• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
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    • 专利摘要:
    vinasse fractionation systems and methods the present invention provides systems and methods for fractioning the entire vinasse of an ethanol production facility. the total vinasse undergoes a separation of its liquid portion (fine vinasse) from the solid portion (fibrous mass). in some embodiments, the solids and liquids throughout the vinasse can be separated using a screening centrifuge. the fibrous mass can be dried to produce a fiber-rich animal food. fine vinasse can be supplied to a three-phase separator for separation into an oil emulsion, a clarified aqueous vinasse, and a protein paste. the protein paste can be dried to generate an animal food with a high protein content, greater than about 45% protein content. the clarified fine vinasse is condensed to obtain a syrup with more than about 60% solids. the oil emulsion is subjected to a pH adjustment to release the oil from the emulsion, which is then separated.
    公开号:BR112013025749B1
    申请号:R112013025749
    申请日:2012-04-12
    公开日:2020-01-14
    发明作者:Alan Bootsma Jason
    申请人:Poet Res Incorporated；
    IPC主号:
    专利说明:

    “SYSTEMS AND METHODS FOR VILLAGE FRACTIONATION”
    Cross Reference
    This application claims the benefits of US Provisional Order Serial Number 61 / 476,702, filed on April 18, 2011, and entitled “SYSTEMS AND METHODS FOR STILLAGE FRACTIONATION”, which is hereby incorporated by reference in its entirety.
    Field of the Invention
    The object description refers to systems and methods for the fractionation of fine and total vinasse in an ethanol production facility.
    Background
    Ethanol has traditionally been produced from raw materials based on grains (for example, maize, sorghum / milo, barley, wheat, soybeans, etc.), or from sugar (for example, sugar cane, beets, etc.).
    In a conventional ethanol facility, corn, sugar cane, another grain, beets, or other plants are used as the raw material and ethanol is produced from the starch contained within the corn, or another vegetable raw material. In the case of a maize facility, maize kernels are cleaned and ground to prepare material containing starch for processing. Corn kernels can also be fractionated to separate starch-containing material (eg, endosperm) from another material (such as fiber and germ). The initial treatment of the raw material varies by the type of raw material. In general, however, the starch and sugar contained in the plant material are extracted using a combination of mechanical and chemical means.
    The starch-containing material is treated to form a paste with water and liquefied to facilitate saccharification, where the starch is converted into sugar (eg, glucose), and fermentation, where the sugar is converted by an ethanologene (eg, yeast) into ethanol. The fermentation product is beer, which comprises a liquid component, including ethanol, water, and soluble components, and a solid component, including unfermented particulate matter (among other things). The fermentation product is sent to a distillation system where the fermentation product is distilled and dehydrated in ethanol. The residual material (for example, total vinasse) comprises water, soluble components, oil, and unfermented solids (for example, the solid component of beer with substantially all of the ethanol removed, which can be dried on a dry distillery grain (DDG) and sold, for example, as an animal feed product). Other co-products (for example, syrup and oil contained in the syrup) can also be recovered from total vinasse.
    In a typical ethanol installation, a massive volume of total vinasse is generally produced. In fact, for a typical ethanol installation, the amount of total vinasse
    2/13 produced can be approximately 13.4 gallons per bushel of processed corn. In general, one third of the corn raw material is present in the total vinasse as dissolved and suspended solids. Vinasse contains almost 90% water. Total vinasse is responsible for a substantial portion of the washing water generated by the ethanol facilities. The financial cost of water, its treatment and its disposal (typically through evaporation) can be significant.
    Although vinasse is typically seen as a liability for an ethanol plant, it is possible to generate a number of high-value co-products from vinasse. For example, vinasse oil, high protein feeds, and syrups are all capable of being generated from vinasse and sold as co-products of higher value. Currently, with the interest of improving the efficiency of ethanol installations, the total vinasse is often separated into two components: a solid component and a liquid component. Separation can be performed using centrifugation, or filter and pressure. The solid component can be dried to generate dry distillery grains (DDG) that are sold as animal feed. The liquid component, known as fine vinasse, can be dried and used to increase the fat content of DDG to produce DDGS (dry distillery grains with soluble). This process requires the drying of a large amount of water, which is very intense and uneconomical energy. Thin vinasse can also be recycled in the installation, such as to replace some portion of the water used during fermentation (opposite fermentation current).
