• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
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  • 优先权
    • 专利摘要:
    CHEMICAL ADDITIVES AND THEIR USE IN VINEMA PROCESSING OPERATIONS. The present invention provides a method for using a chemical additive to improve the separation of oil from the process stream (integral vinasse, fine vinasse or syrup) generated as a by-product in the production of ethanol from corn.
    公开号:BR112013024126B1
    申请号:R112013024126-8
    申请日:2012-02-10
    公开日:2021-02-02
    发明作者:Paul W. Shepperd；McCord Pankonen；Jeffrey T. Gross
    申请人:Solenis Technologies Cayman, L.P.；
    IPC主号:
    专利说明:

    FIELD OF THE INVENTION
    [0001] This invention relates to the recovery of oil in the production of ethanol from corn. BACKGROUND OF THE INVENTION
    [0002] There are two types of ethanol processing from mlho: wet grinding and dry grinding. The central difference between the two processes is the way in which they initially treat the grain. In wet grinding, the corn kernels are immersed in water and then separated for processing in the first stage. Dry grinding, which is more common, requires a different process.
    [0003] The dry milling process for corn used in ethanol production is well known. For example, see Kelly S. Davis, Corn Milling, Processing and Generation of Co-Products, Minnesota Nutrition Conference, Technical Symposium, September 11, 2001. Ethanol plants typically treat the entire vinasse of the beer column by means of centrifugation to produce moist cake and fine vinasse and then additionally treat the thin vinasse stream by subjecting it to multiple-effect evaporation to produce increased solids and recover the distillate for use in the process (Figure 1). As the solids increase, fine vinasse is usually referred to as syrup (see Figure 1). Syrup is typically combined with wet cake or dry distillers grains and sold as animal feed. These processes are well known in the industry and are generally used in the design of industrial plants.
    [0004] In an effort to take advantage of streams of by-products, many plants have been added to oil removal processes in which fine vinasse (syrup) is subjected to processes such as centrifugation or extraction, to remove corn oil from the syrup. For example, the use of centrifuges for separating corn oil from syrup is widely used in the fuel ethanol industry. Although the theoretical oil yield per bushel (35.24 L) of processed corn is 726 g per bushel, many commercial facilities fall far short of that. Thus, there remains a need to improve the process to maximize the process oil yield.
    [0005] Recently, there has been an effort to increase the value model of the ethanol production process from corn by extracting oil from the by-product fine vinasse. Cantrell and colleagues in U.S. Patent No. 7,602,858 B2 describe a mechanical method of separating fine concentrated vinasse oil, referred to as "syrup", using a disc centrifuge. Randhava and colleagues in U.S. Patent Application No. 2008/0176298 A1 describe the use of an alkyl acetate solvent for the extraction of corn oil in an ethanol production process.
    [0006] Although state of the art references are effective, there is still an opportunity to improve the oil extraction process to further maximize the commercial value of the process. Of particular interest are technologies that do not require the adoption of capital expenditures to implement a new mechanical solution and / or do not significantly alter the process, such as the use of an extraction solvent that requires recycling. SUMMARY OF THE INVENTION
    [0007] The present invention describes a method that comprises the step of adding a chemical additive to improve the separation of oil from the process streams (integral vinasse and / or fine vinasse and / or syrup) generated as a by-product in the production of ethanol at from corn. The method can be used in any wet grinding process or a dry grinding process. Preferably, the method is employed in a dry milling process. The method involves the treatment of any of the process streams downstream of the distillation operation in the production of ethanol from corn with a chemical additive that improves the mechanical separation of oil from the said streams.
    [0008] One aspect of the invention is the application of a chemical additive to fine vinasse or syrup, before the oil separation centrifuge, to increase the oil yield. This can comprise an addition point or a combination of addition points in the unit operation of fine vinasse, such as: 1) at the entrance of the premix or heat retention tanks, 2) at the inlets and / or exits of a or more of the evaporators, and / or 3) just before the centrifuge enters.
