JP2709730B2 - Degumming method for fats and oils - Google Patents
Degumming method for fats and oilsInfo
- Publication number
- JP2709730B2 JP2709730B2 JP63308882A JP30888288A JP2709730B2 JP 2709730 B2 JP2709730 B2 JP 2709730B2 JP 63308882 A JP63308882 A JP 63308882A JP 30888288 A JP30888288 A JP 30888288A JP 2709730 B2 JP2709730 B2 JP 2709730B2
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- Prior art keywords
- membrane
- oils
- fats
- ultrafiltration membrane
- concentration
- Prior art date
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Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は限外濾過膜を用いた粗製トリグリセリド油脂
の脱ガム方法に関する。Description: TECHNICAL FIELD The present invention relates to a method for degumming crude triglyceride fats and oils using an ultrafiltration membrane.
（従来の技術） 油糧種子その他の動植物性の油脂原料から圧搾、溶剤
抽出などして得られた粗製トリグリセリド油脂には、通
常、燐脂質等の不純物が含まれており、これらは食用ま
たは工業用の使用において種々の不都合をもたらすの
で、最終製品とするまでには脱ガム、脱酸、脱色、脱臭
等の精製処理を行って、不純物を除去する必要がある。(Prior art) Crude triglyceride fats and oils obtained by squeezing, solvent extraction and the like from oil seeds and other animal and vegetable fats and oils usually contain impurities such as phospholipids, which are edible or industrial. Since it causes various inconveniences in the use of products, it is necessary to remove impurities by performing a purification treatment such as degumming, deacidification, decolorization, and deodorization before obtaining a final product.
従来、燐脂質は、一般に油脂精製の最初に行なわれる
脱ガムと呼ばれる工程で、粗製トリグリセリド油脂に加
水、撹はんすることにより、水和、不溶化させ、遠心分
離等の手段で除去していた。しかし、この方法では処理
された油中には、なお0.2〜0.5％程度の燐脂質が残存
し、その除去率は十分といえない。従って、更に次工程
で酸、またはアルカリ等の薬品を添加して、再度脱ガム
を行い、油中の燐脂質を100ppm程度以下とした後、脱
色、脱臭を行わなければならなかった。Conventionally, phospholipids are generally hydrated and insolubilized by adding water to a crude triglyceride oil and stirring in a step called degumming, which is generally performed at the beginning of oil / fat refining, and removed by means such as centrifugation. . However, in this method, about 0.2 to 0.5% of phospholipids still remain in the treated oil, and the removal rate cannot be said to be sufficient. Therefore, in the next step, a chemical such as an acid or an alkali must be added to perform degumming again to reduce the amount of phospholipids in the oil to about 100 ppm or less, and then to perform decolorization and deodorization.
一方、燐脂質自体には、食用、工業用、更には医薬用
として多くの用途があり、品質の良い状態を得ることが
望まれているが、上記の加水法で得られる燐脂質は乾燥
工程での過熱による着色や、薬剤による分解等が懸念さ
れ、品質的には必ずしも十分とはいえないものであっ
た。On the other hand, the phospholipid itself has many uses for food, industrial use, and even pharmaceutical use, and it is desired to obtain a high quality state. However, there was concern about coloring due to overheating and decomposition by chemicals, and the quality was not always sufficient.
脱ガム方法としては、上記の加水法による方法の他、
粗製トリグリセリド油脂をそのまま、あるいは有機溶剤
で希釈して限外濾過膜に接触させる方法がある。これ
は、分子量の小さいトリグリセリド油脂を主体とする画
分を膜透過液として、分子量の大きい燐脂質を主体とす
る画分を不透過液として、それぞれ分離採取するもので
あり、その例としては特開昭50−153010、同52−84206
号公報等を挙げることができる。As the degumming method, in addition to the above-described method using the water method,
There is a method in which the crude triglyceride oil or fat is brought into contact with an ultrafiltration membrane as it is or diluted with an organic solvent. In this method, a fraction mainly composed of triglyceride oils having a low molecular weight is separated and collected as a membrane permeate, and a fraction mainly composed of a phospholipid having a high molecular weight is used as an impermeable liquid. Kaisho 50-153010, 52-84206
And the like.
