EP0182396A2 - Procédé de traitement d'huiles triglycéridiques - Google Patents

Procédé de traitement d'huiles triglycéridiques Download PDF

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Publication number
EP0182396A2
EP0182396A2 EP85201472A EP85201472A EP0182396A2 EP 0182396 A2 EP0182396 A2 EP 0182396A2 EP 85201472 A EP85201472 A EP 85201472A EP 85201472 A EP85201472 A EP 85201472A EP 0182396 A2 EP0182396 A2 EP 0182396A2
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EP
European Patent Office
Prior art keywords
oil
process according
microfiltration
miscella
range
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.)
Withdrawn
Application number
EP85201472A
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German (de)
English (en)
Other versions
EP0182396A3 (fr
Inventor
Werner Merk
Robert Leo Karel Maria Van De Sande
Achintya Kumar Sen Gupta
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.)
Unilever PLC
Original Assignee
Unilever PLC
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 Unilever PLC filed Critical Unilever PLC
Publication of EP0182396A2 publication Critical patent/EP0182396A2/fr
Publication of EP0182396A3 publication Critical patent/EP0182396A3/fr
Withdrawn legal-status Critical Current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
    • C11B3/00—Refining fats or fatty oils
    • C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter

Definitions

  • the present invention relates to a process for treating triglyceride oil.
  • the present invention relates to a process for degumming triglyceride oil.
  • Triglyceride oils are valuable raw materials. They consist of triglycerides of fatty acids but usually contain minor components such as colouring materials, sugars, glucosides, waxes, free fatty acids, metals and phosphatides. Some of these minor components are preferably removed in smaller or larger amounts. A particularly important and valuable group of these minor components is formed by the phosphatides. "Degumming" is the name given to processes in which inter alia phosphatides are removed from triglyceride oil. The product obtained from the phosphatidecontaining composition that is separated from the oil is commonly called lecithin.
  • the triglyceride oil is contacted under pressure with a semi-permeable membrane.
  • the phosphatides form micelles whose size prevents the phosphatides passing through the membrane.
  • Other impurities can be incorporated in the micelles.
  • Triglyceride oil passes through the membrane, providing a filtrate of refined oil. Further details of the process carried out in the presence of a solvent can be found in GB 1509543.
  • Water degumming and its many variations can be an efficient process. It can, however, suffer from the disadvantage that the aqueous residue formed cannot readily realise its value. It contains not only useful phosphatides, but also other impurities whose presence detracts from the inherent value of the lecithin.
  • Ultrafiltration can provide a way of refining triglyceride oil to a high level of purity. In practice, however, it has been found to suffer from a variety of operational problems.
  • Step (i) of the present process requires that at least a part of the particulate matter in the oil which falls somewhere within the range of 0.0 4 to 25pm, preferably 0.2 to 25pm, more preferably 0.2 to 15pm, is removed.
  • Parficulate matter larger than 25pm can, of course, and normally will be removed as well, either as part of the present process or as part of a separate process.
  • Advantages accruing to the present process are, however, believed to be due to the attention paid to the removal of a substantial part of particulate matter between 0.04um, particularly matter between 0.2pm and 15pm, prior to performing a specific degumming operation.
  • Matter smaller than 0.04pm, in the preferred embodiment matter smaller than 0.2pm, is not removed in step (i), it is retained in the oil and where appropriate is removed from the oil during the degumming step; in particular phosphatides present in micelles of approximately 5-10 nm are removed from the oil in step (ii) of the process, not in step (i).
  • step (i) is directed to removal of particulate matter within the range of from 0.2pm to 15pm, more preferably matter within the range of from 0.2 to l.Opm.