    [0009] Another aspect of the invention is the application of the chemical additive to the vinasse stream of integral vinasse before the separation of the wet cake from the fine vinasse. A good mixing point such as a pump inlet is preferred.
    [00010] Preferably, the chemical additive is a material that is recognized as safe in such a way that it does not include as a raw material the potential end use of the resulting dry distiller grain (GSD).
    [00011] Some embodiments of the invention provide the benefit of producing a cleaner oil (high quality) by minimizing suspended solids and / or the water content of the resulting oil.
    [00012] Some embodiments of the invention provide a benefit for maintaining the centrifuge in the form of reducing deposited materials, thus reducing the need for interruptions and cleaning, as well as allowing an extension of time between backwash purges leading to an increase production and less downtime. This additionally provides simpler and easier cleaning value of the centrifuge in interruptions.
    [00013] Some embodiments of the invention provide a benefit for maintaining evaporators in the form of reducing deposited materials, decreasing the frequency and complexity of cleaning, decreasing downtime and thus reducing costs. BRIEF DESCRIPTION OF THE FIGURES
    [00014] Figure 1: Partial generic view representative of ethanol production from corn, indicating preferred points of addition for the chemical additive: to integral vinasse before separation into moist cake and fine vinasse, at or near the entrance of the centrifuge 1 , point 1; at or near the evaporator inlet, point 2; directly at the evaporator (s), point 3; at a point before or at the entrance of the oil centrifuge, centrifuge 2, point 4. DETAILED DESCRIPTION OF THE INVENTION
    [00015] The present invention relates to a method that can be applied to integral vinasse, fine vinasse or the syrup processing operation in the production of ethanol from corn, preferably employing a dry milling process, to provide an increase in oil yield.
    [00016] The present invention describes a method for recovering oil in the production of ethanol from corn, this method comprising the step of adding at least one chemical additive to a process stream, in which the at least one chemical additive comprises a functionalized polyol derived from a sorbitol, sorbitan or isosorbide.
    [00017] One aspect of the method comprises the application of a chemical additive to the stream of the fine vinasse process and / or to the concentrated syrup before the oil separation step. Preferably, the separation of oil from the concentrated syrup is achieved by means of a mechanical operation such as a membrane or a centrifuge. Most preferably, the separation is achieved by means of a centrifuge such as a disk centrifuge or a horizontal tricanter centrifuge. Other mechanical separators can also be used in the present invention, including, but not limited to, reverse centrifugal cleaners.
    [00018] A second aspect of the method comprises the application of a chemical additive to the whole vinasse before separation into fine wine and wet cake.
    [00019] The chemical additive can be added at different points in the separation system. Addition points for the chemical additive include, but are not limited to, integral vinasse prior to separation into wet cake and fine vinasse, one point after the oil centrifuge feed pump, but before the centrifuge inlet, one point after the evaporators and before the pump that feeds the centrifuge, and one point after the syrup feed tank and before the centrifuge. The syrup feed tank is usually located after the evaporators and before the centrifuge.
    [00020] Figure 1 is a generic partial view representative of the production of ethanol from corn. In general, in the process of producing ethanol from corn, after a number of different stages of maceration and fermentation, corn is converted into material referred to as "beer". The beer is then processed through a distillation process to separate the crude ethanol from the by-product thick (whole) wine. Thick vinasse is subjected to a centrifugation process to separate solids to produce moist grains from distillers and fine vinasse. The fine vinasse is then typically processed using a number of evaporator units to obtain the concentrated syrup. This syrup can then be further processed, for example, by means of centrifugation for oil separation, to separate the oil from the syrup. The remaining syrup is then typically combined with the wet distillers grain, then dried to provide dry distillers grain (GSD). The chemical additive of the present invention is typically added to the process stream at different points in the separation process. Some preferred addition points are shown in figure 1. The addition points include the integral vinasse process stream before separation into wet cake and fine vinasse, the process stream at or near the centrifuge inlet or after the separation centrifuge solids. The chemical additive can be added before or at the entrance and / or exit of one or more of the thin vinasse evaporators, in the evaporators, to the syrup just before the oil separation centrifuge and / or at the entrance of the pre-mixing tanks or heat retention. The areas in the process in which the chemical additive is typically loaded are designated by the area in parentheses ("{...}") in the diagram.
