JPH05117685A - Continuous degumming of triglyceride oil - Google Patents
Continuous degumming of triglyceride oilInfo
- Publication number
- JPH05117685A JPH05117685A JP4108595A JP10859592A JPH05117685A JP H05117685 A JPH05117685 A JP H05117685A JP 4108595 A JP4108595 A JP 4108595A JP 10859592 A JP10859592 A JP 10859592A JP H05117685 A JPH05117685 A JP H05117685A
- Authority
- JP
- Japan
- Prior art keywords
- oil
- gum
- gum phase
- water
- centrifuge
- 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.)
- Pending
Links
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 claims abstract description 59
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000005119 centrifugation Methods 0.000 claims abstract description 24
- 238000005406 washing Methods 0.000 claims abstract description 16
- 239000000203 mixture Substances 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 6
- 231100000252 nontoxic Toxicity 0.000 claims description 3
- 230000003000 nontoxic effect Effects 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 2
- 150000007513 acids Chemical class 0.000 claims 1
- 239000008367 deionised water Substances 0.000 claims 1
- 229910021641 deionized water Inorganic materials 0.000 claims 1
- 238000004064 recycling Methods 0.000 claims 1
- 150000003904 phospholipids Chemical class 0.000 abstract description 15
- 239000003921 oil Substances 0.000 description 92
- 235000019198 oils Nutrition 0.000 description 92
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 9
- 239000011574 phosphorus Substances 0.000 description 9
- 229910052698 phosphorus Inorganic materials 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 8
- 238000004061 bleaching Methods 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 235000019484 Rapeseed oil Nutrition 0.000 description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 235000012424 soybean oil Nutrition 0.000 description 4
- 239000003549 soybean oil Substances 0.000 description 4
- 239000003925 fat Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 2
- 235000019197 fats Nutrition 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 238000001637 plasma atomic emission spectroscopy Methods 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 235000015112 vegetable and seed oil Nutrition 0.000 description 2
- 239000008158 vegetable oil Substances 0.000 description 2
- 235000019482 Palm oil Nutrition 0.000 description 1
- 235000019485 Safflower oil Nutrition 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003086 colorant Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 230000000887 hydrating effect Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 210000002741 palatine tonsil Anatomy 0.000 description 1
- 239000002540 palm oil Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 235000005713 safflower oil Nutrition 0.000 description 1
- 239000003813 safflower oil Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 150000003626 triacylglycerols Chemical class 0.000 description 1
- 235000019871 vegetable fat Nutrition 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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
- C11B3/006—Refining fats or fatty oils by extraction
-
- 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
- C11B3/16—Refining fats or fatty oils by mechanical means
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Microbiology (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Fats And Perfumes (AREA)
- Peptides Or Proteins (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Centrifugal Separators (AREA)
- Treatment Of Liquids With Adsorbents In General (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、トリグリセリド油から
連続的にガム相を除去する方法に関し、その結果とし
て、低油分含量のガム相と、漂白後、物理的に精製され
得る脱ガム油を製造するものである。FIELD OF THE INVENTION The present invention relates to a method for continuously removing a gum phase from a triglyceride oil, which results in a low oil content gum phase and a degummed oil which can be physically refined after bleaching. It is manufactured.
【０００２】[0002]
【従来技術】油糧種子や動物性原料を圧搾および／また
は抽出して得られるような粗製トリグリセリド油は、ト
リグリセリド以外の物質をいくらか含んでいる。リン脂
質、０離脂肪酸、有臭物質、着色物質、ろう、金属化合
物などの混合物は、精製油の味、におい、外観、保存性
に影響を与えるため除去しなければならない。Crude triglyceride oils, such as those obtained by squeezing and / or extracting oilseeds or animal raw materials, contain some substances other than triglycerides. Mixtures of phospholipids, zero fatty acids, odorants, colorants, waxes, metal compounds, etc. affect the taste, odor, appearance and shelf life of refined oils and must be removed.
【０００３】これら不必要な混合物を除去する方法はす
でに知られており、しばしば文献に記載されている。Methods for removing these unwanted mixtures are already known and often described in the literature.
【０００４】トリグリセリド油からガム相を連続的に除
去する方法は、ヨーロッパ特許第０３４８ ００４号に
記載されている。この方法は、第１段階で、リン脂質を
水和する通常の脱ガム法によって油を脱ガムする。そし
て、第２段階で、不溶性及び、遠沈しない分子を任意に
凝集させ、その塊を微細濾過、濾過、遠心、沈降、また
はデカンテーションなどによって脱ガム油から分離す
る。この方法は、２段階でガム相を除去する間に、トリ
グリセリド油がかなり損失する点で不利である。A process for the continuous removal of the gum phase from triglyceride oils is described in EP 0348004. The method degummes the oil in the first step by the conventional degumming method of hydrating phospholipids. Then, in the second step, the insoluble and non-centrifuging molecules are arbitrarily aggregated, and the mass is separated from the degummed oil by microfiltration, filtration, centrifugation, sedimentation, decantation, or the like. This method is disadvantageous in that there is considerable loss of triglyceride oil during the removal of the gum phase in two steps.
