US20070015910A1 - Continuous process for production of oil seed protein isolate - Google Patents

Continuous process for production of oil seed protein isolate Download PDF

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Publication number
US20070015910A1
US20070015910A1 US10/496,071 US49607105A US2007015910A1 US 20070015910 A1 US20070015910 A1 US 20070015910A1 US 49607105 A US49607105 A US 49607105A US 2007015910 A1 US2007015910 A1 US 2007015910A1
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protein
oil seed
solution
seed meal
aqueous
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Larry Barker
Brent Green
Lei Xu
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Priority to US12/230,303 priority patent/US7625588B2/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K14/00—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
    • C07K14/415—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from plants
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/14—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from leguminous or other vegetable seeds; from press-cake or oil-bearing seeds

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  • the defatted protein solution then is concentrated to increase the protein concentration while maintaining the ionic strength substantially constant, after which the concentrated protein solution may be subjected to a further fat removal step.
  • the concentrated protein solution then is diluted to cause the formation of a cloud-like mass of highly aggregated protein molecules as discrete protein droplets in micellar form.
  • the protein micelles are allowed to settle to form an aggregated, coalesced, dense amorphous, sticky gluten-like protein isolate mass, termed “protein micellar mass” or PMM, which is separated from residual aqueous phase and dried.
  • the protein isolate has a protein content, on a dry weight basis, (as determined by Kjeldahl N ⁇ 6.25) of at least about 90 wt %, is substantially undenatured (as determined by differential scanning calorimetry) and has a low residual fat content.
  • protein content refers to the quantity of protein in the protein isolate expressed on a dry weight basis.
  • the yield of protein isolate obtained using this procedure, in terms of the proportion of protein extracted from the oil seed meal which is recovered as dried protein isolate was generally less than 40 wt %, typically around 20 wt %.
  • U.S. Pat. No. 4,208,323 itself was designed to be an improvement on the process described in U.S. Pat. Nos. 4,169,090 and 4,285,862 (Murray IA) by the introduction of the concentration step prior to dilution to form the PMM. The latter step served to improve the yield of protein isolate from around 20 wt % for the Murray IA process.
  • the supernatant from the PMM settling step is processed to remove a protein isolate comprising dried protein from wet PMM and supernatant.
  • This procedure may be effected by initially concentrating the supernatant using ultrafiltration membranes, mixing the concentrated supernatant with the wet PMM and drying the mixture.
  • the resulting canola protein isolate has a high purity of at least about 90 wt %, preferably at least about 100 wt %, protein (N ⁇ 6.25).
  • the supernatant from the PMM settling step is processed to recover a protein from the supernatant.
  • This procedure may be effected by initially concentrating the supernatant using ultrafiltration membranes and drying the concentrate.
  • the resulting canola protein isolate has a high purity of at least about 90 wt %, preferably at least about 100 wt %, protein (N ⁇ 6.25).
  • the initial protein extraction step can be significantly reduced in time for the same or higher level of protein extraction and significantly higher temperatures can be employed in the extraction step, if the extraction step is carried out in a continuous manner, rather than the batch procedure described in the above-mentioned patents and patent applications.
  • the continuous operation disclosed herein may be employed using the concentration and dilution conditions described in the Murray I and II patents but preferably, for the benefits described therein, the continuous operation described herein is preferably effected under the concentration and dilution conditions described in the aforementioned U.S. patent applications Nos. 60/288,415, 60/326,987, 60/331,066, 60/333,494,60/374,801 and 10/137,391.
  • a process of preparing a protein isolate which comprises (a) continuously extracting an oil seed meal at a temperature of at least about 5° C. to cause solubilization of protein in the oil seed meal and to form an aqueous protein solution having a pH of about 5 to about 6.8, (b) continuously separating the aqueous protein solution from residual oil seed meal, (c) continuously conveying the aqueous protein solution through a selective membrane operation to increase the protein concentration of the aqueous protein solution to at least about 50 g/L while maintaining the ionic strength substantially constant to provide a concentrated protein solution, (d) continuously mixing the concentrated protein solution with chilled water having a temperature of below about 15° C.
