CORN PROTEIN PRODUCT HAVING DECREASED FREE SULFITE LEVELS AND METHOD FOR MANUFACTURING SAME
Described herein is a corn protein product comprising greater than about 20% corn protein on a dry weight basis and a free sulfite concentration of less than 150 ppm on an as-is basis. Also disclosed herein is a method to obtain this corn protein product including the steps of providing a protein-rich stream derived from a wet corn milling operation, wherein the protein-rich stream comprises greater than 20% corn protein on a dry weight basis, and treating the protein-rich stream with an oxidant, preferably hydrogen peroxide.
Latest CARGILL, INCORPORATED Patents:
This application claims priority to U.S. Provisional Application 62/312,798 filed on Mar. 24, 2016, which is hereby incorporated by reference in its entirety.
TECHNICAL FIELDThis disclosure relates to corn protein products having low free sulfite concentrations and methods of manufacturing the same.
BACKGROUNDProtein-rich streams (e.g. germ meal, gluten meal, corn protein concentrate for example Empyreal®, corn protein isolate) derived from typical wet corn milling processes contain sulfite in the range of about 500 ppm to about 2000 ppm (as is basis) due to sulfite added to facilitate effective wet milling of corn. The added sulfite plays two major roles during wet milling of corn: firstly to cleave disulfide bonds in the storage protein matrix thereby loosening protein-starch entrapment to facilitate starch/protein separation; and secondly to control unwanted microbial growth during the entire wet milling process. Consequently, the mill protein streams contain a combination of free sulfite (in equilibrium with SO2) and bound sulfite in the form of S-sulfocysteine.
With a movement towards cleaner food labels, there is a desire to reduce the free sulfite content in these protein-rich streams.
SUMMARYDescribed herein is a corn protein product comprising greater than about 20% corn protein on a dry weight basis and a free sulfite concentration of less than 150 ppm on an as-is basis. Also disclosed herein is a method to obtain this corn protein product including the steps of providing a protein-rich stream derived from a wet corn milling operation, wherein the protein-rich stream comprises greater than 20% corn protein on a dry weight basis, and treating the protein-rich stream with an oxidant, preferably hydrogen peroxide.
Described herein is a corn protein product comprising greater than about 20% corn protein on a dry weight basis and a free sulfite concentration of less than 150 ppm on an as-is basis and methods of manufacturing the same.
Oxidation Reaction
A protein-rich stream derived from a wet corn milling process is first provided. The protein-rich stream may be, for example but not limited to, corn germ meal, corn gluten meal (including both pressed and solvent extracted meal), corn protein concentrate for example Cargill Empyreal®, or corn protein isolate. These protein-rich streams typically comprise free sulfite concentration in the range of about 300 ppm to 5000 ppm on an as-is weight basis. For certain food applications, it is desirable to reduce this free sulfite content. Further, these protein-rich streams typically comprise greater than 20% corn protein, and in many aspects greater than 50% corn protein, and in some aspects, greater than 85% corn protein on a dry weight basis.
The protein-rich stream is treated with an oxidant to obtain a corn protein product. Because sulfite is a reducing compound, oxidation treatments have been reported to reduce sulfite levels in various foods and beverages. However, the unique sulfite-protein interaction in wet corn milling presents a challenge in decreasing sulfite concentration in the protein-rich streams described herein. It shall be understood that the term “treatment” includes washing, blending, mixing, etc., the corn protein product with an oxidant. Such treatments can include chemical and enzymatic oxidation of the sulfite in aqueous, organic solvent or gas systems.
The oxidant described herein can be, for example but not limited to, hydrogen peroxide, ozone gas, air, sodium hypochlorite, a combination of potassium bromate and ethanol, catalase, peroxidase, or a combination thereof. In preferred aspects, the oxidant is hydrogen peroxide.
For the production of low-sulfite corn protein products, a range of hydrogen peroxide treatments can be applied depending on the effectiveness and/or applicability of each option and the final target of free sulfite in corn protein products. Two preferred aspects of hydrogen peroxide treatments are to either spray a hydrogen peroxide containing water onto the protein-rich stream during drum filtration or mix hydrogen peroxide with ethanol and add it to a wet cake in an extractor, where the H2O2-ethanol-water mixture and the ethanol-water solvent is predominantly removed by a subsequent separation such as drainage, decanting, centrifugation, filtration of other methods known to the art. Care is taken in the extractor-based approach to create solvent-peroxide solutions that are not dangerously reactive. In aspects of this invention, at least 1.8 moles and no more than 10 moles of oxidant is needed as part of the oxidation treatment to oxidize 1 mole of free sulfite in the protein-rich stream. In preferred aspects, the oxidation reaction may take a total of 10 minutes to 2 hours.
