JPH02155989A - Technique for degumming of oil or fat - Google Patents
Technique for degumming of oil or fatInfo
- Publication number
- JPH02155989A JPH02155989A JP30888288A JP30888288A JPH02155989A JP H02155989 A JPH02155989 A JP H02155989A JP 30888288 A JP30888288 A JP 30888288A JP 30888288 A JP30888288 A JP 30888288A JP H02155989 A JPH02155989 A JP H02155989A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- oil
- solvent
- solution
- triglyceride
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000012528 membrane Substances 0.000 claims abstract description 71
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 35
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 claims abstract description 30
- 150000003904 phospholipids Chemical class 0.000 claims abstract description 25
- 239000004642 Polyimide Substances 0.000 claims abstract description 12
- 229920001721 polyimide Polymers 0.000 claims abstract description 12
- 239000004695 Polyether sulfone Substances 0.000 claims abstract description 10
- 239000003960 organic solvent Substances 0.000 claims abstract description 10
- 229920006393 polyether sulfone Polymers 0.000 claims abstract description 10
- 239000003921 oil Substances 0.000 claims description 32
- 239000003925 fat Substances 0.000 claims description 20
- 239000012530 fluid Substances 0.000 claims description 13
- 239000002904 solvent Substances 0.000 abstract description 21
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 abstract description 12
- IIZPXYDJLKNOIY-JXPKJXOSSA-N 1-palmitoyl-2-arachidonoyl-sn-glycero-3-phosphocholine Chemical compound CCCCCCCCCCCCCCCC(=O)OC[C@H](COP([O-])(=O)OCC[N+](C)(C)C)OC(=O)CCC\C=C/C\C=C/C\C=C/C\C=C/CCCCC IIZPXYDJLKNOIY-JXPKJXOSSA-N 0.000 abstract description 5
- 235000010445 lecithin Nutrition 0.000 abstract description 5
- 239000000787 lecithin Substances 0.000 abstract description 5
- 229940067606 lecithin Drugs 0.000 abstract description 5
- 238000005194 fractionation Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 235000019198 oils Nutrition 0.000 description 29
- 235000019197 fats Nutrition 0.000 description 16
- 239000012466 permeate Substances 0.000 description 12
- 239000007788 liquid Substances 0.000 description 11
- 238000011282 treatment Methods 0.000 description 9
- 238000004042 decolorization Methods 0.000 description 5
- 238000004332 deodorization Methods 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 230000035699 permeability Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- -1 aliphatic ketones Chemical class 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 238000007865 diluting Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 244000068988 Glycine max Species 0.000 description 2
- 235000010469 Glycine max Nutrition 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000012465 retentate Substances 0.000 description 2
- 240000002791 Brassica napus Species 0.000 description 1
- 235000004977 Brassica sinapistrum Nutrition 0.000 description 1
- 244000020518 Carthamus tinctorius Species 0.000 description 1
- 235000003255 Carthamus tinctorius Nutrition 0.000 description 1
- 244000020551 Helianthus annuus Species 0.000 description 1
- 235000003222 Helianthus annuus Nutrition 0.000 description 1
- 241000166636 Hemiceras Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 244000000231 Sesamum indicum Species 0.000 description 1
- 235000003434 Sesamum indicum Nutrition 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000010775 animal oil Substances 0.000 description 1
- AIXAANGOTKPUOY-UHFFFAOYSA-N carbachol Chemical compound [Cl-].C[N+](C)(C)CCOC(N)=O AIXAANGOTKPUOY-UHFFFAOYSA-N 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000001877 deodorizing effect Effects 0.000 description 1
- 238000004807 desolvation Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 238000002845 discoloration Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 108010030727 lens intermediate filament proteins Proteins 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002736 nonionic surfactant Substances 0.000 description 1
- 235000014593 oils and fats Nutrition 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 150000003626 triacylglycerols Chemical class 0.000 description 1
- 235000015112 vegetable and seed oil Nutrition 0.000 description 1
- 235000019871 vegetable fat Nutrition 0.000 description 1
- 239000008158 vegetable oil Substances 0.000 description 1
Abstract
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。DETAILED DESCRIPTION OF THE INVENTION (Industrial Field of Application) 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 from oilseeds and other animal and vegetable oils and fats by squeezing, solvent extraction, etc. usually contain impurities such as phospholipids, and these are not suitable for food or industrial use. Because it causes various inconveniences when used for
Before it can be made into a final product, it is necessary to perform purification treatments such as degumming, deacidification, decolorization, and deodorization to remove impurities.
