DK159975B - PROCEDURE FOR SOLID PHASE LIQUID EXTRACTION OF FLIPPED AND POLYPHENOLS FROM FLAGED, PURPOSED SUNFLOWER SEED AND MEDICINE FOR EXERCISING THE PROCEDURE - Google Patents
PROCEDURE FOR SOLID PHASE LIQUID EXTRACTION OF FLIPPED AND POLYPHENOLS FROM FLAGED, PURPOSED SUNFLOWER SEED AND MEDICINE FOR EXERCISING THE PROCEDURE Download PDFInfo
- Publication number
- DK159975B DK159975B DK510082A DK510082A DK159975B DK 159975 B DK159975 B DK 159975B DK 510082 A DK510082 A DK 510082A DK 510082 A DK510082 A DK 510082A DK 159975 B DK159975 B DK 159975B
- Authority
- DK
- Denmark
- Prior art keywords
- procedure
- solvent
- extraction
- polyphenols
- liquid extraction
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/10—Production of fats or fatty oils from raw materials by extracting
-
- 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
- A23J1/12—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from cereals, wheat, bran, or molasses
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Biochemistry (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Fats And Perfumes (AREA)
- Extraction Or Liquid Replacement (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Peptides Or Proteins (AREA)
- Medicines Containing Plant Substances (AREA)
Description
DK 159975BDK 159975B
Opfindelsen angår en fremgangsmåde til fastfase-væskeekstraktion af lipider og polyphenoler fra flagede, afskallede solsikkefrø, til opnåelse af proteinholdige koncentrater samt et middel til udøvelse af fremgangsmå-5 den.The invention relates to a process for solid-phase liquid extraction of lipids and polyphenols from peeled, peeled sunflower seeds, to obtain protein-containing concentrates and a means for carrying out the process.
Tysk offentliggørelsesskrift nr. 23 55 892 beskriver en fremgangsmåde til ekstraktion af planteprotein fra især sojaflager, hvorved man i to trin først fjerner olie og lechitin med et organisk upolært opløs-ningsmiddel, såsom hexan, og derefter ekstraherer planteproteinet med en tofaseblanding af et organisk upolært og et organisk polært opløsningsmiddel samt vand.German Patent Publication No. 23 55 892 discloses a process for extracting plant protein from soy flakes in particular, first removing oil and lechitin with an organic unpolar solvent such as hexane and then extracting the plant protein with a two-phase mixture of an organic unpolar and an organic polar solvent as well as water.
US patentskrift nr. 4 265 925 beskriver, at man først ekstraherer affedtede vegetabilske proteinflager ^ med en alkohol og derefter fjerner denne alkohol under anvendelse af et flygtigt væskeformigt carbonhydrid, såsom hexan.U.S. Patent No. 4,265,925 discloses first extracting defatted vegetable protein flakes with an alcohol and then removing this alcohol using a volatile liquid hydrocarbon such as hexane.
En faststof-væskeekstraktion kan udføres ved en vilkårlig af de procedurer, der er angivet i den ^ tekniske litteratur. Anvendelsen af den procedure, der er beskrevet i dansk patentansøgning nr. 1980/79, indleveret den 14. maj 1979, har vist sig at være særligt fordelagtig. Den deri beskrevne faststof-væskeekstraktionsproces består i, at frisk opløsningsmiddel eller solvent-blanding tilføres et blandt et antal i serie anbragte ekstraktionskar, hvilke kar hver indeholder det faste materiale og er forsynet med en opløsningsmiddelindgang, en opløsningsmiddeludgang, et kørende røreorgan og et filterelement til at forhindre, at fast materiale med en 30 størrelse, der er større end en given størrelse, undslipper gennem opløsningsmiddeludgangen, idet filterelementet strækker sig ind i karret i nærhed af røreorganet således, at bevægelsen af opløsningsmiddel eller solvent-A solid-liquid extraction can be carried out by any of the procedures set forth in the technical literature. The use of the procedure described in Danish Patent Application No. 1980/79, filed on May 14, 1979, has proved particularly advantageous. The solid-liquid extraction process described therein consists in supplying fresh solvent or solvent mixture to a series of extraction vessels arranged in series, each containing the solid material and being provided with a solvent inlet, a solvent outlet, a moving stirrer and a filter element for preventing solids of a size larger than a given size from escaping through the solvent outlet, the filter element extending into the vessel in the vicinity of the stirrer so that the movement of solvent or solvent
