JPH0280000A - Production of sugar from beet sugar concentrate - Google Patents
Production of sugar from beet sugar concentrateInfo
- Publication number
- JPH0280000A JPH0280000A JP23271888A JP23271888A JPH0280000A JP H0280000 A JPH0280000 A JP H0280000A JP 23271888 A JP23271888 A JP 23271888A JP 23271888 A JP23271888 A JP 23271888A JP H0280000 A JPH0280000 A JP H0280000A
- Authority
- JP
- Japan
- Prior art keywords
- sugar
- concentrate
- beet
- exchange resin
- anion exchange
- 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
- 235000000346 sugar Nutrition 0.000 title claims abstract description 55
- CZMRCDWAGMRECN-UHFFFAOYSA-N Rohrzucker Natural products OCC1OC(CO)(OC2OC(CO)C(O)C(O)C2O)C(O)C1O CZMRCDWAGMRECN-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 239000012141 concentrate Substances 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title claims description 10
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 12
- 235000021537 Beetroot Nutrition 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000007787 solid Substances 0.000 claims abstract 2
- 238000011033 desalting Methods 0.000 claims description 13
- 238000004042 decolorization Methods 0.000 claims description 4
- 235000015191 beet juice Nutrition 0.000 claims description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 claims 1
- 238000000502 dialysis Methods 0.000 claims 1
- 238000000909 electrodialysis Methods 0.000 abstract description 26
- 239000003456 ion exchange resin Substances 0.000 abstract description 16
- 229920003303 ion-exchange polymer Polymers 0.000 abstract description 16
- 239000003014 ion exchange membrane Substances 0.000 abstract description 8
- 235000011389 fruit/vegetable juice Nutrition 0.000 abstract description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract description 2
- 235000011941 Tilia x europaea Nutrition 0.000 abstract description 2
- 239000004571 lime Substances 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract 4
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract 2
- 239000001569 carbon dioxide Substances 0.000 abstract 2
- 238000010979 pH adjustment Methods 0.000 abstract 2
- 238000009738 saturating Methods 0.000 abstract 1
- 238000003809 water extraction Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 26
- 238000000034 method Methods 0.000 description 25
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 14
- 239000007788 liquid Substances 0.000 description 11
- 235000013379 molasses Nutrition 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 6
- 229930006000 Sucrose Natural products 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 5
- 239000003011 anion exchange membrane Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 239000011347 resin Substances 0.000 description 4
- 229920005989 resin Polymers 0.000 description 4
- 150000008163 sugars Chemical class 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 3
- 150000001767 cationic compounds Chemical class 0.000 description 3
- 238000005115 demineralization Methods 0.000 description 3
- 230000002328 demineralizing effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 229910001411 inorganic cation Inorganic materials 0.000 description 3
- 238000005341 cation exchange Methods 0.000 description 2
- 238000004040 coloring Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 229910003460 diamond Inorganic materials 0.000 description 2
- 239000010432 diamond Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 229960004903 invert sugar Drugs 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 235000016068 Berberis vulgaris Nutrition 0.000 description 1
- 241000335053 Beta vulgaris Species 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical group [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000004255 ion exchange chromatography Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Abstract
Description
【発明の詳細な説明】
（発明の対象）
本発明はイオン交換膜電気透析（以下電気透析と称する
）とイオン交換樹脂を用いたビート糖製造工程の改良に
係わるものである。DETAILED DESCRIPTION OF THE INVENTION (Subject of the Invention) The present invention relates to an improvement in a beet sugar production process using ion exchange membrane electrodialysis (hereinafter referred to as electrodialysis) and an ion exchange resin.
