WO2013018412A1 - 精製グリセリド組成物及び該精製グリセリド組成物の製造方法 - Google Patents
精製グリセリド組成物及び該精製グリセリド組成物の製造方法 Download PDFInfo
- Publication number
- WO2013018412A1 WO2013018412A1 PCT/JP2012/062383 JP2012062383W WO2013018412A1 WO 2013018412 A1 WO2013018412 A1 WO 2013018412A1 JP 2012062383 W JP2012062383 W JP 2012062383W WO 2013018412 A1 WO2013018412 A1 WO 2013018412A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- glyceride composition
- mcpd
- clay
- purified
- oil
- 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
- C11B3/00—Refining fats or fatty oils
- C11B3/10—Refining fats or fatty oils by adsorption
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
- A23D9/00—Other edible oils or fats, e.g. shortenings, cooking oils
- A23D9/02—Other edible oils or fats, e.g. shortenings, cooking oils characterised by the production or working-up
- A23D9/04—Working-up
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/12—Naturally occurring clays or bleaching earth
-
- 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
-
- 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
- C11B3/12—Refining fats or fatty oils by distillation
- C11B3/14—Refining fats or fatty oils by distillation with the use of indifferent gases or vapours, e.g. steam
Definitions
- the present invention relates to a purified glyceride composition and a method of producing the purified glyceride composition.
- Some glyceride compositions contain only trace amounts of fatty acid esters of 3-chloropropane-1,2-diol which may be derived from fatty acid esters of glycidol, which is one of the epoxides having such an oxirane structure.
- the fatty acid esters of 3-chloropropane-1,2-diol can yield 3-chloropropane-1,2-diol by liberation of fatty acids.
- the presence of high concentrations of 3-chloropropane-1,2-diol and its derivatives is said to adversely affect health.
- Patent Document 1 discloses at least one selected from the group consisting of 3-chloropropane-1,2-diol, fatty acid ester of 3-chloropropane-1,2-diol, glycidol and fatty acid ester of glycidol.
- a method of deodorizing a glyceride composition containing a species and / or containing 3% by mass or more of diglyceride under specific temperature conditions According to this method, the content of the fatty acid ester of glycidol and the fatty acid ester of 3-chloropropane-1,2-diol in the glyceride composition can be reduced.
- the present invention has been made in view of the above circumstances, and a purified glyceride composition containing 3-chloropropane-1,2-diol and a fatty acid ester of 3-chloropropane-1,2-diol, and the purified glyceride composition
- the purpose is to provide a method of manufacturing an object.
- alkaline clay alkaline clay
- a method for producing a purified glyceride composition comprising an alkali clay treatment in which a glyceride composition not subjected to a deodorizing step is brought into contact with an alkali clay.
- the glyceride composition comprises glycerides in which 1 to 3 fatty acids are esterified to glycerin, and in addition to triglyceride (triacylglycerol) which is a main component of fats and oils, diglyceride (diacylglycerol), It also includes monoglycerides (monoacylglycerols).
- triacylglycerol triacylglycerol
- diglyceride diglyceride
- monoglycerides monoglycerides
- components other than the glyceride derived from animal and vegetable fats and oils for example, plant sterol, lecithin, an antioxidant component, a pigment component etc. may be contained, it is preferable that 95 mass% or more is glyceride.
- the method for producing a purified glyceride composition of the present invention is characterized in that the glyceride composition not subjected to the deodorizing step is brought into contact with an alkali clay.
- the decolorization step of the glyceride composition is carried out using an alkali clay.
- the alkaline clay used in the method for producing the purified glyceride composition of the present invention is a clay (ie, alkaline clay) in which the pH of the aqueous solution containing the alkaline clay exhibits alkalinity when the clay is added to water.
- a clay ie, alkaline clay
- a white clay exhibiting a pH of 8.5 or more is preferable because of its high adsorptivity and degradability to chlorine compounds.
- the alkali clay used in the method for producing a purified glyceride composition of the present invention is not particularly limited, and, for example, those having the following composition (unit: mass%) can be used.
- the amount of alkaline clay used in the alkaline clay treatment step effectively adsorbs or decomposes the chlorine compound in the glyceride composition to produce 3-MCPD and / or 3-MCPD fatty acid ester in the purified glyceride composition.
- the amount of alkaline clay to be used in the alkaline clay treatment step is effective to absorb or decompose chlorine compounds in the glyceride composition effectively, even if it is not excessive, and 3-MCPD and / or 3- in the purified glyceride composition.