    Additionally, there is currently a strong pressure to generate corn oil from vinasse, as oil is a particularly high value commodity, and for legislative and legal considerations. Ideally, an ethanol plant can generate a minimum of 0.603 kg (1.33 pounds) of oil product per bushel of processed corn. A number of methods of oil recovery are known, but to date none have reached more than about 0.454 kg (one pound) of oil per bushel. In addition, conventional processes for recovering oil from fermentation products often sacrifice the quality of the oil so that the oil contains high levels of free fatty acids. The presence of a high level of free fatty acids can leverage the production of final products such as, for example, the yield and quality of any biodiesel eventually produced with oil as the raw material.
    For example, patent application PCT / US2009 / 045163 (entitled “METHODS FOR PRODUCING A HIGH PROTEIN CORN MEAL FROM A WHOLE STILLAGE BYPRODUCT AND SYSTEM THEREFORE ') describes a process for separating total vinasse into a solid portion and fine vinasse. The fine vinasse is again separated into a protein and the water-soluble portion. A fraction of oil can be separated from the water portion via evaporation. In the PCT order method, the oil is recovered after evaporation
    3/13 ration, which probably results in yield reductions and sacrifices oil quality.
    Another current oil recovery method is described in US patent 7,829,680 (entitled “SYSTEM AND METHOD FOR ISOLATION OF GLUTEN AS A CO-PRODUCT OF ETANOL PRODUCTION’). In this method, a plurality of screens are used to separate a fiber product from an oil / protein product. The oil and protein can then be separated via centrifugation.
    Although these known systems and methods can generate valuable co-products from ethanol production vinasse, they have inherent drawbacks related to oil quality, quantity of oil recovered, water balance items, and composition of isolated protein products .
    summary
    The aspects described refer to systems and methods for the fractionation of total vinasse from an ethanol production facility. The fractionation system generates multiple valuable co-products while reducing the demand for energy in many traditional methods of vinasse treatment.
    In the systems and methods described, the total vinasse undergoes a separation of its liquid portion (fine vinasse) from its solid portion (fiber paste). This separation can be accomplished using membranes, screw presses, centrifuges, or other suitable means. In some embodiments, the solids and liquids in total vinasse can be separated using a screening centrifuge.
    The fiber paste can be dried to generate a high fiber feed for animals. Fine vinasse can be provided with a three-phase separator for separation into an oil emulsion, a clarified aqueous vinasse, and a protein paste. In some embodiments, the three-stage separator may include a disc nozzle centrifuge or other suitable separating device.
    The protein paste can be dried to generate a high protein animal feed. In some cases, said food may have more than about 45% protein content. In alternative modalities, the protein paste can be returned to the fiber paste before drying in order to alter the nutritional constitution of the animal feed produced.
    The clarified fine vinasse can be used as a counter current for fermentation, or another source of constitution water, within an ethanol production facility, for example. Alternatively, some or all of the clarified vinasse can be condensed, using an evaporator or other suitable device, to produce a syrup. Syrup (high-solid syrup) can be used as an animal feed product. In general, syrup can contain between about 30% and about 40% moisture,
    4/13 more than about 10% protein, less than about 1% fiber, between about 6% and about 10% fat, and between about 5% to about 7% ash.
    The oil emulsion can be subjected to a pH adjustment to release the oil from the emulsion. The pH adjustment can use a caustic to bring the pH of the emulsion to about 8.0 to about 8.5. The oil can be separated from the emulsion using the centrifuge, or another suitable separation device. The resulting oil can include more than about 97% fat. Additionally, in some embodiments, about 0.603 or more kg (1.33 or more pounds) of oil can be recovered from the total vinasse generated from processing a bushel of corn for ethanol.
    Note that the various characteristics of the various aspects described above can be practiced alone or in combination. These and other features will be described in more detail below in the detailed description and in conjunction with the figures below.
