JP2010284133A - Method for producing purified sugar solution - Google Patents
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Abstract
Description
本発明は精製糖液の製造方法に関するものである。 The present invention relates to a method for producing a purified sugar solution.
固形分を含有する原料糖液から当該固形分を除去して精製糖液を製造する方法として、糖液をダイアフィルトレーション濾過して濃縮液と透過液とに分離し、得られた濃縮液をプレコート濾過する方法が知られている（特許文献１）。しかしながら、プレコート濾過を採用した方法では、大量のプレコート廃材が産業廃棄物として排出されるため、その搬送および処理コストの負担が大きいという欠点がある。 As a method of producing a purified sugar liquid by removing the solid content from the raw sugar liquid containing solids, the sugar liquid is diafiltered and separated into a concentrated liquid and a permeated liquid, and the resulting concentrated liquid There is known a method of pre-coating the solution (Patent Document 1). However, the method employing precoat filtration has a drawback that a large amount of precoat waste material is discharged as industrial waste, so that the burden of the transportation and processing costs is large.
本発明は、上記実情に鑑みなされたものであり、その目的は、産業廃棄物の量を著しく減容化でき、しかも、操作性および収率に優れた精製糖液の製造方法を提供することにある。 The present invention has been made in view of the above circumstances, and an object of the present invention is to provide a method for producing a refined sugar solution that can significantly reduce the amount of industrial waste and that is excellent in operability and yield. It is in.
本発明者らは、上記の目的を達成すべく鋭意検討を重ねた結果、膜濾過システムによる濾過とフィルタープレスによる圧搾とを巧みに組み合せることにより、上記の目的を容易に達成し得るとの知見を得、本発明の完成に至った。 As a result of intensive studies to achieve the above object, the present inventors can easily achieve the above object by skillfully combining filtration by a membrane filtration system and pressing by a filter press. Knowledge was obtained and the present invention was completed.
すなわち、本発明の要旨は、固形分を含有する原料糖液から当該固形分を除去して精製糖液を製造するに当り、先ず、連続式または回分式の膜濾過システムに原料糖液を供給し、以下の式（Ｉ）に定義する濃縮倍率が１０〜６０倍の条件下で濾過を行って濃縮液と透過液とに分離し、次いで、フィルタープレスにて上記の濃縮液を圧搾して当該濃縮液から糖液を回収することを特徴とする精製糖液の製造方法に存する。
［数１］
濃縮倍率＝供給液量／（供給液量−透過液量）・・・（Ｉ）
That is, the gist of the present invention is to supply a raw sugar solution to a continuous or batch-type membrane filtration system in order to produce a purified sugar solution by removing the solid content from the raw sugar solution containing solids. Then, filtration is carried out under the condition that the concentration ratio defined in the following formula (I) is 10 to 60 times to separate into a concentrate and a permeate, and then the above concentrate is squeezed with a filter press. The present invention resides in a method for producing a purified sugar solution, wherein the sugar solution is recovered from the concentrated solution.
[Equation 1]
Concentration magnification = Supply solution amount / (Supply solution amount−Permeate solution amount) (I)
本発明によれば、産業廃棄物の量を著しく減容化でき、しかも、操作性および収率に優れた精製糖液の製造方法が提供される。 ADVANTAGE OF THE INVENTION According to this invention, the quantity of industrial waste can be reduced significantly and the manufacturing method of the refined sugar liquid excellent in operativity and yield is provided.