It is surprising that treating the protein-rich stream with an oxidant such as hydrogen peroxide does not degrade the protein structure (and therefore negatively impact the nutritional value of the protein or functional properties of the protein). Without being bound by any theory, it is believed that the hydrogen peroxide treatment quickly and selectively reacts with free sulfite and hydrogen peroxide is not consumed by other potential impurities (e.g., peroxidases, microbials, typtophans, tyrosine, etc.). It is also surprising that the process of sulfite oxidation works in a range of pH values and a variety of moderate temperatures.
Corn Protein Product
After treating the protein-rich stream with the oxidant, the resulting corn protein product comprises a free sulfite concentration of less than 150 ppm on an as-is basis. In preferred aspects, the free sulfite concentration is less than 100 ppm on an as-is basis, more preferably less than 75 ppm on an as-is basis, 40 ppm on an as-is basis, even more preferably less than 20 ppm on an as-is basis, and even more preferably less than 10 ppm on an as-is basis. Note that free sulfite concentration is measured by the Monier-Williams AOAC 990.28 method or ion-chromatography method of AOAC 990.30. Furthermore, any reference to “sulfite” described herein means free sulfite.
Further, the resulting corn protein product while it may comprise corn protein greater than about 20% on a dry basis, preferred aspects of the corn protein product comprises corn protein between about 55% and 95% on a dry weight basis or between about 90% and 98% on a dry weight basis.
Furthermore, it is also desirable that the corn protein product comprise less than 35% digestible carbohydrate on a dry weight basis.
End-Use Applications
Protein ingredients derived from corn wet milling are commonly used in feeding domestic animals for economic and companion purposes. The invention described here would allow the manufacture of lower sulfite animal feed products. Protein ingredients derived from corn are not widely used in human foods for a variety of reasons, one of which is the presence of sulfite at concentrations higher than commonly acceptable. The invention described here overcomes this limitation. Consequently, corn-derived protein ingredients with low free sulfite concentrations might be economically included in breakfast cereal, nutrition bar, bakery product and processed meat formulations, among other things.
EXAMPLESNote for many of the examples, the specific free sulfite concentration of the raw material is unknown, but the value is typically between 500 and 900 ppm on an as is basis (approximately 800 to 1500 ppm on a dry solids basis).
Example 1: Treating the Alpha-Amylase-Treated Heavy Gluten Slurry (Empyreal® Slurry) with Hydrogen PeroxideCargill Empyreal® slurry is first provided. The slurry is held at 77° C. in an enclosed container. The slurry contains 13% dry solids when measured using METTLER-TOLEDO HALOGEN moisture balance at 110° C. The slurry has a pH 5.3.
The Empyreal® slurry is used at as-is pH or adjusted to pH 7.3 (with 50% NaOH) before use. The slurries are vigorously hand-mixed for homogeneity before 40 g aliquots are added to 50-ml test tubes. Hydrogen peroxide solution (30% active hydrogen peroxide) is added to each test tube at dosages of 0 (control), 500 or 1000 ppm of active hydrogen peroxide on a total mass basis. The test tubes are inverted to ensure a thorough mixing in a hybridizer set at 75° C. Test tubes are removed after a 15-90 minute treatment and centrifuged at 4000 rpm at room temperature for 5 minutes.
For sulfite analysis, the supernatant (liquid portion) is further diluted with 0.05 M tris-buffer pH9.5 then analyzed by ion-chromatography according to AOAC 990.30. The solid portion is re-suspended with the addition of 20-ml 0.05 M tris-buffer pH9.5 at 37° C. in the hybridizer for 10 minutes then centrifuged at 4000 rpm for 5 minutes. The supernatant is directly used or further diluted as needed with the tris-buffer for sulfite analysis on ion-chromatography.
As shown in
Raising the pH seems to have a slight effect on sulfite oxidation in the solid portion when hydrogen peroxide dose is low at 500 ppm. No significant difference is found between pHs for the liquid portion or when enough hydrogen peroxide is added.
