JPH04183795A - Purification of fatty oil - Google Patents
Purification of fatty oilInfo
- Publication number
- JPH04183795A JPH04183795A JP2308841A JP30884190A JPH04183795A JP H04183795 A JPH04183795 A JP H04183795A JP 2308841 A JP2308841 A JP 2308841A JP 30884190 A JP30884190 A JP 30884190A JP H04183795 A JPH04183795 A JP H04183795A
- Authority
- JP
- Japan
- Prior art keywords
- ultrafiltration membrane
- solvent extraction
- oils
- fine particles
- fats
- 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
- 238000000746 purification Methods 0.000 title abstract description 5
- 239000010685 fatty oil Substances 0.000 title abstract 3
- 239000012528 membrane Substances 0.000 claims abstract description 43
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 21
- 239000010419 fine particle Substances 0.000 claims abstract description 18
- 238000000638 solvent extraction Methods 0.000 claims abstract description 10
- 238000001471 micro-filtration Methods 0.000 claims abstract description 9
- 150000003904 phospholipids Chemical class 0.000 claims abstract description 7
- 239000003925 fat Substances 0.000 claims description 21
- 239000003921 oil Substances 0.000 claims description 20
- 238000000034 method Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 7
- 239000012466 permeate Substances 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 6
- 238000007670 refining Methods 0.000 claims description 6
- 239000000706 filtrate Substances 0.000 abstract 2
- 235000019198 oils Nutrition 0.000 description 17
- 239000002904 solvent Substances 0.000 description 13
- 238000000605 extraction Methods 0.000 description 10
- 238000001914 filtration Methods 0.000 description 9
- 238000004821 distillation Methods 0.000 description 5
- 244000068988 Glycine max Species 0.000 description 4
- 235000010469 Glycine max Nutrition 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000011148 porous material Substances 0.000 description 3
- 235000012424 soybean oil Nutrition 0.000 description 3
- 239000003549 soybean oil Substances 0.000 description 3
- 239000001993 wax Substances 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 235000014113 dietary fatty acids Nutrition 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229930195729 fatty acid Natural products 0.000 description 2
- 239000000194 fatty acid Substances 0.000 description 2
- 150000004665 fatty acids Chemical class 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000005909 Kieselgur Substances 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 235000019484 Rapeseed oil Nutrition 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 210000000988 bone and bone Anatomy 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 235000021588 free fatty acids Nutrition 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009291 secondary effect Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Fats And Perfumes (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Extraction Or Liquid Replacement (AREA)
- Filtration Of Liquid (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は油脂の精製方法に関し、さらに詳しくは限外濾
過膜を用いて油脂を精製する場合の前処理方法に関する
。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for refining fats and oils, and more particularly to a pretreatment method for refining fats and oils using an ultrafiltration membrane.
大豆油、菜種油等の食用植物油は、原料の種子をｆｆＪ
！して薄いフレーク状等↓ニしてから特公昭５７−１５
９２２号で例示されるような回転式連続抽出装置（商品
名：ロートセル装置）にて、溶剤のノルマルヘキサンと
向流的に接触することにより、種子中の油脂分を抽出し
て溶剤と油脂の混合液（以下ミセラという）を得て、次
いで両者の沸点差を利用して蒸留操作により溶剤と油脂
に分離し、回収した溶剤は抽出装置に戻して循環使用し
ている。一方分離された精製油脂は、油脂中の不純物で
あるリン脂質、ロウ分、遊離の脂肪酸等を除去するため
、水との水和反応及び酸・アルカリ等との反応による化
学的処理を行い、生成すや油滓。Edible vegetable oils such as soybean oil and rapeseed oil are made from ffJ seeds.
! Then it becomes thin flakes etc. ↓ and then special public service 1984-15
Using a rotary continuous extraction device (trade name: Rotocell device) as exemplified in No. 922, the fats and oils in the seeds are extracted by contacting them with the solvent n-hexane in a countercurrent manner, and the solvent and fats and oils are separated. A mixed solution (hereinafter referred to as miscella) is obtained, and then separated into a solvent and fat by distillation using the difference in boiling point between the two, and the recovered solvent is returned to the extraction device for circulation. On the other hand, the separated refined fats and oils are chemically treated by hydration reaction with water and reaction with acids, alkalis, etc. in order to remove impurities in the fats and oils, such as phospholipids, wax content, and free fatty acids. Generate suds and oil slag.