DK 159975 BDK 159975 B
2 blandingen med røreorganet reducerer det faste materiales tendens til at tilstoppe filterelementet, at opløsningsmiddel med medførte ekstraherede stoffer fra det ene ekstraktionskar føres gennem de efterfølgende ekstrak-5 tionskar i serie, og derefter, efter ekstraktion af de ekstraherbare stoffer fra det faste materiale i det nævnte ene ekstraktionskar, at tilføringen af frisk opløsningsmiddel eller solventblanding skiftes til det i strømmens retning næste ekstraktionskaij fast materiale fjernes 10 fra det nævnte ene ekstraktionskar, og dette ekstraktionskar genfyldes med frisk materiale, idet dette ekstraktionskar tilsluttes i serie i strømmens retning efter det tidligere sidste ekstraktionskar.2 the mixture with the stirrer reduces the tendency of the solid material to clog the filter element, that solvent with entrained extracted substances from one extraction vessel is passed through the subsequent extraction vessels in series, and then, after extraction of the extractable substances from the solid material in the said one extraction vessel, the addition of fresh solvent or solvent mixture being changed to the next extraction solid material 10 is removed from said one extraction vessel, and this extraction vessel is refilled with fresh material, this extraction vessel being connected in series in the flow direction after the previous one. extraction vessel.
Denne fremgangsmåde gør det muligt at ekstrahere 15 nogle få komponenter med et opløsningsmiddel eller en blanding af to eller flere opløsningsmidler gennem et antal n, serielt anbragte beholdere, idet beholderne under hele ekstraktionsforløbet holdes med deres indhold konstant omrørt.This method allows 15 few components to be extracted with a solvent or a mixture of two or more solvents through a plurality of n, serially disposed containers, the containers being constantly stirred with their contents throughout the extraction process.
20 Opløsningsmidlet (eller opløsningsmidlerne) føres til (og fjernes fra) de adskillige kar med en værdi for strømningshastigheden (unitær), der vælges inden for et veldefineret område, i almindelighed fra 2m3 pr. time pr. m2 til 15 m3 pr. time pr. m2, idet strømningen gennem 25 de serieåt anbragte kar er kontinuerlig.The solvent (or solvents) is fed to (and removed from) the several vessels having a value for the flow rate (unitary) selected within a well-defined range, generally from 2m3 per meter. per hour m2 to 15 m3 per square meter. per hour m2, with the flow through the serially arranged vessels being continuous.
I praksis ifyldes hvert kar, efter at være tilført det passende findelte faste materiale, med opløsningsmiddel og omrøring påbegyndes.In practice, each vessel, after being supplied with the appropriate finely divided solid material, is started with solvent and stirring.
Frisk opløsningsmiddel tilføres derefter den før-30 ste beholder således, at det opløsningsmiddel, der allerede er i det, fortyndes og ekstraktionen bliver meget effektiv.Fresh solvent is then added to the first container so that the solvent already in it is diluted and the extraction becomes very efficient.
Det opløsningsmiddel, der udtages fra det første kar, føres til det næste ekstraktionskar, og den samme 35 operation gentages, og denne operation gentages efterfølgende serielt for alle de n ekstraktionskar.The solvent withdrawn from the first vessel is passed to the next extraction vessel, and the same operation is repeated, and this operation is then repeated serially for all the extraction vessels.
Når det faste materiale, der findes i det første ekstraktionskar, er blevet udtømt (i den betydning, at det ekstraherbare stof er blevet ekstraheret) tømmes det*When the solid material contained in the first extraction vessel has been depleted (in the sense that the extractable substance has been extracted) it is emptied *
DK 159975BDK 159975B
3 og frisk opløsningsmiddel tilføres ved at tilslutte karret som det sidste i rækken. Tilføring af frisk opløsningsmiddel skiftes fra det første ekstraktionskar til det næste o.s.v.3 and fresh solvent is added by connecting the vessel as the last in the row. Fresh solvent supply is changed from the first extraction vessel to the next, etc.