When calculated on a molar basis, 500 ppm hydrogen peroxide equals 14.71 mM and 900 ppm sulfite equals 11.25 mM. Data in
This laboratory experiment is conducted to mimic water washing of the wet cake during drum filtration operations. The wash ratio (WR) is calculated based on the ratio of washing solution to the original volume of the slurry. So a wash ratio of 1/10 indicates that 1 L of water is being used to wash the cake created from 10 kg of slurry. Because the washing occurs after the cake is essentially drained, the actual dilution of cake entrained water is much higher. In these experiments, the solids content of the Empyreal slurry is about 13%. Filter cakes moistures are about 60%, so 10 kg of slurry results in a cake containing less than 1300 g of solids and about 1950 mL of liquid. Subsequent washing with 1 L displaces about one-half of the entrained water in the cake. With a wash ratio of 1/25, the cake is washed with about 400 mL of liquid (or about 20% of the entrained water).
Cargill Empyreal® slurry is provided and maintained at 75° C. in a closed container until use. The slurry is vigorously hand-mixed for homogeneity before filtration. About 150 g of the well-mixed slurry is filtered through a filter paper with pore size of 40 micron (VWR Cat. No. 28313-068, 11.0-cm) under about 27-inches of Hg vacuum to yield a wet cake of about 3.2 mm (⅛ inch) thickness. When surface water disappears (takes about 1.5-2 minutes from the beginning of filtration), 6 ml (wash ratio=6/150=1/25 vol/wt) or 15 ml (wash ratio=15/150=1/10) city water containing 0 (control), 0.3% or 1.5% (0, 3000 and 15000 ppm, respectively) active hydrogen peroxide is sprayed to the surface of the wet cake using a spray gun at air pressure of about 15 psig while vacuum is kept on during the spray treatment. After all surface free moisture disappears, the cake is harvested.
The filtrates are used directly or diluted as needed with alkaline 0.05 M tris-buffer pH 9.5 for sulfite analysis with ion-chromatography. The wet cake (1 g) is fully resuspended with 10 ml of the tris-buffer at 37° C. for 30 minutes then centrifuged at 4000 rpm for 5 minutes. The supernatant was used directly or further diluted as needed with the alkaline tris-buffer for sulfite analysis on ion-chromatography (AOAC 990.30).
This starting material has about 1200 ppm of free sulfite. Data in
It is noticed that at a lower wash ratio of 1/25, hydrogen peroxide concentration up to 1.5% does not cause significant change in sulfite levels in the filtrate. However, when wash ratio increased 2.5× to 1/10, sulfite in the filtrate is decreased about 50% to about 600 ppm when wash water contains 0.3% (3000 ppm) active peroxide. Sulfite in the filtrate is decreased to less than 50 ppm when the wash water contains 1.5% (15000 ppm) active peroxide and the wash ratio at 1/10. It is important to note that the filtered cake thickness is maintained to be ˜⅛″-thick to simulate the drum-filtered cake thickness at plant scale. When ½″-thick cake is used in lab experiment, no reduction in filtrate sulfite was detected. However at plant scale, additional cracking of the drum-filtered cake can occur, which may lead to greater peroxide leaching into the filtrates and induce higher sulfite reduction in the filtrate.
Surprisingly, the peroxide treatment has a strong effect on the solids fraction and a smaller effect on the filtrate fraction. For corn wet milling operations, it is important that the sulfite level in the filtrate remains unchanged so that the filtrate can be recycled back to the mill Without being bound to any theories, it is believed that essentially none of the peroxide-containing solution passes through the filter cake into the filtrate (assuming no cake cracking). At 1/25, displacement of the entrained liquid is about 20% and at 1/10 it is about 50%. Assuming a starting concentration of 1200 ppm free sulfite in the slurry, 10 kg of slurry (containing 12,000 mg or 150 mmol) yields 3.25 kg of wet cake (containing 1.95 L of entrained solvent). The cake contains approximately 3900 mg of sulfite (at 81 g/mole, this represents about 48 milimoles) of sulfite in the cake. One liter of wash solution containing 0.3% active H2O2 (3000 mg/L at 34 g/mol) delivers 88 millimoles of peroxide for a molar ratio of oxidant-to-sulfite of about 1.8. About 6.75 kg of filtrate containing 8.1 g (or 100 mmol) of sulfite is removed by filtration before contact with peroxide. Thus filtration before peroxide treatment avoids three-quarters the peroxide that is otherwise required.