  • the protein isolate product in the form of protein micellar mass is described herein as “gluten-like”. This description is intended to indicate the appearance and feel of the isolate are similar to those of vital wheat gluten and is not intended to indicate chemical identity to gluten.
  • supernatant from the settling step is concentrated, batch-wise, semi-continuously or continuously, and the resulting concentrated supernatant is dried to provide a protein isolate having a protein content of at least about 90 wt % (N ⁇ 6.25) on a dry weight basis.
  • supernatant from the settling step is concentrated, batch-wise, semi-continuously or continuously, the resulting concentrated supernatant is mixed with the protein micellar mass prior to drying the same, and the resulting mixture is dried to provide a protein isolate having a protein content of at least about 90 wt % (N ⁇ 6.25) on a dry weight basis.
  • supernatant from the resulting step is concentrated, batch-wise, semi-continuously continuously, and a portion only of the resulting concentrated supernatant is mixed with at least a portion of the protein micellar mass prior to drying the same to provide other novel protein isolates according to the invention having a protein content of at least about 90 wt % (N ⁇ 6.25) on a dry weight basis.
  • FIG. 1 is a schematic flow sheet of a continuous procedure for producing an oil seed protein isolate in accordance with one embodiment of the invention.
  • the initial step of the process of this invention involves solubilizing proteinaceous material from oil seed meal, particularly canola meal, although the process may be applied to other oil seed meals, such as soybean, traditional rapeseed, traditional flax, linola, sunflower and mustard oil seed meals.
  • the invention is more particularly described herein with respect to canola seed meal, which may be low temperature desolventized meal.
  • the proteinaceous material recovered from canola seed meal may be the protein naturally occurring in canola seed or other oil seed or the proteinaceous material may be a protein modified by genetic manipulation but possessing characteristic hydrophobic and polar properties of the natural protein.
  • the canola meal may be any canola meal resulting from the removal of canola oil from canola seed with varying levels of non-denatured protein, resulting, for example, from hot hexane extraction or cold oil extrusion methods.
  • Canola oil seed is also known as rapeseed or oil seed rape.
  • the salt solubilization step is effected rapidly, in a time of generally up to about 10 minutes, preferably to effect the solubilization to extract substantially as much protein from the source material as is practicable, so as to provide an overall high product yield.
  • the solubilization preferably is effected at elevated temperatures, preferably above about 35° C., generally up to about 65° C.
  • the aqueous salt solution and the oil seed meal have a natural pH of about 5 to about 6.8 to enable the protein isolate to be formed by the micellar route, as described in more detail below.
  • the optimum pH value for maximum yield of protein isolate varies depending on the protein source material chosen.
  • pH values of about 5.3 to about 6.2 are preferred.
  • concentration of protein source material in the salt solution during the solubilization step may vary widely. Typical concentration values are about 5 to about 15% w/v.
  • the protein solution resulting from the extraction step generally has a protein concentration of about 5 to about 40 g/L, preferably about 10 to about 30 g/L.
  • the extraction procedure may be effected in a stirred tank into which the mixture of oil seed meal and salt solution is continuously fed and from which the aqueous protein solution is continuously removed.
  • the procedure may be effected in a semi-continuous manner equivalent to continuous wherein a mixture of oil seed meal salt solution is, fed into a first stred vessel in which the extraction is effected to form the aqueous protein solution while aqueous protein solution is continuously fed from a second stirred vessel to the residual meal separation step described below.
  • the first vessel then becomes the first vessel and vice versa.
  • the aqueous phase resulting from the extraction step then may be separated from the residual canola meal in any convenient manner, such as by employing vacuum filtration, followed by centrifugation and/or filtration to remove residual meal.
  • the separated residual meal may be dried for disposal.