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。Conventionally, phospholipids were hydrated and insolubilized by adding water and stirring to crude triglyceride fats in a process called degumming, which is generally performed at the beginning of fat and oil refining, and removed by means such as centrifugation. .
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
Ｉ ＯＯｐｐｍ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。However, this method still contains 0.2
Approximately 0.5% of phospholipids remain, and the removal rate cannot be said to be sufficient. Therefore, in the next step, it was necessary to add a chemical such as an acid or an alkali, degum the oil again, reduce the phospholipids in the oil to less than IOOppm, and then 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、品質の良い状態で得ることが望
まれているが、上記の加水法で得られろ燐脂質は乾燥工
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, phospholipids themselves have many uses for food, industry, and even medicine, and it is desirable to obtain them in a high-quality state. There were concerns about discoloration due to overheating during the process, decomposition due to chemicals, etc., and the quality was not necessarily 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両分を
膜透過液として、分子量の大きい燐脂質を主体とする両
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。Degumming methods include, in addition to the above-mentioned hydrolysis method, a method in which the crude triglyceride oil is brought into contact with an ultrafiltration membrane either as it is or after being diluted with an organic solvent. this is,
Both components, mainly triglyceride fats and oils with a small molecular weight, are separated and collected as a membrane-permeable liquid, and both components, which are mainly composed of phospholipids with a large molecular weight, are separated and collected as an impermeable liquid. -153010, 52-
Publication No. 84206 can be mentioned.
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。Although this membrane treatment method yields phospholipids with fewer quality concerns as mentioned in the above-mentioned hydrolysis method, its major drawback is that the viscosity of the non-permeable liquid increases as the amount of liquid passing through the membrane increases;
Furthermore, phospholipids are deposited on the membrane surface, which causes a rapid decrease in the membrane permeation rate of liquid, and many patent applications in this technical field are concerned with improving this 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５Ｅ１３４８９９）、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５８１９４９９５）、
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価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５１１１９４９９６）、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。Examples of these include a method in which a mixture of oil and solvent (hereinafter referred to as micellar) is brought into contact with ultrafiltration membranes in which two or more ultrafiltration membranes are arranged in series, and at least one of the connecting parts is coated with a solvent, micellar, etc. A method of supplying micella to reduce the viscosity and concentration of micella to be treated (JP 57-63398), a method of intermittently interrupting the supply pressure when feeding micella to an ultrafiltration membrane (JP 5E134899), A method in which the content of crude triglyceride oil and fat in the membrane is 1 to 30%, and the membrane surface is washed with dilute micella at a concentration of 2/3 or less of the micella to recover the amount of membrane permeate (Japanese Patent Application Laid-Open No. 58194995);
The membrane surface is coated with at least one substantially water-free material selected from saturated aliphatic hydrocarbons having 5 to 7 carbon atoms, aliphatic monohydric alcohols having 2 or 3 carbon atoms, and aliphatic ketones having 2 or 3 carbon atoms. A method of restoring membrane permeability by cleaning with an organic solvent for cleaning (Japanese Patent Laid-Open No. 511194996), a method using an organic solvent containing a nonionic surfactant as a cleaning agent for the membrane surface (Japanese Patent Laid-Open No. 59-20394), etc. There is.
（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 a means of recovering the reduced membrane permeability, which is a problem in the membrane treatment method, as mentioned above, diluting the impermeable liquid by adding a solvent or the like, or using a new solvent. However, these methods all require a large amount of solvent, and since the membrane-impermeable fraction is diluted with the solvent, desolvation requires extra energy cost, etc. 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 skillfully utilizes the characteristics of two types of ultrafiltration membranes with different properties, and attempts to achieve efficient degumming of crude triglyceride fats and oils by the membrane without using an unnecessary large amount of solvent. It is something.