（従来の技術）
ビート根を原料に砂糖を製造する場合には第１図に示す
ように、ビート根を細かく切断ｌ＆温水で抽出してビー
ト生汁を得て、石灰を加えて炭酸飽充、イオン交換樹脂
による軟化、脱色の前処理を行って希薄液を得る。この
希薄液は多重効用缶で濃縮され濃縮液を得た後、結晶缶
で結晶化され１番糖の白糖が製造されるが、これらの工
程においては脱塩工程がないために、２番糖以降におい
て灰分が濃縮されるので、２番糖以降の砂糖は白糖を得
ることができず再溶解後、イオン交換樹脂により脱色後
前段の工程にリサイクルされたり、糖蜜として処理（イ
オン交換樹脂処理、ステソフェン処理、イオンクロマト
処理等）して清浄工程にリサイクルされている。２番糖
以降も白糖として製品化するための方法としては希薄液
中の灰分をイオン交換樹脂により脱塩する全量脱塩法が
採用されている。この方法により脱塩を行えば２番糖以
降も白糖として製品化することが可能であるがこの全量
脱塩法は膨大な設備を必要とし、かつイオン交換樹脂の
再生に用いる再生剤も多量に要し、さらには再生廃液処
理の問題、イオン交換樹脂に付着する糖分のロスの問題
も生じている。(Conventional technology) When producing sugar using beet roots as a raw material, as shown in Figure 1, the beet roots are cut into small pieces and extracted with hot water to obtain raw beet juice, which is then added with lime and carbonated. A dilute solution is obtained by pre-treatment of softening and decolorization using an ion exchange resin. This diluted solution is concentrated in a multi-effect can to obtain a concentrated solution, and then crystallized in a crystallizer to produce white sugar, the No. 1 sugar. However, since there is no desalting step in these processes, the No. 2 sugar is Since the ash content is concentrated in the subsequent steps, it is not possible to obtain white sugar from sugars after No. 2 sugar, and after re-dissolving, they are decolorized with ion exchange resin and recycled to the previous process, or treated as molasses (ion exchange resin treatment, Stethofen treatment, ion chromatography treatment, etc.) and recycled to the cleaning process. As a method for commercializing second sugar and subsequent sugars as white sugar, a total desalting method is adopted in which the ash in the dilute solution is desalted using an ion exchange resin. If desalting is performed using this method, it is possible to commercialize sugars from No. 2 to white sugar, but this total desalting method requires a huge amount of equipment and also requires a large amount of regenerating agent used to regenerate the ion exchange resin. In addition, there are also problems in processing recycled waste liquid and loss of sugar adhering to the ion exchange resin.
（発明が解決しようとする問題点）
脱塩を行わない場合には２番糖以降から白糖が得られな
いため多量の糖蜜が生成され、この糖蜜を処理するため
に多量のイオン交換樹脂等を用いるため、前述の再生剤
、再生廃液、糖分のロス等問題をかかえ、なおかつリサ
イクルされる糖は同じ工程を経るため各工程での糖分の
ロスが増え、又リサイクルのため全体の設備がその分大
きくなるという欠点をかかえている。このようにビート
糖製造工程にイオン交換樹脂による脱塩工程を採用して
いない工場では、砂糖の品質向上及び歩留向上の目的で
何らかの脱塩を行なう必要にせまられている。また糖液
に電気透析を用いることは広く紹介されているが、−船
釣には電気透析法では高塩量である程脱塩能力が大きい
という特徴を生かすために、特公昭５５−３８１１９や
特公昭５６−３９６３８に示されているように廃糖蜜の
ような高塩量の糖液に採用されている。しかしこれらの
特許に述べられているように、このような廃糖蜜にはイ
オン交換膜を汚染する有機物も多量に含まれており、前
処理が必要となる。従って電気透析法を用いる場合には
充分前処理された清浄な液で、かつ塩濃度が高い液を処
理する必要がある。またこれまでビート糖液の脱塩に電
気透析法が採用されない理由としては電気透析を行なう
ことによりビート糖液のｐＨが低下し転化糖の増加を起
こし、糖の歩留の低下及び糖の着色が起こることが主な
要因であった。(Problem to be solved by the invention) If desalting is not performed, a large amount of molasses is produced because white sugar cannot be obtained from the second sugar onward, and a large amount of ion exchange resin etc. is used to treat this molasses. However, since recycled sugar goes through the same process, sugar loss increases in each process, and the overall equipment for recycling increases accordingly. It has the disadvantage of being large. As described above, factories that do not employ a desalting process using an ion exchange resin in their beet sugar manufacturing process are forced to carry out some form of desalting for the purpose of improving the quality and yield of sugar. Also, the use of electrodialysis for sugar solutions has been widely introduced, but in order to take advantage of the characteristic that the higher the salt content, the greater the desalination capacity of the electrodialysis method for boat fishing. As shown in Japanese Patent Publication No. 56-39638, it is used for sugar solutions with high salt content such as blackstrap molasses. However, as stated in these patents, such molasses also contains large amounts of organic matter that contaminates ion exchange membranes and requires pretreatment. Therefore, when electrodialysis is used, it is necessary to treat a sufficiently pretreated clean solution with a high salt concentration. In addition, the reason why electrodialysis has not been adopted for desalting beet sugar solution is that electrodialysis lowers the pH of the beet sugar solution and increases invert sugar, resulting in a decrease in sugar yield and coloring of sugar. The main factor was that this occurred.