    Brief Description of Drawings
    In order that the various aspects can be more clearly understood, some modalities will now be described, by way of example, with reference to the attached drawings, in which:
    Figure 1 is a perspective view of a biorefinery comprising an ethanol production facility, according to some modalities;
    Figures 2A and 2B are process flow diagrams illustrating examples of processes for producing ethanol from corn to ethanol, according to some modalities;
    Figure 3 is a schematic block diagram illustrating a system for fractioning vinasse, according to some modalities;
    Figure 4 is an example of a flow chart illustrating a vinasse fractionation process in valuable co-products, according to some modalities;
    Table 1 lists the experimental compositions of the vinasse fractions, according to some modalities; and
    Table 2 lists the expected compositions of commercially derived vinasse fractions, according to some modalities.
    Description of Modalities
    The various aspects will now be described in detail with reference to the various modalities thereof as illustrated in the attached drawings. In the description that follows, numerous specific details are determined in order to provide a true understanding of the various aspects. It will be apparent, however, to those skilled in the t technique, that the modalities can be practiced without some or all of the specific details. In other cases, well-known process steps and / or structures have not been
    5/13 described in detail so as not to unnecessarily obscure the aspects described. The characteristics and advantages of the modalities can be better understood with reference to the drawings and the discussions that follow.
    The following description refers to systems and methods for fractioning vinasse from an ethanol production facility or other processing facility. Ethanol installations generate large quantities of vinasse as a low-value product. Vinasse is generally a low-value co-product that requires substantial energy to dry in solubles for addition to dry distillery grains, or must be disposed of in some other way. There is the potential for generating high-value co-products from vinasse, thus, the aspects described provide systems and methods that enhance the use of vinasse, which can generate multiple high-quality co-products without unduly influencing the water balance of the ethanol production facility. Said systems and methods can provide greater yield from co-products and less impact on the environment.
    The systems and methods described provide a means to substantially improve the quality and value of vinasse by fractioning vinasse into components, each of which is of high value in itself. The fractions generated by the systems and methods described, in addition to being intrinsically valuable, provide an improved water balance for the ethanol production facility, thereby reducing the energy required to process vinasse in traditional evaporation and drying.
    With reference to figure 1, an example of biorefinery 100 comprising an ethanol production facility configured to produce ethanol from corn is shown. Biorefinery example 100 comprises an area 102 where maize (or other suitable material including, but not limited to, biomass, sugars, and other starch products) is shipped and prepared to be supplied to the ethanol production facility. The ethanol production facility comprises an apparatus 104 for the preparation and treatment (for example, milling) of corn in maize flour suitable for fermentation in fermentation product in a fermentation system 106. The ethanol production facility comprises a distillation system 108 in which the fermentation product is distilled and dehydrated in ethanol. The biorefinery may also comprise, in some embodiments, a by-product treatment system 110 (shown as comprising a centrifuge, dryer, evaporator, and associated tanks).
    Referring now to figures 2A and 2B, in an ethanol production process, corn 202 (or other suitable feed material) can be prepared for further treatment in a preparation system 204. As illustrated in figure 2B, the preparation system 204 may comprise cleaning or filtration 206 to remove foreign material, such as rocks, dirt, sand, pieces of corn cobs and stems, and other non-fermenting material
    6/13 removable (for example, removed components). After cleaning or filtering 206, the particle size of the corn can be reduced by shredding 208 to facilitate further processing. Corn kernels can also be fractionated into an endosperm containing starch, fiber, and germ, according to some modalities. The crushed maize 210 or endosperm is treated to form a paste with water, enzymes and agents 212 to facilitate the conversion of starch into sugar (for example, glucose), as in a first treatment system 214. Sugar (for example, treated component 216) is converted into ethanol by an ethanology (eg yeast or other agents 218) in a fermentation system 220. The fermentation product (fermentation product 222) is beer, which comprises a liquid component, including ethanol and water and soluble components, and a solid component, including unfermented particulate matter (among other things). The fermentation product can be treated with agents 224 in a second treatment system 226. The treated fermentation product 228 is sent to a distillation system 230. In the distillation system 230, the fermentation product (treated) is distilled and dehydrated in ethanol 232. In some embodiments, the removed components 234 (for example, total vinasse), which comprises water, soluble components, oil, and unfermented solids (for example, the solid component of beer with substantially all of the ethanol removed), it can be dried on dry distillery grains (DDG) in a third treatment system (where the removed components can be treated with agents) and sold as an animal feed product. Other co-products, for example, syrup (and oil contained in the syrup), can also be recovered from vinasse, as will be described in further details below.
