EP1141182B1 - Verfahren zum behandeln von ölsaatflocken vor der ölgewinnung - Google Patents

Verfahren zum behandeln von ölsaatflocken vor der ölgewinnung

Info

Publication number
EP1141182B1
EP1141182B1 EP99957276A EP99957276A EP1141182B1 EP 1141182 B1 EP1141182 B1 EP 1141182B1 EP 99957276 A EP99957276 A EP 99957276A EP 99957276 A EP99957276 A EP 99957276A EP 1141182 B1 EP1141182 B1 EP 1141182B1
Authority
EP
European Patent Office
Prior art keywords
flakes
mixer
oil
moisture content
temperatures
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.)
Expired - Lifetime
Application number
EP99957276A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP1141182A1 (de
Inventor
Wolfgang Beyer
Rüdiger HEILMANN
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.)
MG Technologies AG
Original Assignee
MG Technologies AG
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 MG Technologies AG filed Critical MG Technologies AG
Publication of EP1141182A1 publication Critical patent/EP1141182A1/de
Application granted granted Critical
Publication of EP1141182B1 publication Critical patent/EP1141182B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • C11B1/02—Pretreatment
    • C11B1/04—Pretreatment of vegetable raw material

Definitions

  • the object of the invention is to deactivate interfering amounts of enzymes in the oilseed to prevent the formation of non-hydratable phosphatides during oil extraction in the oil press and / or extraction turn off, which would otherwise get into the oil obtained and would make degumming and refining difficult.
  • the method is particularly suitable for rape seed, but also for sunflower seeds, soybeans and linseed.
  • the heat treatment with the simultaneous presence of moisture in the transporting mixer and in the annealing zone results in the deactivation of enzymes which would make oil refining more difficult.
  • These enzymes are, in particular, phospholipase and lipoxygenase and, in the case of rapeseed, especially myrosinase.
  • Deactivation completely or largely inhibits the increase of non-hydratable phosphatides in the crude oil during recovery in the oil press and also in solvent extraction. This can the Phosphatidgehalt in the crude oil obtained with a simple water treatment for degumming be lowered so far that you can feed the degummed oil directly to the physical refining.
  • the hydratable phosphatides (lecithin) are separated.
  • non-hydratable phosphatides (NHP) remain in the crude oil which is fed to refining.
  • the relatively simple physical refining (bleaching and deodorization) is sufficient in the present case, since the water degumming of crude oil from rapeseed, sunflower seeds or soybeans already sufficiently lowers the phosphatide content.
  • an important product is not only the oil, but also rapeseed meal, which can be used as feed. If the activity of myrosinase in the rape flakes is too high, the further treatment of the solids (expeller) from the oil press leads to a rapeseed meal containing disturbing amounts of fission products, which are caused by the activity of myrosinase.
  • the interfering enzymes and myrosinase are biochemically inactivated, which facilitates degumming and keeps out of the rapeseed meal disturbing amounts of fission products.
  • the oil seed flakes with a moisture content of 3 to 12 wt .-% in the transporting mixer where then takes place a further supply of moisture.
  • the flakes are heated in the transporting mixer to a temperature of 80 ° C within 3 to 10 seconds. It has been shown that about up to the temperature range of 70 up to 75 ° C, enzymatic reactions in the flakes occur more intensively, which lead to undesired substances. Rapid heating in the transporting mixer can prevent or minimize the formation of these interfering substances.
  • the method is particularly suitable for rapeseed processing, because in addition to the aforementioned lipases and rapeseed typical enzyme myrosinase can be largely deactivated.
  • Non-deactivated myrosinase leads to undesired cleavage processes (hydrolysis) of GLS during oil production in rapeseed varieties with higher or higher content of thioglucosides (GLS), resulting in volatile isothiocyanates (ITC) and non-volatile oxazolidine thiones (VOT) as reaction products containing the presscake, the rapeseed meal and affect the quality of the oil.
  • ITC volatile isothiocyanates
  • VET non-volatile oxazolidine thiones
  • the possibility is opened up to carry out a direct extraction of the rapeseed flakes with economically justifiable means without the use of an oil press.
  • the rapeseed comes from a pre-cleaning, not shown, and is fed with grain sizes of about 1 to 3 mm through the line (1) the flaking (2), which rapeseed flakes with thicknesses of about 0.1 to 0.5 mm and preferably at most 0, 3 mm form.
  • the flakes are preferably at temperatures of about 20 to 50 ° C through the line (3) a transporting mixer (4), in which it is z. B. may be a paddle mixer or screw mixer.