Example 3: Treating the Alpha-Amylase-Treated and Dewatered Heavy Gluten Cake (Empyreal Cake) During Ethanol Extraction with Hydrogen PeroxideCargill Empyreal® slurry is provided and maintained at 75° C. in a closed container till use. 200 g of the well-mixed slurry is filtered through a filter paper with pore size of 40 micron (VWR Cat. No. 28313-068, 11.0-cm) under about 27-inches of Hg vacuum to yield a wet cake. When surface water disappears, 5 ml of city water is added to wash the cake (wash ratio=1/40) without breaking the vacuum. The resulting wet cake contains about 60% moisture when measured using METTLER-TOLEDO HALOGEN moisture balance at 110° C.
50 g of the wet cake is weighed into a 1-L glass Waring blender. After 200 ml of absolute ethanol containing 0 (control) or 0.15% (1500 ppm) active hydrogen peroxide (1 ml of 30% active hydrogen peroxide solution added into 200 ml ethanol) is added, the cake-ethanol mixture is blended at speed setting #1 (3350 rpm) on Waring Commercial Laboratory Blender (Model HGB7WT3) for about 1 minute. The well-blended mixture is immediately filtered through Whatman #4 filter paper under about 27-inches of Hg vacuum to yield a corn protein ingredient first extraction wet cake. The wet cake is dried in a vacuum oven at about 26 inches of Hg and 55° C. overnight. The dry product is ground in a coffee grinder before analysis for sulfite.
For sulfite analysis, 1 g of the ground sample is weighed into a 50-ml test tube then 10 ml of 0.05 M tris-buffer pH9.5 is added. The test tubes are inverted in a hybridizer at 50° C. for 30 min then centrifuged at 4000 rpm for 5 minute. The supernatant is directly used or further diluted as needed for sulfite analysis in ion-chromatography (AOAC 990.30). Results are expressed as SO2 in ppm.
The laboratory corn protein ingredient product made with the Empyreal cake extracted with 4 volumes of absolute ethanol (control) has an average of about 650 ppm sulfite, whereas the product made with 4 volumes of absolute ethanol containing 0.15% active hydrogen peroxide has about 20 ppm sulfite (
Destarched corn gluten cake was collected on a rotary drum vacuum filter with rinsing. The destarched slurry was fed to the drum at 1.2 gal/min at a density of about 1.016 g/mL. The pH was as is, and estimated to be about 5.9 based on typical analysis of the filtered cake. The rinse water supplemented with active hydrogen peroxide at a concentration of 0.3% w/w was applied at 0.12 gal/min (Wash ratio=1/10). Upon completion of the vacuum dewatering, the treated cake was frozen until analysis.
10 kg of the peroxide-treated, destarched corn gluten cake with 60-65% moisture was processed through a dual rotor crusher with a 0.125-inch screen to generate a uniformly sized particle for homogeneous extraction. The cake was fed to a Crown Iron Works Model IV immersion extractor using a drag conveyor dropping through a crossover screw and then a delumper (for a better understanding, an illustration of the Crown Iron Works Model IV immersion extractor may be found on the crowniron.com website) into the extractor. The extractor included a series of inclined drag conveyors arranged so that the lower end of the conveyor was submerged in the extraction solvent and the upper end was above the solvent. The conveyor carried the solids forward such that the material was initially submerged in solvent and then the material emerged from the solvent and excess solvent drained back into the solvent stream. At the end of the conveyor, the solids dropped onto another conveyor with a similar arrangement. The model IV extractor had six extraction stages. Fresh solvent was introduced at the discharge end and flowed towards the inlet end and was ultimately discharged at a point preceding the solids introduction. After the final solvent contact, the solids were conveyed up a long section to allow more extensive draining before falling into a crossover screw for transport to desolventizing. The solvent was fed into the system at different solvent:solids ratios of about 4 to about 18 and the solvent was maintained at different temperatures of about 20° C. to about 60° C. by in situ heat exchangers. Total contact time varied from about 30 to about 60 minutes.
The resulting materials were desolventized in a Bepex Solidaire dryer operated with a surface temperature of about 155-160° C. and an absolute pressure from about 270-330 millibar (with a target of about 300 millibar).
The desolventized material was ground in a hammer mill to yield a fine powder. As shown in Table 1, the resulting corn protein isolate products (all had greater than 85% protein on a dry weight basis) had 37 to 122 ppm SO2, at least 80% decrease from the historical average SO2 level of 530 ppm.
