EP4429471A1 - Procédé d'obtention de protéines à partir de chanvre - Google Patents

Procédé d'obtention de protéines à partir de chanvre

Info

Publication number
EP4429471A1
EP4429471A1 EP22814021.6A EP22814021A EP4429471A1 EP 4429471 A1 EP4429471 A1 EP 4429471A1 EP 22814021 A EP22814021 A EP 22814021A EP 4429471 A1 EP4429471 A1 EP 4429471A1
Authority
EP
European Patent Office
Prior art keywords
protein
hemp
phase
extraction
water
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP22814021.6A
Other languages
German (de)
English (en)
Inventor
Detlef Ullmann
Dominik KRIENKE
Klaus Mannweiler
Steffen Hruschka
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GEA Westfalia Separator Group GmbH
Original Assignee
GEA Westfalia Separator Group GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by GEA Westfalia Separator Group GmbH filed Critical GEA Westfalia Separator Group GmbH
Publication of EP4429471A1 publication Critical patent/EP4429471A1/fr
Pending legal-status Critical Current

Links

Classifications

    • 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
    • A23J1/001—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from waste materials, e.g. kitchen waste
    • A23J1/005—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from waste materials, e.g. kitchen waste from vegetable waste materials
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P21/00—Preparation of peptides or proteins
    • 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
    • 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
    • A23J1/142—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 by extracting with organic solvents
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P2203/00—Fermentation products obtained from optionally pretreated or hydrolyzed cellulosic or lignocellulosic material as the carbon source