ガム質等の重合物をその都度遠心分離機で分離して精製
している。しかしながら以上の化学的精製法では、工程
が多くしかも複雑であるため設備費が高くなるとともに
、薬品代等の用役費も嵩む、さらには遠心分離の際に油
滓とともに油脂が損失する等という問題がある。この問
題点に鑑みて特公昭５８−３３２７９号等で開示された
ような物理的精製法が提案されている。この方法は、最
近進歩の著しい限外濾過膜を油脂の精製に利用するもの
である。すなわち前記のように連続抽出装置から生成さ
れるミセラを、蒸留操作で溶剤と油脂に分離する以前に
、分画分子量２０．０００程度の限外濾過膜で直接処理
巳、非透過液側にリン脂質、ロウ分、脂肪酸等の不純物
の濃縮液を得て、一方透過液側にはこれらの不純物の含
有量の少ない精製されたミセラを得る方法である。そし
てこの精製されたミセラを蒸留操作により溶剤と油脂に
分離し、回収された溶剤は連続抽出装置に戻して循環使
用し、−刃部脂分はこの後脱色、脱臭工程を経て製品の
精製油となる。以上の限外濾過膜を用いた物理的精製法
は工程が簡単であるため、設備費が安価であるとともＣ
二用役費も相当低減する利点があり、今後の普及が期待
されている。Gummy and other polymers are separated and purified using a centrifuge each time. However, the chemical refining methods described above involve many and complicated steps, resulting in high equipment costs, high utility costs such as chemical costs, and furthermore, fats and oils are lost along with the soapstock during centrifugation. There's a problem. In view of this problem, physical purification methods such as those disclosed in Japanese Patent Publication No. 58-33279 have been proposed. This method utilizes ultrafiltration membranes, which have recently made significant progress, for purifying fats and oils. In other words, as mentioned above, before the miscella generated from the continuous extraction device is separated into solvent and fat by distillation, it is directly treated with an ultrafiltration membrane with a molecular weight cutoff of about 20,000, and phosphorus is added to the non-permeate side. This is a method to obtain a concentrated liquid containing impurities such as lipids, waxes, and fatty acids, and on the other hand, to obtain purified micella with a low content of these impurities in the permeate side. The purified miscella is then separated into solvent and oil by distillation, and the recovered solvent is returned to the continuous extraction device for circulation use.The blade fat is then decolorized and deodorized to produce refined oil. becomes. The above-mentioned physical purification method using an ultrafiltration membrane has a simple process, so the equipment cost is low and C.
It has the advantage of considerably reducing dual utility costs, and is expected to become more widespread in the future.
以上説明した限外濾過膜を用いた物理的精製法には、前
記のような利点がある半面次のような解決すべき問題も
有していることが判明した。It has been found that while the above-described physical purification method using an ultrafiltration membrane has the above-mentioned advantages, it also has the following problems that need to be solved.
すなわち回転式連続抽出装置から生成されるミセ７ Ｌ
は、数ミクロンから数１０ミクロン程度の微細粒子が相
当台まれている。これは原料の種子を溶剤とよく接触す
るよう０．３ミリ程度に圧潰し薄いフレーク状にしてい
るが、この圧潰の際に相当の微細粉が発生シこれがミセ
ラ中に混入してくるためである。もしこの微細粒子等を
含んだミセラを直接限外濾過膜装置に供給した場合には
、膜表面に微細粒子が堆積し膜洗浄の頻度が多くなり、
稼動率が低下するという問題がある。もしこの微細粒子
等を通常の濾過機で除去するとすれば数ミクロン程度の
粒子であるため珪藻土をプレコートした濾過機を用いた
濾過操作が必要になり、設備費が嵩むとともに運転労力
も多く要るという問題がある。In other words, Mise 7L produced from a rotary continuous extraction device
There are a considerable number of fine particles ranging from several microns to several tens of microns in size. This is because the seeds used as raw materials are crushed into thin flakes of about 0.3 mm to ensure good contact with the solvent, but during this crushing, a considerable amount of fine powder is generated, which gets mixed into the micella. be. If micellar containing these fine particles is supplied directly to an ultrafiltration membrane device, the fine particles will accumulate on the membrane surface and the frequency of membrane cleaning will increase.
There is a problem that the operating rate decreases. If these fine particles were to be removed using a normal filter, the particles are only a few microns in size, so it would be necessary to use a filter pre-coated with diatomaceous earth, which would increase equipment costs and require a lot of operating labor. There is a problem.
