products.
  • a stillage protein product comprising about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, and about 1 wt% to about 15 wt% of acid detergent fibers, based on a dry weight of the stillage protein product.
  • a stillage protein product comprising about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, about 1 wt% to about 15 wt% of acid detergent fibers, and about 15 wt% to about 30 wt% of yeast, based on a dry weight of the stillage protein product.
  • the stillage protein product according to any one of paragraphs 127 to 129, wherein the stillage protein product comprises about 20 wt% to about 27 wt% of yeast, based on a dry weight of the stillage protein product.
  • the stillage protein product according to any one of paragraphs 127 to 131, wherein the stillage protein product comprises about 40 wt% to about 80 wt% of protein, about 3 wt% to about 20 wt% of fat, about 1 wt% to about 4 wt% of ash, about 2 wt% to about 30 wt% of neutral detergent fibers, about 1 wt% to about 15 wt% of acid detergent fibers, and about 15 wt% to about 35 wt% of yeast, based on a dry weight of the stillage protein product.
  • the stillage protein product according to any one of paragraphs 127 to 132, wherein the stillage protein product comprises about 47 wt% to about 57 wt% of protein, about 3 wt% to about 5 wt% of fat, about 1 wt% to about 3 wt% of ash, about 4 wt% to about 10 wt% of neutral detergent fibers, about 5 wt% to about 10 wt% of acid detergent fibers, and about 20 wt% to about 30 wt% of yeast, based on a dry weight of the stillage protein product.
  • a process for recovering products from a fermentation mash comprising: separating ethanol from a fermentation mash to produce a whole stillage, wherein the fermentation mash is derived from a ground corn product milled from a plurality of corn pieces, wherein the plurality of corn pieces comprises whole corn kernels, fragmented corn kernels, size-reduced corn kernels, milled corn kernels, or any mixture thereof, wherein greater than 80 wt% of the ground corn product has a particle size of 425 ⁇ or less, as measured according to AOAC 965.22-1966; separating the whole stillage to produce a fiber rich product and a filtrate; hydrolyzing the fiber rich product to produce a saccharification mash; and processing the saccharification mash to produce additional ethanol and a stillage protein product.

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Abstract

L'invention concerne des procédés et des systèmes permettant de récupérer des produits à partir d'un moût de fermentation. Dans certains exemples, un procédé de récupération de produits à partir d'un moût de fermentation peut comprendre le traitement d'un produit de maïs broyé pour produire un moût de fermentation qui peut comprendre de l'éthanol. Au moins une partie de l'éthanol peut être séparée du moût de fermentation pour produire une vinasse entière. La vinasse entière peut être séparée pour produire un produit riche en fibres et un filtrat. Le produit riche en fibres peut être hydrolysé pour produire un moût de saccharification. Le moût de saccharification peut être traité pour produire de l'éthanol supplémentaire et un produit protéique de vinasse.
PCT/IB2018/053688 2015-11-25 2018-05-24 Procédés permettant de récupérer des produits à partir d'un moût de fermentation de maïs WO2018215965A1 (fr)

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US11905502B2 (en) 2011-04-18 2024-02-20 Poet Research, Inc. Systems and methods for stillage fractionation
US11248197B2 (en) 2015-11-25 2022-02-15 Poet Grain (Octane), Llc Processes for recovering products from a corn fermentation mash
US11254955B2 (en) 2015-11-25 2022-02-22 Poet Grain (Octane), Llc Processes for separating whole stillage to produce a fiber rich product that includes C5 and C6 polysaccharides
US11286509B2 (en) 2015-11-25 2022-03-29 Poet Grain (Octane), Llc Processes for recovering products from a corn fermentation mash
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US11730172B2 (en) 2020-07-15 2023-08-22 Poet Research, Inc. Methods and systems for concentrating a solids stream recovered from a process stream in a biorefinery

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