    In some systems, the fine vinasse that results when the solids are removed from the total vinasse can be used as a counter current during the fermentation process and can also be used to increase the fat content of DDGS (dry distilled grains with soluble). However, adding fine vinasse to DDGS requires uneconomic evaporation processes that increase DDGS production costs. Described here are systems and methods for the fractionation of total vinasse in order to generate relevant amounts of valuable co-products in a way that in fact reduces the necessary spent fuel on evaporation.
    Referring now to Figure 3, an example schematic block diagram of a system for fractioning the removed vinasse component is provided. In this example diagram, the total vinasse 302 is provided to a vinasse filter 304 for separating the vinasse into a solid component and a thin liquid vinasse 306. The separation can be carried out using a screw press, centrifugation, decanters, or via filtration type methodologies. In some particular embodiments, the separation can be carried out using a concave screen centrifuge. Those versed in the technique
    7/13 will only note that the speed or amount of centrifugal force applied will depend on several factors such as sample size and can be adjusted accordingly depending on said factors. Suitable separators and centrifuges are available from various manufacturers such as, for example, Seital of Vicenza, Italy, Westfalia of Oelde, Germany or Alfa Laval of Lund, Sweden.
    The solid component comprises a high fiber 308 paste, which can be dried in a 310 dryer to dry high grain fiber distillery (DDG) 312 products. Said high fiber DDGs may be particularly suitable to the market for feeding polygastric animals (feeding to ruminants). In some embodiments, the fiber pulp may additionally undergo a washing step before being dried. The washing fluid can be combined with liquid fine vinasse, in some modalities.
    The separation of solid fiber pulp from fine vinasse can be carried out early after the initial production of the fermentation product (total vinasse) in order to maintain the quality of the co-product composition and to avoid undue exposure of co-products. heat products, oxygen, and potential contaminants. If total vinasse or fine vinasse is left exposed for extended periods of time in the presence of moisture, oil hydrolysis can occur which leads to the formation of free fatty acids, which degrades the quality of the oil produced.
    The resulting thin liquid vinasse 306 is provided to a three-stage separator 314, which may include a disc nozzle-type centrifuge or suitable type filter system. The three-stage separator 314 separates fine vinasse 306 into a top layer of oil emulsion 318, a thin aqueous clarified intermediate vinasse 320, and a protein paste 322. Those skilled in the art will note that the speed or amount of centrifugal force applied will depend on various factors such as sample size and can be adjusted accordingly depending on those factors. Suitable separators and centrifuges are available from at least the manufacturer list above.
    Protein slurry 322 can be dried in a dryer 324 in a high protein DDG product 326. High protein DDG can be particularly suitable for feeding to mono-gastric (non-ruminant) and young animals. High protein DDG can have highly metabolizable energy and a lysine content of between about 2% and about 3%, which can be important in feed formulations.
    Clarified fine vinasse 320 can be condensed by evaporation 328 or concentrated by reverse osmosis to produce syrup with a high solid content 330. Due to the low levels of solids suspended in the clarified fine vinasse, high solid content
    8/13 total can be achieved in a concentrated syrup without substantial viscosity limitations. High solids syrup 330 can have between about 30 and 80 percent solids, depending on the desired material handling properties as well as the end use. In some particular embodiments, syrup with a high solid content may contain more than about 60% solids. High solid syrup 330 can be marketed as a high energy food for animal supplements. In alternative embodiments, some portion of the clarified fine vinasse can be used as a counter current for fermentation, thereby further reducing the need for additional evaporation.