本発明において、原料糖液としては、デンプン糖、甜菜糖、甘蔗糖、甘藩糖および多糖類の溶液である糖液などが挙げられる。これらの原料糖液には固形分が含有されており、従って、当該固形分を除去することによりブドウ糖やその異性化糖の精製糖液が得られる。例えば、ブドウ糖の場合、原料デンプン（コーンスターチ等）を酵素液化した後、酵素糖化してブドウ糖溶液（糖液）を製造するが、この糖液中には、コーン等の原料由来の固形分が混入している。この固形分は、マッドと呼ばれ、蛋白質、脂質、繊維質などから成っている。このマッドを除去することにより、精製糖液が得られる。 In the present invention, examples of the raw sugar solution include a sugar solution which is a solution of starch sugar, sugar beet sugar, sugarcane sugar, sugarcane sugar and polysaccharides. These raw sugar solutions contain solids, and therefore, a purified sugar solution of glucose or its isomerized sugar can be obtained by removing the solids. For example, in the case of glucose, raw material starch (such as corn starch) is liquefied with an enzyme, and then saccharified to produce a glucose solution (sugar solution). is doing. This solid content is called mud and is composed of protein, lipid, fiber and the like. By removing this mud, a purified sugar solution is obtained.
先ず、本発明においては、連続式または回分式の膜濾過システムに原料糖液を供給し、濾過を行って濃縮液と透過液とに分離する。 First, in the present invention, the raw sugar solution is supplied to a continuous or batch membrane filtration system, and filtration is performed to separate the concentrate and the permeate.
上記の膜濾過システムの膜としては、一般に、限外濾過（ＵＦ）膜または精密濾過（ＭＦ）膜が使用されるが、ＭＦ膜が好適である。また、膜素材としては、テフロン（登録商標）、ポリスルホン、セラミック、金属など使用される。 As the membrane of the membrane filtration system, an ultrafiltration (UF) membrane or a microfiltration (MF) membrane is generally used, but an MF membrane is preferred. As the membrane material, Teflon (registered trademark), polysulfone, ceramic, metal, or the like is used.
また、膜濾過装置としては、膜を振動させることにより、膜表面付近の流体に大きな剪断力を与えることの出来る振動膜分離装置を使用することも出来る。斯かる振動膜分離装置の市販品としては、例えば、米国のＮＥＷ ＬＯＧＩＣ ＲＥＳＥＡＲＣＨ，ＩＮＣ製の「ＶＳＥＰ Ｓｅｒｉｅｓ Ｌ／Ｐ」が挙げられる。また、膜を回転させる膜分離装置を使用することも出来る。斯かる膜分離装置としては、例えば、株式会社日立プラントテクノロジー製の「回転平膜分離装置」が挙げられる。 In addition, as the membrane filtration device, a vibrating membrane separation device that can apply a large shearing force to the fluid near the membrane surface by vibrating the membrane can be used. As a commercial item of such a diaphragm separation apparatus, for example, “VSEP Series L / P” manufactured by NEW LOGIC RESEARCH, INC. Of the United States can be cited. A membrane separation device that rotates the membrane can also be used. As such a membrane separator, for example, a “rotary flat membrane separator” manufactured by Hitachi Plant Technologies, Ltd. may be mentioned.
通液方式による濾過の種類としては、クロスフロー（連続式）又はデッドエンド（回分式）の何れでもよい。クロスフロー濾過法は、原理的には、膜フィルター表面に濾過対象液を平行に流しながら濾過を行い、平行流によるせん断力により堆積ケーク層を最小に保持する濾過法であり、従って、濾過膜に包囲された流路の一端から供給された濾過対象液（原液）は、流れながら濾過され、濾液は、濾過膜を通過して流路と直交する方向に排出され、濃縮液は、流路の一端から排出される。 The type of filtration by the liquid flow method may be either crossflow (continuous type) or dead end (batch type). In principle, the cross-flow filtration method is a filtration method that performs filtration while flowing the liquid to be filtered on the surface of the membrane filter in parallel, and keeps the deposited cake layer to a minimum by the shear force due to the parallel flow. The liquid to be filtered (raw solution) supplied from one end of the flow path surrounded by the liquid is filtered while flowing, the filtrate passes through the filtration membrane and is discharged in a direction perpendicular to the flow path, and the concentrated liquid is flowed It is discharged from one end.
本発明において、前記の濾過は、以下の式（Ｉ）に定義する濃縮倍率が１０〜６０倍の条件下で行う必要がある。 In the present invention, the filtration needs to be performed under the condition that the concentration factor defined in the following formula (I) is 10 to 60 times.