【０００５】トリグリセリド油から、分離しているガム
相を連続的に除去する別の方法は、ヨーロッパ特許第３
４９ ７１８号に記載されている。この方法では、第１
段階で、単独のガム質相が含まれる油を遠心分離し、ご
く少量の油を含有するガム相と、元から原料油中に存在
するガムの画分を依然として含む油とを製造する。第２
段階で、第１段階から得られる油を２回目の遠心分離に
かけ、ごく少量の残留ガムを含む油と、第１段階で得ら
れたガムよりももっと油分含量の高いガム相とを製造
し、そのガムを自体再循環させる。この再循環により、
結果としてトリグリセリド油の損失は減少する。Another method for the continuous removal of a separating gum phase from triglyceride oils is described in EP 3
49 718. In this method, the first
In a step, the oil containing a single gum phase is centrifuged to produce a gum phase containing only a small amount of oil and an oil still containing the fraction of gum originally present in the feedstock. Second
In a stage, the oil from the first stage is centrifuged a second time to produce an oil with a very small amount of residual gum and a gum phase with a higher oil content than the gum obtained in the first stage, Recycle the gum itself. By this recirculation,
As a result, the loss of triglyceride oil is reduced.
【０００６】しかし、最終的に、もし脱ガム油でリン脂
質含量の低いものを売ろうとするなら、一回、あるいは
それ以上の洗浄段階を設けたほうがよい。というのは、
２回目の遠心分離で得られた油は、なおリン脂質含量が
過度に高いと思われるからである。これらの洗浄段階に
は、特別の遠心分離機が必要であり、そして洗浄段階は
流出の原因となる。それ故、投資や加工費が増額するの
で不利である。Ultimately, however, if one wishes to sell degummed oils having a low phospholipid content, one or more washing steps should be provided. I mean,
This is because the oil obtained by the second centrifugation still seems to have an excessively high phospholipid content. These wash steps require a special centrifuge, and the wash steps cause effluent. Therefore, it is disadvantageous because it increases investment and processing costs.
【０００７】[0007]
【発明が解決しようとする課題】それゆえ、本発明は、
トリグリセリド油からガム相を連続的に除去し、油分含
量の低いガム質とリン脂質含量の低い脱ガム油を得る、
より好ましい方法を提供することを目的とする。Therefore, the present invention is
The gum phase is continuously removed from the triglyceride oil to obtain a degummed oil with low oil content and low phospholipid content.
It is intended to provide a more preferable method.
【０００８】付加的な目的は、トリグリセリド油からガ
ム相を連続的に除去する方法において、高額の投資と加
工費を必要としない方法を提供することである。[0008] An additional object is to provide a process for the continuous removal of the gum phase from triglyceride oils which does not require high investment and processing costs.
【０００９】トリグリセリド油からガム相を連続的に除
去する方法において、流路を汚さない方法を提供するこ
とも、本発明の目的である。[0009] It is also an object of the present invention to provide a method of continuously removing the gum phase from triglyceride oil, which method does not foul the channels.
【００１０】上記の目的及びこの発明の利点は、次に記
載する結果から明白であろう。The above objects and advantages of the present invention will be apparent from the results described below.
【００１１】[0011]
【課題を解決するための手段】本発明は、トリグリセリ
ド油から連続的にガム相を除去する方法に関し、その結
果として、低油分含量のガム相と、漂白後、物質的に精
製され得る脱ガム油を製造するものである。SUMMARY OF THE INVENTION The present invention is directed to a method for continuously removing a gum phase from a triglyceride oil, which results in a low oil content gum phase and degumming that can be materially refined after bleaching. It produces oil.
【００１２】本発明による方法は、トリグリセリド油か
ら連続的にガム相を除去する方法で次に示す段階、すな
わち、ａ）分離しているガム相を含む油を第１の遠心分
離機で遠心分離し、ごく少量の油分を含有するガム相
と、元の原料油のガム画分が依然として残存する油とを
製造する第１段階、ｂ）適量の水を１回目の遠心分離で
得た油に混合し、必要に応じて、混合物をホールディン
グタンクに通す第２段階、ｃ）ｂ）で得た混合物を第２
の遠心分離機で遠心分離し、ごく少量の残留ガムを含有
する油と、ａ）で得たガム相よりももっと油分含量の高
いウェットガム相とを製造する第３段階、及びｄ）ｃ）
で得たウェットガム相を、第１の遠心分離機への油の供
給流路の入口へ再循環する第４段階、を含む工程段階か
ら成る。The process according to the invention is a process for the continuous removal of the gum phase from the triglyceride oil: a) the oil containing the separating gum phase is centrifuged in a first centrifuge. Then, the first step of producing a gum phase containing a very small amount of oil and an oil in which the gum fraction of the original feed oil still remains, b) adding an appropriate amount of water to the oil obtained by the first centrifugation. Mixing, and if necessary, passing the mixture through a holding tank in the second step, c) the mixture obtained in b) in the second step
Third step of centrifuging with a centrifuge to produce an oil containing a very small amount of residual gum and a wet gum phase with a higher oil content than the gum phase obtained in a), and d) c)
The wet gum phase obtained in step 4 above is recycled to the inlet of the oil feed passage to the first centrifuge, a fourth step.