本発明は以上の問題点に鑑みてなされたものであって、
限外濾過膜を用いてミセラを精製する場合に障害となる
ミセラ中の微細粒子の効率的で且つ経済的な除去方法を
提供することを課題とする。The present invention has been made in view of the above problems, and includes:
It is an object of the present invention to provide an efficient and economical method for removing fine particles in micella that are an obstacle when purifying micella using an ultrafiltration membrane.
本発明の要旨とするところは、油脂の溶剤抽出装置から
得られるミセラを限外濾過膜装置で処理してリン脂質等
を除去する油脂の精製の方法において、前記ミセラを精
密濾過膜装置で処理し得られる透過液については、前記
限外濾過膜装置に供給してミセラの精製を行い、一方微
細粒子等が濃縮された非透過液については、溶剤抽出装
置の原料種子が充填された隔室に循環し濾過することを
特徴とする油脂の精製方法である。The gist of the present invention is to provide a method for refining fats and oils in which micella obtained from a solvent extraction device for fats and oils is treated with an ultrafiltration membrane device to remove phospholipids, etc. The resulting permeate is supplied to the ultrafiltration membrane device to purify the miscella, while the non-permeate, which is enriched with fine particles, is sent to the compartment filled with raw seeds of the solvent extraction device. This is a method for refining fats and oils, which is characterized by circulating and filtering them.
すなわち溶剤抽出装置から得られる粗ミセラを限外濾過
膜装置で処理する以前に、精密濾過膜装置で一旦前処理
して粗ミセラ中のミクロン程度の微細粒子を除去してか
ら、ミセラを限外濾過膜装置に供給する。こうすること
により限外濾過膜装置の膜表面への微細粒子の堆積を防
止し、膜洗浄の頻度を少なくして稼動率の向上を図るこ
とができる。ここで精密濾過膜（Ｍｉｃｒｏｆｉｌｔｒ
ａｔｉｏｎＭｅｍｂｒａｎｅ）とは、膜の細孔径が０．
１μｍから１０μｍ範囲のものを意味し、限外濾過膜が
オングストローム範囲の細孔であるものと区別される。In other words, before treating the crude micella obtained from the solvent extraction device with the ultrafiltration membrane device, it is pretreated with the precision filtration membrane device to remove micron-sized particles in the crude micella, and then the micella is ultrafiltered. Supplied to the filtration membrane device. By doing so, it is possible to prevent the accumulation of fine particles on the membrane surface of the ultrafiltration membrane device, reduce the frequency of membrane cleaning, and improve the operating rate. Here, microfiltration membrane (Microfiltr)
ationMembrane) means that the pore size of the membrane is 0.
It means a membrane with pores in the 1 μm to 10 μm range, and is distinguished from ultrafiltration membranes with pores in the angstrom range.
膜の素材としてはアルミナ等の無機系のものが好適であ
るが、有機系の高分子膜であってもよい。また膜の形状
としてはチューブ状のものが好適であるが平膜状であっ
てもよい。The material for the membrane is preferably an inorganic material such as alumina, but an organic polymer membrane may also be used. The shape of the membrane is preferably tubular, but it may also be flat.
精密濾過膜の非透過液、すなわち大豆等の微細粒子を多
（含んだ液は溶剤抽出装置に戻し、大豆等の原料種子の
フレークが充填された抽出が行われる隔室に給液し、細
粒化されている種子自体の充填層の濾過作用を利用して
微細粒子をミセラから分離除去する。微細粒子は充填層
中に捕捉され、抽出後の種子滓とともに系外に搬出され
、一方濾過されたミセラ分は、他の新しいミセラととも
に精密濾過装置に供給される。The non-permeable liquid of the precision filtration membrane, that is, the liquid containing a large amount of fine particles such as soybeans, is returned to the solvent extraction device and supplied to the compartment where the extraction is performed, which is filled with flakes of raw material seeds such as soybeans. The fine particles are separated and removed from the micella using the filtration action of the packed bed of the granulated seeds themselves.The fine particles are captured in the packed bed and are carried out of the system together with the extracted seed dregs, while the filtration The removed micellar fraction is fed to a microfiltration device along with other new micella.