An ozonation apparatus was assembled and placed in a fume hood. Approximately 100 grams of a wet Empyreal cake was weighed and placed in the column. The sample was lightly pressed in the column with a steel rod. The ozone generator was then turned on and allowed to build pressure for 2 minutes. The flow rate was then set to 3 LPM, but varied according to the packing and overall system pressure. The percentage dial down of ozone stream was set to 30% which generates 1.2 g/hr of ozone (resulting in a gaseous concentration in the 2000-ppm range). The ozone/oxygen mixture was passed through the bottom of column for 2.5, 5, 10, and 30 minutes. Residual ozone leaving from the top of column was bubbled through a 2% sodium bisulfite solution (SBS) to reduce and capture escaping ozone. Any remaining ozone dissipated into the air via the ventilation hood exhaust. At the end of each test run, the samples were analyzed for moisture content using a METTLER-TOLEDO HALOGEN moisture balance at 110° C. For sulfite analysis, the samples were extracted with 50 mM tris-buffer containing 5 mM EDTA at sample-to-buffer ratio of 1-to-10 at 37° C. for 10 min, followed by centrifugation at 4000 rpm for 5 min. The resulting supernatant was either directly analyzed or further diluted with the tris-buffer. Sulfite was analyzed in a ion-exchange chromatography (AOAC 990.30).
As shown in
Cargill Empyreal slurry was provided. About 100 g of the slurry was transferred to a 150 ml jacketed glass column (25 mm×300 mm, Ace Glass) fitted with 100 micron filter discs on both ends. Compressed air was passed through the slurry at a flow rate of about 3 ml/sec from the bottom of the columns while the column jacket temperature was kept at 60° C. After 2.5 hour of air treatment, the slurry was filtered with filter paper (40 micron openings) to yield a wet cake of about 60% moisture. A similar cake was also obtained from untreated slurry (the control). Both wet cakes were dried in a vacuum oven dryer at about 26 inches vacuum and 55° C. overnight. The dry samples were ground in a coffee grinder to fine powders. For sulfite analysis, the samples were extracted with 50 mM tris-buffer containing 5 mM EDTA at sample-to-buffer ratio of 1-to-10 at 37° C. for 10 min, followed by centrifugation at 4000 rpm for 5 min. The resulting supernatant was either directly analyzed or further diluted with the tris-buffer. Sulfite was analyzed in an ion-exchange chromatography (AOAC 990.30).
Results showed that the control contained 266 ppm sulfite while the air-treated material had 204 ppm sulfite. The air treatment resulted in about 23% sulfite decrease in this case.
Example 7: Treating Empyreal Slurry with Sodium HypochloriteCargill corn gluten meal slurry was provided. About 200 g of the heavy gluten slurry was weighed into a 500-ml polyethylene container followed by addition of appropriate amounts of sodium hypochlorite solution (Clorox Ultra containing 6.15% NaClO) so that NaClO concentration in the slurry were at 500 ppm (6.76 mM), 1000 ppm (13.52 mM) or 2000 ppm (27.04 mM) respectively. The bottles were placed in a shaking water bath at 130° F. for 15 mM before the contents were filtered through Whatman #4 filter paper to yield wet cakes of about 60% moisture. Separately, the heavy gluten slurry without sodium hypochlorite was filtered through Whatman #4 filter paper to yield a control cake. All wet cakes were dried in a vacuum oven at about 26 inches vacuum and 55° C. overnight. The dry material was ground to fine powder in a coffee grinder. The ground material was analyzed for sulfite concentrations using the Monier-William's procedure of distillation and volumetric titration (AOAC 990.28).
Results showed that the sodium hypochlorite treatment decreased sulfite by 45-90% (Table 2).
About 50 g of Empyreal wet cake was weighed into a 1-L glass Waring blender then potassium bromate was added at 0.2% or 1% levels on a cake dry solid basis. After 200 ml of absolute ethanol was added, the cake-potassium bromate-ethanol mixture was blended at speed setting #1 on Waring Commercial Laboratory Blender (Model HGB7WT 3) for about 1 min. The well-blended mixture was immediately filtered through Whatman #4 filter paper under about 27-inches vacuum to yield a CPI (corn protein isolate) wet cake. Control was obtained by the same ethanol treatment without the addition of potassium bromate. The cake was dried in a vacuum oven at about 26 inches and 55° C. overnight. The dry product was ground to fine powders in a coffee grinder. The fine powders were analyzed for sulfite concentrations according to Monier-William's AOAC procedure (990.28).