- the amount of the fatty acid ester of MCPD can be suppressed and the content thereof can be sufficiently reduced, so 3.0% by mass or less, 2.9% by mass or less, 2.8% by mass or less with respect to the amount of the glyceride composition It is preferable that it is 2.5 mass% or less.
- the conditions in the alkaline clay processing step are not particularly limited, and may be the conditions of the decoloring step used in the usual fat and oil manufacturing method.
- heating may be performed at 80 to 150 ° C. for 5 to 60 minutes under reduced pressure.
- the alkali clay can be removed by filtration or the like to obtain an alkali clay treated glyceride composition (decolorized oil).
- the method for bringing the glyceride composition into contact with the alkali clay is not particularly limited, and for example, after the decolorizing step is carried out with the clay or activated carbon, the treatment can also be performed using the alkali clay.
- the alkaline clay processing step (this step may be a decoloring step), it can be carried out in the coexistence of clay other than alkaline clay and activated carbon.
- it can also be made to contact by packing alkaline clay in a filter or a column, and letting a glyceride composition flow.
- a purified oil that has undergone a purification step for example, a degumming step, a deacidifying step, a water washing step, etc.
- a deodorizing step for example, a degumming step, a deacidifying step, a water washing step, etc.
- the glyceride composition which has not been subjected to the deodorizing step is preferred in that fatty acid esters of 3-MCPD and / 3-MCPD are not produced.
- rapeseed oil soybean oil, rice oil, safflower oil, grape oil, sunflower oil, wheat germ oil, corn oil, cottonseed oil, sesame oil, peanut oil, flax oil, sesame oil, sesame oil, olive oil, palm oil, palm oil etc.
- Vegetable oil mixed vegetable oil obtained by mixing two or more of these, or edible oleic oil such as palm olein, palm stearin, palm super olein, palm mid fraction obtained by fractionating these, hydrogenated oil of these, transesterified oil etc.
- Edible oils produced by direct esterification reactions such as medium chain fatty acid triglycerides can be used.
- fatty acid esters of 3-MCPD and / or 3-MCPD tend to be generated frequently in fats and oils relatively rich in partial glycerides, palm-derived fats and oils, rice oil, transesterified oil, etc. are used as raw materials It is particularly preferable because the effect of reducing the fatty acid ester of 3-MCPD and / or 3-MCPD of the present invention is high.
- the purification method before and after the alkali clay treatment process of the present invention can use a conventional method. Specifically, chemical refining (chemical refining) and physical refining (physical refining) may be used, but any purification method may be used.
- crude oil obtained by squeezing / extracting a plant serving as a raw material is refined through degumming treatment, deacidification treatment, decolorization treatment, dewaxing treatment, deodorizing treatment, and becomes a refined oil.
- the latter physical refining is a method which is often performed in palm oil, coconut oil, etc., and crude oil obtained by squeezing palm, palm, etc. as a raw material is subjected to degumming treatment, decoloring treatment, deacidification, It is refined by passing through deodorizing treatment, and it becomes refined oil.
- the formation of fatty acid esters of 3-MCPD and / or 3-MCPD in the purified glyceride composition can be suppressed by the above-mentioned alkaline clay treatment step, and the content thereof can be reduced.
- the content of fatty acid esters of 3-MCPD and / or 3-MCPD in the purified glyceride composition is freed of these using a modification of the German official method (DGF Standard Methods C-III 18 (09)). Identified as an MCPD equivalent.
- sample fats and oils are collected, an internal standard substance is added, and then a methanol solution of sodium methoxide is added, and the mixture is reacted at room temperature to perform saponification decomposition of the ester.
- an aqueous sodium bromide solution containing a trace amount of acetic acid and hexane are added thereto and mixed, and then the hexane is removed.
- 3-MCPD and 3-MCPD fatty acid esters are all converted to free 3-MCPD. Thereafter, it is derivatized with phenylboric acid, extracted with hexane, and measured with a gas chromatograph mass spectrometer.
- the measured value according to the German official method is a 3-MCPD equivalent value of the total content of 3-MCPD, fatty acid ester of 3-MCPD, glycidol and fatty acid ester of glycidol. Therefore, in such a method, when it is desired to measure the total content of 3-MCPD and only fatty acid esters of 3-MCPD, there is a problem that the content of glycidol and glycidol fatty acid ester is also included.
- the method for producing a purified glyceride composition of the present invention may include a deodorizing step of the glyceride composition which has been subjected to the above-mentioned alkaline clay processing step.