〔実施例〕
以下実施例に基づいて本発明の内容をさらに詳細に説明
する。第１図は本発明の実施例の系統図である。図にお
いて１０は特公昭５７−１５９２２号で例示される回転
式連続抽出装置であり、１１は円筒状のケーシング、１
２；まケーシング１１の中央に立設される竪軸１３に回
転体１４を介して放射状５１配設される隔室である。隔
室１２の水平断面は扇形状をしており、隣接する隔室と
は竪壁で仕切られており、底部には細かい金網からなる
底板１５が扉状に開閉するよう半径方向の一辺で取り付
けられている。隔室１２は減速機１６により緩速回動じ
ており、所定位置にて図示はされないケーシングの上部
に立設される原料供給管より原料の大豆種子１７が充填
される。そして抽出用の溶剤は、ケーシング底部の区分
された液留室から管路２０．循環ポンプ１８．管路２０
′及び散布管１９からなる複数の循環経路により隔室１
２内を流下するとともに隔室１２の回動方向に対し向流
的に移動しながら隔室内の種子と接触し、種子中の油脂
を効率よく抽出する。[Example] The content of the present invention will be explained in more detail based on the following example. FIG. 1 is a system diagram of an embodiment of the present invention. In the figure, 10 is a rotary continuous extractor as exemplified in Japanese Patent Publication No. 57-15922, 11 is a cylindrical casing, 1
2; These are compartments 51 arranged radially around a vertical shaft 13 erected in the center of the casing 11 via a rotating body 14. The compartment 12 has a fan-shaped horizontal cross section and is separated from adjacent compartments by a vertical wall, and a bottom plate 15 made of fine wire mesh is attached to one side in the radial direction so that it can be opened and closed like a door. It is being The compartment 12 is slowly rotated by a speed reducer 16, and at a predetermined position, soybean seeds 17 as a raw material are filled from a raw material supply pipe (not shown) provided upright on the upper part of the casing. The extraction solvent is supplied from the divided liquid storage chamber at the bottom of the casing through a pipe 20. Circulation pump 18. Conduit 20
' and a plurality of circulation paths consisting of a dispersion pipe 19.
While flowing down inside the compartment 12 and moving countercurrently with respect to the rotating direction of the compartment 12, it comes into contact with the seeds in the compartment, and efficiently extracts the fats and oils in the seeds.
このようにして溶剤中の油脂濃度が最も高くなった液留
室からミセラ分は管路２０″を介してミセラタンク２１
に抜き出される。次いでミセラ分は第１ミセラポンプ２
２により昇圧されて多管式熱交換器状の精密濾過膜装置
２３に供給される。ここでミセラ分はチューブ状の濾過
膜の内面をクロスフロー的に流れながら、微細粒子が濃
縮されたチューブ内の非透過液は管路２４を経由して回
転式連続抽出装置１０の適宜位置の散布管１９′に戻さ
れる。ここでミセラ分は隔室内の種子の充填層を流下し
ながら微細粒子は大豆種子の細粒からなる充填層中に捕
捉される。一方精密濾過膜を透過してミクロン程度の微
細粒子が除去されたミセラ分は第２ミセラタンク２５に
流入する。そして第２ミセラタンク２５中のミセラ分は
第２ミセラポンプ２６によって限外濾過膜装置２７に供
給され、ここでミセラ中のリン脂質、ロウ分、脂肪酸−
等の不純物が分離されて、以下図示はされない蒸留工程
に送出されて回収された溶剤は抽出機に戻され、得られ
る油脂骨は脱色、脱臭工程を経て製品の製品大豆油とな
る。In this way, the micellar component is transferred from the liquid distillation chamber where the concentration of oil and fat in the solvent is the highest to the micellar tank 21 via the pipe 20''.
is extracted. Next, the micellar portion is transferred to the first micellar pump 2.
2, and is supplied to a precision filtration membrane device 23 in the form of a shell-and-tube heat exchanger. Here, while the micellar component flows in a cross-flow manner on the inner surface of the tube-shaped filtration membrane, the non-permeate liquid in the tube containing concentrated fine particles is passed through the pipe 24 to the appropriate position of the rotary continuous extraction device 10. It is returned to the dispersion tube 19'. Here, while the micellar components flow down the packed bed of seeds in the compartment, the fine particles are captured in the packed bed made of fine grains of soybean seeds. On the other hand, the micellar portion that has passed through the microfiltration membrane and from which fine particles on the order of microns have been removed flows into the second micellar tank 25 . The micellar components in the second micellar tank 25 are then supplied to the ultrafiltration membrane device 27 by the second micellar pump 26, where the phospholipids, wax components, fatty acids, etc.
Impurities such as soybean oil are separated, and the solvent is sent to a distillation process (not shown below) and recovered, and the recovered solvent is returned to the extractor, and the resulting fat bones undergo decolorization and deodorization processes to become the product soybean oil.
本実施例においては、回転式抽出機について説明したが
、本発明は他の型式の抽出機についても適用できること
は当然である。In this embodiment, a rotary extractor has been described, but it is obvious that the present invention can be applied to other types of extractors.