（問題点を解決するための手段）
本発明は以上の問題点を解決するため、第２図に示すよ
うに、Ｂｘ４０〜６０のビート糖濃縮液を電気透析して
脱塩を行ない、イオン交換樹脂でｐＨ１ｌ整及び脱色処
理する方法を採用する。(Means for Solving the Problems) In order to solve the above problems, the present invention, as shown in FIG. A method of adjusting the pH to 1L and decolorizing with resin is adopted.
即ちビート糖希釈液を所定の濃度に濃縮したビート糖濃
縮液を電気透析法により脱塩することにより２番糖も製
品白糖とし、リサイクルする２番糖を無くし、かつ糖蜜
処理用のイオン交換樹脂等の負荷を軽減するものである
。また電気透析の処理液をＯＨ型のアニオン交換樹脂等
に通しｐＨ１ｌ整を行ない、さらにＣｌ型のアニオン交
換樹脂等により脱色することにより電気透析の欠点を解
決するものである。That is, by desalting the beet sugar concentrate obtained by concentrating the diluted beet sugar solution to a predetermined concentration by electrodialysis, the secondary sugar is also produced as white sugar, eliminating the secondary sugar to be recycled, and using an ion exchange resin for molasses processing. This is to reduce the burden of In addition, the electrodialysis treatment solution is passed through an OH type anion exchange resin or the like to adjust the pH to 11, and then decolorized using a Cl type anion exchange resin or the like, thereby solving the drawbacks of electrodialysis.
（作用）
以下本発明を更に詳細に説明する。本発明は前述のよう
に、イオン交換樹脂による全量脱塩を行わずにビート糖
の製造工程を改良するものであるが、前処理として軟化
、脱色されたビート糖液を原料とする必要がある。これ
は電気透析法のイオン交換膜を汚染する物質を極力除去
してやるためである。また電気透析法の特徴である高塩
量はど電流値が高くとれ処理能力が大きいという利点を
生かすために、希薄液ではなく濃縮液を脱塩する必要が
ある。しかし多重効用缶出口から得られる濃縮液はより
高塩量になるが、その濃縮液はＢｘが６５以上あるため
粘性が高く、逆に電流が流れにくくなるのでＢｘが４０
〜６０に濃縮された時点で効用缶の途中から抜き出し、
電気透析の耐熱温度の５０℃前後に冷却後電気透析にか
ける必要がある。ここで冷却により放熱される熱は再度
効用缶にもどす時の加熱に用いられ、エネルギー的には
わずかの消費ですますことが出来る。また電気透析は温
度が高いほど電流が流れ易くなり処理能力が増大するの
で、電気透析槽の耐熱温度近くの５０℃前後で処理する
のが得策である。ここで用いられる電気透析槽は公知の
フィルタープレスタイプのもので良く多数のカチオン交
換膜とアニオン交換膜が交互に配列され、−室おきに脱
塩室と濃縮室が構成されており、その両端に電極室が設
けられている。ビート糖濃縮液を脱塩室に、無機塩溶液
（通常１重量％程度）を濃縮室に循環流通させながら両
端の電極室に設けられた極板に直流電圧をかけるとビー
ト糖液中の灰分が脱塩される。またここで用いられるイ
オン交換膜は、一般市販品の例えばセラミオン″ＣＭＶ
” “ＡＭＶ″（旭硝子社製品名）でよい。特開昭５
１−７７５８８のようにアニオン交換膜のファウリング
を防ぐために孔径が大きい特殊なイオン交換膜を用いる
と、灰分の脱塩と共に糖分も濃縮液に移行し糖ロスを起
こしてしまう。一般用造膜を用いれば糖ロスは０．２％
以下に押さえることが出来る。電気透析法で灰分を９０
％以上除去することは可能であるが、通常は灰分の脱塩
率を５５〜６０％にとどめた方が電気透析の処理能力を
大きくすることができる。また２番糖を製品とする目的
であればこの脱塩率で充分製品化が可能である。具体的
にはＢｘ５０のビート糖液中には、カリウムを主成分と
する無機カチオンが６ 、 ０００ ｍ ｇ ／ ｌ
ａ度合まれるが、これらが２，４００〜２，７００ｍｇ
／ｌまで除去された時点で処理を停止する方が効率的な
運転が可能となる。ビート糖濃縮液中の無機のカチオン
と対をなすアニオン成分には、分子量が比較的大きな有
機酸成分も含まれている。この有機酸はアニオン交換膜
を通過出来ないため無機カチオンが多く脱塩される。こ
のため電気透析処理を行うとビート糖液のｐＨが８．５
〜９０から７．０〜８．０まで低下してしまう。このｐ
Ｈ低下は糖の分解を引き起こし転化糖が増加するため、
糖の純糖率が下がるばかりでなく、製品が着色するトラ
ブルを引き起こす。そのため電気透析処理液はすぐにｐ
ＨＩｊ＃整を行う必要がある。ｐＨ調整をアルカリを加
えることで行なおうとすれば、基量が増すことになり脱
塩の目的に逆行するので、本発明では例えば強塩基性ア
ニオン交換樹脂等をＯＨ型にした樹脂塔に通液すること
によりｐＨ調整することとする。ここで用いられる強塩
基性アニオン交換樹脂は、ゲル型よりもポラス型の方が
糖液による汚染が少なく有効であることが知られている
が、特にポーラス型に限定するものではない。この樹脂
によるｐＨ調整によりｐ Ｈは１０以上となるが、ビー
ト糖のｐＨコントロール範囲は９前後であるので全量を
通液する必要はなく、一部分を通液しあとで混合してｐ
Ｈを調整する方法が良い。電気透析法のイオン交換膜は