Definitions

  • the present invention relates to a method for obtaining proteins from hemp.
  • Sunflower proteins are usually obtained in dry processes through the selective separation of the hull fraction.
  • WO 2004/043157 A1 uses hemp seed as the starting material for the production of hemp milk and heating to 80° C., which leads to partial denaturation of the proteins and thus to increased loss.
  • WO 2005/094603 A1 treats protein-containing phytate-reduced Food using ultrafiltration.
  • the phytate content is reduced in the end product containing protein by ultrafiltration of the extracts containing sugar, protein and phytate.
  • Phytate and reduced-sugar protein remain in the retentate.
  • Ultrafiltration is associated with the loss of filtered backwash water. Furthermore, prolonged use can lead to so-called membrane fouling.
  • An ultrafiltration process is particularly suitable for low solids content. If there is a quantitative precipitation of proteins, the risk of the membrane clogging with filtrate is comparatively high. The result is blocking.
  • WO 2006/003110 A1 starts after the solvent extraction of a fat from plants. However, such an extraction damages the proteins.
  • WO 2019/213757 A1 uses microcapsules to enclose fat and protein.
  • Another variant converts hemp parts from the pressing process directly into an alkaline suspension, analogous to the soy protein isolate process.
  • the sensory aspects are irrelevant here and are therefore not considered, since the protein is used exclusively for the production of oil-based microcapsules. Since the oil - regardless of whether it is the residual oil in the protein or the capsule oil - is sensorially important as a flavor carrier for the end product, the sensory component of the protein product is ignored.
  • Aqueous sensory enhancement processes typically require large amounts of water. In this case, the extracted proteins are usually washed several times.
  • the task is to develop an effective, economical process for a usable protein fraction with functional properties.
  • the method according to the invention is intended to produce a non-denatured and sensorially acceptable protein concentrate with low proportions of oil-related substances such as polyphenols.
  • a method according to the invention relates to the extraction, in particular the purest possible isolation of proteins from hemp.
  • the procedure has the following steps:
  • hemp press residues in particular a hemp press cake, in particular from the extraction of hemp oil
  • hemp protein product has a high potential for gel formation and therefore this property stands out Focus next to the sensors and the water retention.
  • the aforementioned alcohol is preferably a dilute or aqueous alcohol.
  • the first measure is a pre-wash with a comparatively small amount of water.
  • a water phase is separated with a greenish organic juice that tastes very unpleasantly aromatic and very intensely bitter. Since the extract is watery and the CBD (cannabidiol) contained in the raw material is not water-soluble, only a marginal amount of CBD is transferred to the extract.
  • oil which is generally regarded as a flavor carrier, is also separated off together with carbohydrates.
  • This process step is preferably carried out cold, ie preferably essentially at ambient temperature.
  • the final product is significantly more intense in taste and bitterness.
  • the loss of proteins is limited to less than 30% by weight of the dry matter of the extract. Typically, less than 5% protein is lost with this washing phase, based on the amount of protein contained in the raw material.
  • the second measure is to carry out the precipitation in an aqueous ethanolic environment.
  • several extracts if available, are brought together.
  • EtOH based on the total amount of fluid, are sufficient to produce a compact protein phase that is significantly better in sensory terms than that of an ethanol-free one Precipitation.
  • step B the dwell time is at least 1 hour from the beginning of the formation of the suspension.
  • the solids in the water swell and thus an intensive extraction is achieved.
  • the water is not absorbed during the swelling to the same extent as is the case with the protein production of other plants. If a slow or even continuous addition of water takes place, then the dwelling begins parallel to the addition of water from the point at which a suspension forms.
  • a suspension is in particular a paste which has a liquid phase and solids which are undissolved therein.
  • the hemp press residues provided in step A advantageously have a normal distribution over an average diameter of the particles of 1.2-2.5 mm, preferably 1.5-2 mm, the hemp press residues already being different in comparison to harvested hemp are partially de-oiled. Both the particle distribution and the previous partial deoiling help in the efficient pre-washing and in particular the reduction of phenolic compounds in the hemp intermediate product on the way to protein extraction.
  • step B preferably at least the same up to five times the mass of water, preferably at least twice to four times the mass, in particular 2.5 to 3.5 times the mass of water, is added to the mass of hemp press residues provided .
  • Oil can be removed from the solids in the liquid state or dispersed in water, eg as an oil-water emulsion. Simultaneously removes most of the phenolic compounds from the solids along with the oil and/or emulsion.
  • the suspension formation in step B preferably takes place at 15-50°C, preferably 20-35°C.
  • the proteins are not thermally stressed and the solubility of proteins in wash water is kept low at the same time.
  • the extraction in step C can in particular take place at less than 55°C, in particular 40-50°C.
  • At least one of the aforementioned phase separations take place in a decanter, preferably in a separating decanter.
  • a decanter with a full jacket and preferably a horizontal axis of rotation is used here in particular.
  • the concentration of the alcohol fed in step D can be between 30-70% by volume, preferably 45-55% by volume.
  • the amount of water and the amount of alcohol supplied is adjusted in particular in such a way that the concentration of alcohol in the suspension is less than 8% by weight, preferably 3-7% by weight, in particular 5+/-0.5% by weight.
  • the alcohol supplied in step D can be ethanol and/or isopropanol (isopropyl alcohol), which is intended for use as food. It goes without saying that ethanol or also isopropanol should ideally be largely removed from the protein before the end product is made available.