かかる膜処理法では、上記加水法で述べたような品質
上の懸念の少ない燐脂質が得られるが、その大きな欠点
は、膜通過液量の増加とともに不透過液の粘度が上昇
し、更には膜面に燐脂質が沈着したりして、液の膜透過
速度が急激に低下することであり、本技術分野における
特許出願の多くはこの透過性の改善に関するものであ
る。In such a membrane treatment method, a phospholipid having less quality concerns as described in the above-mentioned water addition method can be obtained, but its major disadvantage is that the viscosity of the impermeable liquid increases with an increase in the amount of liquid passing through the membrane, and furthermore, This is a phenomenon in which phospholipids are deposited on the membrane surface, and the permeation rate of the liquid decreases rapidly. Many patent applications in this technical field relate to the improvement of the permeability.
これらの例としては、２個以上を直列に配した限外濾
過膜に油と溶剤の混合液（以下ミセラと称する）を接触
させる方法において、その連結部の少なくとも一つに溶
剤、ミセラ等を供給して被処理ミセラの粘度、濃度を低
下させる方法（特開昭57−63398）、限外濾過膜にミセ
ラを供給するに際して供給圧力を断続的に中断する方法
（特開昭58−34899）、ミセラ中の粗製トリグリセリド
油脂の含量を１〜30％とし、且つ該ミセラの2/3以下の
濃度の希薄ミセラで膜面を洗浄して膜透過液量を回復さ
せる方法（特開昭58−194995）、膜面を炭素数５〜７の
飽和脂肪族炭化水素、炭素数２又は３の脂肪族１値アル
コール及び炭素数２又は３の脂肪族ケトンから選ばれる
実質的に水を含有しない少なくとも１種の洗浄用有機溶
媒で洗浄して膜透過性を回復させる方法（特開昭58−19
4996）、膜面の洗浄剤として非イオン性界面活性剤を含
む有機溶媒を用いるもの（特開昭59−20394）等があ
る。As an example of these, in a method in which a mixed liquid of oil and a solvent (hereinafter, referred to as a miscella) is brought into contact with an ultrafiltration membrane in which two or more are arranged in series, a solvent, a miscella, etc. A method for lowering the viscosity and concentration of the miscella to be treated by supplying (JP-A-57-63398) and a method for intermittently interrupting the supply pressure when supplying the micelle to the ultrafiltration membrane (JP-A-58-34899) A method in which the content of crude triglyceride fats and oils in the miscella is adjusted to 1 to 30%, and the membrane surface is washed with a dilute miscella having a concentration of 2/3 or less of the miscella to recover the amount of the membrane permeate (Japanese Patent Laid-Open No. 194995), and the film surface is substantially free of water containing at least substantially 5 to 7 carbon atoms selected from saturated aliphatic hydrocarbons, aliphatic monohydric alcohols having 2 or 3 carbon atoms and aliphatic ketones having 2 or 3 carbon atoms. Wash with one kind of washing organic solvent to restore membrane permeability Method (JP-A-58-19
4996) and those using an organic solvent containing a nonionic surfactant as a cleaning agent for the film surface (JP-A-59-20394).
（発明が解決しようとする問題点） 膜処理法の問題点である、低下した膜透過性を回復さ
せる手段としては、上記したように溶剤等の追加による
不透過液の希釈、あるいは新たな溶剤等による膜面の洗
浄が殆どであるが、これらの方法はいずれも多量の溶剤
を必要とし、膜不透過画分が溶剤で希釈されるため、脱
溶剤に余分なエネルギーコストを要する、等の欠点があ
った。(Problems to be Solved by the Invention) As means for restoring the reduced membrane permeability, which is a problem of the membrane treatment method, as described above, dilution of an impermeable liquid by addition of a solvent or the like, or a new solvent is used. Most of these methods require cleaning of the membrane surface, but these methods require a large amount of solvent, and the membrane-impermeable fraction is diluted with the solvent. There were drawbacks.