【００１３】発明者らは、第２の遠心分離機へ供給する
前に、１回目の遠心分離で得られる油に、適量の洗浄水
を混合しても、１回目の遠心分離で得られるガム相のト
リグリセリド含量には、何ら影響を与えないという意外
な発見をした。また、１回目の遠心分離では、２回目の
遠心分離で得られたガム相とともに再循環した追加の水
を効果的に除去できるから、この追加した水は、２回目
の遠心分離で得られる油の水分含量に影響を与えないと
いう意外な発見もした。この追加した水により、さら
に、２回目の遠心分離で得られる油のリン脂質含量がよ
り低くなるのである。この発明によって得られた油を漂
白するには、つまり、許容量と思われるリンレベルを有
する漂白された油を提供するには、漂白土は通常の量で
よいということも見出した。The inventors obtained a gum obtained by the first centrifugation even if the oil obtained by the first centrifugation was mixed with an appropriate amount of washing water before being supplied to the second centrifuge. It was an unexpected discovery that it had no effect on the triglyceride content of the phase. In addition, in the first centrifugation, the additional water recirculated with the gum phase obtained in the second centrifugation can be effectively removed. I also made a surprising discovery that it does not affect the water content of the. This additional water further reduces the phospholipid content of the oil obtained from the second centrifugation. It has also been found that to bleach the oil obtained according to the invention, i.e. to provide a bleached oil with an acceptable level of phosphorus, the bleaching earth may be in a conventional amount.
【００１４】１段、もしくは２段の洗浄段階を省略でき
ることが、本発明による方法の利点であり、ヨーロッパ
特許第０ ３４９ ７１８号に開示された方法より優れ
ている。その結果、洗浄段階でのトリグリセリド油の損
失、流出の問題、遠心機を洗浄する際の投資を避けられ
る。It is an advantage of the method according to the invention that one or two washing steps can be omitted, which is superior to the method disclosed in EP 0 349 718. As a result, the loss of triglyceride oil in the washing stage, spillage problems, and investment in washing the centrifuge are avoided.
【００１５】本発明の理解を深めるために、処理工程を
添付の図１に概略的に表した。For a better understanding of the invention, the process steps are schematically represented in the accompanying FIG.
【００１６】本発明による方法を用いることによって、
米国特許第４，６９８，１８５号の脱ガム方法を改善で
きる。本発明の方法により、水で脱ガムされた植物油脂
が、微細に分散された酸水溶液によって処理され、この
酸が部分的に中和されることにより、油脂中にガム相が
形成される。もし、ガム相を含む油が、本発明によって
加工処理されるなら、そのようにして得られた油は、物
理的に精製されていることだろう。By using the method according to the invention,
The degumming method of US Pat. No. 4,698,185 can be improved. According to the method of the present invention, a vegetable oil or fat degummed with water is treated with a finely dispersed aqueous acid solution, and the acid is partially neutralized to form a gum phase in the oil or fat. If an oil containing a gum phase is processed according to the present invention, the oil thus obtained will be physically refined.
【００１７】同様に、本発明による方法は、ドイツ特許
第１ ５６５ ５６９号の方法で処理された脱ガム油に
有利に応用できる。この方法に応用するには、粗製油に
酸を加えること、塩基でこの酸を部分的に中和するのに
約１０分接触させること、そして、最終的に油から除去
する、分離しているガム相を形成させるために、接触時
間を延長することが必要である。Similarly, the method according to the invention can be advantageously applied to degummed oils treated according to the method of DE 1 565 569. Application to this method is to add acid to the crude oil, contact for about 10 minutes to partially neutralize the acid with base, and finally remove from the oil, separating. Prolonged contact time is required to form the gum phase.
【００１８】本発明による方法は、米国特許第４，０４
９，６８６号の方法によって処理された脱ガム油にも、
有利に応用できる。米国特許第４，０４９，６８６号で
は、油を酸で処理し、４０℃以下に冷却している。そし
て、非水和リン脂質が遠心分離などによって油から除去
された形でガムを形成する。The method according to the invention is described in US Pat.
For degummed oil treated by the method of 9,686,
It can be applied to advantage. In U.S. Pat. No. 4,049,686, the oil is treated with acid and cooled to below 40 ° C. Then, the non-hydrated phospholipids are removed from the oil by centrifugation or the like to form a gum.
【００１９】本発明による方法では脱ガムされる油はど
んな種類であってもよい。食用のトリグリセリド油、例
えば、大豆油、サフラワー油、菜種油、パーム油、その
他の植物油や動物性油脂など、これらすべてが、首尾よ
く加工処理され、油を１回目に遠心分離する前に、首尾
よくガム相が形成する。The oil to be degummed in the process according to the invention may be of any kind. Edible triglyceride oils, such as soybean oil, safflower oil, rapeseed oil, palm oil, other vegetable oils and animal fats, all of which have been successfully processed and processed successfully before the first centrifugation of the oil. Well formed gum phase.