    The oil emulsion 318 can be treated with an alkali in order to break the emulsion. The pH adjustment can be fundamental for the release of the oil from the emulsion, and can result in more oil yield and better oil quality. In particular, adjusting the pH of the oil fraction separates or breaks the oil fraction so that the resulting oil recovered has a low fatty acid content. The age of the fermented product and the organic acid content of the fermented product can affect the optimal pH for separation, however, the oil fraction is treated with the highest possible pH to reduce the total free fatty acid content in the separated oil without sacrificing the quality of the oil. In some modalities, the pH is adjusted in a range from about 7 to about 10. In some particular modalities, the pH is adjusted between around 8.0 and around 8.5.
    Oil 332 can be separated from the remainder of the emulsion / aqueous layer by centrifugation, filtration, distillation or other suitable separator 334. The remainder of the aqueous layer / emulsion can be high in protein and recycled by adding in DDG or sold as a separate feed product.
    The oil composition recovered from the aspects described here can be further processed in a variety of ways. For example, crude oil can be filtered and bleached to provide food grade oil for consumer use. In one embodiment, the crude oil can be degummed, refined with additional caustic, and subjected to a soap removal step according to commercially available processes. Following these steps, the oil can be subjected to one or more clay bleaching steps to achieve an oil of desired content and color. If one or more clay bleaching steps are used, the clay can be either an acidic clay or a non-acidic clay. In one embodiment, the bleaching step can include, for example, an acidic clay or a non-acidic clay at around 1% to about 5% based on the total weight. In addition to or as an alternative to clay bleaching, after the crude oil has been degummed, caustic refined and subjected to a soap removal step, a food grade oil of a desired color can be achieved using a bleaching step a heat.
    9/13
    The oil composition can be used in a wide variety of applications. Examples of such applications include the areas of oleochemicals, food (for example, animal feed) as well as oils suitable for human consumption. Oil chemicals include raw material chemicals that are suitable for the production of biodiesel (fatty acid methyl esters). Industrial oil chemicals are useful in the production of soaps, detergents, wire insulation, industrial lubricants, leather treatments, cutting oils, mining agents for oil drilling, paint removal, plastic stabilizers, paint, and rubber production. Other industrial applications include waxes, shampoos, personal care products and emulsifiers or food additives. It is also possible in some modalities to pre-treat oil for uses downstream, such as conversion to biodiesel.
    The composition of recovered oil may contain low levels of moisture, insoluble and unsaponifiable (MIU content). Moisture, as contemplated herein, includes water and any volatile material such as, for example, hexane, ethanol, methanol, or a combination thereof. Insoluble matter (that is, "insoluble"), as contemplated here, refers to and includes any matter incapable of being dissolved in the aqueous portion, fraction of oil or composition of oil. Non-saponifiable matter (ie, “non-saponifiable”) includes any variety of possible non-triglyceride materials that act as contaminants during the production of biodiesel. Non-saponifiable matter can significantly reduce the yield of the final product of the oil composition and can, in turn, reduce the yield of the final product of processes such as, for example, biodiesel production processes.
    Keeping the moisture levels low is especially desirable because the moisture stimulates the formation of free fatty acids instead of esters. In one embodiment, the oil composition contains no more than about 1% weight by weight of total moisture content, alone, based on the total weight of the oil composition. In some embodiments, the moisture content alone is no more than about 0.5% weight by weight or about 0.1% weight by weight.
    In one embodiment, the oil composition comprises no more than approximately 3% weight by weight non-saponifiable, based on the total weight of the oil composition. In some embodiments, the oil composition comprises no more than about 2% weight by weight or about 1% weight by weight of non-saponifiables.
    In one embodiment, the oil composition contains no more than about 1% insoluble weight by weight, alone, based on the total weight of the oil composition. In some embodiments, the insoluble content alone is not more than approximately 0.5% weight by weight or approximately 0.1% weight by weight.
    The oil composition may, in some modalities, exhibit an acceptable iodine value for biodiesel production and, in some modalities, exhibit a higher iodine value
    10/13 or than expected from a pure oil sample. The oil may additionally comprise various carotene, carotenoid, and antioxidant or neutraceutical compounds.
    In one embodiment, the oil composition contains no more than about 5% weight by weight free fatty acid content, based on the total weight of the oil composition. In some embodiments, the free fatty acid content is no more than around 3% weight by weight.