本発明は、性質の異なった２種の限外濾過膜の特性を
巧みに利用し、不必要に多くの溶剤を用いることなく、
膜による粗製トリグリセリド油脂の効率的な脱ガムを達
せんとするものである。The present invention takes advantage of the properties of two types of ultrafiltration membranes having different properties, without using unnecessarily many solvents,
It is intended to prevent efficient degumming of crude triglyceride fats and oils by a membrane.
（問題点を解決するための手段） 本発明者らは限外濾過膜による粗製トリグリセリド油
脂の脱ガム法につき、詳細な検討を加えるなかで、限外
濾過膜は、その種類により特性が異なり、ポリイミド限
外濾過膜では濃縮倍率（供給ミセラ量／濃縮ミセラ量）
が昂進してミセラ濃度が40〜50重量％に達したり、ミセ
ラ中の水分が増加すると、透過速度（通常、単位面積、
単位時間当たりの通液量「フラックス（/m2・hr）」
で表す）が急激に低下すること、一方ポリエーテルサル
ホン限外濾過膜は濃縮倍率の増加に伴う透過速度の低下
は前者より小さいが、燐脂質の除去性能は前者に劣り、
透過液中に油脂の数100ppmに相当する燐脂質が浸出す
る、等の知見を得た。(Means for Solving the Problems) The present inventors have conducted detailed studies on a method for degumming crude triglyceride fats and oils using an ultrafiltration membrane, and the ultrafiltration membrane has different characteristics depending on its type. Concentration ratio for polyimide ultrafiltration membrane (supply miscella amount / concentrated miscella amount)
When the concentration of miscella reaches 40 to 50% by weight or the water in the miscella increases, the permeation rate (usually, unit area,
Liquid flow rate per unit time “Flux (/ m 2 · hr)”
), On the other hand, the polyethersulfone ultrafiltration membrane has a smaller decrease in the permeation rate with an increase in the concentration ratio than the former, but the phospholipid removal performance is inferior to the former,
It was found that phospholipids equivalent to several hundred ppm of fats and oils leached into the permeate.
本発明は、かかる知見を粗製トリグリセリド油脂の脱
ガムに応用すべく鋭意研究した結果完成したものであ
り、粗製トリグリセリド油脂を有機溶剤で希釈し限外濾
過膜に連続的に供給接触させて燐脂質を除去する油脂の
脱ガム方法において、限外濾過膜として不透過中のトリ
グリセリド濃度が10〜50重量％の範囲ではポリイミド限
外濾過膜を、不透過液中のトリグリセリド濃度が40〜80
重量％の範囲ではポリエーテルサルホン限外濾過液を、
それぞれ組み合わせて使用することを特徴とする。The present invention has been completed as a result of intensive studies to apply such findings to the degumming of crude triglyceride fats and oils. In the method of degumming fats and oils, the polyimide ultrafiltration membrane is used as the ultrafiltration membrane when the triglyceride concentration in the impermeable liquid is in the range of 10 to 50% by weight, and the triglyceride concentration in the impermeable liquid is 40 to 80%.
In the weight percent range, the polyether sulfone ultrafiltrate is
It is characterized by being used in combination with each other.
使用する膜の分画分子量は、ポリイミド系では10,000
〜100,000、より好ましくは20,000〜40,000、ポリエー
テルサルホン系では10,000〜200,000、より好ましくは4
0,100,000が、それぞれ適当である。これらの具体的な
例としては、前者では日当等電気工業（株）製NTU−422
0、後者ではダイヤル化学工業（株）製DUS−40、それぞ
れ挙げることができる。The molecular weight cutoff of the membrane used is 10,000 for polyimide
~ 100,000, more preferably 20,000 ~ 40,000, and for polyethersulfones, 10,000 ~ 200,000, more preferably 4
0,100,000 is each suitable. As a specific example of these, in the former, NTU-422 manufactured by Nichido Electric Industry Co., Ltd.
0 and the latter include DUS-40 manufactured by Dial Chemical Industry Co., Ltd., respectively.
