JPH0730355B2 - Method for separating fatty acids from crude oils and fats - Google Patents
Method for separating fatty acids from crude oils and fatsInfo
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- JPH0730355B2 JPH0730355B2 JP61008413A JP841386A JPH0730355B2 JP H0730355 B2 JPH0730355 B2 JP H0730355B2 JP 61008413 A JP61008413 A JP 61008413A JP 841386 A JP841386 A JP 841386A JP H0730355 B2 JPH0730355 B2 JP H0730355B2
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Description
【発明の詳細な説明】 発明の目的 （産業上の利用分野） 本発明は粗油脂類、特に、米ぬか油から脂肪酸を分離す
る方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION Object of the Invention (Field of Industrial Application) The present invention relates to a method for separating fatty acids from crude oils and fats, particularly rice bran oil.
（従来の技術） 従来、米ぬか油を原料にしてそこから脂肪酸を分離方法
として溶剤脱酸方法が周知である。この方法は米ぬか油
をｎ−ヘキサン、ｉ−プロピルアルコール及び／又はエ
チールアルコール、並びに苛性ソーダと混合した後、得
られた混合物を静置分離して軽比重層と重比重層の二液
に分離させるとともに、それらの中間にガム質を含有す
る中間層を形成させる工程を含んでいる。(Prior Art) Conventionally, a solvent deoxidizing method is well known as a method for separating fatty acids from rice bran oil as a raw material. In this method, rice bran oil is mixed with n-hexane, i-propyl alcohol and / or ethyl alcohol, and caustic soda, and the resulting mixture is allowed to stand to separate into two liquids, a light specific gravity layer and a heavy specific gravity layer. And the step of forming an intermediate layer containing a gum in the middle thereof.
又、この方法は前記重比重層に硫酸を添加して石ケン液
を酸分解した後、そのまま蒸溜に処している（特公昭50
−19567号公報他）。Also, in this method, sulfuric acid is added to the above-mentioned specific gravity layer to decompose the soap solution with acid, and then directly subjected to distillation (Japanese Patent Publication No. Sho 50).
-19567, etc.).
（発明が解決しようとする問題点） この方法によると、ある程度収率よく粗油脂類から脂肪
酸が分離される。(Problems to be Solved by the Invention) According to this method, fatty acids are separated from crude fats and oils with a good yield to some extent.
しかしながら、この方法は次の問題を有している。However, this method has the following problems.
第一は、この方法は溶剤を多く使用するという問題であ
る。The first is that this method uses a lot of solvent.
溶剤の使用量が多いと、米ぬか油と苛性ソーダとの接触
反応時に多くのエネルギーを要するばかりでなく、溶剤
回収のためにも多くのエネルギーを必要とし、さらに、
溶剤を貯留させたり循環させたりするために過大な設備
を必要する。従って、前記周知の方法は省エネルギー、
省資源という観点から改良が必要である。If the amount of solvent used is large, not only a large amount of energy is required during the catalytic reaction between rice bran oil and caustic soda, but also a large amount of energy is required for solvent recovery.
Excessive equipment is required to store and circulate the solvent. Therefore, the known method is energy saving,
Improvement is necessary from the viewpoint of resource saving.
第二は、酸分解液から脂肪酸を分離するのに使用される
装置、例えば、蒸溜装置が腐蝕し易いという問題であ
る。Secondly, there is a problem that a device used for separating a fatty acid from an acid decomposition liquid, for example, a distillation device is easily corroded.
本発明の目的は粗油脂類からの脂肪酸の分離収率を高く
維持しながら、溶剤の使用量が低減させることが可能な
脂肪酸の分離方法を確立するとともに、装置の腐蝕を軽
減し得る脂肪酸の分離方法を確立することにある。The object of the present invention is to establish a method for separating fatty acids that can reduce the amount of solvent used while maintaining a high separation yield of fatty acids from crude oils and fats that can reduce the corrosion of equipment. Establishing a separation method.