    The fatty acid content of the oil composition is comprised of several fatty acids known in the art. In one embodiment, the oil composition comprises C 16 palmitic acid which represents no more than about 15% weight by weight of the total fatty acid content, based on the total weight of the oil composition. In another embodiment, the C 16 palmitic acid content is no more than about 10% weight by weight of the total fatty acid content. In one embodiment, the oil composition comprises C 18 stearic acid which represents at least about 3% weight by weight of the total fatty acid content, based on the total weight of the oil composition. In another embodiment, the C 18 stearic acid content is at least about 1.5% by weight of the total fatty acid content. In one embodiment, the oil composition comprises C 18-1 oleic acid which represents at least about 30% weight by weight of the total fatty acid content, based on the total weight of the oil composition. In another embodiment, the C 18-1 oleic acid content is at least about 25% weight by weight of the total fatty acid content. In one embodiment, the oil composition comprises C 18-2 linoleic acid which represents at least about 60% weight by weight of the total fatty acid content, based on the total weight of the oil composition. In another embodiment, the C 18-2 linoleic acid content is at least around 50% weight by weight of the total fatty acid content. In one embodiment, the oil composition comprises C 18-3 linoleic acid which represents at most about 1.5% weight by weight of the total fatty acid content, based on the total weight of the oil composition. In another embodiment, the C 18-3 linoleic acid content is no more than about 0.5% weight by weight of the total fatty acid content.
    Since all fine vinasse is not evaporated, in the aforementioned modalities, there is a substantial fuel and cost savings in relation to the traditional vinasse handling which includes the substantial evaporation of fine vinasse by adding back to DDG to generate dry grains of distillery with soluble (DDGS). As such, not only are more quantities of higher value products generated through the described treatment of the total vinasse, but additionally, the process uses less fuel thereby reducing the pollution generated and reducing operating costs.
    Figure 4 provides an example flow diagram 400 for the process of generating high value co-products. In this process, the total vinasse is separated into solids and the
    11/13 thin liquid vinasse (in 402). The solids include fiber paste which is dried (at 404) to a high fiber dry grain distillery co-product (HF-DDG).
    In some embodiments, due to the composition of the fiber paste, there is less water retention of the product after the separation of fine vinasse and washing. As the fiber pulp includes less water, there is a substantial reduction in drying costs associated with the production of dry fiber co-product with high fiber content (HF-DDG) compared to the more traditional DDG product . In some embodiments, the solid content of the fiber pulp can be as high as between about 40% and about 45% solids before drying, unlike wet pulp (used to produce conventional DDG) which typically includes only about 30% to about 35% solids before drying.
    In some modalities, fine vinasse is fractionated (in 406) into an oil emulsion, protein paste, and clarified fine vinasse. The protein paste, which includes a high content of lysine, is dried (at 408) to generate dry distillery grains with a high protein content (DDG HP). In some embodiments, the protein paste can also be returned to the fiber paste and dried together to generate an intensified DDG product. The handling of the protein paste can be determined by market considerations and the equipment available at the ethanol production facility.
    Fine vinasse can then be condensed (in 410) to a high solids content (for example, between about 30 to 80 percent solids) to generate a syrup with a high solids content. Syrups with a high solids content are usable as an effective substitute feed for animals, however the generation of syrup with a high practical solid content can be difficult to obtain. This is due to the fact that most syrups generated from fine vinasse, once the solid content approaches around 30 percent, become prohibitively viscous, and are useless as a marketable co-product. When processing fine vinasse into clarified fine vinasse, ultra high solids content (for example, more than about 30%) is achievable in a syrup that retains the molasses viscosity. Thus, the co-product is easily transported and handled by potential buyers.
    Finally, the oil emulsion is treated to extract valuable oil (in 412). Oil extraction is made easier by adjusting the pH of the emulsion with an alkaline. The addition of a caustic agent breaks the emulsion and releases the oil. The released oil can be extracted from the remaining emulsion by means of decantation, centrifugation, filtration or other suitable method. In some modalities, more than about 0.603 kg (1.33 pounds of corn oil is achieved per bushel of corn using the described modalities.