（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（供給ミセラ儀／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（Ｑ／１・ｈｒ
）ｊ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１００ ｐｐｍ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 conducted a detailed study on the method of degumming crude triglyceride fats and oils using ultrafiltration membranes, and found that ultrafiltration membranes have different characteristics depending on their type. With polyimide ultrafiltration membranes, when the concentration ratio (supplied micella/concentrated micellar amount) increases and the micellar concentration reaches 40 to 50% by weight, or when the water content in the micella increases, the permeation rate (usually unit area, unit Amount of liquid passed per hour [flux (Q/1・hr
)) (represented by j) sharply decreases.On the other hand, with polyethersulfone ultrafiltration membranes, the decrease in permeation rate as the concentration ratio increases is smaller than the former, but the phospholipid removal performance is inferior to the former, and the permeate It was found that phospholipids equivalent to several hundred ppm of fats and oils were leached into the water.
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媒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液中のトリグ
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重徂％の範囲ではポリエーテルザルホン限外濾過
膜を、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 was completed as a result of intensive research to apply this knowledge to the degumming of crude triglyceride fats and oils.
In a fat and oil degumming method in which phospholipids are removed by diluting crude triglyceride fat with an organic solvent and continuously supplying the diluted fat and oil to an ultrafiltration membrane to remove phospholipids, the triglyceride concentration in the retentate as an ultrafiltration membrane is 10 to 50% by weight. % range, polyimide ultrafiltration membrane is used when the triglyceride concentration in the retentate is 40%.
In the range of 80% by weight, polyethersulfone ultrafiltration membranes are used in combination.
使用する膜の分画分子量は、ポリイミド系では１０．０
００〜１００，０００、より好ましくは２ｏ、ｏｏｏ〜
４０，０００、ポリエーテルサルホン系では１０，００
０〜２００，０００、より好ましくは４０，０００〜１
００，０００が、それぞれ適当である。これらの具体的
な例としては、前者では日東電気工業（株）製ＮＴＵ−
４２２０、後者ではダイセル化学工業（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 10.0 for polyimide-based membranes.
00 to 100,000, more preferably 2o, ooo to
40,000, 10,000 for polyether sulfone type
0-200,000, more preferably 40,000-1
00,000 are appropriate. As a specific example of these, in the former case, NTU-
4220, and the latter is DUS- manufactured by Daicel Chemical Industries, Ltd.
40, each can be mentioned.
本発明法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、これらを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 crude triglyceride fats and oils to which the method of the present invention can be applied include those collected from oil seeds such as soybeans, rapeseed, corn, cottonseed, sunflower, safflower, and sesame by means such as compression and solvent extraction. Can be done. In addition, as an organic solvent for diluting these, the molecular weight is 50.
~200 hydrocarbons, lower fatty acid esters, aliphatic ketones, or mixtures thereof, although hexane is usually preferred. In addition, when a solvent extraction method is employed as a method for obtaining crude triglyceride fats and oils, micella 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）中の原論の濃度が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, an organic solvent solution of crude triglyceride oil (
The concentration of the so-called micella is adjusted to 10 to 40% by weight, more preferably 25 to 35% by weight, and then 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、
限外濾過膜ヘ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 implementing the present invention, the above two types of ultrafiltration membranes,
Equipment equipped with a pump, piping, and a tank for pumping and circulating the ultrafiltration membrane Hemicera, and a valve for switching the supply destination of the ultrafiltration membrane is used. Micella was first circulated between a polyimide ultrafiltration membrane and a tank and brought into contact with the ultrafiltration membrane under pressure to concentrate phospholipids in the circulating fluid that did not pass through the membrane, while the phospholipids were removed. Micella 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 fluid reaches 40 to 60% by weight, the supply destination is switched to the polyethersulfone ultrafiltration membrane, Continue circulation as before. Cyclic contact with the polyethersulfone membrane is
This is carried out until the concentration of the triglyceride component in the circulating fluid reaches approximately 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
と限定したのは、この範囲を超えろ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θ〜７０．より好
ましくは４０〜６０℃、接触圧力は２〜５０、より好ま
しくは３〜２０ ｋｇ７ｃｍ”か、それぞれ適当である
。The reason why circulating contact with the polyimide ultrafiltration membrane was limited to until the concentration of triglyceride components in the circulating fluid reached 40 to 60% by weight was because the permeation rate of the polyimide membrane would drop sharply if this range was exceeded. It is. The various conditions such as temperature and pressure during the above membrane treatment should be determined by taking into consideration the viscosity of the circulating fluid, the type of solvent, the heat resistance and durability of the ultrafiltration membrane, etc. The processing temperature is θ~70. The contact pressure is more preferably 40 to 60°C, and the contact pressure is 2 to 50°C, more preferably 3 to 20kg7cm'', as appropriate.