発明の構成 （問題点を解決するための手段） 本発明は前記の目的を達成するために、脱ガム処理がさ
れた粗油脂類100重量部に対して30〜100重量部の割合の
ｎ−ヘキサン並びに前記粗油脂類における酸価の0.5〜
２重量倍に相当するエチルアルコール、同じく0.5〜２
重量倍に相当する水及び同じく0.07〜0.15重量倍に相当
する苛性ソーダの混合を行なう混合工程と、 前記混合の後、10分以内に該混合工程で得られた混合物
を遠心分離機に通して強制的に液・液の二層に分離する
遠心分離工程と、 前記遠心分離工程で得られた重比重層を酸分解する酸分
解工程と、 該酸分解工程で得られた酸分解物をｎ−ヘキサンの共存
下で静置分離する静置分離工程と、 該静分離工程で得られた重比重層に苛性ソーダを添加し
た後、その重比重層からエチルアルコールを分離するア
ルコール分離工程と、軽比重層をｎ−ヘキサンと脂肪酸
とに分離するｎ−ヘキサン分離工程と からなる方法を採用する。Structure of the Invention (Means for Solving Problems) In order to achieve the above-mentioned object, the present invention has a ratio of 30 to 100 parts by weight of n- with respect to 100 parts by weight of degummed crude fats and oils. Hexane and the crude oils and fats having an acid value of 0.5 to
Ethyl alcohol equivalent to 2 times by weight, 0.5-2
A mixing step of mixing water equivalent to a weight ratio and caustic soda equivalent to 0.07 to 0.15 weight ratio, and after the mixing, the mixture obtained in the mixing step is forced through a centrifuge within 10 minutes. A centrifuge step of separating the liquid / liquid into two layers, an acid decomposing step of acid decomposing the polypyrroleum layer obtained in the centrifuge step, and an acid decomposing product obtained in the acid decomposing step by A static separation step of static separation in the presence of hexane, an alcohol separation step of separating ethyl alcohol from the gravity layer after adding caustic soda to the gravity layer obtained in the static separation step, and a light specific gravity An n-hexane separation step of separating the layer into n-hexane and fatty acid is adopted.
（作用） 本発明においては粗油脂類と溶媒としてのｎ−ヘキサ
ン、エチルアルコール及び粗油脂類中の遊離脂肪酸のケ
ン化に必要な苛性ソーダとの混合が行なわれる。(Function) In the present invention, crude fats and oils are mixed with n-hexane as a solvent, ethyl alcohol, and caustic soda necessary for saponification of free fatty acids in the crude fats and oils.
得られた混合物は前記の混合が完了してから10分以内と
いう短い時間に遠心分離機に通され、強制的に液・液の
二層に分離される。粗油脂類とエチルアルコールと接触
時間が短いのでエステルがほとんど副生しない。The obtained mixture is passed through a centrifuge for a short time within 10 minutes after the above mixing is completed, and is forcibly separated into two layers of liquid and liquid. Since the contact time between crude oil and fat and ethyl alcohol is short, almost no ester is by-produced.
さらに、混合物中には実質上ガム質が含まれておらず、
又、遠心分離という強制的分離手段が採用されているの
で、前記混合物は容易に二層に分離し、ｎ−ヘキサン・
脱酸油溶液と、含水エチールアルコール・石けん溶液と
に分離する。そのため、溶媒の使用量が少なくてもよく
なる。Furthermore, the mixture contains substantially no gum,
Moreover, since a forced separation means called centrifugation is adopted, the mixture is easily separated into two layers, and n-hexane.
Separate into a deoxidized oil solution and a hydrous ethyl alcohol / soap solution. Therefore, the amount of solvent used may be small.