    [00021] Chemical additives useful in the present invention are those that provide an increase in oil production, if added to the processing of integral vinasse, before the separation of the wet cake, or of the fine vinasse before the oil separation operation. The application of chemical additives may include one or more points of addition within the unit operation of fine vinasse processing. Preferably, chemical additives are applied to the resulting syrup from the concentration of fine vinasse in an evaporator.
    [00022] A class of chemical additives useful in the present invention are functionalized polyols derived from sorbitol, isosorbide or a sorbitan, including 1,4-sorbitan. Preferred chemical additives are functionalized polyols comprising alkoxylated sorbitan monoalkylates, alkoxylated sorbitan dialkylates, alkoxylated sorbitan trialkylates and mixtures thereof. Preferably, the alkoxylated sorbitan alkylates have an alkyl chain length of about 6 to about 24 carbon atoms, preferably about 8 to about 18 carbon atoms; preferable as alkoxylated sorbitan alkylates are alkoxylated sorbitan esters. The alkoxylated sorbitan alkylate is preferably alkoxylated with about 5 to about 100 moles of alkyl oxide, preferably from 5 to 60 moles, preferably from 10 to 30 moles, more preferably from 12 to 30 moles; alkoxylated sorbitan alkylates are alkoxylated sorbitan esters. Preferred alkyl oxides are ethylene oxide and propylene oxide or a combination thereof. Preferred alkoxylated sorbitan alkylate is sorbitan monolaurate, sorbitan monooleate, sorbitan monopalmitate or sorbitan monostearate that has been alkoxylated with less than 50 moles of ethylene oxide or propylene oxide or a combination thereof. More preferred alkoxylated sorbitan alkylates are sorbitan monolaurate, sorbitan monooleate, sorbitan monopalmitate or sorbitan monostearate which have been ethoxylated with about 10 moles to about 30 moles of ethylene oxide or propylene oxide or a combination thereof; preferably, the alkoxylated sorbitan alkylates are alkoxylated sorbitan esters. More preferred alkoxylated sorbitan alkylates are sorbitan monolaurate, sorbitan mono-oleate, sorbitan monopalmitate or sorbitan monostearate which have been alkoxylated with about 12 moles to about 25 moles of ethylene oxide or propylene oxide or a combination of these; preferably, the alkoxylated sorbitan alkylates are alkoxylated sorbitan esters. Particularly preferred are sorbitan monolaurate, sorbitan monooleate, sorbitan monopalmitate or sorbitan monostearate which have been alkoxylated with approximately 20 moles of ethylene oxide or propylene oxide or a combination thereof. Another preference is for compositions / grades of this class of materials that are, or can be, classified as known to be safe in such a way that they do not understand the potential end use of the resulting dry distiller grain as a raw material.
    [00023] Classes of chemical additives that may be useful in the present patent application are alkoxylated sorbitan esters, alkoxylated fatty alcohols, alkoxylated fatty acids, sulfonated alkoxylates, quaternary alkylammonium compounds, alkylamine compounds, alkylphenol ethoxylates and mixtures thereof. Additional classes of chemical additives that may be useful for the invention include salts of fatty acids (sodium, ammonium or potassium) and low molecular weight silicone surfactants. The alkoxylate portion of the preceding chemical classes can be any mixture of ethylene oxide and propylene oxide added as a block or random to the base molecule. Most preferred are alkoxylated sorbitan esters.