［数２］
濃縮倍率＝供給液量／（供給液量−透過液量）・・・（Ｉ）
[Equation 2]
Concentration magnification = Supply solution amount / (Supply solution amount−Permeate solution amount) (I)
膜濾過システムにおける濃縮倍率が１０倍未満の場合は、フィルタープレスにて濃縮液を圧搾する際に固形分が十分に捕捉される透明な糖液を回収することが出来ない。その理由は、膜濾過システムにおける濾過の際に濃縮倍率が高くなるに従って濃縮液中の固形分が徐々に凝集すると考えられるが、濃縮倍率が１０倍未満の場合は、凝集体（フロック）が十分な大きさにまで成長していないことによるためと推測される。一方、膜濾過システムにおける濃縮倍率が６０倍超過の場合は、濃縮液の粘性が高くなり過ぎて膜濾過システムの操作性が低下する。すなわち、濾過効率が低下し濾過圧力が高くなる。膜濾過システムにおける濃縮倍率の好ましい範囲は２０〜５０倍である。膜濾過システムの運転条件は特に制限されないが、濾過温度（原料糖液の温度）は通常５０〜８０℃、濾過圧力は膜濾過システムの種類により適宜選択される。振動膜分離装置の場合の濾過圧力（膜入口圧力）は通常０．１〜１ＭＰａである。 When the concentration rate in the membrane filtration system is less than 10 times, it is not possible to recover a transparent sugar solution in which the solid content is sufficiently captured when the concentrate is squeezed with a filter press. The reason for this is thought to be that the solid content in the concentrate gradually aggregates as the concentration factor increases during filtration in the membrane filtration system, but if the concentration factor is less than 10 times, the aggregate (floc) is sufficient. This is presumably because it has not grown to a large size. On the other hand, when the concentration rate in the membrane filtration system exceeds 60 times, the viscosity of the concentrate becomes too high and the operability of the membrane filtration system decreases. That is, the filtration efficiency is lowered and the filtration pressure is increased. A preferable range of the concentration ratio in the membrane filtration system is 20 to 50 times. The operating conditions of the membrane filtration system are not particularly limited, but the filtration temperature (the temperature of the raw sugar solution) is usually 50 to 80 ° C., and the filtration pressure is appropriately selected depending on the type of the membrane filtration system. The filtration pressure (membrane inlet pressure) in the case of the vibration membrane separator is usually 0.1 to 1 MPa.
次いで、本発明においては、フィルタープレスにて上記の濃縮液を圧搾して当該濃縮液から糖液を回収する。フィルタープレスは、複数並設された濾板の間に一対の濾布を配置した状態で濾板相互を締め付けて密着させ、濾板間に濾室を形成すると共に、濾布間にスラリーを供給し、液分を濾布を介して排出させて濾布間にケーキを形成し、その後、濾板相互および濾布相互を離間させ、濾布間に形成されたケーキを落下排出する装置である。本発明においては、例えば、合成繊維マルチフィラメント糸を主体に構成された濾布を備えた通常のフィルタープレスを使用することが出来る。 Next, in the present invention, the concentrated liquid is squeezed with a filter press to recover the sugar liquid from the concentrated liquid. The filter press is a state in which a pair of filter cloths are arranged between a plurality of filter plates arranged side by side, and the filter plates are fastened together to form a filter chamber between the filter plates and supply slurry between the filter cloths. The liquid is discharged through a filter cloth to form a cake between the filter cloths, and then the filter plate and the filter cloth are separated from each other, and the cake formed between the filter cloths is dropped and discharged. In the present invention, for example, a normal filter press provided with a filter cloth mainly composed of synthetic fiber multifilament yarn can be used.