  • the defatting steps described therein on the separated aqueous protein solution and on the concentrated aqueous protein solution may be effected.
  • the colour improvement step is carried out, such step may be effected after the first defatting step.
  • the aqueous phase resulting from the oil seed meal extraction step then is separated from the residual canola meal, in any convenient manner, such as by employing vacuum filtration, followed by centrifugation and/or filtration to remove residual meal.
  • the separated residual meal may be dried for disposal.
  • the aqueous protein solution resulting from the high or low pH extraction step then is pH adjusted to the range of about 5 to about 6.8, preferably about 5.3 to about 6.2, as discussed above, prior to filcher processing as discussed below.
  • pH adjustment may be effected using any convenient acid, such as hydrochloric acid, or alkali, such as sodium hydroxide, as appropriate.
  • the aqueous protein solution then is concentrated to increase the protein concentration thereof while maintaining the ionic strength thereof substantially constant.
  • concentration may be effected to provide a concentrated protein solution having a protein concentration of at least about 50 g/L.
  • concentration is effected preferably to provide a concentrated protein solution having a protein concentration of at least about 200 g/L, more preferably at least about 250 g/L.
  • the concentration step may be effected in any convenient manner consistent with a continuous operation, such as by employing any convenient selective membrane technique, such as ultrafiltration, using membranes, such as hollow-fibre membranes or spiral-wound membranes, with a suitable molecular weight cut-off such as from about 3000 to about 50,000 daltons, having regard to differing membrane materials and configurations, and dimensioned to permit the desired degree of concentration of the aqueous protein solution as the aqueous protein solution passes through the membranes.
  • any convenient selective membrane technique such as ultrafiltration
  • membranes such as hollow-fibre membranes or spiral-wound membranes
  • a suitable molecular weight cut-off such as from about 3000 to about 50,000 daltons
  • the concentration step may be effected at any convenient temperature, generally about 20° to about 60° C., and for the period of time to effect the desired degree of concentration.
  • the temperature and other conditions used to some degree depend upon the membrane equipment used to effect the concentration and the desired protein concentration of the solution.
  • the low molecular weight species include not only the ionic species of the food grade salt but also low molecular weight materials extracted from the source material, such as, carbohydrates, pigments and anti-nutritional factors, as well as any low molecular weight forms of the protein.
  • the molecular weight cut-off of the membrane is usually chosen to ensure retention of a significant proportion of the protein in the solution, while permitting contaminants to pass through having regard to the different membrane materials and configurations.
  • the concentrated protein solution may be warmed to a temperature of about 20° to about 60° C., preferably about 25° to about 35° C., to decrease the viscosity of the concentrated protein solution to facilitate the subsequent dilution step and micelle formation.
  • the concentrated protein solution should not be heated beyond a temperature above which the temperature of the concentrated protein solution does not permit micelle formation on dilution into chilled water.
  • the concentrated protein solution may be subject to a further defatting operation, if required, as described in the aforementioned U.S. Pat. Nos. 5,844,006 and 6,005,076.
  • the concentrated protein solution resulting from the concentration step and optional defatting step then is diluted to effect micelle formation by mixing the concentrated protein solution with chilled water having the volume required to achieve degree of dilution desired.
  • the degrees of dilution may be varied. With higher dilution levels, in general, a greater proportion of the canola protein remains in the aqueous phase.
  • the concentrated protein solution is diluted by less than about 15 fold, more preferably about 10 fold or less.
  • the dilution operation may be carried out by continuously passing the concentrated protein solution to one inlet of a T-shaped pipe while the diluting water is fed to the other inlet of the T-shaped pipe, permitting mixing in the pipe.
  • the diluting water is fed into the T-shaped pipe at a rate sufficient to achieve the desired degree of dilution.
  • the diluting water has a temperature of less than about 15° C., generally about 30 to about 15° C., preferably less than about 10° C., since improved yields of protein isolate in the form of protein micelles are attained with these colder temperatures at the dilution factors used.