本発明が適用できる粗製トリグリセリド油脂として
は、例えば、大豆、なたね、とうもろこし、綿実、ヒマ
ワリ、サフラワー、ゴマ等の油糧種子から圧搾、溶剤抽
出等の手段によって採取されたものを挙げることができ
る。また、これらの希釈する有機溶剤としては分子量50
〜200の炭化水素、低級脂肪酸エステル、脂肪族ケト
ン、またはこれらの混合物を挙げることができるが、通
常ヘキサンが好ましい。なお、粗製トリグリセリド油脂
の取得方法として溶剤抽出法を採用した場合には、脱溶
剤前のミセラをそのまま膜処理に供することができる。Examples of the crude triglyceride fats and oils to which the present invention can be applied include those collected from oil seeds such as soybeans, rapeseed, corn, cottonseed, sunflower, safflower, and sesame by pressing, solvent extraction, and the like. Can be. In addition, these organic solvents to be diluted have a molecular weight of 50
200200 hydrocarbons, lower fatty acid esters, aliphatic ketones, or mixtures thereof, but hexane is usually preferred. When a solvent extraction method is employed as a method for obtaining crude triglyceride fats and oils, miscella before solvent removal can be directly subjected to membrane treatment.
本発明では、粗製トリグリセリド油脂の有機溶剤溶液
（所謂、ミセラ）中の原油の濃度が10〜40重量％、より
好ましくは25〜35重量％となるよう調整し、これを膜処
理に供する。In the present invention, the concentration of crude oil in an organic solvent solution of crude triglyceride fat (so-called miscella) is adjusted to 10 to 40% by weight, more preferably 25 to 35% by weight, and is subjected to membrane treatment.
本発明の実施に当たっては、前記２種類の限外濾過
膜、限外濾過膜へミセラを圧送循環するためのポンプ、
配管及びタンク、並びに限外濾過膜の供給先を切り替え
るためのバルブ等を備えた設備を用いる。ミセラはまず
ポリイミド限外濾過膜とタンクの間を循環しつつ加圧下
で該限外濾過膜と接触させ、膜を通過しない循環液中に
燐脂質を濃縮し、一方、燐脂質が除去されたミセラを透
過液として得る。このようにしてポリイミド限外濾過膜
との循環接触を続け、循環液中のトリグリセリド成分の
濃度が40〜60重量％に到達した時点で、供給先をポリエ
ーテルサルホン限外濾過膜に切り替え、前記同様に循環
を継続する。ポリエーテルサルホン膜への循環接触は、
循環液中のトリグリセリド成分の濃度が70〜80重量％程
度に達するまで行う。In carrying out the present invention, the two types of ultrafiltration membranes, a pump for pumping and circulating the miscella to the ultrafiltration membrane,
Equipment equipped with a pipe, a tank, and a valve for switching the supply destination of the ultrafiltration membrane is used. Misera first contacted the ultrafiltration membrane under pressure while circulating between the polyimide ultrafiltration membrane and the tank, and concentrated the phospholipids in the circulating fluid that did not pass through the membrane, while the phospholipids were removed Misera is obtained as permeate. In this way, the circulating contact with the polyimide ultrafiltration membrane is continued, and when the concentration of the triglyceride component in the circulating liquid reaches 40 to 60% by weight, the supply destination is switched to the polyethersulfone ultrafiltration membrane, The circulation is continued as described above. The circulating contact with the polyethersulfone membrane is
The process is performed until the concentration of the triglyceride component in the circulating fluid reaches about 70 to 80% by weight.