前述のように、糖ロスを押さえるために一般用のイオン
交換膜を用いるが、これは逆に色度成分は除去されにく
いという性質を有している。従って砂糖の結晶化時にこ
の色度成分も濃縮され製品が着色してしま、うので、脱
色の必要がある。本発明では例えば強塩基性アニオン交
換樹脂等をＯＨ型にした樹脂塔に通液することにより脱
色することとする。用いられるアニオン交換樹脂は例え
ばダイヤイオンＰＡ−３０８（三菱化成社製）のような
一般市販品で良（、ＮａＣ１で再生してＯＨ型で使用す
る。これによりビート糖濃縮液の色価は８０％以上脱色
される。この脱色されたビート糖濃縮液は前述のように
加温され、多重効用缶に戻しＢｘ６５以上の濃縮液とし
てから結晶缶に送られ製品砂糖を製造する。(Function) The present invention will be explained in more detail below. As mentioned above, the present invention improves the manufacturing process of beet sugar without performing total desalting using an ion exchange resin, but it is necessary to use a softened and decolorized beet sugar solution as a raw material as a pretreatment. . This is to remove as much as possible the substances that contaminate the ion exchange membrane in electrodialysis. Furthermore, in order to take advantage of the advantages of electrodialysis, which are characterized by a high salt content, a high current value, and a large processing capacity, it is necessary to desalt a concentrated solution rather than a diluted solution. However, the concentrated liquid obtained from the outlet of the multi-effect can has a higher salt content, but since the concentrated liquid has a Bx of 65 or more, it has a high viscosity, and conversely, it becomes difficult for current to flow, so the Bx is 40.
When it is concentrated to ~60%, it is extracted from the middle of the can,
It is necessary to apply electrodialysis after cooling to around 50°C, which is the allowable temperature for electrodialysis. The heat radiated by cooling is used for heating when returning to the canister, resulting in a small amount of energy consumption. In addition, in electrodialysis, the higher the temperature, the easier the current flows and the higher the processing capacity, so it is advisable to perform the treatment at around 50° C., which is close to the allowable temperature limit of the electrodialysis tank. The electrodialysis tank used here is a well-known filter press type, in which a large number of cation exchange membranes and anion exchange membranes are alternately arranged, and a demineralization chamber and a concentration chamber are configured in every other chamber, with both ends An electrode chamber is provided in the chamber. While circulating the beet sugar concentrate into the desalination chamber and the inorganic salt solution (usually about 1% by weight) into the concentration chamber, applying a DC voltage to the electrode plates installed in the electrode chambers at both ends will remove the ash in the beet sugar solution. is desalted. The ion exchange membrane used here is a general commercially available product such as Ceramion "CMV".