- the alkali clay treatment step corresponds to the decolorization step of the glyceride composition.
- Deodorization may be carried out under the temperature condition of 100 to 260 ° C. used in the usual fat and oil production method, or may be carried out under the lower temperature condition of 100 to 250 ° C.
- Preferred temperature conditions in the deodorizing step are 150 to 230 ° C., more preferably 180 to 220 ° C.
- the other conditions in the deodorizing step are not particularly limited, but it is preferable to perform depressurization or steam injection, and it is more preferable to perform depressurization and steam injection.
- the deodorizing time is preferably 15 to 150 minutes, more preferably 20 to 100 minutes.
- the purified glyceride composition subjected to the above-mentioned deodorizing step may be purified again.
- the re-refining step can perform the above-described refining step, and can include, for example, a re-deodorizing step, a re-decoloring step, or a re-deodorizing step. In particular, it is preferable to carry out the re-decoloring step.
- the white clay used in the recoloring step is not particularly limited, and may be alkaline white clay, acid white clay, or activated white clay which is acid white clay that has been subjected to an activation treatment.
- the glyceride composition and the alkali clay are brought into contact in the first decolorization step (alkali clay treatment step) prior to the recolorization step, the residual amount of chlorine compounds in the purified glyceride composition is sufficiently reduced. Ru. Therefore, regardless of the type of white earth used in the re-decoloring step, the amount of 3-MCPD that can be generated in the re-deodorizing step after the re-decoloring step can be significantly reduced.
- the conditions in the recoloring step are not particularly limited, and may be the conditions used in a conventional method for producing fats and oils, as in the first decoloring step before the recoloring step.
- heating may be performed at 80 to 150 ° C. for 5 to 60 minutes under reduced pressure.
- the white earth can be removed by filtration or the like to obtain a re-decolorized oil.
- the re-decolorized oil obtained after the re-decolorization step may be further re-deodorized.
- the conditions in the re-deodorizing process are not particularly limited, and may be the conditions used in the usual fat and oil manufacturing method as in the first deodorizing process.
- the purified glyceride composition of the present invention is characterized by being obtained by the method for producing the purified glyceride composition of the present invention described above. According to the purified glyceride composition of the present invention, it can be expected that the content of 3-MCPD and fatty acid ester of 3-MCPD in the purified glyceride composition is reduced.
- Comparative Example 1 Add 1% by mass of acid clay (product name: Super A, manufactured by Wantotik Clay Products Sdn Bhd) to crude palm oil (3-MCPD equivalent amount: 0.0 ppm) under reduced pressure After decolorizing at 110 ° C. for 30 minutes, the acid clay was removed by filtration to obtain a decolorizing oil. Then, while the steam was blown into the decolorized oil, deodorization was performed at 260 ° C. for 1 hour under reduced pressure to obtain a purified glyceride composition of Comparative Example 1.
- acid clay product name: Super A, manufactured by Wantotik Clay Products Sdn Bhd
- crude palm oil 3-MCPD equivalent amount: 0.0 ppm
- Example 1 Purification of Example 1 in the same manner as Comparative Example 1 except that 1% by mass of alkaline white earth (product name: Bleaching Earth, Natural Bleach Sdn Bhd) is used instead of 1% by mass of acid white earth A glyceride composition was obtained.
- alkaline white earth product name: Bleaching Earth, Natural Bleach Sdn Bhd
- Example 2 The purified glyceride composition of Example 2 was obtained in the same manner as in Example 1 except that the temperature of the deodorizing treatment was changed to 230 ° C.
- Comparative Example 2 A purified glyceride composition of Comparative Example 3 was obtained in the same manner as in Comparative Example 1 except that the amount of acid clay was 2% by mass.
- Example 3 The purified glyceride composition of Example 3 was obtained in the same manner as in Example 1 except that the amount of alkaline clay was 2% by mass.
- Example 4 The purified glyceride composition of Example 4 was obtained in the same manner as in Example 2 except that the amount of alkali clay was changed to 2% by mass.
- Comparative Examples 1 and 2 and Examples 1 to 4 are shown in Table 1.
- the “3-MCPD equivalent amount” in the table indicates the total amount of 3-MCPD and fatty acid esters of 3-MCPD in the purified glyceride composition, converted to the amount of free 3-MCPD.
- the clay treatment step in the present invention may be a bleaching step.