  • the mixing of the concentrated protein solution and the diluting water in the pipe initiates the formation of protein micelles and the mixture is continuously fed from the outlet from the T-shaped pipe into a setting vessel, from which, when fill, supernatant is permitted to overflow.
  • the settling vessel may be initially charged full with chilled water which gradually is displaced by the inflowing mixture from the exit to the pipe.
  • the mixture is fed into the body of liquid in the settling vessel in a manner which minimizes turbulence within the body of liquid to permit proper settling of the micelles.
  • the mixture usually is fed from the outlet to the T-shaped pipe below the surface of the body of liquid in the settling vessel.
  • the outlet may be configured and structured so that the liquid flows out of the pipe in a radial direction in the upper levels of the settling vessel.
  • the protein micelles are allowed to settle in the settling vessel to form an aggregated, coalesced, dense amorphous gluten-like protein micellar mass (PWM and the procedure is continued until a desired quantity of the PMM has accumulated in the bottom of the settling vessel, whereupon the accumulated PMM is removed from the settling vessel.
  • the protein micellar mass may be subjected to centrifugation to decrease the liquid content of the mass prior to removal of accumulated PMM from the settling vessel. Centrifugation may decrease the moisture content of the protein micellar mass from about 70 wt % to about 95 wt % to a value of generally about 50% by weight to about 80 wt % of the total micellar mass. Decreasing the moisture content of the protein micellar mass in this way also decreases the occluded salt content of the protein micellar mass, and hence the salt content of dried isolate.
  • the settling step may be effected under continuous centrifugation.
  • the recovered PMM may be used in wet form or may be dried, by any convenient technique, such as spray drying, freeze drying or vacuum drum drying, to a dry form.
  • the dry PMM has a high protein content of at least about 90 wt %, usually in excess of about 100 wt % protein (calculated as Kjeldahl N ⁇ 6.25), and is substantially undenatured (as determined by differential scanning calorimetry).
  • the dry PMM isolated from fatty oil seed meal also has a low residual fat content, when the procedure of the aforementioned U.S. Pat. Nos. 5,844,086 and 6,005,026 is employed, which may be below about 1 wt %.
  • the supernatant from the PMM formation step may be processed to recover further protein therefroin
  • Such procedure may include an initial concentration of the supernatant.
  • concentration is effected using any convenient selective membrane technique, such as ultrafiltration, using membranes with a suitable molecular weight cut-off permitting low molecular weight species, including salt and other non-proteinaceous low molecular weight material extracted from the protein source material, to pass through the membrane, while retaining canola protein in the solution.
  • Ultrafiltration membranes having a molecular weight cut-off of about 3000 to about 10,000, having regard to differing membrane materials and configuration, may be used.
  • the concentration preferably is effected continuously on the continuously overflowing supernatant, although a batch procedure on collected volumes of the overflowing supernatant may be employed, if desired.
  • the membranes are dimensioned to permit the desired degree of concentration of the supernatant as the supernatant passes through the membranes.
  • the supernatant generally is concentrated to a protein concentration of about 100 to about 400 g/L, preferably about 200 to about 300 g/L, prior to drying.
  • the concentrated supernatant may be dried in any convenient manner, such as by spray drying, freeze drying or vacuum drum drying, to a dry form, to provide a further canola protein isolate having a protein content of at least about 90 wt %, preferably at least about 100 wt %, (N ⁇ 6.25), and which is substantially undenatured (as determined by differential scanning calorimetry).
  • the concentrated supernatant may be mixed with the wet PMM and the resulting mixture dried, to provide a further canola protein isolate having protein content of at least about 90 wt %, preferably at least about 100 wt % (N ⁇ 6.25) and which is substantially undenatured (as determined by differential scanning calorimetry).
  • the remainder of the concentrated supernatant may be dried as may any of the remainder of the PMM. Further, dried PMM and dried supernatant also may be dry mixed in any desired relative proportions, as discussed above.