” “AMV” (Asahi Glass product name) is sufficient.
If a special ion exchange membrane with a large pore diameter is used to prevent fouling of the anion exchange membrane, such as No. 1-77588, the sugar content will also transfer to the concentrate as the ash is desalted, causing sugar loss. Sugar loss is 0.2% when using general purpose membrane formation.
It can be held below. Ash content reduced to 90% by electrodialysis method
Although it is possible to remove more than 50% of the ash content, the throughput of electrodialysis can usually be increased by keeping the ash removal rate to 55 to 60%. Moreover, if the purpose is to make No. 2 sugar into a product, this desalting rate is sufficient to make it into a product. Specifically, the beet sugar solution of Bx50 contains 6,000 mg/l of inorganic cations whose main component is potassium.
It is mixed to a degree, but these are 2,400 to 2,700 mg
Efficient operation is possible by stopping the process when the amount of water per liter has been removed. The anion component that pairs with the inorganic cation in the beet sugar concentrate also contains an organic acid component with a relatively large molecular weight. Since this organic acid cannot pass through an anion exchange membrane, many inorganic cations are desalted. Therefore, when the electrodialysis treatment is performed, the pH of the beet sugar solution becomes 8.5.
It drops from ~90 to 7.0-8.0. This p
Since H reduction causes sugar decomposition and invert sugar increases,
This not only lowers the pure sugar ratio, but also causes problems such as coloring of the product. Therefore, the electrodialyzed solution is immediately p
It is necessary to perform HIj# adjustment. If we attempt to adjust the pH by adding alkali, the amount of bases will increase, which goes against the purpose of desalting. Therefore, in the present invention, for example, a strongly basic anion exchange resin is passed through a resin tower in an OH type. The pH will be adjusted by diluting. It is known that the porous type of strongly basic anion exchange resin used here is more effective than the gel type because it is less contaminated by sugar solution, but it is not particularly limited to the porous type. The pH is adjusted to 10 or more by adjusting the pH with this resin, but since the pH control range of beet sugar is around 9, there is no need to pass the entire amount of the solution, but only a portion of the solution is passed and mixed afterwards.
A better method is to adjust H. As mentioned above, a general ion exchange membrane is used in the electrodialysis method in order to suppress sugar loss, but this has the property that, conversely, chromatic components are difficult to remove. Therefore, when sugar crystallizes, this color component is also concentrated and the product becomes colored, so it is necessary to decolorize it. In the present invention, for example, decolorization is carried out by passing a strongly basic anion exchange resin or the like through a resin tower in an OH type. The anion exchange resin used is a general commercially available product such as Diaion PA-308 (manufactured by Mitsubishi Kasei Corporation).It is regenerated with NaCl and used in the OH type.As a result, the color value of the beet sugar concentrate is 80. This decolorized beet sugar concentrate is heated as described above and returned to the multi-effect can to form a concentrate with Bx65 or higher, and then sent to the crystallization can to produce product sugar.
（実施例）
以下実施例により本発明実施の態様を例示するが、例示
は勿論説明のものであって発明精神の限定を意味するも
のではない。(Examples) Hereinafter, embodiments of the present invention will be illustrated by Examples, but the examples are, of course, for illustration and do not mean a limitation on the spirit of the invention.
実施例： ビート糖製造工程の多重効用缶の３段目の出
口より濃縮液（シックジュース）を抜き出した。この液
はＢｘ５０．５ 、ｐＨ８，８，純糖率９２．２％、灰
分２．８７％、スタンマー色価６．７６、電気伝導度５
，７４０μｓ ／ ｃ ｍであった。Example: A concentrated liquid (thick juice) was extracted from the third stage outlet of a multi-effect can in the process of manufacturing beet sugar. This liquid has Bx50.5, pH 8.8, pure sugar rate 92.2%, ash content 2.87%, Stanmer color value 6.76, and electrical conductivity 5.