本発明においては、濾布の表面に珪藻土などによるプレコート層を形成する必要はないが、濃縮液に濾過助剤を添加して圧搾性を高めることが出来る。濾過助剤としては、珪藻土の他、活性炭、セルロース、パーライト等を使用することが出来、その使用量は、濃縮液中の固形分に対する割合として、通常１〜１００重量％、好ましくは５〜５０重量％である。フィルタープレスの運転条件は特に制限されないが、濾過温度（濃縮液の温度）は通常５０〜８０℃、濾過圧力は通常０．１〜２ＭＰａである。圧力は多段階に高めてもよい。 In the present invention, it is not necessary to form a precoat layer of diatomaceous earth or the like on the surface of the filter cloth, but the filterability can be increased by adding a filter aid to the concentrate. As the filter aid, diatomaceous earth, activated carbon, cellulose, pearlite and the like can be used, and the amount used is usually 1 to 100% by weight, preferably 5 to 50, as a ratio to the solid content in the concentrate. % By weight. The operating conditions of the filter press are not particularly limited, but the filtration temperature (concentrated liquid temperature) is usually 50 to 80 ° C., and the filtration pressure is usually 0.1 to 2 MPa. The pressure may be increased in multiple stages.
本発明においては、フィルタープレスの濾布間に形成されたケーキに水を供給して当該ケーキに付着した糖液を回収することが出来る。斯かる操作は、洗浄機構を備えた市販のフィルタープレスを使用することにより、容易に行うことが出来る。 In the present invention, the sugar solution adhering to the cake can be recovered by supplying water to the cake formed between the filter cloths of the filter press. Such an operation can be easily performed by using a commercially available filter press equipped with a cleaning mechanism.
実施例１：
先ず、澱粉原料を糖化して得られたブドウ糖原液（糖濃度２８重量％、固形分濃度０．３重量％）６５０Ｌを、循環式の供給タンク（液温５３〜５５℃）から、濾過膜（テフロン（登録商標）製、孔経０．１μｍ、膜面積１．７ｍ２）を装填した振動膜分離装置（米国のＮＥＷ ＬＯＧＩＣ ＲＥＳＥＡＲＣＨ，ＩＮＣ製の「ＶＳＥＰ Ｓｅｒｉｅｓ Ｌ／Ｐ」）に供給し、濾過温度（ブドウ糖原液温度）５３〜５５℃、濾過圧力０．５５ＭＰａ（膜入口圧力）にてクロスフロー法で濾過し、濃縮液（固形分濃度６．１重量％）２６Ｌと透過液（ブドウ糖濃度２８重量％）６２４Ｌを得た。循環液流量は１．２ｍ３／ｈ、濃縮倍率は６５０／（６５０−６２４）＝２５倍である。
Example 1:
First, 650 L of a glucose stock solution obtained by saccharifying the starch raw material (sugar concentration: 28 wt%, solid content concentration: 0.3 wt%) is filtered from a circulation supply tank (liquid temperature: 53 to 55 ° C.) Supplied to a vibration membrane separator (“VSEP Series L / P” manufactured by NEW LOGIC RESEARCH, INC., USA) loaded with Teflon (registered trademark), pore diameter 0.1 μm, membrane area 1.7 m 2 , and filtered Filtration was performed by a cross flow method at a temperature (glucose stock solution temperature) of 53 to 55 ° C. and a filtration pressure of 0.55 MPa (membrane inlet pressure), and 26 L of concentrated liquid (solid content concentration: 6.1% by weight) and permeated liquid (glucose concentration of 28 624 L was obtained. The circulating fluid flow rate is 1.2 m 3 / h, and the concentration factor is 650 / (650−624) = 25 times.