    A series of limited examples was conducted according to an exemplary system modality (as shown in figure 3) in an effort to determine the appropriate and operational conditions for the total vinasse fractionation. The
    The following examples are intended to provide clarity to some types of systems and means of operation; considering the limited nature of these examples, they do not limit the scope of the described aspects.
    Example 1
    In this experiment example, total vinasse was sieved using a sieve centrifuge in order to obtain a fiber paste and fine vinasse. The fiber paste was dried and tested for composition. The fine vinasse was further processed by decanting centrifuge to produce an oil emulsion, clarified fine vinasse and the protein paste. The protein slurry was dried. The clarified fine vinasse was evaporated to more than 60% solids content. The oil emulsion was treated using a caustic agent to adjust the pH to about 8. The oil emulsion was again subjected to centrifugation in order to remove the oil emulsion. The oil, dry protein paste and high solid content syrup were then subjected to composition analysis. The results of this analysis are provided in relation to TABLE 1.
    In short, the oil product had 0.9% moisture content, 3.03% free fatty acids (FFA), <0.01% insoluble, and 1.13% non-saponifiable. The syrup with the high solids content was 31.6% moisture, 10.9% protein, 0.1% fiber, 6.1% ash, and 8.2% fat. The protein paste composition was 58.6% protein, 12.6% fat, and <1% fiber. The DDG composition with a high fiber content was 26.0% protein, 10% fiber, 3.5% fat, and 0.7% ash.
    The yields of the four products on a percentage basis are approximately 9% oil, 13% syrup, 40% protein, and 38% fiber. Said yields correspond to 0.54 kg (1.3 lb) of oil, 0.907 kg (2 lb) of syrup, 2.72 kg (6 lb) of protein, and 2.72 kg (6 lb) of fiber in pound base per bushel. The expected yields can lead to changes in the expected compositions due to the trade-offs between yield and purity. The expected composition varies from the commercial production of the said products are shown in TABLE 2.
    The modalities as illustrated and described in the present application (including the figures and the Examples) are intended to be illustrative and explanatory. Modifications and variations of the described modalities, for example, of the apparatus and of the processes used (or to be used) as well as the compositions and treatments used (or to be used), are possible; all such modifications and variations are intended to be within the scope of the various aspects presented here.
    The term "exemplary" is used to mean serving as an example, case, or illustration. Any modality or design described as “exemplary” should not necessarily be constructed as preferred or advantageous in relation to other modalities or designs, nor is it intended to prevent exemplary structures and techniques
    13/13 known equivalents to those skilled in the art. Instead, the use of the term exemplary is intended to present concepts in a concrete way, and the subject described here is not limited to those examples.
    Reference through the present specification to “an aspect,” or “the aspect,” or “a modality,” or “the modality” means that a particular characteristic, structure, or characteristic described in relation to the aspect or modality is included in at least least one aspect or modality. Thus, the appearances of the phrase "in one aspect," or "in aspect," or "in a modality," or "in modality" at various points throughout the present specification may, but are not necessarily, referring to the same aspect or 10 modality, depending on the circumstances. In addition, the particular features, structures, or features can be combined in any suitable way into one or more aspects or modalities.
    The term "or" is intended to mean an inclusive "or" instead of an exclusive "or". To the extent that the terms "comprise", "has", "contains", and other similar terms are used either in the detailed description or in the claims, for the avoidance of doubt, these terms are intended to be inclusive in a similar way to the term "comprising ”As an open transition word without preventing any other or additional elements.
    权利要求:
    Claims (21)
    [1]
    1. System for fractioning vinasse FEATURED for understanding:
    a first separator configured to separate the entire vinasse into a solid portion and a liquid portion of liquid vinasse, wherein the solid portion comprises a moist mass with a high fiber content;
    a three-phase separator, configured to receive the liquid portion of liquid vinasse and separate the liquid portion of liquid vinasse into clarified vinasse, an oil emulsion and a protein paste;
    a first dryer configured to dry the wet mass with a high fiber content to generate a feed product with a high fiber content;
    a second dryer configured to dry the protein paste to generate a feed product with a high protein content;
    an evaporator configured to condense the clarified vinasse in a syrup; and a second separator configured to separate the oil from the oil emulsion.