ポリイミド限外濾過膜への循環接触を、循環液中のト
リグリセリド成分濃度が40〜60重量％に到達するまでの
限定したのは、この範囲を超えるとポリイミド膜の透過
速度が急激に低下するためである。上記膜処理時の温
度、圧力等の諸条件は、いずれも循環液の粘度、溶剤の
種類、限外濾過膜の耐熱・耐久性、等を勘案して決定さ
れるべきであるが、通常、処理温度は０〜70、より好ま
しくは40〜60℃、接触圧力は２〜50、より好ましくは３
〜20kg/cm2が、それぞれ適当である。The reason for limiting the circulating contact to the polyimide ultrafiltration membrane until the triglyceride component concentration in the circulating fluid reaches 40 to 60% by weight is that if it exceeds this range, the permeation rate of the polyimide membrane will decrease rapidly. It is. Various conditions such as temperature and pressure during the membrane treatment should be determined in consideration of the viscosity of the circulating fluid, the type of solvent, the heat resistance and durability of the ultrafiltration membrane, etc. The treatment temperature is 0 to 70, more preferably 40 to 60 ° C, and the contact pressure is 2 to 50, more preferably 3
~ 20 kg / cm 2 is appropriate respectively.
上記の膜透過液からは、これを脱溶剤することにより
燐脂質含量が100ppm程度以下の脱ガム油が得られ、以降
常法による脱色、脱臭処理を施して高品位の精製油脂を
取得することができる。From the above-mentioned membrane permeate, a degummed oil having a phospholipid content of about 100 ppm or less can be obtained by removing the solvent to obtain a high-quality refined oil and fat by performing decolorization and deodorization treatment by a conventional method. Can be.
一方、燐脂質が濃縮された膜不透過の循環液からは、
これを脱溶剤することにより高純度、かつ淡色の品質の
良好なレシチンを得ることができる。On the other hand, from the membrane-impermeable circulating fluid in which phospholipids are concentrated,
By removing this solvent, lecithin of high purity and good quality of light color can be obtained.
以下に実施例及び比較例を示す。 Examples and comparative examples are shown below.
（実施例） 実施例１ ヘキサンを溶剤とする抽出法により大豆から得られた
ミセラ（トリグリセリド濃度30％、油中の燐脂質濃度1.
4％）を、日東電気工業（株）製NTU−4220（ポリイミド
限外濾過膜 分画分子量20,000）及びダイセル化学工業
（株）製DUS−40（ポリエーテルサルホン限外濾過膜分
画分子量40,000）を用いて処理した。(Example) Example 1 Misera (triglyceride concentration 30%, phospholipid concentration in oil 1.) obtained from soybean by extraction method using hexane as a solvent.
4%) by NTU-4220 (polyamide ultrafiltration membrane fractionation molecular weight 20,000) manufactured by Nitto Electric Industries, Ltd. and DUS-40 (polyether sulfone ultrafiltration membrane fractionation molecular weight: 40,000) manufactured by Daicel Chemical Industries, Ltd. ).
ミセラは、まずNTU−4220モジュール（平板型 膜面
積1.86m2）に圧力4kg/cm2、温度50℃で供給、循環接触
させた。循環液中のトリグリセリド濃度が50重量％に達
した時点で通液先をDUS−40モジュール（集合管状型
膜面積2.0m2）に切り替え、循環液中のトリグリセリド
濃度が70重量％になるまで、上記と同一条件で循環を継
続した。The miscella was first supplied to an NTU-4220 module (flat plate membrane area 1.86 m 2 ) at a pressure of 4 kg / cm 2 at a temperature of 50 ° C. and brought into circulating contact. When the triglyceride concentration in the circulating fluid reaches 50% by weight, the liquid is passed through the DUS-40 module (collective tubular type).
The membrane area was changed to 2.0 m 2 ), and the circulation was continued under the same conditions as above until the triglyceride concentration in the circulating fluid became 70% by weight.
処理過程での循環液中の各トリグリセリド濃度（重量
％）における、透過速下（/m2・時）及び膜透過ミセ
ラの油脂中の燐脂質含量、並びに膜透過性および不透過
性の各画分を脱溶剤して得た脱ガム油およびレシチンの
品質を表１にまとめた。Phospholipid content in permeation speed (/ m 2 · h) and oil and fat of membrane permeable micelle, and membrane permeability and impermeability at each triglyceride concentration (wt%) in circulating fluid during treatment Table 1 summarizes the quality of degummed oil and lecithin obtained by desolvation.