【００２０】１回目の遠心分離で得られた油に混合する
洗浄水は、水、希釈されたクエン酸などの無毒の酸、塩
類を含む水、または任意の洗浄段階の結果生じる流出水
であってもよい。１回目の遠心分離機に残る油に混合さ
れる適量の洗浄水は、一般に、０．５乃至１０重量％、
好ましくは０．５乃至５重量％の範囲であるようにす
る。The wash water mixed with the oil obtained in the first centrifugation is water, non-toxic acid such as diluted citric acid, water containing salts, or effluent resulting from any washing step. May be. An appropriate amount of wash water mixed with the oil remaining in the first centrifuge is generally 0.5 to 10% by weight,
The preferred range is 0.5 to 5% by weight.
【００２１】油と洗浄水の混合物は、必要に応じてホー
ルディングタンクに通す。この保持時間は、一般に、１
０秒乃至３０分間、好ましくは０．５乃至１５分間の範
囲であるようにする。ホールディングタンクでの温度
は、６０乃至１１０℃であるのが好ましい。The mixture of oil and wash water is optionally passed through a holding tank. This retention time is typically 1
It should be in the range of 0 seconds to 30 minutes, preferably 0.5 to 15 minutes. The temperature in the holding tank is preferably 60 to 110 ° C.
【００２２】本発明の方法で使用される遠心分離機は、
ディスクの遠心分離機、デカンター、または他の油相か
らガム相を連続的に分離できる装置であってもよい。そ
のような装置の性能は、一般に、ヨーロッパ特許第３４
９ ７１８号に詳しく記載されているように、油分含量
の低いガム相かガム含量の低い油相かどちらを製造する
かによって調節される。The centrifuge used in the method of the present invention comprises:
It may be a disk centrifuge, a decanter, or any other device capable of continuously separating the gum phase from the oil phase. The performance of such devices is generally described in European Patent No. 34.
As detailed in No. 9 718, it is controlled by whether to produce a low oil content gum phase or a low gum content oil phase.
【００２３】本発明の方法によって得られる油相は、さ
らに乾燥され、一般に、公知の漂白法で漂白された後、
物理的にまたは、アルカリ中和によって精製される。The oily phase obtained by the process according to the invention is further dried and, after bleaching, in general by known bleaching methods,
Purified physically or by alkali neutralization.
【００２４】次の実施例でこの発明を説明する。The present invention will be described in the following examples.
【００２５】[0025]
（実施例１）実施例１では、本発明の方法に従って、ト
リグリセリド油から連続的にガムを除去することについ
て説明する。Example 1 Example 1 illustrates continuous gum removal from triglyceride oil according to the method of the present invention.
【００２６】原料油は、水で脱ガムされた大豆油で温度
が約９０℃のもの、約１２０ｐｐｍの残留するリン、約
１．１５ｐｐｍの鉄を含有していた。単独のガム相を、
米国特許第４，６９８，１８５号の方法、すなわち、８
０％強のリン酸０．２ｖｏｌ．％を２．５分間接触させ
（９．３ｔｏｎｓ／ｈの処理量で）、１２°Ｂｅの苛性
ソーダでリン酸を５０％中和するという方法に従って形
成させた。The feedstock was water degummed soybean oil having a temperature of about 90 ° C., containing about 120 ppm of residual phosphorus and about 1.15 ppm of iron. A single gum phase,
The method of US Pat. No. 4,698,185, namely 8
0% strong phosphoric acid 0.2 vol. % For 2.5 minutes (at a throughput of 9.3 tons / h) and neutralized to 50% phosphoric acid with caustic soda at 12 ° Be.
【００２７】分離しているガム相を含む大豆油を、この
発明の方法の第１段階で、遠心分離機に供給した。結果
として、この油から約１９重量％のトリグリセリド油を
含むガム相（乾燥物質として計算して）と元の原料油の
リン脂質画分が残存するトリグリセリド油が生じた。１
回目の遠心分離で生じた油に４．１０％の洗浄水を混合
し、この混合物をホールディングタンクに通し、約２分
間保持した後、第２の遠心分離機に供給した。The soybean oil containing the separating gum phase was fed to the centrifuge in the first step of the process of this invention. As a result, this oil yielded a triglyceride oil with a gum phase (calculated as dry matter) containing about 19% by weight triglyceride oil and the phospholipid fraction of the original feedstock. 1
The oil produced in the second centrifugation was mixed with 4.10% of wash water, this mixture was passed through a holding tank, held for about 2 minutes, and then fed to a second centrifuge.
【００２８】２回目の遠心分離の段階で、ウェットガム
相をトリグリセリド油から除去し、そしてガム相を、第
２のホールディングタンクに通して、約１時間保持した
後完全に、第１の遠心分離機への油の供給流路の入口へ
再循環した。この再循環の流路の流出率は、２，３ｔｏ
ｎｓ／ｈと見積もられた。In the second centrifugation step, the wet gum phase was removed from the triglyceride oil, and the gum phase was passed through the second holding tank and held for about 1 hour, after which it was completely centrifuged. It was recirculated to the inlet of the oil supply flow path to the machine. The outflow rate of this recirculation channel is 2,3 to
It was estimated to be ns / h.