本発明においては酸分解して得られた生成物がｎ−ヘキ
サンの共存下で静置分離され、重比重層が得られる。こ
の重比重層は苛性ソーダの添加によりpH調整されるの
で、その重比重層をその後分離装置に供給してもその装
置は腐蝕しない。In the present invention, the product obtained by acid decomposition is allowed to stand and separate in the coexistence of n-hexane to obtain a specific gravity layer. Since the pH of this specific gravity layer is adjusted by the addition of caustic soda, even if the specific gravity layer is subsequently supplied to the separation device, the device will not be corroded.
（実施例） 本発明の前提構成を第一図に基づいて説明する。(Example) The premise structure of the present invention will be described with reference to FIG.
公知の方法により脱ガム処理された酸価が24の米ぬか油
100重量部をそれぞれ貯槽１から、そして、ｎ−ヘキサ
ン50重量部をその貯槽２からそれぞれ撹拌槽３に供給し
て、それを撹拌下で脱ガム米ぬか油・ミセラを調整し
た。Rice bran oil with an acid value of 24 degummed by a known method
100 parts by weight of each was supplied from the storage tank 1 and 50 parts by weight of n-hexane was supplied from each of the storage tanks 2 to the stirring tank 3 to prepare degummed rice bran oil / miscella under stirring.
又、含水率５重量％のエチルアルコール100重量部をそ
の貯槽４から、そして、水100重量部をその貯槽５から
それぞれ撹拌槽６に供給して含水率50重量％の含水エチ
ルアルコール溶液を調整した。Further, 100 parts by weight of ethyl alcohol having a water content of 5% by weight is supplied from the storage tank 4 and 100 parts by weight of water is supplied from the storage tank 5 to the stirring tank 6 to prepare a water-containing ethyl alcohol solution having a water content of 50% by weight. did.
さらに、水100重量部を前記貯槽５から撹拌槽８に供給
し、そして、25重量部の苛性ソーダの顆粒７を撹拌槽８
に供給して含水率75重量％の苛性ソーダ水溶液を調整し
た。Further, 100 parts by weight of water is supplied from the storage tank 5 to the stirring tank 8, and 25 parts by weight of the caustic soda granules 7 are stirred.
Was supplied to prepare a caustic soda aqueous solution having a water content of 75% by weight.
次に、前記各撹拌槽３、６、８から前記脱ガム米ぬか油
・ミセラ、含水エチルアルコール及び苛性ソーダ水溶液
をそれぞれポンプ９によって、米ぬか油100重量部につ
きｎ−ヘキサンが50重量部の割合になるように、そして
前記粗油脂の酸価に対してのエチルアルコールが１重量
倍の量に相当し、水が１重量倍の量に相当し、さらに、
苛性ソーダが0.09重量倍の量に相当するように連続的に
混合槽10に供給した。Next, the degummed rice bran oil / miscella, hydrous ethyl alcohol and caustic soda aqueous solution are respectively pumped from the respective stirring tanks 3, 6 and 8 by a pump 9 at a ratio of 50 parts by weight of n-hexane per 100 parts by weight of rice bran oil. In addition, and corresponding to the acid value of the crude oil and fat, the amount of ethyl alcohol is 1 times by weight, the amount of water is 1 times by weight, and
Caustic soda was continuously supplied to the mixing tank 10 in an amount corresponding to 0.09 times by weight.
そして、前記混合槽10を50℃に加熱して前記脱ガム米ぬ
か油・ミセラ、含水エチルアルコール及び苛性ソーダ水
溶液を撹拌下で混合した（混合工程Ａ）。Then, the mixing tank 10 was heated to 50 ° C., and the degummed rice bran oil / miscella, hydrous ethyl alcohol and caustic soda aqueous solution were mixed under stirring (mixing step A).