, 740 μs/cm.
カチオン交換膜としてセレミオンＣＭＶ、アニオン交換
膜としてセレミオンＡＭＶの１１対で構成される、脱塩
室９室、有効全膜面ａ［１５，５ａｄのＤＵ−ｏｂ型電
気透析槽（旭硝子社！！りを使用し、脱塩室に前述のシ
ックジュース２２を、濃縮室と電極室には１％食塩水を
仕込み、温度５０〜５２℃、初期電流密度０．７Ａ／ｄ
％（極間電圧？、５Ｖ）の条件下に回分方式で１．５時
間電気透析を行った。その結果Ｂｘ４８．５．電気伝導
度１．０５０μｓ／ｃｍ、灰分０．９２％、スタンマー
色価５．４０．ｐＨ７，２，純糖率９６．７％の液２１
を得た。Consisting of 11 pairs of Selemion CMV as the cation exchange membrane and Selemion AMV as the anion exchange membrane, 9 demineralization chambers, DU-ob type electrodialysis tank (Asahi Glass Co., Ltd.) with an effective total membrane area of 15.5ad. using the above-mentioned Sick Juice 22 in the demineralization chamber, and 1% saline in the concentration chamber and electrode chamber, at a temperature of 50 to 52°C and an initial current density of 0.7 A/d.
% (electrode voltage, 5 V) in a batch manner for 1.5 hours. As a result, Bx48.5. Electrical conductivity 1.050μs/cm, ash content 0.92%, Stanmer color value 5.40. Liquid 21 with pH 7.2 and pure sugar rate 96.7%
I got it.
次にジャケット付ガラスカラムにダイヤイオンＰＡ−３
１２を２０ｒｎｌ充填し、４％ＮａＯＨ溶液１００ｍｊ
？を用いてＳＶ（通液空間速度）２で再生後、純水１０
０ｍ１（ＳＶ２）でＮａＯＨを押し出し、更に純水２０
０ｍｆ （ＳＶ５）で洗浄した。この再生イオン交換樹
脂に電気透析処理液５００ｍ／を５１）’Ｃ，ＳＶ５で
５時間を要シテ通液した。この時の処理液のｐＨはｌＯ
１θ〜１０３で安定していた。この処理液５００ｍ１ｌ
と電気透析処理成約７００ ｍ ｌを混合し、ｐ Ｈを
９゜０に調整した。Next, add Diamond Ion PA-3 to the jacketed glass column.
Fill 20rnl of 12 with 100mj of 4% NaOH solution.
? After regeneration at SV (liquid hourly space velocity) of 2 using
Push out NaOH with 0 m1 (SV2) and then add 20 m of pure water.
Washed with 0 mf (SV5). 500 m of the electrodialyzed solution was passed through the regenerated ion exchange resin at 51)'C, SV5 for 5 hours. The pH of the treatment solution at this time is lO
It was stable at 1θ~103. 500ml of this treatment liquid
and about 700 ml of electrodialyzed solution were mixed and the pH was adjusted to 9.0.
次にジャケット付ガラスカラムにダイヤイオンＰＡ−３
０８を商品型（Ｃｌ型）のまま２０ ｍ ｊ！充填し、
上記混合液５００ｍｌを５０℃、ＳＶ５で５時間かけて
通液した。この処理液はＢｘ４７８、ｐ）ｌａ、ｓ、電
気伝導度１，２５０．！ＪＳ／ｃｍ、灰分０，８９％、
スタンマー色価０．９２、純糖率９７６８％の液であっ
た。Next, add Diamond Ion PA-3 to the jacketed glass column.
20 m j with 08 as a product type (Cl type)! Fill and
500 ml of the above mixed solution was passed through at 50° C. and SV5 over 5 hours. This treatment liquid has Bx478, p)la,s, and electrical conductivity of 1,250. ! JS/cm, ash content 0.89%,
The liquid had a Stanmer color value of 0.92 and a pure sugar rate of 9768%.
以上のように電気透析処理後、イオン交換樹脂によりｐ
Ｈ調整及び脱色を行うと高品質の濃縮液が得られること
がわかる。After electrodialysis treatment as described above, p
It can be seen that a high quality concentrate can be obtained by H adjustment and decolorization.