- an additional bleaching step i.e. re-bleaching step
- the clay used in the clay treatment step decolorization step
- it exerts an effect on suppression of formation of 3-MCPD and 3-MCPD fatty acid ester in the purified glyceride composition.
- Comparative Example 3 To the purified glyceride composition obtained in Comparative Example 2, 1.5% by mass of acid clay (manufactured by Mizusawa Chemical Industry Co., Ltd.) is added, and after decolorization under reduced pressure at 110 ° C. for 20 minutes, filtration is performed by filtration. The acid clay was removed to obtain a re-decolorized oil. Then, while deaerating the re-decolorized oil, deodorization was carried out again at 260 ° C. for 90 minutes under reduced pressure to obtain a purified glyceride composition of Comparative Example 3.
- acid clay manufactured by Mizusawa Chemical Industry Co., Ltd.
- Example 5 With respect to the purified glyceride composition obtained in Example 4, the purified glyceride composition of Example 5 was obtained in the same manner as in Comparative Example 3.
- Example 6 The purified glyceride composition of Example 6 was obtained in the same manner as in Example 5 except that the temperature was 240 ° C.
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Wood Science & Technology (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Food Science & Technology (AREA)
- Polymers & Plastics (AREA)
- Dispersion Chemistry (AREA)
- Fats And Perfumes (AREA)
- Edible Oils And Fats (AREA)
- Treatment Of Liquids With Adsorbents In General (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
Description
本発明の精製グリセリド組成物の製造方法は、脱臭工程を経ていないグリセリド組成物と、アルカリ白土と、を接触させることを特徴とする。好ましくは、上記グリセリド組成物の脱色工程がアルカリ白土を使用して行われる。
従来、グリセリド組成物中の色素等の除去のために、酸性白土が使用されてきた。しかし、本発明者が鋭意研究した結果、酸性白土ではなくアルカリ性の白土(アルカリ白土)を使用することにより、グリセリド組成物中の色素等の除去だけではなく、グリセリド組成物中の3-クロロプロパン-1,2-ジオール(以下、3-MCPDと称する)及び/又は3-クロロプロパン-1,2-ジオールの脂肪酸エステル(以下、3-MCPDの脂肪酸エステルと称する)の生成が抑制され、これらの含有量の低減を効果的に実現できることを見出した。
SiO2 (50~60)
Al2O3 (10~20)
Fe2O3 (3~10)
MgO (2~9)
CaO (1~5)
本発明の精製グリセリド組成物の製造方法では、グリセリド組成物として、脱臭工程を除く精製工程(例えば、脱ガム工程、脱酸工程、水洗工程等)を経た精製油を用いてもよい。脱臭工程を経ていないグリセリド組成物は、3-MCPD、及び/3-MCPDの脂肪酸エステルが生成していない点で好ましい。特に未精製の粗油、定法に従って精製された脱ガム油、脱酸油、もしくは脱色油が好ましく、脱酸油もしくは脱色油がより好ましい。例えば、菜種油、大豆油、米油、サフラワー油、ぶどう油、ひまわり油、小麦はい芽油、とうもろこし油、綿実油、ごま油、落花生油、フラックス油、エゴマ油、オリーブ油、パーム油、ヤシ油等の植物油、これら2種以上を混合した調合植物油、又は、これらを分別したパームオレイン、パームステアリン、パームスーパーオレイン、パームミッドフラクション等の食用分別油、これらの水素添加油、エステル交換油等のほか、中鎖脂肪酸トリグリセリドのような直接エステル化反応により製造された食用油を用いることができる。なお、3-MCPD、及び/又は3-MCPDの脂肪酸エステルは、部分グリセリドが比較的多い油脂において多く発生する傾向にあることから、パーム由来の油脂、米油、エステル交換油等を原料に用いることが本発明の3-MCPD、及び/又は3-MCPDの脂肪酸エステルの低減効果が高いという理由から特に好ましい。本発明のアルカリ白土処理工程の前後の精製方法は、定法を用いることができる。具体的には、ケミカル精製(ケミカルリファイニング)と、フィジカル精製(フィジカルリファイニング)とがあるが、いずれの精製方法を用いてもよい。なお、前者のケミカル精製は、原料となる植物を圧搾・抽出した原油が、脱ガム処理、脱酸処理、脱色処理、脱ろう処理、脱臭処理を経ることで精製され、精製油となる。これに対し、後者のフィジカル精製は、パーム油やヤシ油等にてよく行われている方法であり、原料となるパームやヤシ等を圧搾した原油が、脱ガム処理、脱色処理、脱酸・脱臭処理を経ることで精製され、精製油となる。