  • the alkalization in step C is carried out with sodium hydroxide solution, in particular with a concentration of 10-50%, in particular 12-40% by weight.
  • the acid is added in step D with the addition of hydrochloric acid, phosphoric acid and/or citric acid, the acid being present in at least half the concentration.
  • a concentrated hydrochloric acid for example, is about 37%, with 370 g HCl to one kilogram of water.
  • the residence time after the acid addition can advantageously be at least 10 minutes, preferably at least 15 minutes. This enables precipitation to be as quantitative as possible.
  • step C takes place at less than 55°C, in particular 40-50°C.
  • the extraction should advantageously be carried out warm in order to achieve a high protein yield.
  • the protein should not denature.
  • the protein-rich phase obtained in step E can be washed by adding water and then separating the phases.
  • the washing water from this step can be used again in steps B and C.
  • the temperature of 55° C., preferably 50° C. is not exceeded during the entire process for obtaining proteins from hemp.
  • the hemp press residues are provided by mechanically squeezing out oil, without the addition of an organic solvent. This also prevents denaturing.
  • FIG. 2 detailed method sequence of a second method step of the method of FIG. 1;
  • FIG. 3 detailed method sequence of a third method step of the method of FIG. 1 ;
  • FIG. 4 detailed method sequence of a fourth method step of the method of FIG. 1 ;
  • FIG. 5 detailed method sequence of a fifth method step of the method of FIG. 1 ;
  • FIG. 6 detailed method sequence of a final method step of the method of FIG. 1 ;
  • Fig. 9 Representation of an intermediate stage of protein extraction with and without previous pre-washing.
  • a hemp press cake 1 shows the course of an embodiment variant of the method according to the invention.
  • a hemp press cake 1 is provided.
  • the hemp press cake can result from oil extraction. It still contains a considerable amount of residual oil.
  • a pre-wash is carried out, which is shown in detail in FIG.
  • a suspension 102-1 of comminuted hemp press cake 1 with water 2 takes place as part of the prewash 102.
  • This suspension 102-1 is also referred to below as mashing.
  • the hemp press cake 1 preferably has a normal distribution over an average particle diameter of approx. 1.5-2 mm.
  • Soluble oils and/or oil-related substances are dissolved in the water or specifically lighter oil is partially emulsified in the water.
  • this type of prewash is surprisingly possible with the hemp press cake, since the solids in the hemp press cake swell to a significantly reduced extent compared to other plants.
  • oil is a flavor carrier, the taste of hemp and the products derived from it, such as proteins, is usually very intensely bitter.
  • oil and the oil-accompanying substances it is possible and at the same time advantageous for the oil and the oil-accompanying substances to be at least partially separated off before the protein extraction.
  • the amount of water based on the weight of the hemp press cake, is used for the suspension 102-1. It has been shown that individual ingredients in a thick mash dissolve better than a thin suspension due to better shearing of the solid particles.
  • the suspension 102 - 1 is followed by a dwell 102 - 2 as part of the prewash. This is preferably done with stirring. It will Constituents of the press cake can be further dissolved or suspended in water.
  • the residence 102-2 of the mash (presscake-water mixture) under stirring should preferably not be less than one hour.
  • a step of phase separation 102-3 then takes place, preferably by centrifugation.
  • the protein content in the washing water is approx. 1% at 25°C, which corresponds to 1/3 of the dry matter content in the washing water.
  • a fifth to a quarter of the dry matter in the wash water is oil. The rest is sugar, measured at around 2°Brix.
  • the second fraction of the phase separation 102-3 is a pre-washed protein-rich phase 4, in particular in the form of a moist hemp press cake solid fraction.
  • This moist, washed solid with approx. 50% dry matter and 36% protein /TS and ⁇ 2% oil on the dry matter is used for protein extraction in the next step.
  • a portion of the washing water from the last stage can also be used as a portion of the water.
  • a first extraction 103 of the prewashed solid 4 then takes place. This is shown in more detail in FIG. This first extraction is added to the pre-washed solid 4 water 5 . The solid is thus suspended again 103 - 1 .
  • alkalization 103-2 by adding dilute sodium hydroxide solution 6.
  • concentration concentration 10-50% by weight based on the amount of sodium hydroxide solution
  • pH value 9 to 11, preferably 10.
  • enough fluid i.e. water and lye, is to be added so that the dry matter content in the suspension is approx. 20-26% m/m, preferably 23% m/m.
  • This is followed by another dwell 103-3, preferably at 10-55° C., particularly preferably for at least 10 minutes, in particular at least 30 minutes.
  • the dwell can take place with stirring. Alternatively, a dwell time is only necessary until the working temperature for the subsequent separation step is reached.
  • the stirrer speed is optimal for up to 3 m/s at the periphery.
  • Subsequent phase separation 103-4 can preferably be carried out centrifugally and particularly preferably by a decanter. This separates the suspension into about 2/3 light phase 7 and 1/3 heavy phase, the shell fraction 8.
  • the operating temperature during phase separation is preferably less than 60°C, preferably 40-55°C, in particular 50°C.
  • the light phase 7 comprises a high protein aqueous extract.
  • the shell fraction 8 is fed to a second extraction.
  • the protein extract 7 is fed to a precipitation together with the protein extract of the second stage or any further extracts produced from further extraction stages. This will be explained in more detail later
  • a subset of the wash water from the last stage of the process which is described below as protein wash water 12, can also be used as a subset of the water 5.
  • the solid 8 from the first extraction is used for the second extraction 104, as illustrated in FIG.
  • the protein wash water 12 can also be used to some extent for this purpose.
  • alkalising 104-2 takes place with the addition of sodium hydroxide solution 10.
  • the dry matter value before separation can advantageously be around 22% +/- 3% m/m.
  • the working temperature can preferably be in the range of maximum 55°C, preferably 40-50°C.