    [00024] The chemical additive can be a mixture of materials as described above. Various functionalized polyols derived from a sorbitol, isosorbide and / or sorbitan, including 1,4-sorbitan, can be mixed together and used as a chemical additive for the present invention. Other additives that may be useful in conjunction with functionalized polyols include triglycerides, such as vegetable oil; liquid mixtures containing up to 5% by weight of hydrophobic silica; and high melting point waxes (above 60 ° C). These additives are well known in the defoamer industry. Vegetable oils include, but are not limited to, soy oil, canola oil and corn oil. Triglyceride or liquid mixtures containing up to 5% by weight of hydrophobic silica or high melting point wax can be added in an amount of 1 to 100% by weight based on the weight of the chemical additive.
    [00025] The chemical additive can be added to the process stream (whole vinasse, fine vinasse or syrup) in an amount of 50 to 5,000 ppm based on the weight of the process stream, or from 100 to 5,000 ppm, or from 200 to 2,500 ppm, preferably from 300 to 1,300 ppm, from 500 to 1,100 ppm, from 500 to 800 ppm. The chemical additive is added to the process stream (whole vinasse, fine vinasse or syrup) in an amount of at least 50 ppm, preferably at least 100 ppm, more preferably at least 200 ppm, more preferably at least 300. Preferably, the amount of chemical additive is less than 10,000 ppm, less than 5,000 ppm, less than 2,500 ppm, less than 1,500 ppm or less than 1,000 ppm.
    [00026] These chemicals can be applied in the normal ranges of temperatures and pHs found in a variety of process streams typical of commercial operations. For example, according to, but not limited to, the teachings of Cantrell and colleagues in U.S. Patent No. 7,602,858 B2, a preferred syrup composition, resulting from fine vinasse concentration, for centrifugal oil separation, is located in a temperature between 150212 ° C, pH between 3-6 and a moisture content of more than 15% and less than 90% by weight.
    [00027] The chemical additive can be heated and applied to the process stream (whole vinasse, fine vinasse or syrup) in a temperature range of 18 ° C to 100 ° C, preferably from 25 ° C to 85 ° C, more preferably from 30 ° C and 80 ° C. In some embodiments, when the heated additive is added to the process stream, there is a better separation of the oil compared to the use of a chemical additive at 18.3 ° C.
    [00028] A negative impact of processing the syrup at higher temperatures to improve oil yield, for example, temperatures above 90 ° C or 96 ° C, depending on the process, is that discoloration of the syrup results which gives a negative appearance to distillers dry grain (GSD) and decreases the value of this material. Higher processing temperatures can produce a higher color of the oil itself. As such, an additional benefit of the invention is the ability to increase oil yield at lower processing temperatures and to minimize the potential for the processed syrup to negatively impact the appearance and value of GSD and oil. Reducing processing temperatures also leads to global energy savings. EXAMPLES Example 1
    [00029] Ashland PTV M-5309, an ethoxylated sorbitan monolaurate ester (20 moles) was added with a dosage of 611 ppm to the syrup feed line on the inlet side of the feed pump of a disc centrifuge with producer of ethanol from corn in the Midwest to achieve an approximately 29% increase in corn oil production (from about 1.7 gpm before treatment to about 2.2 gpm after treatment). In addition, it was observed that the content of suspended solids in a 50 ml aliquot of the oil isolated after centrifugation in the laboratory dropped from ~ 4 ml to ~ 1 ml after treatment.