得られた膜透過液を合して脱溶剤して得た脱ガム油の
品質は表１に示すとおりであり、この脱ガム油を常法に
より脱色（活性白土使用量0.5％、105℃、15分）、脱臭
（250℃、2mmHg、45分）したところ、色相4.0Y＋0.3R
（ロビボンド比色計133.4mmセル使用）、酸価0.05、燐
脂質含量11ppmと品質の良好な精製油が得られた。 The quality of the degummed oil obtained by combining the obtained membrane permeated liquids and desolvating is shown in Table 1. The degummed oil is decolorized by a conventional method (active clay usage 0.5%, 105 ° C, 15 minutes), deodorized (250 ° C, 2mmHg, 45 minutes) gives a hue of 4.0Y + 0.3R
(Use of a 133.4 mm cell with a Lovibond colorimeter), an acid value of 0.05, and a phospholipid content of 11 ppm gave a high-quality refined oil.
一方、膜不透過の循環液を脱溶剤して得たレシチン
は、表１に示すとおり淡色で純度が高い、高品位のもの
であった。On the other hand, as shown in Table 1, lecithin obtained by removing the solvent from the circulating liquid impermeable to the membrane was light-colored, high in purity, and of high quality.
（比較例１及び２） 比較のため、上記と同一のNTU−4220及びDUS−40膜モ
ジュール各２セットを用意し、そのうちの各１つに上記
と同じミセラを供給、循環接触させた（いずれも圧力6k
g/cm2、温度50℃）。循環液中の原油濃度が50重量％に
達した時点で、通液先をそれぞれ同種の新しい膜モジュ
ールに変え、循環液中の原油濃度が70重量％になるまで
循環を続けた。(Comparative Examples 1 and 2) For comparison, two sets each of the same NTU-4220 and DUS-40 membrane modules as described above were prepared, and one of them was supplied with the same miscella as described above and brought into circulating contact. Also pressure 6k
g / cm 2 , temperature 50 ° C). When the crude oil concentration in the circulating fluid reached 50% by weight, the flow destination was changed to a new membrane module of the same type, and circulation was continued until the crude oil concentration in the circulating fluid reached 70% by weight.
両膜での各濃度段階における透過液速度と透過液油中
の燐脂質含量、並びに合した透過液及び不透過液を脱溶
剤して得た脱ガム油及びレシチンの品質について表２に
まとめた。Table 2 summarizes the permeate speed and the phospholipid content in the permeate oil at each concentration step in both membranes, and the quality of degummed oil and lecithin obtained by desolvating the combined permeate and non-permeate. .
表２に見られるように、ポリイミド限外濾過膜及びポ
リエーテルサルホン限外濾過膜を、それぞれ単独で使用
する場合、前者ではミセラの濃縮に伴う透過液速度の減
少が顕著であり、これを回復させるためには途中でヘキ
サン等の適当な溶剤による希釈または膜の洗浄が必要で
ある、また、後者では透過液速度の落ち込みは比較的小
さいものの、燐脂質の除去が不十分なため、常法の脱
色、脱臭工程に先立ち、アルカリ剤等を用いた更なる脱
ガムを経なければ食品用として品質に問題のない精製油
を得ることができない、等の問題点があることが明らか
となった。 As seen in Table 2, when the polyimide ultrafiltration membrane and the polyethersulfone ultrafiltration membrane are used alone, the former has a remarkable decrease in the permeate speed due to the concentration of the miscella in the former. For recovery, dilution with an appropriate solvent such as hexane or washing of the membrane is required on the way.Also, in the latter, although the drop in permeate speed is relatively small, the removal of phospholipids is insufficient, so Prior to the decolorization and deodorization steps of the method, it is clear that there is a problem that a purified oil having no problem in quality can be obtained for food without further degumming using an alkali agent or the like. Was.