本発明においては、上記のアルカリ白土処理工程により、精製グリセリド組成物中の3-MCPD及び/又は3-MCPDの脂肪酸エステルの生成を抑制し、これらの含有量を低減させることができる。精製グリセリド組成物中の3-MCPD及び/又は3-MCPDの脂肪酸エステルの含有量は、ドイツ公定法(DGF Standard Methods C-III 18(09))の変法を用いて、これらを遊離3-MCPD換算量として特定する。
本発明の精製グリセリド組成物の製造方法においては、上記アルカリ白土処理工程を経たグリセリド組成物の脱臭工程を含んでもよい。この場合、上記アルカリ白土処理工程は、グリセリド組成物の脱色工程に相当する。脱臭は、通常の油脂の製造方法で用いられる100~260℃の温度条件下で行ってもよく、より低い100~250℃の温度条件にて行ってもよい。脱臭工程において好ましい温度条件は150~230℃であり、より好ましくは180~220℃である。通常の油脂の製造方法で用いられる温度条件よりも低い温度条件下でグリセリド組成物の脱臭を行うことにより、精製グリセリド組成物中の3-MCPD及び/又は3-MCPDの脂肪酸エステルの生成抑制効果、及びこれらの含有量の低減効果が大きくなることが期待できる。
本発明の精製グリセリド組成物の製造方法においては、上記脱臭工程を経た精製グリセリド組成物を再度精製してもよい。再精製工程は、前述の精製工程を行うことができ、例えば、再脱臭工程、再脱色工程、又は再脱臭工程を含むことができる。特に、再脱色工程を行うことが好ましい。再脱色工程において使用される白土としては特に制限されず、アルカリ白土、酸性白土、又は、活性化処理を施されている酸性白土である活性白土等であってもよい。
本発明の精製グリセリド組成物は、上述の本発明の精製グリセリド組成物の製造方法により得られることを特徴とする。本発明の精製グリセリド組成物によれば、精製グリセリド組成物中の3-MCPD、及び3-MCPDの脂肪酸エステルの含有量が低減していることが期待できる。
白土処理工程において使用する白土が、精製グリセリド組成物中の3-MCPD、及び3-MCPDの脂肪酸エステルの生成抑制に対して及ぼす影響について検討した。
イオン交換水20gに、実施例において使用するアルカリ白土又は比較例において使用する酸性白土を0.1g加え、スターラーを用いて撹拌しながら、携帯型pHメータ(機種名:PH-81、東京硝子器械株式会社製)を用いて、白土のpHを測定した。その結果、酸性白土(製品名:Super A、Wantotik Clay Products Sdn Bhd社製)のpHは6.05であり、アルカリ白土(製品名:NB14000、Natural Bleach Sdn Bhd社製)のpHは9.53だった。
粗パーム油(3-MCPD換算量 0.0ppm)に、粗パーム油の量に対して1質量%の酸性白土(製品名:Super A、Wantotik Clay Products Sdn Bhd社製)を添加し、減圧下、110℃で30分間脱色した後、ろ過により酸性白土を除去して、脱色油を得た。次いで、該脱色油に水蒸気を吹き込みながら、減圧下、260℃で1時間脱臭処理し、比較例1の精製グリセリド組成物を得た。
1質量%の酸性白土の代わりに、1質量%のアルカリ白土(製品名:Bleaching Earth、Natural Bleach Sdn Bhd社製)を用いる以外は、比較例1と同様の方法にて、実施例1の精製グリセリド組成物を得た。
脱臭処理の温度を230℃とする以外は、実施例1と同様の方法にて、実施例2の精製グリセリド組成物を得た。
酸性白土の量を2質量%にする以外は、比較例1と同様の方法にて、比較例3の精製グリセリド組成物を得た。
アルカリ白土の量を2質量%にする以外は、実施例1と同様の方法にて、実施例3の精製グリセリド組成物を得た。
アルカリ白土量を2質量%にする以外は、実施例2と同様の方法にて、実施例4の精製グリセリド組成物を得た。
精製グリセリド組成物中の3-MCPD、3-MCPD脂肪酸エステルの定量を、ドイツ公定法(DGF Standard Methods C-III 18(09))の変法に準拠して行った。この方法では、測定試料を調製する際に、3-MCPD及び3-MCPD脂肪酸エステルが遊離3-MCPDに変換されるため、3-MCPD及び3-MCPD脂肪酸エステルの総量を遊離3-MCPDとして測定できる。
分析装置:島津製作所株式会社製、機種名:QP-2010
カラム:製品名:HP-5MS、Agilent Technology社製(長さ30m、径0.25mm)
カラム温度:60℃(1分)~120℃(昇温速度10℃/分)~190℃(昇温速度6℃/分)~280℃(昇温速度20℃/分)
検出器:MS(EI,SIMモード)
スプリットレス:1μL注入
キャリアガス:He
本発明における白土処理工程は脱色工程であってもよい。この場合、さらなる脱色工程(すなわち再脱色工程)を設けることができる。そこで、白土処理工程(脱色工程)において使用する白土が、グリセリド組成物をさらに再脱色した場合に、精製グリセリド組成物中の3-MCPD、及び3-MCPDの脂肪酸エステルの生成抑制に対して及ぼす影響について検討した。
比較例2で得た精製グリセリド組成物に対して、1.5質量%の酸性白土(水澤化学工業株式会社製)を添加し、減圧下、110℃で20分間、再脱色した後、ろ過により酸性白土を除去し、再脱色油を得た。次いで、該再脱色油に水蒸気を吹き込みながら、減圧下、260℃にて90分間、再脱臭し、比較例3の精製グリセリド組成物を得た。