  • the alkalizing 104-2 is optionally followed by a dwell 104-3 with stirring.
  • the optional residence time is preferably less than 20 minutes, preferably 0-15 minutes.
  • a subsequent phase separation 104-4 preferably takes place centrifugally and in particular with a decanter.
  • a shell fraction 11 and an aqueous protein fraction 13 are formed.
  • the shell fraction 11 it is also possible to continue using the shell fraction 11 directly or to dispose of it.
  • a residual protein content of 10-15% remains in the shell fraction 8 and can be reduced by further extraction stages.
  • the main component of the peel powder 20 is the roughage.
  • the extract 13 of the second extraction 104 there are about 5% dry matter, about 2/3 of which are proteins.
  • the percentage of protein is thus higher than that in extract 7 from the first extraction 103.
  • the oil content of ⁇ 1% based on the dry matter is lower than that in the first extract 7 of 1-2% m/m.
  • Both protein-rich aqueous fractions 13 together contain about 60-70% of the protein contained in the raw material, about 80% of which originate from the first extraction and 20% from the second extraction.
  • the said step of precipitation 105 follows the second extraction 104 . This is explained in more detail in FIG.
  • the extracts from the previous extraction stages are mixed with one another by blending 105-1.
  • 105-3 in particular by adjusting the isoelectric point, which has a pH value of 5.0 +/- 0.8.
  • acid 18, in particular hydrochloric acid is used in a concentration with a mass fraction of 35%.
  • the dwell time is not necessary in any process step in the precipitation stage 105, but a dwell time of at least 10 minutes after addition of the acid is advantageous for the flocculation of the protein.
  • the process steps should also be agitated at a maximum of 3 m/s on the periphery of the agitator.
  • the addition of acid 105-3 results in two phases, a clear phase 14 and a heavy phase (protein curd) 15, which are separated from one another by phase separation, in particular centrifugal phase separation 105-4, particularly preferably by a decanter, in particular a separating decanter.
  • the clear phase 14 usually has a dry matter content of about 2%, and this again contains oil with about 10% based on the dry matter in this clear phase. This means that the protein quark with approx. 20% +/- 4% dry matter is significantly lower in oil, namely with only 0.6% +/- 0.4%.
  • the fraction of the total protein that separates as albumin with the light phase is significantly small compared to the fraction of protein that separates as globulin with the protein curd. Typical here are quantitative ratios of 5 to 8% by weight of albumin protein based on the amount of protein in the globulin.
  • the final step in the process is the washing 106 of the protein 15. This is shown in FIG. Here, water 16 is added to the protein quark 15 from the precipitation stage 105 in the preferred proportion of 70-130% by weight, by mixing
  • 106-1 formed a suspension, by staying 106-2 a favorable one Washing out of soluble components achieved and then separated again in the separating step 106-3.
  • the mixture thus has a TS value of approx. 10% m/m.
  • About 50% by volume is obtained as washed quark with about 20% dry matter m/m as a solid suspension (quark).
  • the residence time is relatively short at at least 5 minutes, preferably 6-15 minutes.
  • the temperature is around 40-55°C, preferably 50°C.
  • the separated washing water 12 contains less than 2% DS and can be fed to the first and/or second extraction step 103, 104 as protein washing water.
  • the separation is carried out centrifugally with a separating decanter into a quark-like solids dispersion 17 and an almost aqueous overflow as protein washing water.
  • the washing water can be used as dilution water for the first and/or second extraction, if necessary after purification.
  • washing water for the prewash 102 can also be used as washing water for the prewash 102.
  • the latter even has the advantage that the wash water from the pre-wash is lost water and therefore there is little or no interim enrichment of washed-out aroma substances and oil components in the extract.
  • the absolute protein losses in the washing water 12 are less than 1% by weight. With less than 2% by weight of the protein in the raw material, its proportion represents a small amount. In contrast, the protein content in the washed protein quark remained almost unchanged at over 70%, even over 73%, compared to the value before washing.
  • the protein-rich protein quark 17 is dried 107 , in particular below 55° C. and preferably optionally under reduced pressure, to form a protein powder 21 .
  • Figure 8 shows a plot of dry matter yield versus ethanol concentration after precipitation in step D at neutral to acidic pH.
  • the marked measurement points 151 show the proportion of dry matter yield in the alcoholic-aqueous phase after the addition of ethanol at a neutral pH and the upper measurement points 150 show the proportion of dry matter in the separated protein phase after addition of acid.
  • Fig. 9 schematically shows the phases of centrifuge tubes after centrifugal treatment at the respective stages of the process.
  • a first depiction shows the course of the process with a pre-wash and a second depiction shows the course of the process without a pre-wash.
  • an emulsion phase 201 comprising oil, proteins and, if appropriate, proportions of water is obtained.
  • aqueous extraction phase 202 comprising proteins, sugars and undesirable phenols as oil-accompanying substances is also obtained.
  • a solid phase 203 consisting of shells, protein, phenols and other compounds is obtained.
  • a liquid extract phase 204 comprising dissolved substances such as phenols and a solid phase 205 comprising proteins.
  • a solid phase 207 was formed, which includes shells, proteins, phenols and the like.
  • a liquid phase 202 comprising proteins, sugars and phenols is formed therefrom after the extraction.
  • the solid phase 203 itself contained only shells and proteins. Finally, a precipitation takes place providing a protein phase 205 and a liquid phase 204.
  • a special feature of protein extraction from hemp is the formation of a gel in the protein-rich phase. Compared to water and the other fractions, this gel has a higher viscoelasticity. The gel is thus a fluid with a higher viscoelasticity—compared to water and the other fractions that occur in the process. This is also surprising insofar as this rheological peculiarity did not occur in other plants, eg oilseed rape, or at least not to this extent.