    [00030] Table 1 summarizes a dose response for two 4-hour trials and the result of a five-day trial, carried out at different times on this site. The observed amount of Ashland PTV M5309 is based on the product in relation to the syrup feed. For the 4-hour tests, the reported data are the oil production rate after the system has balanced itself against the untreated production rate (0 ppm) at the beginning of the study. For the 5-day trial, the result is the average production rate over that period of time in relation to the untreated production rate (0 ppm) at the beginning of the study. TABLE 1
    Example 2
    [00031] This field test analyzed the difference between adding 680 ppm of Ashland PTV M-5309, an alkoxylated sorbitan ester, to the syrup stream with an ethanol producer from corn from the Midwest at different points addition. One of the points of addition was the inlet side of the feed pump of a disk centrifuge as in Example 1. The other point of addition examined was after the pump and directly at the inlet of the disk centrifuge. Regarding the daily production rate of untreated oil immediately before the test, an increase in daily oil production of approximately 15% and 17% after treatment, respectively, was measured. Example 3
    [00032] This field test was similar to that of Example 1, except for the use of 690 ppm Ashland PTV M-5309 was added to the syrup stream with an ethanol producer from corn from the Midwest on the inlet side of the feed pump in a horizontal tricanter centrifuge. After treatment, an increase in the oil production rate of approximately 45% was observed in relation to the untreated production rate at the beginning of the test. Example 4
    [00033] This field test examined the effect of temperature on the performance of the chemical additive. Ashland PTV M-5309, at a temperature of 18.3 ° C, was added just before the oil extraction centrifuge to produce oil at a rate of 10.5 gallons per minute. Ashland PTV M-5309 was then heated to a temperature of 48.9 ° C and added immediately before the oil extraction centrifuge to produce oil at a rate of 12.3 gallons per minute. The higher temperature of the chemical additive increased the oil recovery by 17%. Example 5
    [00034] Ashland PTV M-5309 was added at a dosage of 980 ppm to the syrup feed line on the inlet side of the feed pump of a disc centrifuge with an ethanol producer from corn in the Midwest to obtain a corn oil output of approximately 5.47 gpm. In a second phase of the trial, Ashland PTV M-5309 was added at a dosage of 490 ppm to the syrup feed along with 490 ppm of Nofoam 7077 (SSC Industries, East Point, GA) to provide a production of 5.76 corn oil gpm. This corresponded to a 5% increase in oil production. Example 6
    [00035] This laboratory experiment examined the effect of the length of the alkyl chain on the effectiveness of the product. Several alkoxylated sorbitan esters have been tested. The ethoxylated portion of the product was maintained at 20 moles. Products with different alkyl, lauric, palmitic, stearic and oleic chains were tested by adding 0.03 g of additive to 100 ml of corn syrup at 85 ° C, followed by 0.5 minutes of intense mixing. 10 ml of each sample was transferred to a centrifuge tube and then centrifuged for 10 minutes at 3,000 rpm. The amount of oil was determined by measuring the height of the oil layer in the centrifuge tube. TABLE 2

    [00036] As can be seen in Table 2, a comparable performance was observed for the different chain lengths tested. Example 7
    [00037] This laboratory experiment examined the effect of unsaturation on the alkyl chain on the product's effectiveness. Several alkoxylated sorbitan esters have been tested. The ethoxylated portion of the product was maintained at 20 moles. The tested products were prepared from stearic and oleic acids. The tests were carried out with 0.12 g, 0.15 g and 0.18 g of additive for 100 ml of corn syrup at 85 ° C, followed by 0.5 minutes of intense mixing. 10 ml of each sample was transferred to a centrifuge tube and then centrifuged for 10 minutes at 3,000 rpm. The amount of oil was determined by measuring the height of the oil layer at the top of the centrifuge tube. TABLE 3

    [00038] As can be seen in Table 3, a better performance of the saturated chain product was observed. Example 8
    [00039] This study examined the effectiveness of chemistry on whole vinasse using the method of Example 5. PTV M-5309 was added to whole vinasse before the wet pie centrifuge at a commercial corn ethanol plant. Samples of the fine vinasse from the centrifuge were collected. The samples of fine vinasse were subjected to laboratory centrifugation. The following results show that adding the product to the whole vinasse does not improve the oil separation. TABLE 4
    Example 9
    [00040] This laboratory experiment analyzed the effect of mixing various polysorbates on oil separation. Several alkoxylated sorbitan esters have been tested. The table below shows the various mixtures of alkoxylated sorbitan esters. In each example, 0.18 grams of mixed material was added to 100 ml of corn syrup at 85 ° C, followed by 0.5 minutes of intense mixing. 10 ml of each sample was transferred to a centrifuge tube and then centrifuged for 10 minutes at 3,000 rpm. The amount of oil was determined by measuring the height of the oil layer at the top of the centrifuge tube. Polysorbitan monooleate (5 moles of ethylene oxide): psmo5 Polysorbitan oleate (20 moles of ethylene oxide): psmo20 Polysorbitan monolaurate (20 moles of ethylene oxide): psml20 Polysorbitan monostearate (20 moles of ethylene oxide): psms20 TABLE 5

    [00041] Although the present invention has been described with respect to particular embodiments thereof, it is evident that numerous other forms and modifications will be obvious to those skilled in the art. The appended claims and this invention should generally be interpreted to cover all of these obvious forms and modifications, which are within the true scope of the present invention.