実施例4で得た精製グリセリド組成物に対して、比較例3と同様の方法にて実施例5の精製グリセリド組成物を得た。
温度を240℃とする以外は、実施例5と同様の方法にて、実施例6の精製グリセリド組成物を得た。
Claims (8)
- 脱臭工程を経ていないグリセリド組成物と、
アルカリ白土と、
を接触させるアルカリ白土処理工程を含むことを特徴とする精製グリセリド組成物の製造方法。 - 前記アルカリ白土処理工程が脱色工程であり、前記アルカリ白土処理工程の後に、さらに脱臭工程を含むことを特徴とする請求項1に記載の精製グリセリド組成物の製造方法。
- 前記脱臭工程は、100~260℃の温度条件下にて行われることを特徴とする請求項2に記載の精製グリセリド組成物の製造方法。
- 前記脱臭工程の後に、さらに再精製工程を含むことを特徴とする請求項2又は3に記載の精製グリセリド組成物の製造方法。
- 前記再精製工程は、再脱色工程を含むことを特徴とする請求項4に記載の精製グリセリド組成物の製造方法。
- 前記再脱色工程は、酸性白土と接触させることを特徴とする請求項5に記載の精製グリセリド組成物の製造方法。
- 前記グリセリド組成物は、パーム油であることを特徴とする請求項1~6のいずれか1項に記載の精製グリセリド組成物の製造方法。
- 請求項1~7のいずれか1項に記載の製造方法により得られることを特徴とする精製グリセリド組成物。
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ES12820381.7T ES2609117T3 (es) | 2011-07-29 | 2012-05-15 | Composición de glicérido purificado y procedimiento de producción de la composición de glicérido purificado |
JP2012543823A JP5216942B1 (ja) | 2011-07-29 | 2012-05-15 | 精製グリセリド組成物及び該精製グリセリド組成物の製造方法 |
EP12820381.7A EP2738243B1 (en) | 2011-07-29 | 2012-05-15 | Purified glyceride composition and method for producing purified glyceride composition |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2011-166894 | 2011-07-29 | ||
JP2011166894 | 2011-07-29 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2013018412A1 true WO2013018412A1 (ja) | 2013-02-07 |
Family
ID=47628953
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2012/062383 WO2013018412A1 (ja) | 2011-07-29 | 2012-05-15 | 精製グリセリド組成物及び該精製グリセリド組成物の製造方法 |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP2738243B1 (ja) |
JP (1) | JP5216942B1 (ja) |
ES (1) | ES2609117T3 (ja) |
MY (1) | MY159241A (ja) |
WO (1) | WO2013018412A1 (ja) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104289176A (zh) * | 2014-11-06 | 2015-01-21 | 中国农业科学院油料作物研究所 | 一种风味油脂固体脱色剂的制备方法 |
JP2016123331A (ja) * | 2014-12-26 | 2016-07-11 | ミヨシ油脂株式会社 | 食用油脂の製造方法 |
JP2016123330A (ja) * | 2014-12-26 | 2016-07-11 | ミヨシ油脂株式会社 | 食用油脂中のクロロプロパノール類を低減する方法 |
EP3058054A4 (en) * | 2013-10-14 | 2017-06-14 | Aak Ab | Mitigation of 2-mcpd, 3-mcpd, esters therof and glycidyl esters in vegetable oil |
JP2018095758A (ja) * | 2016-12-15 | 2018-06-21 | 日清オイリオグループ株式会社 | 油脂組成物 |
EP3739027A1 (de) | 2019-05-14 | 2020-11-18 | Clariant International Ltd | Verfahren zur reduzierung des 3-mcpd-gehalts in raffinierten pflanzenölen |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DK2672834T4 (da) * | 2011-02-10 | 2022-11-28 | Cargill Inc | Fremgangsmåde til fremstilling af en raffineret olie |
MY159241A (en) | 2011-07-29 | 2016-12-30 | Nisshin Oillio Group Ltd | Purified glyceride composition and method for producing purified glyceride composition |
CN108239573A (zh) * | 2016-12-27 | 2018-07-03 | 中粮集团有限公司 | 油脂及其制备方法 |