この混合槽10で得られた混合物を同混合槽10の液面に設
けられた溢流管11から溢流させて、同溢流管11の上部開
口部から3m離れている遠心分離機12（溢流管11の長さは
0.5mである）に連続的に供給した。The mixture obtained in this mixing tank 10 is caused to overflow from an overflow pipe 11 provided on the liquid surface of the mixing tank 10, and a centrifugal separator 12 (3 m apart from the upper opening of the overflow pipe 11 ( The length of the overflow pipe 11 is
0.5 m) was continuously fed.
前記混合槽10への供給量及び同混合槽10の容量、前記溢
流管11内を溢流する流量及び前記溢流管11の長さ等から
前記脱ガム米ぬか油・ミセラ、含水エチルアルコール及
び苛性ソーダ水溶液の接触時間を算出したら約20秒であ
った。The degummed rice bran oil / miscella, hydrous ethyl alcohol and the amount supplied to the mixing tank 10 and the capacity of the mixing tank 10, the flow rate of overflow in the overflow pipe 11, the length of the overflow pipe 11, etc. The contact time of the caustic soda solution was calculated to be about 20 seconds.
次に、前記混合物を遠心分離機12に供給して軽比重層と
重比重層の二液に分離させたが、前記軽比重層は遊離の
脂肪酸が除去された脱酸油とｎ−ヘキサンとからなる、
いわゆる脱酸油・ミセラであり、前記重化重層は含水エ
チルアルコールと石ケンとの溶液であった（遠心分離工
程Ｂ）。Next, the mixture was supplied to a centrifuge 12 and separated into two liquids, a light specific gravity layer and a heavy specific gravity layer. The light specific gravity layer contained deoxidized oil from which free fatty acids were removed and n-hexane. Consists of,
It was a so-called deoxidized oil / miscella, and the above-mentioned superposed layer was a solution of hydrous ethyl alcohol and soap (centrifugation step B).
脱酸油・ミセラは貯槽13に移され、次いで、蒸溜装置
（図示なし）によりｎ−ヘキサンと脱酸油とに分離され
た。脱酸油の収率は86.5％であった。The deoxidized oil / miscella was transferred to a storage tank 13 and then separated into n-hexane and deoxidized oil by a distillation device (not shown). The yield of deoxidized oil was 86.5%.
他方、重比重層はポンプ15によって酸分解槽14に移送さ
れ、貯槽16からの硫酸と混合され、石ケンが分解された
（酸分解工程Ｃ）。On the other hand, the specific gravity layer was transferred to the acid decomposition tank 14 by the pump 15 and mixed with the sulfuric acid from the storage tank 16 to decompose soap (acid decomposition step C).
該酸分離工程Ｃで得られた酸分解物は公知の溶媒分離工
程Ｅにより脂肪酸と含水エチルアルコールとに分離され
た。脂肪酸の収率は13.5％で、粗油脂類の酸価が低い割
には高い値であった。The acid decomposition product obtained in the acid separation step C was separated into fatty acid and hydrous ethyl alcohol by a known solvent separation step E. The yield of fatty acids was 13.5%, which was high despite the low acid value of crude oils and fats.
このようにして本発明が実施され、粗米ぬか油中から脂
肪酸を分離することができた。Thus, the present invention was carried out, and fatty acids could be separated from crude rice bran oil.
上記のように構成される本発明に係る実施例において
は、次の効果が発揮される。The following effects are exerted in the embodiment of the present invention configured as described above.
実質上ガム質が含有されていない粗米ぬか油が使用され
ているので、脱ガム米ぬか油・ミセラ、含水エチルアル
コール及び苛性ソーダ水溶液の混合後に得られた混合物
を遠心分離機12で処理しても中間層が形成されずに、前
記混合物は重比重層と軽比重層の二液に分離する。Since crude rice bran oil containing substantially no gum is used, even if the mixture obtained after mixing degummed rice bran oil / miscella, hydrous ethyl alcohol and caustic soda solution is treated with a centrifuge 12, it is intermediate. Without forming a layer, the mixture separates into two parts, a heavy layer and a light layer.