（発明の効果） 本発明方法により、ポリイミド系限外濾過膜とポリエ
ーテルサルホン系限外濾過膜とを組み合わせることによ
って、高い作業効率を保持しながらの粗製トリグリセリ
ドの有機溶媒溶液の膜による脱ガムが可能となった。本
発明法により得られた脱ガム油は、その後常法による脱
色、脱臭処理を行うことによって、食用あるいは工業用
途に好適な品質の良好な精製油を得ることができる。一
方、膜不透過液からは、これを脱溶剤することによって
淡色で高純度のレシチンを得ることができる。(Effects of the Invention) By combining a polyimide-based ultrafiltration membrane and a polyethersulfone-based ultrafiltration membrane according to the method of the present invention, it is possible to remove a crude triglyceride from an organic solvent solution by a membrane while maintaining high working efficiency. Gum is now possible. The degummed oil obtained by the method of the present invention is then subjected to decolorization and deodorization treatment by a conventional method, whereby a refined oil of good quality suitable for edible or industrial use can be obtained. On the other hand, light-colored and high-purity lecithin can be obtained from the membrane impermeable liquid by removing the solvent.
Claims (1)
し限外濾過膜に循環、接触させて燐脂質を除去する油脂
の脱ガム方法において、トリグリセリド濃度10〜40重量
％の粗製トリグリセリド油脂の有機溶媒溶液を処理温度
０〜70℃、接触圧力２〜50kg/cm2の条件下において分画
分子量10,000〜100,000のポリイミド系限外濾過膜で膜
処理をし、トリグリセリド濃度を40〜60重量％に到達さ
せた後、分画分子量10,000〜200,000のポリエーテルサ
ルホン系限外濾過膜で膜処理して濃度60重量％以上のト
リグリセリド油脂を取得する油脂の脱ガム方法。1. A method for degumming fats and oils wherein crude triglyceride fats and oils are diluted with an organic solvent and circulated and contacted with an ultrafiltration membrane to remove phospholipids. The solution is treated with a polyimide ultrafiltration membrane having a molecular weight cut-off of 10,000 to 100,000 under the conditions of a treatment temperature of 0 to 70 ° C. and a contact pressure of 2 to 50 kg / cm 2 to reach a triglyceride concentration of 40 to 60% by weight. A method for degumming fats and oils in which a triglyceride fat having a concentration of 60% by weight or more is obtained by treating the membrane with a polyethersulfone-based ultrafiltration membrane having a cut-off molecular weight of 10,000 to 200,000.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63308882A JP2709730B2 (en) | 1988-12-08 | 1988-12-08 | Degumming method for fats and oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63308882A JP2709730B2 (en) | 1988-12-08 | 1988-12-08 | Degumming method for fats and oils |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02155989A JPH02155989A (en) | 1990-06-15 |
| JP2709730B2 true JP2709730B2 (en) | 1998-02-04 |
Family
ID=17986397
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63308882A Expired - Fee Related JP2709730B2 (en) | 1988-12-08 | 1988-12-08 | Degumming method for fats and oils |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2709730B2 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6140519A (en) * | 1998-12-07 | 2000-10-31 | Archer-Daniels-Midland Company | Process for producing deoiled phosphatides |
| 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 |
| WO2002034062A1 (en) * | 2000-10-27 | 2002-05-02 | Nv Marc Boone | Method for obtaining products enriched in phospho- and sphingolipids |
| JP5143067B2 (en) * | 2009-03-27 | 2013-02-13 | 日清オイリオグループ株式会社 | Method for producing edible oil and fat and edible oil and fat obtained therefrom |
| SG11201402192WA (en) * | 2011-11-09 | 2014-06-27 | Evonik Membrane Extraction Technology Ltd | Membrane-based processes for reducing at least one impurity and making a concentrate comprising at least one natural component from a non-marine fatty acid oil mixture, and compositions resulting thereof |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5763398A (en) * | 1980-10-03 | 1982-04-16 | Nisshin Oil Mills Ltd | Treatment of oil and fat |
| JPS58198597A (en) * | 1982-05-16 | 1983-11-18 | 日東電工株式会社 | Purification of crude glyceride oil composition |
-
1988
- 1988-12-08 JP JP63308882A patent/JP2709730B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02155989A (en) | 1990-06-15 |
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