以上の構成と作用を有する本発明によれば、油脂抽出機
から生成されるミセラは、精密濾過膜装置で微細粒子が
除去されてから限外濾過膜装置に供給されるため、限外
濾過膜装置の目詰まり頻度を少なくして稼動率を向上で
きるとともに、精密濾過膜装置で分離された微細粒子は
連続抽出装置の隔室内の種子の充填層の濾過作用を利用
して捕捉されるため、このための新たな設備を必要とし
ないので少ない設備費で済む効果がある。また限外濾過
膜装置で副生するリン脂質には、微細粒子が同伴しない
ため、リン脂質の精製が容易であるという副次的効果も
得られる。According to the present invention having the above-described configuration and operation, the miscella produced from the fat and oil extractor is supplied to the ultrafiltration membrane device after fine particles are removed by the microfiltration membrane device. In addition to reducing the frequency of equipment clogging and improving operating efficiency, the fine particles separated by the microfiltration membrane equipment are captured using the filtration action of the seed packed bed in the compartment of the continuous extraction equipment. Since new equipment for this purpose is not required, there is an effect that equipment costs can be reduced. Furthermore, since the phospholipids produced as a by-product in the ultrafiltration membrane device are not accompanied by fine particles, a secondary effect is obtained in that the phospholipids can be easily purified.
第１図は本発明の実施例の系統図である。
１０：回転式連続抽出装置、１１：ケーシング。
１２：隔室、１３：竪軸、１４：回転体、１５：底板、
１６：減速機、１７：原料種子、１８：溶剤循環ポンプ
、１９：散布管、２ｏ：管路、２１：第１ミセラタンク
、２２：第１ミセラポンブ。
２３：精密濾過膜装置、２４：管路、２５：第２ミセラ
タンク、２６：第２ミセラボンプ、２７：限外濾過膜装
置。FIG. 1 is a system diagram of an embodiment of the present invention. 10: Rotary continuous extraction device, 11: Casing. 12: Compartment, 13: Vertical shaft, 14: Rotating body, 15: Bottom plate,
16: Reducer, 17: Raw material seed, 18: Solvent circulation pump, 19: Spray pipe, 2o: Pipe line, 21: First micellar tank, 22: First micellar pump. 23: Microfiltration membrane device, 24: Pipe line, 25: Second micellar tank, 26: Second micellar bomb, 27: Ultrafiltration membrane device.
Claims (1)
置で処理してリン脂質等を除去する油脂の精製の方法に
おいて、前記ミセラを精密濾過膜装置で処理し得られる
透過液については、前記限外濾過膜装置に供給してミセ
ラの精製を行い、一方微細粒子等が濃縮された非透過液
については、溶剤抽出装置の原料種子が充填された隔室
に循環し濾過することを特徴とする油脂の精製方法。In a method for purifying fats and oils in which miscella obtained from a solvent extraction device for fats and oils is treated with an ultrafiltration membrane device to remove phospholipids, etc., the permeate obtained by treating the miscella with a microfiltration membrane device is as described above. The micella is purified by being supplied to an ultrafiltration membrane device, while the non-permeate liquid containing concentrated fine particles is circulated to a compartment filled with raw material seeds of a solvent extraction device and filtered. A method for refining fats and oils.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30884190A JP3200434B2 (en) | 1990-11-16 | 1990-11-16 | Oil and fat refining method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30884190A JP3200434B2 (en) | 1990-11-16 | 1990-11-16 | Oil and fat refining method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04183795A true JPH04183795A (en) | 1992-06-30 |
| JP3200434B2 JP3200434B2 (en) | 2001-08-20 |
Family
ID=17985929
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP30884190A Expired - Lifetime JP3200434B2 (en) | 1990-11-16 | 1990-11-16 | Oil and fat refining method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3200434B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| JP2006198575A (en) * | 2005-01-24 | 2006-08-03 | Central Res Inst Of Electric Power Ind | Method for removing water of water-containing solid and its system |
-
1990
- 1990-11-16 JP JP30884190A patent/JP3200434B2/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| JP2006198575A (en) * | 2005-01-24 | 2006-08-03 | Central Res Inst Of Electric Power Ind | Method for removing water of water-containing solid and its system |
| JP4671700B2 (en) * | 2005-01-24 | 2011-04-20 | 財団法人電力中央研究所 | Method and system for removing moisture from moisture-containing solids |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3200434B2 (en) | 2001-08-20 |
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