5 Eftersom ca. 10% af det faste materiale (de fine ste dele) for hvert kar går over i opløsningsmiddelstrømmen, er det ud over de serieforbundne ekstraktionskar nødvendigt med et filter, der adskiller det af opløsningsmiddelstrømmen medførte faste stof fra væskefasen, 10 og ekstraktionen færdiggøres.5 Since approx. 10% of the solid material (the finest parts) for each vessel goes into the solvent stream, in addition to the series-connected extraction vessels, a filter separating the solids produced by the solvent stream from the liquid phase is required, 10 and the extraction is completed.
Fremgangsmådens gennemførlighed og effektiviteten er nært forbundet med et antal variable, og disse skal være tilpasset hinanden.The feasibility and efficiency of the process are closely linked to a number of variables and these must be matched.
Det er allerede blevet angivet, at en grundpara-15 meter er den specifikke (unitære) strømningshastighed af det opløsningsmiddel, der tilføres og udtages fra hvert ekstraktionskar. Denne skal i almindelighed ligge fra 2 til 15 in3 /time/m2.It has already been stated that a base pair of 15 meters is the specific (unitary) flow rate of the solvent supplied and extracted from each extraction vessel. This should generally be from 2 to 15 in3 / hour / m2.
Andre parametre må vælges korrekt, såsom højde: 20 diameter-forholdet for karret, filterelementets geometriske egenskaber, filterelementets åbningers størrelse, det materiale, der udgør filterelementet,dets tykkeIse,opslam-ningens kinematiske viskositet og intensiteten af den i karret opretholdte omrøring.Other parameters must be selected correctly, such as height: the diameter of the vessel, the geometric properties of the filter element, the size of the filter element openings, the material constituting the filter element, its thickness, the kinematic viscosity of the slurry and the intensity of the stirring maintained in the vessel.
25 I beskrivelsen til den ovennævnte tidligere an søgning er det anført, at enhver fagmand ville være i stand til at vælge de korrekte værdier for de ovenfor anførte parametre for at kunne optimisere fremgangsmåden og effektiviteten af ekstraktionen i overensstemmelse med 30 det faste materiale, der håndteres, dets størrelse, opløsningsmidlet og alle de andre involverede karakteristika.In the description of the aforementioned prior application, it is stated that any person skilled in the art would be able to select the correct values for the above parameters in order to optimize the method and efficiency of the extraction according to the solid material being handled. , its size, the solvent and all the other characteristics involved.
Den nævnte tidligere danske patentansøgning nr.The previously mentioned Danish patent application no.
1980/79 indeholder imidlertid ikke nogen hentydning til 35 den mulige anvendelse af en ternær blanding med forskellige faser, og det synes tværtimod, som om den beskrevne fremgangsmåde i dansk patentansøgning nr. 1980/79 finder sin vante anvendelse netop ved brug af et enkelt opløsningsmiddel eller af en blanding af gensidigt blandbareHowever, 1980/79 contains no reference to the possible use of a ternary mixture with different phases, and on the contrary, it seems as if the process described in Danish Patent Application No. 1980/79 finds its usual use precisely with the use of a single solvent. or of a mixture of mutually miscible
DK 159975 BDK 159975 B
4 og gensidigt forenelige opløsningsmidler.4 and mutually compatible solvents.
Det har nu overraskende vist sig, hvilket udgør grundlaget for den omhandlede opfindelse, at det er muligt til det formål samtidigt fra solsikkefrø at ekstra-2 here mere end én uønsket komponent, at anvende en blanding bestående af tre opløsningsmidler, der er fordelt over forskellige faser.It has now surprisingly been found, which forms the basis of the present invention, that it is possible for the purpose of simultaneously extracting from sunflower seeds more than one undesirable component a mixture of three solvents distributed over different phases.
I overensstemmelse hermed er fremgangsmåden ifølge opfindelsen ejendommelig ved, at man i ét trin ekstrahe-*jq rer solsikkefrøene med en tofaseblanding bestående af 40-70 vol% carbonhydridopløsningsmiddel, 20-55% vol% ethanol, og 5-10 vol% vand, og midlet til udøvelse af denne fremgangsmåde er ejen-Ί5 datimeligt * ved, at midlet består af en tofaseblanding af: 40-70 vol% carbonhydridopløsningsmiddel, 20- 55 vol% ethanol, og 5-10 vol% vand.Accordingly, the process of the invention is characterized in that in one step, the sunflower seeds are extracted with a two-phase mixture consisting of 40-70 vol% hydrocarbon solvent, 20-55% vol% ethanol, and 5-10 vol% water, and The agent for carrying out this process is proprietary ved5 in that the agent consists of a two-phase mixture of: 40-70 vol% hydrocarbon solvent, 20-55 vol% ethanol, and 5-10 vol% water.