  • FIG. 1 there is illustrated schematically a flow sheet of one embodiment to the invention.
  • Canola oil seed meal and aqueous extraction medium are fed by lines 10 and 12 respectively to a blender 14 wherein the oil seed meal and aqueous extraction medium are mixed and the mixture is passed by line 16 to a mixing pipe 18 .
  • the mixing pipe 18 the oil seed meal is extracted and an aqueous protein solution is formed.
  • the slurry of aqueous protein solution and residual oilseed meal is passed by line 20 to a vacuum filter belt 22 for separation of the residual oil seed meal which is removed by line 24 .
  • the aqueous protein solution then is passed by line 26 to a clarification operation 28 wherein the aqueous protein solution is centrifuged and filtered to remove fines, which are recovered by line 30 .
  • the clarified aqueous protein solution is pumped by line 32 through ultrafiltration membranes 34 sized to provide the desired degree of concentration of the aqueous protein solution to produce a concentrated protein solution as the retentate in line 36 with the permeate being recovered by line 38 .
  • the concentrated protein solution is passed into the inlet of a mixing tee 40 , with cold water being fed thereto by line 42 in a volume sufficient to achieve the desired degree of dilution.
  • the resulting solution is fed by line 44 to a settling tank 46 to permit the protein micellar mass to settle. Protein micellar mass settled in the settling vessel 46 is removed by line 48 from time to time and passed through a spray dryer 50 to provide dry canola protein isolate 52 .
  • Supernatant from the settling tank is removed by line 54 and pumped through ultrafiltration membranes 52 to produce a concentrated protein solution as the retentate in line 58 with the permeate being removed by line 60 .
  • the concentrated protein solution is passed through a spray dryer 62 to provide further dry canola protein isolate 64 .
  • the concentrated protein solution in line 58 may be passed by line 66 to mix with the protein micellar mass before the mixture then is dried in spray dryer 50 .
  • This Example illustrates a continuous process for the production of canola protein isolate in accordance with one embodiment of the invention.
  • Example 2 8 litres of a concentrated retentate with a protein content of 296 g/L was prepared by a batch procedure as described in Example 2 (see BW-AH014-H29-O1A).
  • the concentrated retentate at a temperature of 30° C., was pumped into one inlet of a T-shaped connection pipe at a rate of 64 ml/minute to mix with 4° C. water pumped into the other inlet of the T-shaped connection pipe at a rate to provide a dilution ratio of 1:10.
  • the T-shaped connector served as a device to mix the two streams and to cause the formation of a white cloud of protein micelles.
  • the mixture then passed from the outlet from the T-shaped connection pipe into a 50 litre settling vessel filled with 4° C. water where the mixture exited the pipe through a outlet designed to minimize turbulene in the settling vessel. Supernatant was removed from the top of the settling vessel maintaining the vessel at a constant volume. The system ran for two hours.
  • the PMM removed from the bottom of the vessel following the settling period had a solids content of 29.8 wt % and represented 49 wt % of the protein in the retentate.
  • the protein extract solution was reduced in volume on an ultrafiltration system using membranes having a molecular weight cut-off of 3000 daltons.
  • the resulting concentrated protein solution had a protein content of “f” g/L.
  • the concentrated solution at “g”° C. was diluted 1:10 into 4° C. tap water. A white cloud formed immediately and was allowed to settle. The upper diluting water was removed and the precipitated, viscous, sticky mass was dried.
  • the product was given designation
  • This Example illustrates the application of the continuous extraction stage of the continuous process to mustard, non-GMO canola, high euricic acid rapeseed (H.E.A.R), white flake canola meal and cold pressed canola meal.
  • H.E.A.R high euricic acid rapeseed
  • Oil seed meals were added to separate 500 ml aliquots of 55° C., 0.15 M NaCl solution to provide mixtures having the following concentrations:
  • This Example illustrates the application of the continuous dilution stage of the continuous process to mustard, non-GMO canola, high euricic acid rapeseed, white flake canola meal and cold pressed canola meal.