Results showed that potassium bromate at 0.2% and 1% decreased sulfite concentrations in the final corn protein isolate by 62% and 78% respectively (Table 3).
A corn protein isolate containing 92.3% protein on a dry weight basis (5.7% loss on drying) was produced in a pilot plant in Savage, Minn. Aliquots of about 5 g of the CPI product were weighed into 50-ml test tubes with screw caps. Calcium peroxide was added at concentrations of 0 (control, no calcium peroxide addition), 2170 ppm, 3300 ppm or 5080 ppm on a dry weight basis. The dry blend of calcium peroxide and CPI were further gently mixed by inverting the test tubes at ambient temperature for 1 week. Sulfite concentrations were analyzed according to Monier-Williams AOAC procedure (990.28).
Results showed about 76-78% sulfite reduction by dry blending calcium peroxide with the corn protein isolate (Table 4).
Heavy corn slurry was provided. About 100 g aliquots of the well agitated material containing 13% dry solids and greater than 80% protein on a dry weight basis were dispensed into 250-ml polypropylene bottles with screw-caps. Catalase (Catazyme L25, Novozymes) was added to the test tubes at 0 (control), 0.1% or 1% (v/w) levels while peroxidase (from horseradish, Sigma-Aldrich) was added at 0.1% or 0.3% (w/w) levels based on dry solids of the slurry. The bottles were placed in an orbitally shaking incubator set at 60° C. and 120 rpm. After 2 hours incubation, the slurries were filtered through 40 micron paper filters to yield wet cakes of about 60% moisture. The wet cakes were dried in a vacuum oven dryer at about 26 inches vacuum and 55° C. overnight. The dry samples were ground to fine powders in a coffee grinder. The fine powders were analyzed for sulfite according to the Monier-William's AOAC procedure (990.28). Results showed that the catalase treatment decreased sulfite by 25% and 38% at 0.1% and 1% enzyme dosages while peroxidase decreased sulfite by 15% and 29% at enzyme dosages of 0.1% and 0.3% respectively (Table 5).
Destarched corn gluten cake was collected on a rotary drum vacuum filter without rinsing. The destarched slurry was fed to the drum at 1.2 gal/min at a density of about 1.016 g/ml. The pH was as is, and estimated to be about 5.9 based on typical analysis of the filter cake. Upon completion of the vacuum dewatering, the treated cake was frozen until it was ready for extraction.
98 kg of the untreated, destarched corn gluten cake with 60-65% moisture, which is in irregular flake form, was passed through a ¼-inch screen mounted on a Sweco shaker. This produced a more uniform particle to feed to the fluid bed dryer. The fluid bed dryer was fed at a rate of about 5.4 kg/hour, with inlet air temperatures of 120° C., bed temperature of 50° C. to obtain products of about 30-40% moisture content. The product recovered after drying was returned to refrigerated storage until extraction.
The cake was fed through a dual rotor crusher with 0.125-inch screen to generate a uniformly sized particle for homogeneous extraction. The cake was fed into a Crown Iron Works Model IV immersion extractor using a drag conveyor dropping through a crossover screw and then a delumper (for a better understanding, and illustration of the Crown Iron Works Model IV immersion extractor may be found on the crowniron.com website) into the extractor. The extractor included a series of inclined drag conveyors arranged so that the lower end of the conveyor was submerged in the extraction solvent and the upper end was above the solvent. The conveyor carried the solids forward such that the material was initially submerged in solvent and then the material emerged from the solvent and excess solvent drained back into the solvent steam. At the end of the conveyor, the solids dropped onto another conveyor with a similar arrangement. The model IV extractor has six extraction stages. Fresh solvent (98 wt % EtOH) then was supplemented with hydrogen peroxide to about 125 to 2000 ppm (see Table 6 for hydrogen peroxide concentrations). Solvent was introduced at the discharge end and flowed towards the inlet end and was ultimately discharged at a point preceeding the solids introduction. After the final solvent contact, the solids were conveyed up a long section to allow more extensive draining before falling into a crossover screw for transport to desolventizing. The solvent was fed into the system at a solvent:solids ratio of about 10 and the solvent was maintained at a temperature of about 25° C. Total contact time was about 30 minutes and the initial concentration of free sulfite in the unextracted material was 517 ppm of SO2.