Ved den omhandlede fremgangsmåde og i midlet til 20 udøvelse af denne er carbonhydridopløsningsmidlet fortrinsvis n-hexan.In the present process and in the means for practicing it, the hydrocarbon solvent is preferably n-hexane.
Anvendelsen af en sådan blanding muliggør, at der kan opnås et stort ekstraktionsudbytte, og såfremt den anvendes ved den ovenfor beskrevne ekstraktionsprocedure, 25 er et sådant resultat kombineret med den nævnte fremgangsmådes lethed og anerkendelse.The use of such a mixture enables a large extraction yield to be obtained, and if used in the extraction procedure described above, such a result is combined with the ease and recognition of said method.
Faststof-væskeekstraktionsprocessen udføres fortrinsvis indenfor en temperatur på fra 20 til 50°C, i et tidsrum på fra 30 minutter til 6 timer og med et vægt 30 (kg): rumfang (liter)-forhold mellem de flagede frø og solventblandingen liggende fra 1:1 til 1:10 (d.v.s. fra 1 kg til 1 liter, til 1 kg til 10 liter).The solid-liquid extraction process is preferably carried out within a temperature of from 20 to 50 ° C, for a period of from 30 minutes to 6 hours and with a weight 30 (kg): volume (liter) ratio of the seeded seeds to the solvent mixture ranging from 1 : 1 to 1:10 (ie from 1 kg to 1 liter, to 1 kg to 10 liters).
Analytiske metoder til kemisk karakterisering af solsikkefrøene og de deraf opnåede produkter.Analytical methods for chemical characterization of the sunflower seeds and the products obtained.
35 Vandindhold, aske og råfibre er blevet bestemt efter standardmetoderne fra A.O.A.C. (Association of Official Analytical Chemists, 12. udgave, 1975).35 Water content, ash and crude fiber have been determined by the standard methods of A.O.A.C. (Association of Official Analytical Chemists, 12th Edition, 1975).
DK 159975BDK 159975B
55
Proteinindholdet blev udtrykt som macroKieldahl-nitrogen multipliceret med koefficienten 5,70. Totallipid bestemtes efter petroleumsethermetoden, som angivet i A.A.C.C. nr. 30-26. Polyphenolforbindelserne måltes ved 5 den kolorimetriske metode af Bittoni et al (Riv. Ital.The protein content was expressed as macroKieldahl nitrogen multiplied by the coefficient 5.70. Total lipid was determined by the petroleum ether method, as set forth in A.A.C.C. Nos. 30-26. The polyphenol compounds were measured by the colorimetric method of Bittoni et al (Riv. Ital.
Sost. Grasse, 54, 421, 1977). Totalsukkerindhold bestemtes ved metoden af M. Dubois et al (Analytical Chemistry, 28, 350-356, 1968), modificeret ved, at isolation af de individuelle sukkerarter blev udeladt, og at kun det to-10 tale sukkerindhold betragtedes som værende til stede i produktet.Sost. Grasse, 54, 421, 1977). Total sugar content was determined by the method of M. Dubois et al (Analytical Chemistry, 28, 350-356, 1968), modified by the isolation of the individual sugars being omitted and only the dual sugar content considered to be present in product.
P. D. I. (Proteindispersibilitetsindekset),der anvendtes til at bestemme den mængde nitrogen, der var i stand til at blive dispergeret i vand, under naturlige 15 pH-betingelser, var i overensstemmelse med den fremgangsmåde, der er anført i A.O.C.S. (Metode Ba 10-65, revideret 1969).The P. D. I. (Protein Dispersibility Index) used to determine the amount of nitrogen capable of being dispersed in water under natural pH conditions was in accordance with the procedure set out in A.O.C.S. (Method Ba 10-65, revised 1969).