そのため、遠心分離機12により前記混合物が容易に重比
重層と軽比重層とに分離し、重比重層に中性油がほとん
ど溶解していないので、脱酸収率は理論値に近い値とな
る。又、軽比重層には石ケン分がほとんど含まれないの
で、水洗して石ケン分を洗浄除去する必要がなくなり、
洗浄排水設備を設ける必要もなくなる。Therefore, the mixture is easily separated into a heavy specific gravity layer and a light specific gravity layer by the centrifugal separator 12, since the neutral oil is hardly dissolved in the heavy specific gravity layer, the deoxidation yield is close to the theoretical value. Become. Also, since the light specific gravity layer contains almost no soap components, there is no need to wash and remove soap components with water,
There is no need to install a cleaning drainage system.
又、脱ガム米ぬか油・ミセラ、含水エチルアルコール及
び苛性ソーダ水溶液の接触時間が20秒と短いので、中性
油のケン化物がエチルアルコールと反応してエステルに
なる量は少ない。Further, since the contact time of degummed rice bran oil / miscella, hydrous ethyl alcohol and aqueous caustic soda solution is as short as 20 seconds, the saponification product of neutral oil reacts with ethyl alcohol to form an ester in a small amount.
30℃において前記接触時間とともにどの程度エステルが
生成するかを実験したところ、第２図に示すように約10
分を経過すると急激にケン化分解率が上昇し、接触時間
が１分以下、特に、40秒以下になるとエステルのケン化
分解率が極めて低くなった。An experiment was conducted to find out how much ester was formed with the contact time at 30 ° C.
After a lapse of minutes, the saponification decomposition rate rapidly increased, and when the contact time was 1 minute or less, particularly 40 seconds or less, the saponification decomposition rate of the ester was extremely low.
又、この実施例に使用されるｎ−ヘキサンの使用量は従
来の方法に比較して少なく、約1/4〜1/6でよいという効
果が発揮される。そのため、溶媒を蒸溜・回収するため
の熱エネルギーが少なくなる。さらに、溶媒を貯えた
り、循環したりするための設備容量又は能力を少なくで
きるので、省資源化が可能になるという附随した効果も
発揮される。Further, the amount of n-hexane used in this example is smaller than that in the conventional method, and about 1/4 to 1/6 is sufficient. Therefore, the heat energy for distilling and recovering the solvent is reduced. Furthermore, since the equipment capacity or capacity for storing or circulating the solvent can be reduced, an accompanying effect that resource saving can be achieved is also exhibited.
次に、本発明の要部構成を第３図に基づいて説明する。Next, the configuration of the main part of the present invention will be described with reference to FIG.
前記実施例では酸分解工程で得た酸分解物を公知の方法
に従ってエチルアルコールと脂肪酸とに分離する手段が
採用されたが、この実施例では前記手段として特定の分
離手段を採用しようとするものである。In the above-mentioned embodiment, the means for separating the acid decomposition product obtained in the acid decomposition step into ethyl alcohol and fatty acid according to a known method was adopted, but in this embodiment, a specific separation means is adopted as the means. Is.
第３図に示すように前記実施例と同じ工程を経由し、し
かも同じ条件で米ぬか油を原料にして酸分解までの工程
を実施した（混合工程Ａ、遠心分離工程Ｂ、酸分解工程
Ｃ）。As shown in FIG. 3, the steps up to the acid decomposition were carried out using the rice bran oil as a raw material under the same conditions as the above-mentioned example (mixing step A, centrifugation step B, acid decomposition step C). .
ただし、この実施例では貯槽２からｎ−ヘキサンを酸分
解工程Ｃに供給してｎ−ヘキサンの共存下で酸分解を実
施した。このとき、ｎ−ヘキサンの共存量は重比重層10
0重量部につき100重量部であった。However, in this example, n-hexane was supplied from the storage tank 2 to the acid decomposition step C to carry out acid decomposition in the coexistence of n-hexane. At this time, the coexisting amount of n-hexane is 10
It was 100 parts by weight per 0 parts by weight.