【００２９】比較例では、上記の方法で形成した単独の
ガム相を含む同様の大豆油を、２段の洗浄段階を含むヨ
ーロッパ特許第０ ３４９ ７１８号の方法に従って処
理した。In a comparative example, a similar soybean oil containing the sole gum phase formed by the above method was treated according to the method of EP 0 349 718 which contained two washing steps.
【００３０】それぞれの方法における、異なる段階での
油の品質を表１に要約した。油中のリンと鉄はプラズマ
発光分光法で分析した（Ａ．Ｊ．Ｄｉｊｋｓｔｒａ ａ
ｎｄＤ．Ｍｅｅｒｔ，Ｊ．Ａ．Ｏ．Ｃ．Ｓ． ５９，１
９９（１９８２））。The oil qualities at different stages in each method are summarized in Table 1. Phosphorus and iron in oil were analyzed by plasma emission spectroscopy (AJ Dijkstra a.
ndD. Meert, J .; A. O. C. S. 59,1
99 (1982)).
【００３１】[0031]
【表１】 [Table 1]
【００３２】上の表から、２回目の遠心分離で生じる油
に残留するリン含量はヨーロッパ特許第０ ３４９ ７
１８号より、この発明の操作をおこなったときの方が、
かなり低かったことが明らかである。加えて、この発明
で得られた油のリン含量は２段の洗浄段階を含むヨーロ
ッパ特許第０ ３４９ ７１８号による油のリン含量と
ほぼ同じである。これより、この発明では、２段の洗浄
段階を省略できることが説明できた。From the table above, the phosphorus content remaining in the oil resulting from the second centrifugation can be found in EP 0 349 7
From No. 18, when performing the operation of this invention,
It is clear that it was quite low. In addition, the phosphorus content of the oil obtained according to the invention is about the same as the phosphorus content of the oil according to EP 0 349 718, which comprises two washing steps. From this, it has been explained that the present invention can omit the two cleaning steps.
【００３３】また、上の表から２回目の遠心分離で生じ
た油の水分含量は、この発明に従って操作したとき増加
していないということも明らかである。また、１回目の
遠心分離は、各段階の遠心分離の間に、油に入る余分の
水を除去できることも説明している。It is also clear from the table above that the water content of the oil produced in the second centrifugation is not increased when operated according to the invention. It also explains that the first centrifugation can remove excess water entering the oil during each stage of centrifugation.
【００３４】（実施例２）実施例２では、本発明の方法
に従って、トリグリセリド油から連続的にガムを除去す
ることについて説明する。Example 2 Example 2 illustrates the continuous removal of gum from triglyceride oil according to the method of the present invention.
【００３５】原料油は、水で部分的に脱ガムされた菜種
油で温度が約９０℃のもの、約１５８ｐｐｍの残留する
リン、約１．５８ｐｐｍの鉄を含有していた。単独のガ
ム相を、米国特許第４，６９８，１８５号の方法、すな
わち、８０％強のリン酸０．１６ｖｏｌ％を２．５分接
触させ（９．０ｔｏｎｓ／ｈの処理量で）、１２°Ｂｅ
の苛性ソーダでリン酸を５０％中和するという方法に従
って形成させた。The feedstock was rapeseed oil, partially degummed with water, at a temperature of about 90 ° C., contained about 158 ppm residual phosphorus, and about 1.58 ppm iron. The sole gum phase was contacted with the method of US Pat. No. 4,698,185, ie 0.16 vol% phosphoric acid at 80% strength for 2.5 minutes (at a throughput of 9.0 tons / h), 12 ° Be
It was formed according to the method of 50% neutralization of phosphoric acid with sodium hydroxide.
【００３６】分離しているガム相を含む菜種油を、この
発明の方法の第１段階で、遠心分離機に供給した。結果
として、この油から約１４重量％のトリグリセリド油を
含むガム相（乾燥重量で）と元の原料油に存在するリン
脂質画分を依然として含んでいるトリグリセリド油が生
じた。The rapeseed oil containing the separating gum phase was fed to the centrifuge in the first step of the process according to the invention. The result was a triglyceride oil which still contained the gum phase (on a dry weight basis) containing about 14% by weight of triglyceride oil and the phospholipid fraction present in the original feedstock.
【００３７】２回目の遠心分離で生じた油に、２％の洗
浄水を混合し、この混合物を、ホールディングタンクに
通し、約２分保持した後、第２の遠心分離機に供給し
た。The oil produced in the second centrifugation was mixed with 2% of wash water, this mixture was passed through a holding tank, held for about 2 minutes, and then fed to a second centrifuge.
【００３８】第２の遠心分離の段階で、ウェットガム相
をトリグリセリド油から除去し、そしてガム相を、完全
に、約３０分間保持して、第２のホールディングタンク
を通して、第１の遠心分離機への供給流路の入口へ再循
環した。この再循環の流路の流出率は、２，４ｔｏｎｓ
／ｈと見積もられた。In the second centrifugation step, the wet gum phase is removed from the triglyceride oil and the gum phase is kept completely for about 30 minutes and passed through the second holding tank to the first centrifuge. Was recirculated to the inlet of the feed channel to. The outflow rate of this recirculation channel is 2,4 tons.