Alle driftsdetailler vil fremgå af de følgende eksempler, der har til formål at belyse den omhandlede 20 opfindelse, uden at begrænse dens område.All operating details will be apparent from the following examples, which are intended to illustrate the present invention, without limiting its scope.
Eksempel 1Example 1
Solsikkefrø med den i tabel 1 anførte sammensætning, afskalledes fuldstændigt i et "Hydromecanique & 25 Frottement"-afskalningsapparat, og de afskallede frø ma-ledes til en tykkelse på 0,25 mm i en Diefenbach L2/30/30 mølle. Det således opnåede produkt behandledes med en blanding med følgende sammensætning: n -hexan 60 rumfang, % 30 ethanol 35 rumfang % vand 5 rumfang· %.Sunflower seeds of the composition set out in Table 1 were completely peeled off in a "Hydromecanique & 25 Frottement" peeler and the peeled seeds were ground to a thickness of 0.25 mm in a Diefenbach L2 / 30/30 mill. The product thus obtained was treated with a mixture of the following composition: n -hexane 60 volumes,% 30 ethanol 35 volumes% water 5 volumes ·%.
Driftsbetingelserne ved faststof-væskeekstraktionen var som følger:The operating conditions of the solid-liquid extraction were as follows:
DK 159975 BDK 159975 B
6 fyldningskoefficient for ekstraktionskarrene (vægt (kg): rumfang(liter)) 1:4 ekstraktionstid 6 timer6 filling coefficient for extraction vessels (weight (kg): volume (liter)) 1: 4 extraction time 6 hours
ekstraktionstemperatur 45°Cextraction temperature 45 ° C
5 ekstraktionsforhold (vægt: rumfang) 1:7,5.5 extraction ratio (weight: volume) 1: 7.5.
Tabel 1Table 1
Kemisk sammensætning af en solsikkefrøprøve.Chemical composition of a sunflower seed sample.
1 q Vandindhold 6% I tørstof:1 q Water content 6% in dry matter:
Lipider 60,0%Lipids 60.0%
Proteiner 22,0%Proteins 22.0%
Aske 2*9% Råfibre 3,5% 15 Sukker 4,4%Ash 2 * 9% Raw fiber 3.5% 15 Sugar 4.4%
Phenoler 2,4%Phenols 2.4%
Andre nitrogenfrie estere 4,8%Other nitrogen-free esters 4.8%
Slutproduktet havde den følgende kemiske sammensætning : 2o Vandindhold 6,5% I tørstof:The final product had the following chemical composition: 2o Water content 6.5% in dry matter:
Lipider 0,5%Lipids 0.5%
Phenoler 0,8%Phenols 0.8%
Proteiner (Nx5,7) 65,1% 25 Sukker 1,9% P.D.I. (Proteindispersibilitets- index) 8,9%.Proteins (Nx5.7) 65.1% Sugar 1.9% P.D.I. (Protein Dispersibility Index) 8.9%.
Eksempel 2 2Q Solsikkefrø med en sammensætning svarende til sammensætningen af frøene i eksempel 1, og som underkastedes en behandling som den i eksempel 1, ekstraheredes med en solventblanding, bestående af: n-hexan 60 rumfang % 3ethanol 30 rumfang. % vand 10 rumfang %Example 2 2Q Sunflower seeds having a composition similar to the composition of the seeds of Example 1, which were subjected to a treatment like that of Example 1, were extracted with a solvent mixture consisting of: n-hexane 60 volume% 3ethanol 30 volume. % water 10 volumes%
Claims (4)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT2517581 | 1981-11-19 | ||
| IT25175/81A IT1144945B (en) | 1981-11-19 | 1981-11-19 | CONTEMPORARY EXTRACTION OF LIPIDS AND POLYPHENOLS FROM LAMINATED ALMONDS OF SUNFLOWER |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| DK510082A DK510082A (en) | 1983-05-20 |
| DK159975B true DK159975B (en) | 1991-01-07 |
| DK159975C DK159975C (en) | 1991-06-03 |
Family
ID=11215914