次に、前記酸分解工程Ｃで得られた酸分解物を静置分離
器18に供給し、重比重層と軽比重層とに分離させた（静
置分離工程Ｄ）。Next, the acid decomposition product obtained in the acid decomposition step C was supplied to the static separator 18 to separate it into a heavy specific gravity layer and a light specific gravity layer (static separation step D).
そして、静置分離器18の重比重層を中和槽19に供給する
とともに、重比重層のpH調整をするために貯槽８から苛
性ソーダ水溶液を前記中和槽19に添加した。Then, the specific gravity layer of the stationary separator 18 was supplied to the neutralization tank 19, and the caustic soda aqueous solution was added to the neutralization tank 19 from the storage tank 8 in order to adjust the pH of the specific gravity layer.
このpH調整されたエチルアルコール溶液を貯槽20に抜き
出し、次いで、蒸溜装置に供給してエチルアルコールを
回収した（アルコール分離工程E2）。The pH-adjusted ethyl alcohol solution was extracted into the storage tank 20, and then supplied to a distillation apparatus to recover ethyl alcohol (alcohol separation step E 2 ).
他方、軽比重層を貯槽17に抜き出し、次いで、蒸溜装置
に供給して軽比重層を脂肪酸とｎ−ヘキサンとに分離
し、脂肪酸を得た（ｎ−ヘキサン分離工程E1）。On the other hand, the light specific gravity layer was extracted into a storage tank 17, and then fed to a distillation apparatus to separate the light specific gravity layer into fatty acid and n-hexane to obtain a fatty acid (n-hexane separation step E 1 ).
このようにして、本発明により米ぬか油から脂肪酸を分
離することが可能になった。In this way, the invention makes it possible to separate fatty acids from rice bran oil.
本発明の要部構成により次の効果が発揮される。The following effects are exhibited by the main part configuration of the present invention.
静置分離工程Ｄで脂肪酸をｎ−ヘキサン側に移行させて
から蒸溜しているので脂肪酸の収率が向上する。Since the fatty acids are transferred to the n-hexane side in the stationary separation step D and then distilled, the yield of fatty acids is improved.
又、アルコール分離工程E2では酸分解物を静置分離して
得られた軽比重層がpH調整された後、蒸溜されるので、
その蒸溜に使用されている装置の腐蝕を抑制することが
できる。Further, in the alcohol separation step E 2 , the light specific gravity layer obtained by statically separating the acid decomposition product is subjected to pH adjustment and then distilled,
Corrosion of the device used for the distillation can be suppressed.
本発明は前記実施例に限定されることなく、次の態様で
実施することができる。The present invention is not limited to the above embodiments and can be implemented in the following modes.
（１）油脂類としては脂肪酸を含有する種々の油脂を使
用することができる。特に、本発明ではエチルアルコー
ルが使用されているので、食用に供される植物油を使用
することができる。(1) As fats and oils, various fats and oils containing a fatty acid can be used. In particular, since ethyl alcohol is used in the present invention, edible vegetable oil can be used.
（２）ｎ−ヘキサンの使用量は油脂類100重量部につき3
0〜100重量部の割合で使用される。ｎ−ヘキサンの使用
量が30重量部より少ないと中性油の収率が低下し、又、
100重量部より多くなると溶媒の使用量を低減させるこ
とによる効果が顕著に現れない。(2) The amount of n-hexane used is 3 per 100 parts by weight of fats and oils.
It is used in a proportion of 0 to 100 parts by weight. If the amount of n-hexane used is less than 30 parts by weight, the yield of neutral oil decreases, and
If the amount is more than 100 parts by weight, the effect of reducing the amount of the solvent used is not significant.