    [2]
    System according to claim 1, CHARACTERIZED in that it further comprises a pH adjuster configured to adjust the pH of the oil emulsion before separation by the second separator.
    [3]
    3. System according to claim 2, CHARACTERIZED by the fact that the pH adjuster is further configured to adjust the pH of the oil emulsion from about 8.0 to about 8.5.
    [4]
    4. System according to claim 1, CHARACTERIZED by the fact that the second separator is configured to separate at least 0.6 L (1.33 pounds) of oil from all vinasse generated by the processing of a bushel of corn for ethanol.
    [5]
    5. System according to claim 1, CHARACTERIZED by the fact that the evaporator is still configured to condense the clarified vinasse in at least 60% solids.
    [6]
    6. System according to claim 1, CHARACTERIZED by the fact that the second dryer is still configured to dry the protein paste to generate the feed product with a high protein content with at least 45% protein.
    [7]
    7. System according to claim 1, CHARACTERIZED by the fact that the second separator is still configured to separate oil with at least 97% fat.
    [8]
    8. System according to claim 7, CHARACTERIZED by the fact that the second separator is further configured to separate oil with less than 1% by weight of moisture content and less than 1% by weight of insoluble.
    [9]
    9. System according to claim 7, CHARACTERIZED by the fact that the
    Petition 870190063894, of 07/08/2019, p. 8/10
    2/3 second separator is further configured to separate oil with less than 5% by weight of the free fatty acid content.
    [10]
    10. System according to claim 1, CHARACTERIZED by the fact that the three-phase separator is a disc nozzle type centrifuge, and in which the first separator is a screening centrifuge.
    [11]
    11. Vinasse fractionation method CHARACTERIZED by understanding: separate all vinasse into a solid portion and a liquid portion of liquid vinasse, in which the solid portion includes a moist mass with a high fiber content;
    separate the whole vinasse into a clarified vinasse, an oil emulsion and a protein paste;
    drying wet dough with a high fiber content to generate a fiber-rich animal food;
    drying the protein paste to generate a protein-rich animal food;
    condense the clarified vinasse to generate a syrup; and separating the oil from the oil emulsion.
    [12]
    12. Method according to claim 11, CHARACTERIZED by the fact that it further comprises adjusting the pH of the oil emulsion before oil separation.
    [13]
    13. Method according to claim 12, CHARACTERIZED by the fact that the adjustment comprises adjusting the pH of the oil emulsion from about 8.0 to about 8.5.
    [14]
    14. Method according to claim 11, CHARACTERIZED by the fact that at least about 0.6 L (1.33 pounds) of oil is separated from all vinasse generated by processing a bushel of corn for ethanol .
    [15]
    Method according to claim 11, CHARACTERIZED in that it further comprises combining at least a portion of the protein paste with the high fiber wet mass.
    [16]
    16. Method according to claim 11, CHARACTERIZED by the fact that the condensation comprises condensing the syrup in at least about 60% solids.
    [17]
    17. Method according to claim 11, CHARACTERIZED by the fact that the protein-rich animal food comprises at least about 45% protein.
    [18]
    18. Method according to claim 11, CHARACTERIZED by the fact that the oil is composed of at least about 97% fat.
    [19]
    19. Method according to claim 18, CHARACTERIZED by the fact that the oil comprises less than 1% by weight of moisture content and less than 1% by weight of insoluble.
    [20]
    20. Method according to claim 18, CHARACTERIZED by the fact that the oil comprises less than about 5% by weight of free fatty acid content.
    Petition 870190063894, of 07/08/2019, p. 9/10
    3/3
    [21]
    21. Method according to claim 11, CHARACTERIZED by the fact that the entire vinasse is separated using a sieving centrifuge, and in which the liquid portion of the liquid vinasse is separated using a three-stage disc nozzle type centrifuge.
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    法律状态:
    2018-12-18| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-04-16| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|
    2019-11-12| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2020-01-14| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 12/04/2012, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US201161476702P| true| 2011-04-18|2011-04-18|
    PCT/US2012/033346|WO2012145230A1|2011-04-18|2012-04-12|Systems and methods for stillage fractionation|
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