MY190874A (en) * | 2017-03-30 | 2022-05-13 | Sime Darby Plantation Berhad | Process for producing a refined vegetable oil |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010063450A1 (de) * | 2008-12-02 | 2010-06-10 | Süd-Chemie AG | Verfahren zur reduzierung des 3-mcpd-gehalts in raffinierten pflanzenöllen |
WO2010126136A1 (ja) * | 2009-04-30 | 2010-11-04 | 不二製油株式会社 | グリセリド油脂中のクロロプロパノール類及びその形成物質の生成を抑制する方法 |
WO2011040539A1 (ja) * | 2009-09-30 | 2011-04-07 | 不二製油株式会社 | グリセリド油脂中のクロロプロパノール類及びその形成物質、グリシドール脂肪酸エステルを低減する方法 |
JP2011074358A (ja) | 2009-09-07 | 2011-04-14 | Nisshin Oillio Group Ltd | グリセリド組成物及び該グリセリド組成物の製造方法 |
WO2011081119A1 (ja) * | 2009-12-29 | 2011-07-07 | 不二製油株式会社 | グリセリド油脂中のクロロプロパノール類及びその形成物質の生成を抑制する方法 |
JP2011147436A (ja) * | 2010-01-19 | 2011-08-04 | Cj Cheiljedang Corp | 3−mcpd−fsが低減化された食用油脂の製造方法 |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5151211A (en) | 1988-12-05 | 1992-09-29 | Oil-Dri Corporation Of America | Oil bleaching method and composition for same |
US5252762A (en) * | 1991-04-03 | 1993-10-12 | W. R. Grace & Co.-Conn. | Use of base-treated inorganic porous adsorbents for removal of contaminants |
JP2010126136A (ja) * | 2008-12-01 | 2010-06-10 | Denso Corp | 車両用空調装置 |
AU2010325890A1 (en) | 2009-12-04 | 2012-06-07 | Archer Daniels Midland Company | Glycidyl ester reduction in oil |
MY159241A (en) | 2011-07-29 | 2016-12-30 | Nisshin Oillio Group Ltd | Purified glyceride composition and method for producing purified glyceride composition |
-
2012
- 2012-05-15 MY MYPI2014000233A patent/MY159241A/en unknown
- 2012-05-15 JP JP2012543823A patent/JP5216942B1/ja active Active
- 2012-05-15 ES ES12820381.7T patent/ES2609117T3/es active Active
- 2012-05-15 WO PCT/JP2012/062383 patent/WO2013018412A1/ja active Application Filing
- 2012-05-15 EP EP12820381.7A patent/EP2738243B1/en not_active Revoked
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010063450A1 (de) * | 2008-12-02 | 2010-06-10 | Süd-Chemie AG | Verfahren zur reduzierung des 3-mcpd-gehalts in raffinierten pflanzenöllen |
WO2010126136A1 (ja) * | 2009-04-30 | 2010-11-04 | 不二製油株式会社 | グリセリド油脂中のクロロプロパノール類及びその形成物質の生成を抑制する方法 |
JP2011074358A (ja) | 2009-09-07 | 2011-04-14 | Nisshin Oillio Group Ltd | グリセリド組成物及び該グリセリド組成物の製造方法 |
WO2011040539A1 (ja) * | 2009-09-30 | 2011-04-07 | 不二製油株式会社 | グリセリド油脂中のクロロプロパノール類及びその形成物質、グリシドール脂肪酸エステルを低減する方法 |
WO2011081119A1 (ja) * | 2009-12-29 | 2011-07-07 | 不二製油株式会社 | グリセリド油脂中のクロロプロパノール類及びその形成物質の生成を抑制する方法 |