  • the degumming step can, for example, be a water degumming operation or involve ultrafiltration. In the former, practice of the present invention can remove impurities such as iron-containing particles prior to water degumming so that a high quality, pale, transparent phosphatide phase having a low iron content can be obtained. If water degumming is to be performed, step (i) is preferably carried out in the absence of a solvent If desired, however, step (i) may be carried out in the presence of a solvent
  • step (i) is preferably carried out in the presence of a solvent, preferably a non- acidic, non-alcoholic, non-polar organic solvent
  • a solvent preferably a non- acidic, non-alcoholic, non-polar organic solvent
  • the solvent has a molecular weight within the range 50-200, especially 60-150.
  • suitable solvents include esters of lower fatty acids and lower monohydric alcohols, in which the total number of carbon atoms is at most 12, halogenated hydrocarbons and inert hydrocarbons, particularly alkanes, cycloalkanes and simple aromatic hydrocarbons, e.g. benzene and its homologues containing alkyl substituents having up to 4 carbon atoms.
  • step (i) is performed on the miscella obtained direct from solvent extraction of the triglyceride oil.
  • the solvent employed is preferably hexane.
  • Ultrafiltration is preferably performed in the presence of the same solvent using a suitable semipermeable membrane of a cut-off limit between 1000 and 1,000,000, preferably between 10,000 and 1 00,000 at temperatures between 10°C and 80°C at pressures of 1.5-10 bar absolute.
  • Membranes may be flat plate type, or tubular or capillary bundles or a combination of these types in parallel or series.
  • the module construction is not of primary importance for good flux and all types of commercial modules of any geometry may be used, either alone or in combination with each other, parallel or in series. Further details for carrying out an ultrafiltration step are found in the above-mentioned GB 1509543.
  • Step (i) preferably includes microfiltration to remove insoluble particles down to 0.04pm, preferably down to 0.1pm, more preferably down to 0.2pm in dimension.
  • step (i) can include one or more conditioning steps such as one or multiple heat treatment steps, an adsorbtive treatment with a suitable adsorbent (e.g. bleaching earth) or a pretreatment with alkali followed in each case by settling or microfiltration. Where more than one conditioning step is applied they can be employed in any order.
  • a suitable adsorbent e.g. bleaching earth
  • the present process can thus include the following sequence of steps: in a first step the oil to be degummed is subjected to a pre-treatment consisting of:
  • crossflow-microfiltration use of a microfiltration means in which the material being filtered flows along the surface of the microfiltration means.
  • a microfiltration means in which the material being filtered flows along the surface of the microfiltration means.
  • This same principle is used also in ultrafiltration.
  • the main difference between crossflow microfiltration and ultrafiltration lies in the configuration of the pores in the membranes used for these two processes. Since microfiltration is concerned with suspended particles of micron size, the pores of the membrane are of a similar order of magnitude. Ideally these pores should be slightly smaller than the particles so as to avoid clogging of the pores by the particles on the one hand and ensure maximum filtrate flow on the other.
  • a comparative trial employing one and the same crude soyabean oil miscella without heat treatment it required about 4 days for more or less complete sedimentation of the suspended matters, whereas the heat-treated miscella (1 min., 100°C) deposited suspended matter in less than 1 hour.
  • the sedimented matter of the heat-treated miscella was, moreover, somewhat slimy in consistence and did not whirl up when shaken, in contrast to the non-heated miscella.
  • the amount of the sediments from the heat-treated miscella was about 50-100% higher than in the case of the non-heated miscella and could be separated from the miscella by decantation or by microfiltration. Alternative separation techniques, such as rotary decanters and clarifiers, could be employed.
  • adsorbent 0.1% of a mixture of a fitter aid Celite 535 (Trade-mark) and of an acid- activated bleaching earth Tonsil ACFF (Trade-mark) of Südchemie, Kunststoff (ratio 15/85), can be added to the crude soyabean miscella containing 30% crude soyabean oil, stirred at a temperature of 50°C and then filtered through a Funda filter (Trade-mark) (manufactured by A.G. für Chemieapparatebau, Mannedorf, Zurich) with a built-in stainless steel filter of 75pm aperture. The rate of filtration was 4 m 3 /h per square metre of filter surface.