  • the mixer In the vicinity of the mixer input, the mixer is supplied with water vapor through line (5), which condenses in the mixer (4) and wets the rapeseed flakes. In addition to the steam, you can spray water into the mixer (4) to achieve the desired moistening.
  • At Migloausgang (3a) gives flakes with temperatures in the range of 90 to 110 ° C and a moisture content of 8 to 20 wt .-% and usually 10 to 16 wt .-%.
  • the tempering space (7) has steam-heated trays (8) and also a steam-heated heating jacket (7a), for this purpose it is provided with a vertical rotatable shaft (9) and stirring arms (10) arranged thereon.
  • the agitator arms (10) move the rape flakes over the heated trays, which have openings (11) through which the flocs fall down onto the underlying soil.
  • exhaust ducts (13) and a fan (14) steam is sucked out of the annealing space (7).
  • the rapeseed flakes fall through the channel (17) into the drying chamber (18), which is fed through the line (19) warm air from 90 to 120 ° C, which first passes into a distribution chamber (20) and then passed through a perforated bottom (21) up through the rape flakes.
  • the exhaust air is discharged through the line (22).
  • a channel (23) the dried flakes, which are formed by shrinking into granules, in a cooling chamber (24), which is supplied cold air of about 20 ° C through the conduit (25) and distributed through the granules passes , Cold exhaust air is exhausted in line (26).
  • the dried and cooled granules leave the cooling chamber (24) through the channel (27) at temperatures in the range of 40 to 70 ° C and a moisture content which is in the range of about 4 to 10 wt .-%.
  • the oil press (30) Before the granules of the oil press (30) is supplied, it is first brought in the heat exchanger (28) by indirect heating by means of steam to temperatures of 105 to 120 ° C and then fed through the line (29) of the oil press. Crude oil is withdrawn from the press (30) through line (31) and fed to the water degumming and refining process (not shown) as known per se. If the oil press is a pre-press, the resulting rapeseed expeller via a line (32) to a known solvent extraction (33) out where by means of non-polar solvent (hexane) the residual oil from the rapeseed expellers (Rapeseed meal) is largely removed. Oil-containing solvent (Miscella) leaves the extraction (33) through the line (34) and enters the Miscella distillation, where the solvent is separated from the crude oil.
  • non-polar solvent hexane
  • the extracted rapeseed expeller arrive via a line (35) to a known Entbenzinierer, also called toaster (36) to remove the rapeseed meal located in the solvent (hexane).
  • the finished shot is withdrawn in the line (37) and fed to a shot cooling unit, not shown.
  • a variant of the method exists in that the granules in the dashed line (27a) bypasses the oil press (30) and is led directly into the extraction (33).
  • Purified rapeseed with an oil content of 40 wt .-% and a H 2 O content of 6 wt .-% is crushed and treated at a temperature of about 40 ° C in a process according to the drawing on.
  • From the Flockierwalzen (2) come rapeseed flakes with a thickness of 0.1 to 0.3 mm and a temperature of 43 ° C, which are fed to a paddle mixer (4).
  • water vapor of 5 bar and 150 ° C. is fed to the mixer and the flakes are heated to 80 ° C. within 6 to 7 seconds.
  • the flakes After a residence time in the mixer of 20 seconds, the flakes reach the tempering space (7) at a temperature of 103 ° C. and with a moisture content of 13% by weight. There, the residence time is 30 minutes, and it pulls the flakes at a temperature of 100 ° C through the channel (17). In the drying chamber (18) temperatures reach 115 ° C, the flakes shrink to granules. Granules of 60 ° C. are withdrawn from the subsequent cooling chamber (24). The granules in the channel (27) has a moisture content of 5 wt .-%, it is placed in heatpans to 105 ° C before it enters the oil press (30).
  • the recovered crude oil is supplied in the line (31) of a Wasserentschleimung; From 100 t of purified rapeseed, the oil press (30) delivers 27.2 t of crude oil, and another 12.2 t of crude oil is extracted from the cooled expeller by extraction.
  • the de-oiled rapeseed meal which is obtained after extraction, de-mineralization and drying, accumulates in an amount of 62 t.
  • the by means of 0.5 t of water degummed oil contains only 0.04 wt .-% phosphatides.
  • the water degumming provides 1 t of lecithin sludge from which 0.5 t of dried crude lecithin can be obtained.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Fats And Perfumes (AREA)
  • Drying Of Solid Materials (AREA)
EP99957276A 1998-12-16 1999-11-02 Verfahren zum behandeln von ölsaatflocken vor der ölgewinnung Expired - Lifetime EP1141182B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19858015A DE19858015A1 (de) 1998-12-16 1998-12-16 Verfahren zum Behandeln von Ölsaatflocken vor der Ölgewinnung
DE19858015 1998-12-16
PCT/EP1999/008364 WO2000036058A1 (de) 1998-12-16 1999-11-02 Verfahren zum behandeln von ölsaatflocken vor der ölgewinnung