/ H was estimated.
【００３９】比較例では、上記の方法で形成させた単独
のガム相を含む同様の菜種油を、２段の洗浄段階を含む
ヨーロッパ特許第０ ３４９ ７１８号の方法に従って
処理した。ヨーロッパ特許０ ３４９ ７１８の方法で
得たガム相の油分含量は約１２．６％（乾燥物質として
計算して）だった。In a comparative example, a similar rapeseed oil containing the sole gum phase formed as described above was treated according to the method of EP 0 349 718 which contained two washing steps. The oil content of the gum phase obtained by the method of European Patent 0 349 718 was about 12.6% (calculated as dry substance).
【００４０】そのようにして得た油を、０．５重量％の
漂白土（Ｔｏｎｓｉｌ ＡＣＣＦＦ，Ｓｕｄ Ｃｈｅｍ
ｉｅ，Ｍｕｎｉｃｈ，Ｇｅｒｍａｎｙ）で、１００℃、
減圧下、３０分間漂白した、そして、油を、９０℃以下
に冷却した後、漂白土を濾去した。次に、漂白した油を
２４０℃、２時間、４００Ｐａ（３０ｍｍＨｇ）以下の
減圧下で物理的精製した。油は、両方とも口当たりがよ
く、嫌な味がしないものであり、優れた保存性を示し
た。The oil thus obtained was treated with 0.5% by weight of bleaching earth (Tonsil ACCFF, Sud Chem.
ie, Munich, Germany) at 100 ° C.,
It was bleached for 30 minutes under reduced pressure, and after cooling the oil to below 90 ° C., the bleaching earth was filtered off. Next, the bleached oil was physically refined under reduced pressure of 400 Pa (30 mmHg) or less at 240 ° C. for 2 hours. Both oils were palatable, did not have an unpleasant taste and showed excellent shelf life.
【００４１】それぞれの油の品質を表１に要約した。再
度、油中のリンと鉄をプラズマ発光分光法で分析した
（Ａ．Ｊ．Ｄｉｊｋｓｔｒａ ａｎｄ Ｄ．Ｍｅｅｒ
ｔ，Ｊ．Ａ．Ｏ．Ｃ．Ｓ． ５９（１９８２），１９
９））。The quality of each oil is summarized in Table 1. Again, phosphorus and iron in the oil were analyzed by plasma emission spectroscopy (A. J. Dijkstra and D. Meer.
T. J. A. O. C. S. 59 (1982), 19
9)).
【００４２】[0042]
【表２】 [Table 2]
【００４３】上の表２から、２回目の遠心分離で生じる
油に残留するリン含量はヨーロッパ特許第０ ３４９
７１８号より、この発明の操作をおこなったときの方
が、かなり低かったことが明らかである。さらに、上の
表から、高品質の精製油を得るために、この発明による
油は、乾燥後、通常量の漂白土で漂白されたことが明ら
かである。From Table 2 above, the phosphorus content remaining in the oil resulting from the second centrifugation can be found in EP 0 349.
From No. 718, it is clear that the operation of this invention was much lower. Furthermore, it is clear from the above table that the oil according to the invention was bleached with a normal amount of bleaching earth after drying in order to obtain a refined oil of high quality.
【００４４】[0044]
【発明の効果】本発明の方法では、従来の方法で脱ガム
するよりも、１回の遠心分離でリン脂質を多量に除去す
ることができ、また２段の洗浄段階を省略しても、リン
脂質含量の低い脱ガム油を得ることができる。さらに、
２回目の遠心分離で生成したウェットガム相は、再循環
させることができるので効率的である。According to the method of the present invention, a large amount of phospholipid can be removed by a single centrifugation as compared with the conventional method of degumming, and even if two washing steps are omitted, A degummed oil having a low phospholipid content can be obtained. further,
The wet gum phase produced in the second centrifugation is efficient as it can be recycled.
【図１】この発明の方法を実施するためのフローチャー
トの一例である。FIG. 1 is an example of a flow chart for implementing the method of the present invention.