（３）エチールアルコールは油脂類の酸価の0.5〜２重
量倍、水は同じく0.5〜２重量倍に相当する範囲で使用
される。前記範囲を外れると、収率が低下したり、溶媒
の使用量を低減させることによる効果が顕著に現れな
い。(3) Ethyl alcohol is used in a range corresponding to 0.5 to 2 times by weight the acid value of fats and oils, and water is used in a range corresponding to 0.5 to 2 times by weight. When the amount is out of the above range, the yield is lowered, and the effect of reducing the amount of the solvent used is not remarkable.
苛性ソーダの使用量は粗油脂類の酸価から算出される理
論量よりわずかに多い量であるが、この値は酸価を基準
にして0.07〜0.15重量倍の範囲が好ましい。The amount of caustic soda used is slightly larger than the theoretical amount calculated from the acid value of crude oils and fats, but this value is preferably in the range of 0.07 to 0.15 times by weight based on the acid value.
（４）本発明は混合時間を10分以内、好ましく１分、さ
らに好ましくは40秒以内にする限り回分法でも実施する
ことができるが、接触時間の制御が容易であるという観
点からは連続法が採用される。(4) The present invention can be carried out by a batch method as long as the mixing time is within 10 minutes, preferably 1 minute, more preferably within 40 seconds, but from the viewpoint of easy control of contact time, it is a continuous method. Is adopted.
（５）実施例では種々の貯槽を設けるようにしたが、必
要に応じてそれらをなくした工程にすることもできる。(5) Although various storage tanks are provided in the embodiment, they may be eliminated if necessary.
（６）混合工程における温度はケン化を促進するに足り
る範囲の温度あればよく、例えば、20〜50℃に維持され
る。(6) The temperature in the mixing step may be a temperature within a range sufficient to promote saponification, and is maintained at, for example, 20 to 50 ° C.
発明の効果 以上詳述したように、本発明は粗油脂類から脂肪酸を分
離する方法において高い収率を維持しながら、溶媒の使
用量を少なくすることができるという優れた効果を発揮
する。Effects of the Invention As described in detail above, the present invention exhibits an excellent effect that the amount of solvent used can be reduced while maintaining a high yield in the method for separating fatty acids from crude oils and fats.
又、本発明は溶媒分離装置の腐蝕を低減させることがで
きるという優れた効果を発揮する。Further, the present invention exerts an excellent effect that the corrosion of the solvent separation device can be reduced.
第１図は前提構成の工程図、第２図は接触時間と中性油
のケン化分解率との関係を示す線図、第３図は全実施例
の工程図である。 Ａ……混合工程、Ｂ……遠心分離工程、Ｃ……酸分解工
程、Ｄ……静置分離工程、E1……ｎ−ヘキサン分離工
程、E2……アルコール分離工程、12……遠心分離機FIG. 1 is a process diagram of a premise structure, FIG. 2 is a diagram showing the relationship between contact time and saponification decomposition rate of neutral oil, and FIG. 3 is a process diagram of all examples. A ...... mixing step, B ...... centrifugation step, C ...... acid degradation step, D ...... standing separation step, E 1 ...... n-hexane separation step, E 2 ...... alcohol separation step, 12 ...... centrifugal Separator
Claims (1)
0重量部に対して30〜10重量部の割合のｎ−ヘキサン並
びに前記粗油脂類における酸価の0.5〜２重量倍に相当
するエチルアルコール、同じく0.5〜２重量倍に相当す
る水及び同じく0.07〜0.15重量倍に相当する苛性ソーダ
の混合を行う混合工程Ａと、 （ロ）該混合の後、10分以内に該混合工程Ａで得られた
混合物を遠心分離機（12）に通して強制的に液・液の二
層に分離する遠心分離工程Ｂと、 （ハ）該遠心分離工程Ｂで得られた重比重層を酸分解す
る酸分解工程Ｃと、 （ニ）該酸分解工程Ｃで得られた酸分解物をｎ−ヘキサ
ンの共存下で静置分離する静置分離工程Ｄと、 （ホ）該静置分離工程Ｄで得られた重比重層に苛性ソー
ダを添加した後、その重比重層からエチルアルコールを
分離するアルコール分離工程E2と、軽比重層を脂肪酸と
ｎ−ヘキサンとに分離するｎ−ヘキサン分離工程E1と からなることを特徴とする粗油脂類から脂肪酸を分離す
る方法。1. (a) Crude oils and fats that have been degummed 10