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１００ ｐｐ＋ｍ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。By removing the solvent from the above membrane permeate, a degummed oil with a phospholipid content of about 100 pp+m or less is obtained, which is then subjected to decolorization and deodorization treatment by conventional methods to obtain high-grade refined oils and fats. be able to.
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, by removing the solvent from the membrane-impermeable circulating fluid enriched with phospholipids, it is possible to obtain high-purity, light-colored lecithin of good quality.
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！
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
１４％）を、日東電気工業（株）製ＮＴＯ−４２２０（
ポリイミド限外濾過膜 分画分子ｆｆ１２０，０００）
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万両分子ｆｆ１４０，０００）
を用いて処理した。(Example) Example! Micella (triglyceride concentration 30%, phospholipid concentration in oil 14%) obtained from soybeans by an extraction method using hexane as a solvent was extracted with NTO-4220 (manufactured by Nitto Denki Kogyo Co., Ltd.).
Polyimide ultrafiltration membrane fractionation molecules ff120,000)
and DUS-40 manufactured by Daicel Chemical Industries, Ltd. (polyether sulfone ultrafiltration membrane ten thousand molecules ff140,000)
was processed using
ミセラは、まずＮＴＵ−４２２０モジユール（平板型
膜面積１．８６１’）に圧力４ ｋｇ／ｃｍ”、温度５
０℃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光をＤＯＳ−４
０モジユール（集合管状型 膜面積２．Ｏ１２）に切り
替え、循環液中のトリグリセリド濃度が７０重１％にな
るまで、上記と同一条件て循環を継続した。First of all, Micera was manufactured using the NTU-4220 module (flat plate type).
Membrane area 1.861'), pressure 4 kg/cm", temperature 5
The mixture was supplied at 0°C and circulated in contact. When the triglyceride concentration in the circulating fluid reaches 50% by weight, the liquid passing light is switched to DOS-4.
0 module (collecting tubular type, membrane area 2.012), and circulation was continued under the same conditions as above until the triglyceride concentration in the circulating fluid reached 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、透過速度（Ｃ／Ｉ”・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
性の各両分を脱溶剤して得た脱ガム４１１およびレシチ
ンの品質を表１にまとめた。Concentration of each triglyceride in the circulating fluid during the treatment process (wt%)
), the permeation rate (C/I''・hr) and the phospholipid content in the oil and fat of membrane-permeable micella, as well as the membrane permeability and impermeability of degummed 411 and lecithin obtained by solvent removal. The quality is summarized in Table 1.
（以下余白）
表１
実施例
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ｆｆ１０．５％、１０５℃、１５
分）、脱臭（２５０℃、２１肩Ｈｇ。(The following is a blank space) Table 1 The quality of the degummed oil obtained by combining the membrane permeate obtained in the example and removing the solvent is as shown in Table 1. Used ff10.5%, 105℃, 15
minutes), deodorization (250°C, 21 shoulder Hg).
４５分）したところ、色相４．ＯＹ ＋ ０．３
Ｒ（ロビボンド比色計１３３．４ｘｍセル使用）、酸価
０．０５、燐脂質含量１１ ｐｐｍと品質の良好な精製
油が得られた。45 minutes), the hue was 4. OY+0.3
A refined oil of good quality was obtained, with an acid value of 0.05 and a phospholipid content of 11 ppm.
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, lecithin obtained by removing solvent from membrane-impermeable circulating fluid is
As shown in Table 1, it was light in color, highly pure, 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ＤＯＳ
−４０膜モジユール各２セツトを用意し、そのうちの各
１う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６ ｋｇ７ｃｍ”ＳＩＡ度５０℃）。循環液中
の原油濃度が５０重爪形に達した時点で、通液光をそれ
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, the same NTU-4220 and DOS as above
Two sets of -40 membrane modules were prepared, and one of them was supplied with the same miscella as above and brought into circulation contact (both at a pressure of 6 kg and 7 cm, SIA degree of 50°C).When the crude oil concentration in the circulating fluid was 50. When the shape was reached, the liquid passing light was changed to a new membrane module of the same type, and circulation was continued until the crude oil concentration in the circulating liquid 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 velocity and phospholipid content in the permeate oil at each concentration stage in both membranes, as well as the quality of the degummed oil and lecithin obtained by removing the solvent from the combined permeate and non-permeate liquid. .