１ 油供給口（分離しているガム相を含む油） ２ ミキサー（Ｉ） ３ 第１遠心分離機 ４ ミキサー（II） ５ 第２遠心分離機 ６ 洗浄水 ７ 第１ホールディングタンク ８ 第２ホールディングタンク ９ ガム相（ごく少量の油を含有するガム相） １０ ポンプ １１ 再循環ガム相（ウェットガム相） １２ 油出口 1 oil supply port (oil containing separated gum phase) 2 mixer (I) 3 first centrifuge 4 mixer (II) 5 second centrifuge 6 wash water 7 first holding tank 8 second holding tank 9 gum phase (gum phase containing a very small amount of oil) 10 pump 11 recirculating gum phase (wet gum phase) 12 oil outlet
───────────────────────────────────────────────────── フロントページの続き (72)発明者 アルベルト・ヤン・デイクストラ ベルギー国Ｂ−8500コルトラーフ・アルバ ーン・ヴアン・デン・アベーレラン２ ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Albert Jan Dixtra Belgium B-8500 Coltraf Alban Vuan den Averelan 2
Claims (9)
において、ａ）分離しているガム相を含む油から、ごく
少量の油分を含有するガム相と、元の原料油のガム画分
が残存する油とを、第１の遠心分離機で遠心分離し、製
造する第１段階、ｂ）適量の水を１回目の遠心分離で得
た油に混合し、混合物を、必要に応じてホールディング
タンクに通す第２段階、ｃ）ｂ）で得た混合物を第２の
遠心分離機で遠心分離し、ごく少量の残留ガムを含有す
る油と、ａ）で得たガム相よりももっと油分含量の高い
ウェットガム相とを製造する第３段階、及びｄ）ｃ）で
得たウェットガム相を、第１の遠心分離機への油の供給
流路の入口へ再循環する第４段階、を含むことを特徴と
する方法。1. In a continuous degumming method from triglyceride oil, a) a gum phase containing a very small amount of oil and a gum fraction of the original feed oil remain from a separated oil containing a gum phase. The oil to be treated is centrifuged in a first centrifuge to produce the first step, b) an appropriate amount of water is mixed with the oil obtained in the first centrifugation, and the mixture is held in a holding tank if necessary. The mixture obtained in the second step, c) b), is passed through a second centrifuge to give an oil containing a very small amount of residual gum and a more oil content than the gum phase obtained in a). A third step of producing a high wet gum phase and d) a fourth step of recycling the wet gum phase obtained in c) to the inlet of the oil feed passage to the first centrifuge. A method characterized by the following.
する洗浄水の量が、０．０５乃至１０重量％、好ましく
は１乃至５重量％の範囲であることを特徴とする方法。2. The method according to claim 1, wherein the amount of washing water added in b) is in the range of 0.05 to 10% by weight, preferably 1 to 5% by weight.
浄水が、水、希釈した無毒の酸、及び塩類を含有する水
から成るグループから選択されることを特徴とする方
法。3. A method according to claim 1 or 2, characterized in that the wash water is selected from the group consisting of water, diluted non-toxic acids and water containing salts.
において、洗浄水が脱イオン水であることを特徴とする
方法。4. The method according to claim 1, wherein the wash water is deionized water.
において、洗浄水が希釈した無毒の酸、好ましくはクエ
ン酸であることを特徴とする方法。5. A method according to any one of claims 1 to 3, characterized in that the wash water is a diluted non-toxic acid, preferably citric acid.
浄水が随意の洗浄段階で生じたものであることを特徴と
する方法。6. A method according to claim 1 or 2, characterized in that the wash water is produced in an optional washing step.
において、ｂ）で得た混合物が、ホールディングタンク
に通される際に、１０秒乃至３０分間、好ましくは０．
５乃至１５分間保持されることを特徴とする方法。7. The method according to claim 1, wherein the mixture obtained in b) is passed through a holding tank for 10 seconds to 30 minutes, preferably 0.
A method characterized by being held for 5 to 15 minutes.
において、加工処理の間の温度が、６０乃至１１０℃、
好ましくは８０乃至１００℃の範囲であることを特徴と
する方法。8. The method according to claim 1, wherein the temperature during processing is 60 to 110 ° C.
The method is preferably in the range of 80 to 100 ° C.
において得られた脱ガム油。9. A degummed oil obtained by the method according to any one of claims 1 to 8.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP91105198 | 1991-04-02 | ||
| BE91105198.5EP | 1991-04-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH05117685A true JPH05117685A (en) | 1993-05-14 |
Family
ID=8206595
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4108595A Pending JPH05117685A (en) | 1991-04-02 | 1992-03-31 | Continuous degumming of triglyceride oil |
Country Status (13)
| Country | Link |
|---|---|
| EP (1) | EP0507363B1 (en) |
| JP (1) | JPH05117685A (en) |
| AT (1) | ATE89599T1 (en) |
| CA (1) | CA2063929A1 (en) |
| CZ (1) | CZ289672B6 (en) |
| DE (1) | DE69200004T2 (en) |
| DK (1) | DK0507363T3 (en) |
| ES (1) | ES2055634T3 (en) |
| HU (1) | HU212977B (en) |
| MX (1) | MX9201460A (en) |
| PL (1) | PL169760B1 (en) |
| RU (1) | RU2008328C1 (en) |
| SK (1) | SK279220B6 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2017112908A (en) * | 2015-12-24 | 2017-06-29 | 日清オイリオグループ株式会社 | Roasted oil and method for producing the same, edible fat and oil composition, and method for producing cooked product |
| WO2021124444A1 (en) * | 2019-12-17 | 2021-06-24 | 株式会社Ｉｈｉ原動機 | Degumming device for crude plant oil |