30 parts by weight to 0 parts by weight of n-hexane, ethyl alcohol corresponding to 0.5 to 2 times the acid value of the crude oil and fats, water equivalent to 0.5 to 2 parts by weight and 0.07 parts of the same. Mixing step A in which caustic soda equivalent to 0.15 weight times is mixed, and (b) after the mixing, the mixture obtained in the mixing step A is forced to pass through a centrifuge (12) within 10 minutes. In the centrifugal separation step B for separating the liquid / liquid into two layers, (c) the acid decomposition step C for acid-decomposing the multi-specific gravity layer obtained in the centrifugation step B, and (d) the acid decomposition step C. The stationary decomposition step D in which the obtained acid decomposition product is stationary separated in the coexistence of n-hexane, and (e) after adding caustic soda to the specific gravity layer obtained in the stationary separation step D, alcohol separation step E 2 separating the ethyl alcohol from the specific gravity layer, a fatty acid a light specific gravity layer n- hexane Method of separating the fatty acids that consist separated into a down n- hexane separation step E 1 Metropolitan from crude oils, characterized.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61008413A JPH0730355B2 (en) | 1986-01-17 | 1986-01-17 | Method for separating fatty acids from crude oils and fats |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61008413A JPH0730355B2 (en) | 1986-01-17 | 1986-01-17 | Method for separating fatty acids from crude oils and fats |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62167397A JPS62167397A (en) | 1987-07-23 |
| JPH0730355B2 true JPH0730355B2 (en) | 1995-04-05 |
Family
ID=11692454
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61008413A Expired - Lifetime JPH0730355B2 (en) | 1986-01-17 | 1986-01-17 | Method for separating fatty acids from crude oils and fats |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0730355B2 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4568565B2 (en) * | 2004-09-17 | 2010-10-27 | 花王株式会社 | Method for producing fats and oils with reduced free fatty acids |
| JP2006279008A (en) * | 2005-03-02 | 2006-10-12 | Ushio Inc | Heater and heating device provided with heater |
| JP2009238552A (en) * | 2008-03-27 | 2009-10-15 | Ushio Inc | Filament lamp |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50103506A (en) * | 1974-01-23 | 1975-08-15 | ||
| JPS5318715A (en) * | 1976-08-04 | 1978-02-21 | Hideki Ishihara | Simultaneous separation of neutral lipid * fatty acid and phenols from rice bran oil * rice embryo oil and their treated oil and apparatus |
| JPS5318605A (en) * | 1976-08-04 | 1978-02-21 | Hideki Ishihara | Method and apparatus for separating recovering simultaneousely neutral oil* fatty acid and phenolic substrate from rice bran* rice germ oil or treating oil thereof |
| JPS5337698A (en) * | 1976-09-17 | 1978-04-06 | Hideki Ishihara | Method and apparatus for separately recovering neutral oil * aliphatic acid and phenolic substance from rice bran * rice germ and treated oil thereof |
| JPS5337699A (en) * | 1976-09-17 | 1978-04-06 | Hideki Ishihara | Method and apparatus for separately recovering neutral oil * aliphatic acid and phenolic substance from rice bran * rice germ and treated oil thereof |
-
1986
- 1986-01-17 JP JP61008413A patent/JPH0730355B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62167397A (en) | 1987-07-23 |
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