  • the starting miscella contained 0.01% of suspended matter, whereas the filtrate was free of suspended matter. Additionally, water, chlorophyll and phospholipid contents were lowered by about 2% only, compared to the initial content of these components of the crude miscella.
  • Other adsorbents such as active carbon, non-activated bleaching earths, e.g. Tonsil 13 (Trade-mark) (Sudchemie), or organic filter aids, e.g. Porvacel HB 150 and Highflow (Trade-marks) were effective.
  • Other filtering equipments e.g. Niagara Filter (Trade-mark) (of Messrs AMA Filter BV, Alkmaar, Netherlands) were also effective.
  • the treatment could suitably be carried out at a temperature in the range of from 20 to 150°C.
  • soaps Addition of aqueous lye to the miscella neutralises the free fatty acids present and produces soaps in situ. A major part of the soaps form mixed micelles with the phospholipids present in the miscella and remain dissolved, but a minor part form double-salt type complexes with proteins, lipoproteins and phospholipids and separate out as finely divided particles, which, if present in the uftrafiltration stage, cause low flux and flux decline. These materials can effectively be removed by crossflowmicrofiltration.
  • the suspended particulate matter which can be removed by use of the present process is believed to comprise lipoproteins and other insoluble materials.
  • the particulate matter was collected by using a 0.2p Teflon (Trade-mark) microfilter and analysed for the chemical composition.
  • Teflon Trade-mark
  • the analysis of the material recovered from a crude soyabean miscella obtained by extracting crushed soyabeans with industrial hexane is given below:
  • the particles are smaller than 24 ⁇ m and they are not easily separated by usual commercial 25 pm sieve-type filters.
  • the rate of sedimentation can be very slow in a 30% oil-hexane miscella and it can take 3 to 7 days for the material to settle down more or less completely, although some finer particles can still remain in suspension after a week.
  • Pumping the miscella using a centrifugal pump at a high linear velocity through a membrane module shifts the particle size distribution in favour of smaller particles. Storage for a longer period of time shows slow agglomeration in favour of the particles with bigger particle sizes.
  • the seeds are usually crushed with various types of high speed mills (e.g. hammer mill) using a fine screen (e.g. 1/32 inch). Higher speed of the mills allows a better extraction of the oil, but at the same time promotes the formation of lipid-protein complexes by cell disruption. Deposition of lipid-protein complexes on the surface of the ultrafiltration membrane is, we believe, a reason for flux decline during ultrafiltration. By use of the present process the lipoproteins, whether soluble or insoluble, can be removed from the oil prior to degumming.
  • high speed mills e.g. hammer mill
  • fine screen e.g. 1/32 inch
  • the heat treatment for example can lead to accelerated decomposition of the lipoproteins rendering them to agglomerate and be separated readily by sedimentation or filtration.
  • Addition of an adsorbent like bleaching earth leads to decomposition and adsorption of the lipoproteins with resulting easier separation by the following microfiltration or sedimentation.
  • Addition of aqueous lye or other scavengers to the crude miscella prior to ultrafiltration can be effective too, leading to a better and more consistent flux rate in a subsequent ultrafiltration step.
  • the present pretreatment of triglyceride oil prior to ultrafiltration can thus not only improve the flux rate to a great extent, but also reduce the tendency for flux decline during operation of the ultrafiltration significantly.
  • the present invention is applicable to all triglyceride oils, but is of particular use in refining of soyabean oil, sunflower oil, safflower oil, cottonseed oil, rapeseed oil, corn oil, grapeseed oil, rice bran oil, tallow and fish oil.
  • soyabean oil sunflower oil, safflower oil, cottonseed oil, rapeseed oil, corn oil, grapeseed oil, rice bran oil, tallow and fish oil.