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DK510082A DK159975C (en) | 1981-11-19 | 1982-11-16 | PROCEDURE FOR SOLID PHASE LIQUID EXTRACTION OF FLIPPED AND POLYPHENOLS FROM FLAGED, PURPOSED SUNFLOWER SEED AND MEDICINE FOR EXERCISING THE PROCEDURE |
Country Status (30)
| Country | Link |
|---|---|
| JP (1) | JPS5889696A (en) |
| KR (1) | KR860000215B1 (en) |
| AR (1) | AR245770A1 (en) |
| AU (1) | AU556440B2 (en) |
| BE (1) | BE894902A (en) |
| BR (1) | BR8205517A (en) |
| CA (1) | CA1207320A (en) |
| CH (1) | CH650938A5 (en) |
| CS (1) | CS235965B2 (en) |
| DD (1) | DD206787A5 (en) |
| DE (1) | DE3238359A1 (en) |
| DK (1) | DK159975C (en) |
| ES (1) | ES8402702A1 (en) |
| FR (1) | FR2516537A1 (en) |
| GB (1) | GB2110519B (en) |
| GR (1) | GR76782B (en) |
| HU (1) | HU189617B (en) |
| IL (1) | IL67064A0 (en) |
| IN (1) | IN157613B (en) |
| IT (1) | IT1144945B (en) |
| MA (1) | MA19637A1 (en) |
| NL (1) | NL8203924A (en) |
| PL (1) | PL134642B1 (en) |
| PT (1) | PT75716B (en) |
| RO (1) | RO85787B (en) |
| SE (1) | SE458281B (en) |
| SU (1) | SU1512487A3 (en) |
| TR (1) | TR21426A (en) |
| YU (1) | YU43923B (en) |
| ZA (1) | ZA827498B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2565789B1 (en) * | 1984-06-15 | 1990-07-06 | Univ Toronto Innovation Found | PROCESS FOR THE SOLVENT TREATMENT OF PROTEIN MATERIALS FROM CRUCIFER OLEAGINOUS SEEDS TO OBTAIN PROTEIN FLOUR WITH REDUCED GLUCOSINOLATE CONTENT |
| MD4299C1 (en) * | 2013-09-16 | 2015-03-31 | Институт Генетики И Физиологии Растений Академии Наук Молдовы | Process for producing antioxidant compounds from walnut kernel skin (Juglans regia L.) |
| KR101702741B1 (en) | 2015-02-06 | 2017-02-06 | 김주철 | Lamp Switch Position Indicating Apparatus |
| EP3850067A1 (en) * | 2018-09-13 | 2021-07-21 | Bunge Global Innovation, LLC. | Oilseed extraction method |
| FR3090008B1 (en) * | 2018-12-17 | 2023-03-31 | Pennakem Europa | Process for the production of a crude oil rich in polyphenol by solid/liquid extraction |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3714210A (en) * | 1970-06-05 | 1973-01-30 | Grain Processing Corp | Process for extracting full fat soybean flakes or meal |
| GB1449123A (en) * | 1972-11-08 | 1976-09-15 | Unilever Ltd | Vegetable protein extraction |
| SE7601543L (en) * | 1975-02-21 | 1976-08-23 | Snam Progetti | PROCEDURE FOR EXTRACTING PHENOLES AND OLIGOSACCARIDES FROM VEGETABLE MATERIAL |
| IT1096315B (en) * | 1978-05-24 | 1985-08-26 | Snam Progetti | METHOD FOR SOLID-LIQUID EXTRACTION AND APPARATUS SUITABLE FOR THE PURPOSE |
-
1981
- 1981-11-19 IT IT25175/81A patent/IT1144945B/en active
-
1982
- 1982-09-15 SE SE8205282A patent/SE458281B/en not_active IP Right Cessation
- 1982-09-17 BR BR8205517A patent/BR8205517A/en not_active IP Right Cessation
- 1982-09-21 GR GR69331A patent/GR76782B/el unknown
- 1982-09-21 KR KR8204257A patent/KR860000215B1/en not_active IP Right Cessation
- 1982-09-21 AU AU88571/82A patent/AU556440B2/en not_active Ceased
- 1982-09-28 PL PL1982238400A patent/PL134642B1/en unknown
- 1982-10-11 NL NL8203924A patent/NL8203924A/en not_active Application Discontinuation
- 1982-10-11 YU YU2281/82A patent/YU43923B/en unknown
- 1982-10-12 GB GB08229150A patent/GB2110519B/en not_active Expired
- 1982-10-13 ZA ZA827498A patent/ZA827498B/en unknown
- 1982-10-14 JP JP57179182A patent/JPS5889696A/en active Granted
- 1982-10-15 AR AR82290989A patent/AR245770A1/en active
- 1982-10-15 DE DE19823238359 patent/DE3238359A1/en active Granted