| WO2021124443A1 (en) * | 2019-12-17 | 2021-06-24 | 株式会社Ｉｈｉ原動機 | Power-generation system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0560121A3 (en) * | 1992-03-09 | 1994-07-27 | Vandemoortele Int Nv | Method for refining glyceride oil |
| EP0583648A3 (en) * | 1992-08-19 | 1995-02-01 | Vandemoortele Int Nv | Continuous refining process with reduced waste streams. |
| ID19109A (en) * | 1996-01-05 | 1998-06-18 | Grow Green Pty Ltd | PROTEIN RAW MATERIALS, COMPOSITIONS AND METHODS AND EQUIPMENT TO PRODUCE IT |
| WO1999002630A1 (en) * | 1997-07-09 | 1999-01-21 | Crystallisation And Degumming Sprl | Method for eliminating metals from fatty substances and gums associated with said metals |
| US6426423B1 (en) * | 1998-11-20 | 2002-07-30 | I.P. Holdings | Methods for treating phosphatide-containing mixtures |
| US6844458B2 (en) | 1998-11-20 | 2005-01-18 | Ip Holdings, L.L.C. | Vegetable oil refining |
| WO2003011873A2 (en) | 2001-07-27 | 2003-02-13 | Neptune Technologies & Bioressources Inc. | Natural marine source phospholipids comprising flavonoids, polyunsaturated fatty acids and their applications |
| WO2009132463A1 (en) * | 2008-05-02 | 2009-11-05 | Neptune Technologies & Bioressources Inc. | New deodorization method and organoleptic improvement of marine oil extracts |
| DE102008048009A1 (en) | 2008-09-19 | 2010-03-25 | Rmenergy Umweltverfahrenstechnik Gmbh | Device for decentralized processing of native oils and fat for the utilization as fuel or raw material for producing bio-diesel, has three containers, and three arrangements for feeding reaction starting material into containers |
| CN104434935B (en) | 2009-10-29 | 2019-07-16 | 阿卡斯蒂制药股份有限公司 | Concentrated therapeutic phospholipid composition |
| CN107011991B (en) * | 2017-04-12 | 2021-04-13 | 西北大学 | A kind of cation resin dephosphorization method of grease |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE507650A (en) * | ||||
| GB481580A (en) * | 1935-06-29 | 1938-03-11 | Sharples Specialty Co | Improvements in or relating to the treatment of fatty oils |
| FR1108998A (en) * | 1954-07-10 | 1956-01-19 | Separation Sa Franc Pour La | Improvements in the treatment of vegetable oils |
| MX7580E (en) * | 1981-10-15 | 1989-11-23 | Cpc International Inc | PROCEDURE FOR THE REFINING OF RAW VEGETABLE OILS |
| US4927544A (en) * | 1988-07-06 | 1990-05-22 | N.V. Vandemoortele International | Process for the continuous removal of a gum phase from triglyceride oil |
-
1992
- 1992-02-26 DK DK92200543.4T patent/DK0507363T3/en active
- 1992-02-26 DE DE9292200543T patent/DE69200004T2/en not_active Expired - Lifetime
- 1992-02-26 AT AT92200543T patent/ATE89599T1/en not_active IP Right Cessation
- 1992-02-26 EP EP92200543A patent/EP0507363B1/en not_active Expired - Lifetime
- 1992-02-26 ES ES92200543T patent/ES2055634T3/en not_active Expired - Lifetime
- 1992-03-25 CA CA002063929A patent/CA2063929A1/en not_active Abandoned
- 1992-03-31 MX MX9201460A patent/MX9201460A/en unknown
- 1992-03-31 CZ CS1992957A patent/CZ289672B6/en not_active IP Right Cessation
- 1992-03-31 SK SK957-92A patent/SK279220B6/en unknown
- 1992-03-31 JP JP4108595A patent/JPH05117685A/en active Pending
- 1992-04-01 PL PL92294068A patent/PL169760B1/en unknown
- 1992-04-01 HU HU9201094A patent/HU212977B/en not_active IP Right Cessation
- 1992-04-01 RU SU925011279A patent/RU2008328C1/en active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2017112908A (en) * | 2015-12-24 | 2017-06-29 | 日清オイリオグループ株式会社 | Roasted oil and method for producing the same, edible fat and oil composition, and method for producing cooked product |
| WO2021124444A1 (en) * | 2019-12-17 | 2021-06-24 | 株式会社Ｉｈｉ原動機 | Degumming device for crude plant oil |
| WO2021124443A1 (en) * | 2019-12-17 | 2021-06-24 | 株式会社Ｉｈｉ原動機 | Power-generation system |
Also Published As
| Publication number | Publication date |
|---|---|
| PL294068A1 (en) | 1992-12-14 |
| DE69200004T2 (en) | 1993-09-09 |
| SK279220B6 (en) | 1998-08-05 |
| CZ289672B6 (en) | 2002-03-13 |
| HU212977B (en) | 1997-01-28 |
| HU9201094D0 (en) | 1992-06-29 |
| ATE89599T1 (en) | 1993-06-15 |
| MX9201460A (en) | 1992-10-01 |
| HUT62646A (en) | 1993-05-28 |
| CA2063929A1 (en) | 1992-10-03 |
| EP0507363A1 (en) | 1992-10-07 |
| PL169760B1 (en) | 1996-08-30 |
| ES2055634T3 (en) | 1994-08-16 |
| CS95792A3 (en) | 1992-10-14 |
| DK0507363T3 (en) | 1993-08-30 |
| EP0507363B1 (en) | 1993-05-19 |
| RU2008328C1 (en) | 1994-02-28 |
| DE69200004D1 (en) | 1993-06-24 |
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