  • a crude soyabean oil miscella fresh from the extraction plant analysing was subjected to a crossflow microfiltration using a Mycrodyn Filter (trade-mark) module HA 1124 H 22 of Messrs ENKA AG, Wuppertal, Germany, length 50 cm, total filter surface 0.05m 2 , pore diameter 0.2p, material polypropylene.
  • the operational conditions were:
  • the average flux was 2.82 m 3 /m 2 h.
  • the flux diagram illustrating the backflushing is shown in Fig. 1.
  • Total suspended matter (lipoproteins etc.) dropped after microfiltration to 5 ppm.
  • the filtered miscella was immediately ultrafiltered using a PCI-BX3 (Trade-mark) tubular polysulphone membrane at 45°C, 4.5 bar pressure and 3.7 m/sec linear velocity.
  • the membrane was conditioned prior to use by soaking 2 hours each in isopropanol and hexane.
  • the permeate leaving the ultrafiltration module was collected, whereas the retentate leaving the ultrafiltration unit was mixed with the miscella to be ultrafiltered.
  • the initial flux was 232 l/m 2 h of miscella (corresponding to 50 kg hexane-free oil/m 2 h), which dropped to 210 I/m 2 h miscella corresponding to 47 kg/m 2 h hexane-free oil after 8 hours run.
  • Phosphorus content in the permeate oil was 7 ppm.
  • a sample of crude extraction soyabean miscella from the same source as employed in Example 1 was ultrafiltered as above after having been heat-treated at 100°C for 1 minute, at a pressure higher than the vapour pressure of the miscella, and separated from the coagulated sediments.
  • the initial and the final flux during ultrafiltration after 8 hours run was very similar to themicrofiftered miscella and showed the same constancy.
  • a crude soyabean oil miscella which was purified by crossflow microfiltration as described under Example 1 , was immediately ultrafiftered as also described under Example 1.
  • the initial rate of ultrafiltration was 165 l/m 2 h, which decreased to 122 l/m 2 h after 4 hours run.
  • the P-contents of the permeate oil and of the retentate oil were 7 ppm and 3246 ppm, respectively.
  • Figure 2 shows the flux diagrams of the microfiltered miscella as compared to the non-microfiltered miscella.
  • the following Table shows the analytical data of the crude miscella, the microfiltered miscella and the ultrafiltered mis- cellas.
  • a crude rapeseed oil miscella containing 1.2% free fatty acids (based on oil) was neutralised by addition of the theoretical amount of 40% aq. KOH solution.
  • the major part of the soap formed in situ went into micellar solution, but complexes of soaps, phospholipids, lipoproteins etc. remained suspended in the miscella.
  • the miscella was subjected to a pretreatment by heating at 90°C for 20 sec. and then crossflow microfiltered as described under Example 1 .
  • the microfiltered miscella was immediately cooled down to 45°C and ultrafiltered as described under Example 1. After 4.5 hours the total yield of permeate was 77% of the input; the P-content in the retentate oil was 1507 ppm.
  • the flux rate in dependence on time is shown in Fig. 3.
  • the analytical results of the crude miscella after addition of lye, after crossflow microfiltration, and ultrafiltration are shown in the Table below.
  • Hexane-free crude extracted soyabean oil was passed through a crossflow microfiltration unit with back flushing and then water degummed.
  • the water content of the aqueous phase obtained was reduced to yield a lecithin of high transparency and good quality.
  • Crossflow microfiltration was carried out on a Microdyn Filter Module HA 11 24 H 22 unit ex Enka AG, Wuppertal pore dia 0.2 ⁇ . The filtration was carried out at 45°C/2 bar. For the back flushing, a cycle time of 3.5 min. and a back flushing time of 2 sec. were used. The linear flow velocity was about 2 m/sec. The mean filtration rate was about 95 kg oil/m 2 h.
  • the starting oil contained 230 ppm total suspended solids and 7.4 ppm Fe.
  • the filtered oil contained 8 ppm total suspended solids and 0.6 ppm Fe.
  • the filtrate was conventionally degummed with water at 85°C, the gum was centrifuged off, and water removed under vacuum at a temperature of 50°C.
  • the lecithin contained 1.95% P and 15 ppm FE and was more than 90% transparent
  • the same extraction oil without previous crossflow microfiltration yielded, following the same degumming step, a lecithin having
  • the experiment was repeated once more, but the bleaching earth was mixed with the crude miscella at room temperature prior to the heat treatment.
  • the amount of bleaching earth used in this experiment was 2 wt% (calculated on the amount of oil present in the miscella).