    权利要求:
    Claims (20)
    [0001]
    1. Method for the recovery of oil from ethanol production from corn, the method characterized by the fact that it comprises the step of adding at least one chemical additive to a process stream of corn to ethanol, in which the at least one chemical additive comprises a functionalized polyol derived from a sorbitol, a sorbitan or an isosorbide.
    [0002]
    2. Method according to claim 1, characterized by the fact that the functionalized polyol is derived from 1,4-sorbitan or isosorbide.
    [0003]
    Method according to claim 1 or 2, characterized in that the functionalized polyol comprises an alkoxylated sorbitan alkylate.
    [0004]
    4. Method according to claim 3, characterized by the fact that the length of the alkylate chain is 6 to 24 carbon atoms.
    [0005]
    5. Method according to claim 4, characterized by the fact that the length of the alkylate chain is 8 to 18 carbon atoms.
    [0006]
    6. Method according to claims 3 to 5, characterized in that the alkoxylated sorbitan alkylate has been alkoxylated with 5 to 60 moles of alkyl oxide.
    [0007]
    Method according to claims 3 to 6, characterized in that the alkoxylated sorbitan alkylate has been alkoxylated with 10 to 30 moles of alkyl oxide.
    [0008]
    8. Method according to claims 3 to 7, characterized by the fact that the alkyl oxide is selected from ethylene oxide, propylene oxide and mixtures thereof.
    [0009]
    9. Method according to claims 3 to 8, characterized in that the alkoxylated sorbitan alkylate comprises a sorbitan monolaurate which has been alkoxylated with about 10 to about 30 moles of an alkoxylate in which the alkoxylate is selected from ethylene oxide, propylene oxide or mixtures thereof.
    [0010]
    10. Method according to claims 3 to 9, characterized in that the alkoxylated sorbitan alkylate comprises a sorbitan mono-oleate which has been alkoxylated with about 10 to about 30 moles of an alkoxylate in which the alkoxylate is selected from ethylene oxide, propylene oxide or their mixtures.
    [0011]
    11. Method according to claims 3 to 10, characterized in that the alkoxylated sorbitan alkylate comprises a sorbitan monolaurate, sorbitan mono-oleate, sorbitan mono-palmitate or sorbitan monostearate which has been ethoxylated with about 12 to about 25 moles of an acoxylate in which the alkoxylate is selected from ethylene oxide, propylene oxide or mixtures thereof.
    [0012]
    12. Method according to any one of claims 1 to 11, characterized in that the amount of chemical additive added is 300 to 1,300 ppm.
    [0013]
    13. Method according to claim 12, characterized by the fact that the amount of chemical additive added is 500 to 1,100 ppm, based on the weight of the process stream.
    [0014]
    Method according to any one of claims 1 to 13, characterized in that the added chemical additive is heated to at least 30 ° C, prior to addition to the process stream.
    [0015]
    Method according to any one of claims 1 to 14, characterized in that it further comprises the step of adding a triglyceride to the process stream.