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Biochemistry (AREA)
  • Polymers & Plastics (AREA)
  • Food Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Wood Science & Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Zoology (AREA)
  • Biotechnology (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Molecular Biology (AREA)
  • Peptides Or Proteins (AREA)
  • Extraction Or Liquid Replacement (AREA)

Abstract

L'invention concerne un procédé d'obtention de protéines à partir de chanvre, comprenant les étapes suivantes : A fournir des résidus de pressage de chanvre (101), en particulier un tourteau de chanvre (1), en particulier provenant de l'obtention d'huile de chanvre ; B) prélaver (102) les résidus de pressage de chanvre avec addition d'eau (5), avec suspension (102-1) des résidus de pressage de chanvre pour former une suspension aqueuse ayant un pH < 7, séparer les phases (102-3) pour former une phase aqueuse de contaminant pauvre en protéines (3) comprenant de l'huile et/ou des substances associées à l'huile et une phase prélavée à haute teneur en protéines (4) ; C extraire (103) les protéines par alcalinisation (103-2) de la phase prélavée à haute teneur en protéines (4), avec nouvelle suspension (103-1) pour former une suspension aqueuse, et séparer les phases (103-3) pour former une fraction de coque (8) et une fraction protéique aqueuse (7) ; D précipiter (105) les protéines avec addition d'un alcool à chaîne courte (19) (105-2) ayant moins de quatre atomes de carbone et avec addition (105-3) d'un acide (18) pour déplacer le pH dans la plage acide ; et E) séparer les phases (105-4), en particulier par séparation de phase par centrifugation, en une phase pauvre en protéines (13) et une phase riche en protéines (14).
EP22814021.6A 2021-11-08 2022-11-08 Procédé d'obtention de protéines à partir de chanvre Pending EP4429471A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102021128968.8A DE102021128968A1 (de) 2021-11-08 2021-11-08 Verfahren zur Gewinnung von Proteinen aus Hanf
PCT/EP2022/081050 WO2023079159A1 (fr) 2021-11-08 2022-11-08 Procédé d'obtention de protéines à partir de chanvre

Publications (1)

Publication Number Publication Date
EP4429471A1 true EP4429471A1 (fr) 2024-09-18

Family

ID=84366237

Family Applications (1)

Application Number Title Priority Date Filing Date
EP22814021.6A Pending EP4429471A1 (fr) 2021-11-08 2022-11-08 Procédé d'obtention de protéines à partir de chanvre

Country Status (6)

Country Link
US (1) US20250019734A1 (fr)
EP (1) EP4429471A1 (fr)
CA (1) CA3236761A1 (fr)
DE (1) DE102021128968A1 (fr)
IL (1) IL312604A (fr)
WO (1) WO2023079159A1 (fr)

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT414206B (de) 2002-11-14 2006-10-15 Atb & G Frenkenberger Consulti Verfahren zur herstellung von hanfmilch
WO2005094603A1 (fr) 2004-03-29 2005-10-13 Cargill, Incorporated Aliment a teneur reduite en phytate
ITMI20041308A1 (it) 2004-06-29 2004-09-29 Fraunhofer Ges Zur Foerderung... Processo per la purificazione da seme di lupiom di frazioni proteiche attive sul metabolismo lipidico
DE102011050905A1 (de) * 2011-06-07 2012-12-13 Gea Mechanical Equipment Gmbh Verfahren zur Gewinnung von Proteinen aus einem nativen Stoffgemenge
WO2019213757A1 (fr) 2018-05-07 2019-11-14 POS Management Corp. Protéine de chanvre et son utilisation pour la microencapsulation

Also Published As

Publication number Publication date
US20250019734A1 (en) 2025-01-16
WO2023079159A1 (fr) 2023-05-11
IL312604A (en) 2024-07-01
CA3236761A1 (fr) 2023-05-11
DE102021128968A1 (de) 2023-05-11

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