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  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Fats And Perfumes (AREA)
EP85201472A 1984-09-14 1985-09-10 Procédé de traitement d'huiles triglycéridiques Withdrawn EP0182396A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8423229 1984-09-14
GB848423229A GB8423229D0 (en) 1984-09-14 1984-09-14 Treating triglyceride oil

Publications (2)

Publication Number Publication Date
EP0182396A2 true EP0182396A2 (fr) 1986-05-28
EP0182396A3 EP0182396A3 (fr) 1987-06-16

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EP (1) EP0182396A3 (fr)
JP (1) JPS61136597A (fr)
AU (1) AU4742785A (fr)
GB (1) GB8423229D0 (fr)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2193219A (en) * 1986-05-08 1988-02-03 Denis Bowes Verity Treatment of oil
EP0348004A3 (fr) * 1988-06-21 1991-07-10 Unilever N.V. Procédé pour raffiner les huiles glycéridiques
US5286886A (en) * 1988-06-21 1994-02-15 Van Den Bergh Foods Co., Division Of Conopco, Inc. Method of refining glyceride oils
FR2696184A1 (fr) * 1992-09-28 1994-04-01 Pall Corp Procédé de fractionnement d'une composition de matière grasse et produit ainsi obtenu.
FR2760756A1 (fr) * 1997-03-17 1998-09-18 Richard De Nyons Procede de production des huiles vegetales hypoallergeniques
US6207209B1 (en) 1999-01-14 2001-03-27 Cargill, Incorporated Method for removing phospholipids from vegetable oil miscella, method for conditioning a polymeric microfiltration membrane, and membrane
US6833149B2 (en) 1999-01-14 2004-12-21 Cargill, Incorporated Method and apparatus for processing vegetable oil miscella, method for conditioning a polymeric microfiltration membrane, membrane, and lecithin product
EP2087087A4 (fr) * 2006-10-31 2013-04-03 Due Miljo As Procédé de purification d'huile, et utilisations de celle-ci pour les aliments et l'alimentation
US9422506B2 (en) * 2007-09-13 2016-08-23 Givaudan, S.A. Dewaxing

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4629588A (en) * 1984-12-07 1986-12-16 W. R. Grace & Co. Method for refining glyceride oils using amorphous silica

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2261067A1 (de) * 1972-12-14 1974-06-27 Henkel & Cie Gmbh Verfahren zur reinigung von fettsaeureoder fettsaeureestergemischen
GB1509543A (en) * 1974-05-16 1978-05-04 Unilever Ltd Purification process
GB1585166A (en) * 1976-09-10 1981-02-25 Unilever Ltd Oil purification by adding hydratable phosphatides
GR74979B (fr) * 1980-10-02 1984-07-12 Unilever Nv
JPS5950718B2 (ja) * 1981-11-30 1984-12-10 旭化成株式会社 植物性油の膜による精製方法

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2193219A (en) * 1986-05-08 1988-02-03 Denis Bowes Verity Treatment of oil
US5516924A (en) * 1988-06-21 1996-05-14 Van Den Bergh Foods Co., Division Of Conopco, Inc. Method of refining glyceride oils
EP0526954A3 (en) * 1988-06-21 1993-04-28 Unilever N.V. Method of refining glyceride oils
US5286886A (en) * 1988-06-21 1994-02-15 Van Den Bergh Foods Co., Division Of Conopco, Inc. Method of refining glyceride oils
EP0348004A3 (fr) * 1988-06-21 1991-07-10 Unilever N.V. Procédé pour raffiner les huiles glycéridiques
FR2696184A1 (fr) * 1992-09-28 1994-04-01 Pall Corp Procédé de fractionnement d'une composition de matière grasse et produit ainsi obtenu.
BE1007448A3 (fr) * 1992-09-28 1995-07-04 Pall Corp Procede de fractionnement d'une composition de matiere grasse et produit ainsi obtenu.
FR2760756A1 (fr) * 1997-03-17 1998-09-18 Richard De Nyons Procede de production des huiles vegetales hypoallergeniques
US6207209B1 (en) 1999-01-14 2001-03-27 Cargill, Incorporated Method for removing phospholipids from vegetable oil miscella, method for conditioning a polymeric microfiltration membrane, and membrane
US6833149B2 (en) 1999-01-14 2004-12-21 Cargill, Incorporated Method and apparatus for processing vegetable oil miscella, method for conditioning a polymeric microfiltration membrane, membrane, and lecithin product
US7494679B2 (en) 1999-01-14 2009-02-24 Cargill Incorporated Method and apparatus for processing vegetable oil miscella, method for conditioning a polymeric microfiltration membrane, membrane, and lecithin product
US7923052B2 (en) 1999-01-14 2011-04-12 Cargill, Incorporated Method and apparatus for processing vegetable oil miscella, method for conditioning a polymeric microfiltration membrane, membrane, and lecithin product
EP2087087A4 (fr) * 2006-10-31 2013-04-03 Due Miljo As Procédé de purification d'huile, et utilisations de celle-ci pour les aliments et l'alimentation
US9422506B2 (en) * 2007-09-13 2016-08-23 Givaudan, S.A. Dewaxing

Also Published As

Publication number Publication date
GB8423229D0 (en) 1984-10-17
EP0182396A3 (fr) 1987-06-16
JPS61136597A (ja) 1986-06-24
AU4742785A (en) 1986-03-20

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