    [0016]
    16. Method according to claim 15, characterized by the fact that the amount of triglyceride is from 1 to 100% by weight, based on the weight of the chemical additive.
    [0017]
    17. Method according to any one of claims 1 to 16, characterized in that the chemical additive is heated before being added to the process stream.
    [0018]
    18. Method according to claim 17, characterized by the fact that the chemical additive is heated between 25 ° C and 85 ° C.
    [0019]
    19. Method according to any one of claims 1 to 18, characterized in that the addition point in the process stream is selected from the integral vinasse process stream prior to removal of the wet cake, from the vinasse process stream fine at the entrance and / or exits of one or more of the evaporators, at the evaporator, at the entrance to the premix or heat retention tanks, in the syrup, just before the oil separation centrifuge or any combination thereof.
    [0020]
    20. Method according to any one of claims 1 to 19, characterized in that it further comprises the step of adding an additional process additive in which the additional process additive is selected from the group consisting of mixtures of liquids which contain up to 5% by weight of hydrophobic silica; and high melting point waxes (above 60 ° C).
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US6266379B1|1997-06-20|2001-07-24|Massachusetts Institute Of Technology|Digital transmitter with equalization|
    US7497955B2|2004-07-09|2009-03-03|Nalco Company|Method of dewatering thin stillage processing streams|
    US20060006116A1|2004-07-09|2006-01-12|Scheimann David W|Method of dewatering thin stillage processing streams|
    WO2006099456A1|2005-03-16|2006-09-21|Gs Ethanol Technologies, Inc.|Method of recovering oil from corn byproducts and related subsystem |
    US20100331580A1|2006-11-15|2010-12-30|Growmark, Inc.|Oil recovery and syngas production from biomass-based processes|
    US20080176298A1|2006-11-15|2008-07-24|Randhava Sarabjit S|Oil recovery from dry corn milling ethanol production processes|US9776105B2|2010-11-19|2017-10-03|Nalco Company|Method for conditioning and processing whole or thin stillage to aid in the separation and recovery of protein and oil fractions|
    US8962059B1|2011-05-27|2015-02-24|Superior Oil Company, Inc.|Bio-based oil composition and method for producing the same|
    WO2013134234A1|2012-03-07|2013-09-12|Abengoa Bioenergy New Technologies, Llc|Methods for enhancing the recovery of oil during biofuel production|
    US9394505B2|2012-12-04|2016-07-19|Flint Hills Resources, Lp|Recovery of co-products from fermentation stillage streams|
    AU2013364289B2|2012-12-19|2016-07-14|Buckman Laboratories International, Inc.|Methods and systems for bio-oil recovery and separation aids therefor|
    US9090851B2|2013-03-13|2015-07-28|Hydrite Chemical Co.|Oil extraction method and composition for use in the method|
    WO2015009485A1|2013-07-18|2015-01-22|Croda, Inc.|A method of separating oil from a liquid stillage|
    CN105579566B|2013-08-28|2020-01-10|索理思科技公司|Oil extraction aid in grain processing|
    WO2015057191A1|2013-10-15|2015-04-23|General Electric Company|Methods and compositions for improving oil recovery in corn processing|
    US20150284659A1|2014-04-07|2015-10-08|U.S. Water Services, Inc.|Method and composition for increasing recovery of oil from fermentation processes|
    US9816050B2|2014-10-27|2017-11-14|Dean Blankenburg|Oil extraction method and composition for use in the method|
    US10377652B1|2014-12-05|2019-08-13|Fremont Industries, Inc.|Process for enhanced fractionation of recovered waste streams|
    AR103032A1|2014-12-16|2017-04-12|Polymer Ventures Inc|OIL RECOVERY ASSISTANT|
    US10597603B2|2014-12-16|2020-03-24|Polymer Ventures, Inc.|Oil recovery aid|