JP2011147436A (ja) * | 2010-01-19 | 2011-08-04 | Cj Cheiljedang Corp | 3−mcpd−fsが低減化された食用油脂の製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2738243A4 * |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP3058054A4 (en) * | 2013-10-14 | 2017-06-14 | Aak Ab | Mitigation of 2-mcpd, 3-mcpd, esters therof and glycidyl esters in vegetable oil |
CN104289176A (zh) * | 2014-11-06 | 2015-01-21 | 中国农业科学院油料作物研究所 | 一种风味油脂固体脱色剂的制备方法 |
JP2016123331A (ja) * | 2014-12-26 | 2016-07-11 | ミヨシ油脂株式会社 | 食用油脂の製造方法 |
JP2016123330A (ja) * | 2014-12-26 | 2016-07-11 | ミヨシ油脂株式会社 | 食用油脂中のクロロプロパノール類を低減する方法 |
JP2018095758A (ja) * | 2016-12-15 | 2018-06-21 | 日清オイリオグループ株式会社 | 油脂組成物 |
WO2018110637A1 (ja) * | 2016-12-15 | 2018-06-21 | 日清オイリオグループ株式会社 | 油脂組成物 |
EP3739027A1 (de) | 2019-05-14 | 2020-11-18 | Clariant International Ltd | Verfahren zur reduzierung des 3-mcpd-gehalts in raffinierten pflanzenölen |
Also Published As
Publication number | Publication date |
---|---|
MY159241A (en) | 2016-12-30 |
EP2738243A1 (en) | 2014-06-04 |
JP5216942B1 (ja) | 2013-06-19 |
ES2609117T3 (es) | 2017-04-18 |
JPWO2013018412A1 (ja) | 2015-03-05 |
EP2738243A4 (en) | 2015-03-04 |
EP2738243B1 (en) | 2016-10-05 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2013018412A1 (ja) | 精製グリセリド組成物及び該精製グリセリド組成物の製造方法 | |
JP5973530B2 (ja) | グリセリド組成物及び該グリセリド組成物の製造方法 | |
CA2859924C (en) | Method of treating a vegetable oil | |
RU2672605C1 (ru) | Удаление нежелательных пропаноловых компонентов | |
JP2018515674A (ja) | 塩基性第四級アンモニウム塩処理を含む、グリセリド油精製法 | |
WO2010126136A1 (ja) | グリセリド油脂中のクロロプロパノール類及びその形成物質の生成を抑制する方法 | |
JP5399544B1 (ja) | 精製油脂の製造方法 | |
JP2018517037A (ja) | 金属汚染物質をグリセリド油から除去する方法、及びそれを組み込んだグリセリド油を精製する方法 | |
WO2014081279A1 (en) | An improved palm oil refining process | |
WO2011055732A1 (ja) | グリセリド油脂中のクロロプロパノール類及びその形成物質を低減する方法 | |
WO2015146248A1 (ja) | 精製パーム系油脂の製造方法 | |
JP6639149B2 (ja) | 精製油脂の製造方法 | |
TW201320901A (zh) | 油脂的製造方法 | |
JP6857017B2 (ja) | 油脂組成物 | |
JP2009108145A (ja) | 脱酸油脂の製造方法またはそれによって得られる精製油脂 | |
JP5924755B2 (ja) | グリセリド組成物の製造方法 | |
WO2013145808A1 (ja) | 精製グリセリド組成物の製造方法 | |
JP6021382B2 (ja) | グリセリド組成物の製造方法 | |
JP5917975B2 (ja) | グリセリド組成物の製造方法 | |
JP2015067692A (ja) | 精製油脂の製造方法 | |
CN113614212A (zh) | 精制油脂的制造方法和生育酚类的制造方法 | |
JP2016169391A (ja) | パーム系油脂 | |
WO2013145398A1 (ja) | グリセリド組成物の製造方法、及び第1の精製工程後のグリセリド組成物に対する第2の精製工程の必要性を判断する判断方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
ENP | Entry into the national phase |
Ref document number: 2012543823 Country of ref document: JP Kind code of ref document: A |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 12820381 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
REEP | Request for entry into the european phase |
Ref document number: 2012820381 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2012820381 Country of ref document: EP |