The resulting materials were desolventized in a screw desolventizer, operated with a surface temperature of about 95° C. and an absolute pressure of about −26 inches of Hg. To improve evaporation, a sweep of nitrogen gas is injected into the vapor space of the desolventizer and is allowed to flow to the vacuum discharge.
Example 12. Hydrogen Peroxide Treatment in the Pilot Drum and Pilot ExtractionDestarched corn gluten cake was collected on a rotary drum vacuum filter with rinsing. The destarched slurry was fed to the drum at 1.2 gal/min at a density of about 1.016 g/mL. The pH was as is, and estimated to be about 5.9 based on typical analysis of the filtered cake. The rinse water supplemented with active hydrogen peroxide at a concentration of 0.3% w/w was applied at 0.12 gal/min (Wash ratio=1/10). Upon completion of the vacuum dewatering, the treated cake was frozen until it was ready for extraction.
98 kg of the untreated, destarched corn gluten cake with 60-65% moisture, which is in irregular flake form, was passed through a ¼-inch screen mounted on a Sweco shaker. This produced a much more uniform particle to feed to the fluid bed dryer. The fluid bed dryer was fed at a rate of about 5.4 kg/hour, with inlet air temperatures of 120° C., bed temperature of 50° C. to obtain products of about 30-40% moisture content. The product recovered after drying was returned to refrigerated storage until extraction.
The cake was fed through a dual rotor crusher with 0.125-inch screen to generate a uniformly sized particle for homogeneous extraction. The cake was fed into a Crown Iron Works Model IV immersion extractor using a drag conveyor dropping through a crossover screw and then a delumper (for a better understanding, and illustration of the Crown Iron Works Model IV immersion extractor may be found on the crowniron.com website) into the extractor. The extractor included a series of inclined drag conveyors arranged so that the lower end of the conveyor was submerged in the extraction solvent and the upper end was above the solvent. The conveyor carried the solids forward such that the material was initially submerged in solvent and then the material emerged from the solvent and excess solvent drained back into the solvent steam. At the end of the conveyor, the solids dropped onto another conveyor with a similar arrangement. The model IV extractor has six extraction stages. Fresh solvent was supplemented with hydrogen peroxide to about 350 ppm. Solvent was introduced at the discharge end and flowed towards the inlet end and was ultimately discharged at a point preceding the solids introduction. After the final solvent contact, the solids were conveyed up a long section to allow more extensive draining before falling into a crossover screw for transport to desolventizing. The solvent was fed into the system at a solvent:solids ration of about 10 and the solvent was maintained at a temperature of about 25° C. Total contact time was about 30 min.
The resulting materials were desolventized in a screw desolventizer, operated with a surface temperature of about 95° C. and an absolute pressure of about 26 inches of Hg. To improve evaporation a sweep of nitrogen gas is injected into the vapor space of the desolventizer and is allowed to flow to the vacuum discharge.
The resulting material had a residual SO2 of about 56 ppm.
Claims
1. A corn protein product, comprising:
- (a) greater than about 20% corn protein on a dry weight basis; and
- (b) a free sulfite concentration of less than 150 ppm on an as-is basis, wherein the source of the corn protein is corn protein isolate.
2. The product of claim 1, comprising a free sulfite concentration of less than 75 ppm on an as-is basis.
3. The product of claim 1, comprising a free sulfite concentration of less than 40 ppm on an as-is basis.
4. The product of claim 1, comprising a free sulfite concentration of less than 10 ppm on an as-is basis.
5. The product of claim 1, wherein the corn protein is between about 55% and 95% on a dry weight basis.
6. The product of claim 1, wherein the corn protein is between about 90% and 98% on a dry weight basis.
7-10. (canceled)
11. The product of claim 1, comprising a digestible carbohydrate content less than 35% on a dry weight basis.
12. The product of claim 1, wherein the corn protein product is for human and animal consumption.
13-38. (canceled)
Type: Application
Filed: Jun 21, 2022
Publication Date: Oct 6, 2022
Applicant: CARGILL, INCORPORATED (Wayzata, MN)
Inventors: Michael A. PORTER (Maple Grove, MN), Hadi Nayef YEHIA (Beavercreek, OH), Guo-Hua ZHENG (Centerville, OH)
Application Number: 17/808,003