    US9255239B1|2014-12-30|2016-02-09|Ivanhoe Industries, Inc.|Formulation for corn oil recovery and method of use thereof|
    WO2016109642A1|2014-12-30|2016-07-07|Ivanhoe Industries, Inc.|Formulation for corn oil recovery and method of use thereof|
    WO2016114983A1|2015-01-16|2016-07-21|Croda, Inc.|Method of separating oil|
    CA2969345A1|2015-01-16|2016-07-21|Croda, Inc.|Method of separating oil|
    US9399750B1|2015-06-22|2016-07-26|Ivanhoe Industries, Inc.|Formulation for corn oil recovery and method of use thereof|
    US10005982B2|2015-07-18|2018-06-26|Ecolab Usa Inc.|Chemical additives to improve oil separation in stillage process operations|
    US20180206526A1|2015-07-20|2018-07-26|Cidra Corporate Services Inc.|Applying measurement, control and automation to a dry corn milling ethanol production process to maximize the recovery of ethanol and co-products|
    US9714398B2|2015-07-31|2017-07-25|General Electric Company|Method for improving corn oil extraction using alkyl polyglycosides|
    US11220663B2|2015-10-23|2022-01-11|Fluid Quip Technologies, Llc|System and process for clarifying thin stillage|
    US20170166834A1|2015-12-10|2017-06-15|Fluid Quip Process Technologies, Llc|Systems and methods to improve co-product recovery from grains and/or grain components used for biochemical and/or biofuel production using emulsion disrupting agents|
    US9738850B1|2016-04-11|2017-08-22|Ivanhoe Industries|Use of alkoxylyated mono- and diglycerides for corn oil recovery|
    RU2760772C2|2017-01-17|2021-11-30|Соленис Текнолоджиз Кеймэн, Л.П.|Means of separating oils in production of bioproducts|
    US10782241B2|2017-07-27|2020-09-22|Ecolab Usa Inc.|Method of determining residual flocculant in effluent of an industrial clarification process|
    US10711221B2|2018-02-09|2020-07-14|Poet Research, Inc.|Method of refining a grain oil composition to make one or more grain oil products, and related systems|
    US10745283B1|2018-05-11|2020-08-18|Applied Material Solutions, Inc.|Demulsification compound and method for oil separation from waste streams|
    EP3799598A1|2018-06-11|2021-04-07|POET Research, Inc.|Methods of refining a grain oil composition feedstock and related systems compositions and uses|
    EP3820928A1|2018-09-05|2021-05-19|Lonza Guangzhou Nansha Ltd.|Method for making polyoxyethylene 1,4 sorbitan fatty acid ester|
    US10443017B1|2019-01-21|2019-10-15|Trucent, Inc.|Process and method for the recovery of oil from the processing of grains into biofuels and other chemicals|
    US10981087B2|2019-01-21|2021-04-20|Trucent, Inc.|Process and method for the recovery of oil from the processing of grains into biofuels and other chemicals|
    EP3831915A1|2019-12-06|2021-06-09|Basf Se|Additives and use thereof in corn fermentation process streams and other bioprocesses|
    法律状态:
    2018-03-06| B25A| Requested transfer of rights approved|Owner name: SOLENIS TECHNOLOGIES CAYMAN, L.P. (CH) |
    2018-04-03| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-07-16| B06T| Formal requirements before examination [chapter 6.20 patent gazette]|
    2020-07-21| B06A| Notification to applicant to reply to the report for non-patentability or inadequacy of the application [chapter 6.1 patent gazette]|
    2020-11-24| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2021-02-02| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 10/02/2012, OBSERVADAS AS CONDICOES LEGAIS. |
    2021-08-24| B25G| Requested change of headquarter approved|Owner name: SOLENIS TECHNOLOGIES CAYMAN, L.P. (CH) |
    优先权:
    申请号 | 申请日 | 专利标题
    US201161454634P| true| 2011-03-21|2011-03-21|
    US61/454,634|2011-03-21|
    PCT/US2012/024599|WO2012128858A1|2011-03-21|2012-02-10|Chemical additives and use thereof in stillage processing operations|
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