  • Extraction of oil seed meals were performed in 0.15 M NaCl solution at room temperature with a 30-minute mixing period for each oil seed meal.
  • the seed concentrations were 10% w/v for white flake and cold pressed canola meals and. 15% w/v for H.E.A.R., non-GMO canola meal and mustard meal.
  • the solid material was separated from the extraction protein solution by centriftigation at 10,000 ⁇ g for 10 minutes.
  • the protein solutions were further clarified by filtering through Weaning #4 filter papers on a vacuum filter apparatus.
  • Each clarified was concentrated on a Amicon mini stirred-cell concentration system using membranes of MWCO sufficient to retain the soluble protein while allowing water and contaminating small molecular weight material to pass through the permeate.
  • Each protein solution was concentrated to 200 mg/ml or greater.
  • the retentates were diluted in a continuous manner by using two peristaltic pumps and a t-shaped connector.
  • the pump speeds were adjusted to allow the first pump to move fluid at a rate 10 times faster than the first pump, to provide a dilution ratio of retentate to water of 1:10.
  • the pumps were started simultaneously and the retentates and water were pumped into a common line through the t-shaped connector where they were mixed and micehe formation commenced.
  • the present invention provides a continuous process for the production of oil seed protein isolate. Modifications are possible within the scope of the invention.

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US12/230,303 US7625588B2 (en) 2001-11-20 2008-08-27 Continuous process for production of oil seed protein isolate

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US33164601P 2001-11-20 2001-11-20
US38380902P 2002-05-30 2002-05-30
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US12/230,199 Expired - Lifetime US7704534B2 (en) 2001-11-20 2008-08-26 Continuous process for production of oil seed protein isolate
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US12/230,303 Expired - Lifetime US7625588B2 (en) 2001-11-20 2008-08-27 Continuous process for production of oil seed protein isolate

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WO2010003245A1 (en) 2008-07-11 2010-01-14 Burcon Nutrascience (Mb) Corp. Soluble canola protein isolate production
US20100036099A1 (en) * 2008-07-11 2010-02-11 Martin Schweizer Soluble canola protein isolate production ("nutratein")
US20100068370A1 (en) * 2008-09-17 2010-03-18 Segall Kevin I Emulsified Foods
US8486675B2 (en) 2009-11-11 2013-07-16 Bioexx Specialty Proteins Ltd. Protein concentrates and isolates, and processes for the production thereof from macroalgae and/or microalgae
US8535907B2 (en) 2009-11-11 2013-09-17 Bioexx Specialty Proteins Ltd. Protein concentrates and isolates, and processes for the production thereof from toasted oilseed meal
US8623445B2 (en) 2008-05-16 2014-01-07 Bio-Extraction Inc. Protein concentrates and isolates, and processes for the production thereof
US8821955B2 (en) 2008-05-16 2014-09-02 Siebte Pmi Verwaltungs Gmbh Protein concentrates and isolates, and processes for the production thereof

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RU2316223C2 (ru) 2001-05-04 2008-02-10 Баркон Ньютрасайнс (Мб) Корп. Производство белкового изолята из семян масличных культур
CN1658763B (zh) 2002-04-15 2010-05-12 伯康营养科学(Mb)公司 卡诺拉蛋白分离物组合物
US7989017B2 (en) 2002-10-22 2011-08-02 Burcon Nutrascience (Mb) Corp. Canola protein isolate functionality II
RU2293365C2 (ru) * 2002-11-13 2007-02-10 Сириал Текнолоджиз Гмбх Устройство для восстановления видеоголограмм
AU2004248870B2 (en) * 2003-06-20 2010-08-19 Burcon Nutrascience (Mb) Corp. Oil seed meal preparation
US8470385B2 (en) 2004-01-20 2013-06-25 Burcon Nutrascience (Mb) Corp. Beverage having purified or isolate protein component
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