（以下余白）
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ａ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。(Left below) As shown in Table 2, when polyimide ultrafiltration membranes and polyethersulfone ultrafiltration membranes are used alone, the permeate velocity decreases significantly due to a-condensation of miscella. In order to recover this, it is necessary to dilute with an appropriate solvent such as hexane or wash the membrane during the process.Also, in the latter case, although the drop in the permeate rate is relatively small, the removal of phospholipids is insufficient. For sufficient, conventional decolorization,
It has become clear that, prior to the deodorizing step, there are problems such as the fact that it is not possible to obtain refined oil of good quality for food use without further degumming using an alkaline agent or the like.
（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、膜下透過液からは、これを脱溶剤することによって
淡色で高純度のレンチンを得ることができる。(Effect of the invention) By combining a polyimide-based ultrafiltration membrane and a polyethersulfone-based ultrafiltration membrane, the method of the present invention allows for the membrane-based removal of organic solvent solutions of crude triglycerides while maintaining high work efficiency. Gum is now available. The degummed oil obtained by the method of the present invention is then subjected to decolorization and deodorization treatment by conventional methods to obtain a refined oil of good quality suitable for food or industrial use. On the other hand, light-colored and highly pure lentin can be obtained from the submembrane permeate by removing the solvent.
Claims (1)
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、限外濾過膜として循環液中のトリグリセリ
ド濃度が１０〜５０重量％の範囲ではポリイミド系限外
濾過膜に、循環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系限外濾過膜に
、それぞれ接触させることを特徴とする油脂の脱ガム方
法。In a fat and oil degumming method in which crude triglyceride fats and oils are diluted with an organic solvent and circulated and brought into contact with an ultrafiltration membrane to remove phospholipids, the triglyceride concentration in the circulating fluid as an ultrafiltration membrane is in the range of 10 to 50% by weight. In this case, the polyimide ultrafiltration membrane has a triglyceride concentration of 40 to 80 in the circulating fluid.
A method for degumming fats and oils, which comprises contacting polyethersulfone ultrafiltration membranes in a range of weight percent.
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 true JPH02155989A (en) | 1990-06-15 |
| JP2709730B2 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) |
Cited By (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 |
| WO2002034062A1 (en) * | 2000-10-27 | 2002-05-02 | Nv Marc Boone | Method for obtaining products enriched in phospho- and sphingolipids |
| 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 |
| JP2010227039A (en) * | 2009-03-27 | 2010-10-14 | Nisshin Oillio Group Ltd | Method for producing edible oil and fat, and edible oil and fat obtained by the method |
| JP2015501851A (en) * | 2011-11-09 | 2015-01-19 | エボニック メンブレイン イクストラクション テクノロジー リミテッドＥｖｏｎｉｋ Ｍｅｍｂｒａｎｅ Ｅｘｔｒａｃｔｉｏｎ Ｔｅｃｈｎｏｌｏｇｙ Ｌｔｄ． | Membrane-based method and composition resulting therefrom for producing a concentrate comprising a non-marine fatty acid oil mixture for reducing at least one impurity and comprising at least one natural ingredient |
Citations (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
Patent Citations (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 |
Cited By (8)
| 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 |
| 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 |
| WO2002034062A1 (en) * | 2000-10-27 | 2002-05-02 | Nv Marc Boone | Method for obtaining products enriched in phospho- and sphingolipids |
| JP2010227039A (en) * | 2009-03-27 | 2010-10-14 | Nisshin Oillio Group Ltd | Method for producing edible oil and fat, and edible oil and fat obtained by the method |
| JP2015501851A (en) * | 2011-11-09 | 2015-01-19 | エボニック メンブレイン イクストラクション テクノロジー リミテッドＥｖｏｎｉｋ Ｍｅｍｂｒａｎｅ Ｅｘｔｒａｃｔｉｏｎ Ｔｅｃｈｎｏｌｏｇｙ Ｌｔｄ． | Membrane-based method and composition resulting therefrom for producing a concentrate comprising a non-marine fatty acid oil mixture for reducing at least one impurity and comprising at least one natural ingredient |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2709730B2 (en) | 1998-02-04 |
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