Publications (2)

Publication Number Publication Date
EP1141182A1 EP1141182A1 (de) 2001-10-10
EP1141182B1 true EP1141182B1 (de) 2006-08-16

Family

ID=7891272

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99957276A Expired - Lifetime EP1141182B1 (de) 1998-12-16 1999-11-02 Verfahren zum behandeln von ölsaatflocken vor der ölgewinnung

Country Status (10)

Country Link
US (1) US6518443B1 (enrdf_load_stackoverflow)
EP (1) EP1141182B1 (enrdf_load_stackoverflow)
CN (1) CN1122709C (enrdf_load_stackoverflow)
AT (1) ATE336562T1 (enrdf_load_stackoverflow)
CA (1) CA2354397C (enrdf_load_stackoverflow)
DE (2) DE19858015A1 (enrdf_load_stackoverflow)
IN (1) IN183540B (enrdf_load_stackoverflow)
RU (1) RU2241025C2 (enrdf_load_stackoverflow)
TW (1) TW589370B (enrdf_load_stackoverflow)
WO (1) WO2000036058A1 (enrdf_load_stackoverflow)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CZ20013237A3 (cs) * 1999-03-17 2002-02-13 Fraunhofer Gesellschaft Zur Förderung Der Angewand Způsob úpravy a zpracování semen vlčího bobu, obsahujících alkaloidy, oleje a proteiny
RU2243989C1 (ru) * 2003-12-31 2005-01-10 Кубанский государственный технологический университет Способ подготовки масличных семян к хранению и переработке
RU2243990C1 (ru) * 2003-12-31 2005-01-10 Кубанский государственный технологический университет Способ послеуборочной обработки свежеубранных масличных семян
RU2254363C1 (ru) * 2004-06-07 2005-06-20 Кубанский государственный технологический университет Способ разделения масличных семян на фракции
US7721186B2 (en) * 2006-04-28 2010-05-18 International Business Machines Corporation Redundancy protection for data recorded across multiple layers of recording media
RU2443766C1 (ru) * 2010-09-15 2012-02-27 Юрий Антонович Кошелев Способ обработки семян льна
GB2535501B (en) * 2015-02-19 2020-10-28 Desmet Ballestra Eng N V /S A Vegetable oil extraction improvement
EP3356501A4 (en) * 2015-10-02 2019-04-03 Crown Iron Works Company HEAT RECOVERY FOR SAUCE CONDITIONER AND COOKER OPERATION
CN105087147A (zh) * 2015-10-09 2015-11-25 黑龙江林加林油脂有限公司 冷压榨制备大豆油的方法
MY206995A (en) * 2017-01-24 2025-01-23 Crown Iron Works Company Modular vertical seed conditioner heating section
EP3550004B1 (de) * 2018-04-03 2020-09-09 Euro-Protein GmbH Verfahren und vorrichtung zur industriellen verarbeitung von rapssaat unter gewinnung von kaltgepresstem raps-kernöl

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE450927B (sv) 1983-12-22 1987-08-17 Svenska Lantmennens Riksforbun Sett och anordning for behandling av raps- eller rypsfro sa att mjolkavkastningen hos mjolkkor hojs samt anvendning av den erhallna produkten
NL9101643A (nl) 1991-09-27 1993-04-16 Schouten Group Nv Werkwijze en inrichting voor het reduceren van de hoeveelheid anti-nutritionele factoren in een grondstofmengsel voor diervoeder.
RU2118654C1 (ru) * 1997-08-07 1998-09-10 Товарищество с ограниченной ответственностью Научно-производственная коммерческая фирма "Техноком" Способ послеуборочной обработки масличных семян

Also Published As

Publication number Publication date
IN183540B (enrdf_load_stackoverflow) 2000-02-05
CN1122709C (zh) 2003-10-01
RU2241025C2 (ru) 2004-11-27
CN1330702A (zh) 2002-01-09
WO2000036058A1 (de) 2000-06-22
TW589370B (en) 2004-06-01
US6518443B1 (en) 2003-02-11
DE19858015A1 (de) 2000-06-21
CA2354397C (en) 2009-01-13
DE59913782D1 (de) 2006-09-28
ATE336562T1 (de) 2006-09-15
CA2354397A1 (en) 2000-06-22
EP1141182A1 (de) 2001-10-10

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