- 1982-10-15 ES ES516936A patent/ES8402702A1/en not_active Expired
- 1982-10-15 CS CS827363A patent/CS235965B2/en unknown
- 1982-10-18 HU HU823311A patent/HU189617B/en not_active IP Right Cessation
- 1982-10-21 PT PT75716A patent/PT75716B/en not_active IP Right Cessation
- 1982-10-25 IL IL67064A patent/IL67064A0/en not_active IP Right Cessation
- 1982-10-25 CA CA000414102A patent/CA1207320A/en not_active Expired
- 1982-10-25 RO RO108880A patent/RO85787B/en unknown
- 1982-11-02 MA MA19849A patent/MA19637A1/en unknown
- 1982-11-03 BE BE0/209391A patent/BE894902A/en not_active IP Right Cessation
- 1982-11-04 SU SU823508328A patent/SU1512487A3/en active
- 1982-11-16 DK DK510082A patent/DK159975C/en active
- 1982-11-16 DD DD82244956A patent/DD206787A5/en not_active IP Right Cessation
- 1982-11-16 CH CH6677/82A patent/CH650938A5/en not_active IP Right Cessation
- 1982-11-17 FR FR8219249A patent/FR2516537A1/en active Granted
- 1982-11-18 TR TR21426A patent/TR21426A/en unknown
- 1982-11-19 IN IN1347/CAL/82A patent/IN157613B/en unknown
Also Published As
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP2004535914A (en) | Process and system for removing oils from food staff using a membrane filter | |
| US11807828B2 (en) | Agitator for solventless extraction of cannabis essential oils | |
| CN111315458B (en) | Terpene enrichment methods and systems | |
| CA3000255A1 (en) | Method of continuous extraction and separation of useful compounds from plant or animal material | |
| DK159975B (en) | PROCEDURE FOR SOLID PHASE LIQUID EXTRACTION OF FLIPPED AND POLYPHENOLS FROM FLAGED, PURPOSED SUNFLOWER SEED AND MEDICINE FOR EXERCISING THE PROCEDURE | |
| US4387110A (en) | Method and apparatus for solid-liquid extraction steps | |
| WO1993016607A1 (en) | Method for decholesterolization of egg yolk with simultaneous production of cholesterol as a by-product | |
| WO1995002962A1 (en) | Method for producing azadirachtin concentrates from neem seed materials | |
| Fauduet et al. | Rapeseed meal upgrading—pilot scale preparation of rapeseed meal materials with high or low glucosinolate contents | |
| DK2904075T3 (en) | ETHANOL HEAT EXTRACTION OF PLANT OR ANIMAL MATERIAL LIPIDS | |
| KR850001433B1 (en) | Process of producing peanut oil | |
| RHEE et al. | Aqueous process for pilot plant‐scale production of peanut protein concentrate | |
| ES2969435T3 (en) | Method for combined cell disruption and extraction of oil-containing seeds | |
| CN210856046U (en) | Essential oil refining equipment | |
| RU2076899C1 (en) | Process for manufacturing sea-buckthorn oil concentrate | |
| NO803050L (en) | PROCEDURE FOR MANUFACTURING FOOD OR FOR KRILL | |
| KR830000401B1 (en) | Solid-liquid extraction method | |
| Mangold | Extraction with supercritical fluids: A progress report from Germany | |
| RU2701856C1 (en) | Vegetable raw material extraction unit | |
| RU2245627C1 (en) | Biologically active oil manufacture process | |
| RU2051596C1 (en) | Method of preparing extract from gourd seeds | |
| SU1678282A1 (en) | Method for processing bones into feed meal and fat | |
| WO1996031579A1 (en) | Process for extracting oils or fats from oleaginous natural substances and use thereof | |
| PL135809B1 (en) | Method of manufacture of powdered vegetable lecithin,especially rape lecithin | |
| UA56006C2 (en) | A process for preparing a biologically active substance complex of lipids and extracts |