次いで、上記の濃縮液を、供給タンク（液温５９〜６２℃）から、濾過面積１００ｃｍ２の濾布（ポリプロピレン製二重織り）を装填した内容積１５０ｃｍ３（１７８ｍｍ×１７８ｍｍ×１室）のフィルタプレス（株式会社栗田機械製作所製の試験機）に０．４ＭＰａの圧力で供給し、０．７ＭＰａの圧力で圧搾した。この操作により、濃縮液４７６ｍｌに対し、濾液（ブドウ糖濃度２８重量％）４１８ｍｌと廃ケーキ（含水率３９．４重量％）６７．６ｇが得られた。計算により求めたブドウ糖の回収率は９９．５重量％であった。また、ブドウ糖原液１ｍ３当りに換算した廃ケーキ量は５．７ｋｇ／ｍ３であった。 Next, the concentrated liquid was supplied from a supply tank (liquid temperature 59 to 62 ° C.) with an inner volume of 150 cm 3 (178 mm × 178 mm × 1 chamber) loaded with a filter cloth (polypropylene double weave) having a filtration area of 100 cm 2 . A filter press (tester manufactured by Kurita Machinery Co., Ltd.) was supplied at a pressure of 0.4 MPa and squeezed at a pressure of 0.7 MPa. By this operation, 418 ml of filtrate (glucose concentration 28% by weight) and 67.6 g of waste cake (water content 39.4% by weight) were obtained with respect to 476 ml of the concentrated solution. The glucose recovery determined by calculation was 99.5% by weight. Moreover, the amount of waste cakes converted per 1 m 3 of glucose stock solution was 5.7 kg / m 3 .
実施例２：
実施例１と同様にして得られた濃縮液３．３Ｌに対し、珪藻土１０５ｇ（固形分濃度に対して５７重量％）を添加し、実施例１と同様にフィルタプレスで処理した。この操作により、濃縮液７６２ｍｌに対し、濾液（ブドウ糖濃度２８重量％）６６１ｍｌと廃ケーキ（含水率２９．１重量％）１３１．４ｇを得た。計算により求めたブドウ糖の回収率は９９．５重量％であった。また、ブドウ糖原液１ｍ３当りに換算した廃ケーキ量は６．９ｋｇ／ｍ３であった。
Example 2:
To 3.3 L of the concentrated liquid obtained in the same manner as in Example 1, 105 g of diatomaceous earth (57% by weight with respect to the solid content concentration) was added and treated with a filter press in the same manner as in Example 1. By this operation, 661 ml of filtrate (glucose concentration 28% by weight) and 131.4 g of waste cake (water content 29.1% by weight) were obtained with respect to 762 ml of the concentrated liquid. The glucose recovery determined by calculation was 99.5% by weight. Moreover, the amount of waste cake converted per 1 m 3 of glucose stock solution was 6.9 kg / m 3 .
比較例１：
澱粉原料を糖化して得られたブドウ糖原液（糖濃度２８重量％、固形分濃度０．３重量％）１０００Ｌを、プレコート濾過装置で濾過した。プレコートに使用した珪藻土の量は５ｋｇとした。廃ケーキ（含水率３０．６重量％）は１１．５ｋｇであった。計算により求めたブドウ糖の回収率は９９．５重量％であった。また、ブドウ糖原液１ｍ３当りに換算した廃ケーキ量は１１．５ｋｇ／ｍ３であった。
Comparative Example 1:
1000 L of glucose stock solution (sugar concentration 28 wt%, solid content concentration 0.3 wt%) obtained by saccharifying the starch raw material was filtered with a precoat filtration device. The amount of diatomaceous earth used for the precoat was 5 kg. The waste cake (water content 30.6% by weight) was 11.5 kg. The glucose recovery determined by calculation was 99.5% by weight. Moreover, the amount of waste cake converted per 1 m 3 of glucose stock solution was 11.5 kg / m 3 .
Claims (4)
［数１］
濃縮倍率＝供給液量／（供給液量−透過液量）・・・（Ｉ） In producing a purified sugar solution by removing the solid content from a raw material sugar solution containing solids, first, the raw material sugar solution is supplied to a continuous or batch-type membrane filtration system, and the following formula (I) The filtrate is filtered under the condition that the concentration ratio defined in 10 to 60 times is separated into a concentrate and a permeate, and then the concentrate is squeezed with a filter press to recover a sugar solution from the concentrate A method for producing a purified sugar solution, comprising:
[Equation 1]
Concentration magnification = Supply solution amount / (Supply solution amount−Permeate solution amount) (I)
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| KR20180076028A (en) * | 2016-12-27 | 2018-07-05 | 주식회사 삼양사 | Method of purification allulose |
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