さらにこの高品質濃縮液を用いて結晶糖の品質を評価す
るために煎糖試験を実施した。イオン交換樹脂処理後の
高品質濃縮液を更に濃縮して、Ｂｘ６Ｂ、８．ｐＨ８，
７，電気伝導度１，８５０ｐｓ／ｃｍ、純糖率９７．６
％、灰分０．９０％スタンマー色債１．２６の煎糖試験
用の糖液を得た。これをできるだけ実工程に準じた方法
で煎糖試験を行った結果、１番糖で色価３．６．灰分０
．００４％の高品質の砂糖が回収できた。更に２番糖に
おいても色価１２．６．灰分０，０１９％の通常工程の
１番糖並の製品が回収できた。Furthermore, a decoction test was conducted using this high-quality concentrate to evaluate the quality of crystalline sugar. The high quality concentrate after ion exchange resin treatment was further concentrated to produce Bx6B, 8. pH8,
7. Electrical conductivity 1,850 ps/cm, pure sugar rate 97.6
%, ash content 0.90%, Stanmer color bond 1.26, a sugar solution for decoction sugar test was obtained. We conducted a roasting sugar test using a method similar to the actual process as much as possible, and found that the color value was 3.6 with No. 1 sugar. Ash content 0
．． 0.004% of high quality sugar was recovered. Furthermore, the color value of No. 2 sugar is 12.6. A product with an ash content of 0.019% and comparable to No. 1 sugar produced in the normal process was recovered.
（発明の効果）
以上のようにビート糖製造工程に、電気透析法とイオン
交換樹脂法を組み合わせたプロセスを導入することによ
り以下に述べるような驚くべき効果が発揮される。(Effects of the Invention) As described above, by introducing a process that combines an electrodialysis method and an ion exchange resin method into the beet sugar production process, the following surprising effects are exhibited.
（１）１番糖は従来よりも灰分含量が低く、色価も良好
な高品質の砂糖が製造される。(1) No. 1 sugar has a lower ash content than conventional sugar, and high-quality sugar with good color value is produced.
（２）従来再溶解してリサイクルしていた２番糖以降も
、従来同様の品質の砂糖として回収することが可能であ
る。(2) It is possible to recover sugar of the same quality as that of conventional sugars, even from No. 2 sugar onward, which was conventionally redissolved and recycled.
（３）リサイクルされる２番糖がなくなるため糖のロス
が少なくなり、又各設備に余裕ができるため、原料ビー
トの処理量を増やすことが可能である。(3) Since there is no second sugar to be recycled, there is less sugar loss, and there is more room in each facility, so it is possible to increase the amount of raw beets processed.
（４）糖蜜処理用のイオン交換樹脂等の負荷は、糖蜜品
質が向上するため減少し、通液時間が延び排水量の低減
、糖ロスの低減等のメリットも期待できる。(4) The load on ion-exchange resins for molasses treatment will be reduced due to improved molasses quality, and benefits such as extended liquid passage time, reduced wastewater volume, and reduced sugar loss can be expected.
第１図は従来のビート糖製造工程図である。第２図は本
発明を採用した時のビート糖製造工程図である。図中の
工程図は勿論説明用の例示であって本発明精神の限定を
意味するものではない。
特許出願人 ホクレン農業協同組合連合会同
日本錬水株式会社
ソ１四 ： 従来の工ｇ−FIG. 1 is a diagram of a conventional beet sugar manufacturing process. FIG. 2 is a process diagram for manufacturing beet sugar when the present invention is adopted. The process diagrams in the drawings are, of course, illustrative examples and are not intended to limit the spirit of the present invention. Patent applicant Hokuren Agricultural Cooperative Federation
Nippon Rensui Co., Ltd. So14: Conventional engineering g-
Claims (2)
汁を炭酸飽充し、軟化、脱色の前処理を行った後、多重
効用缶で濃縮して得られる濃縮液を、イオン交換膜電気
透析法により脱塩した後、ＯＨ型アニオン交換樹脂等で
ｐＨ調整し、かつＣｌ型アニオン交換樹脂等で脱色する
ことを特徴とするビート糖濃縮液からの砂糖の製造方法
。(1) Cut the beetroot into small pieces, extract the raw beet juice with warm water, fill it with carbonic acid, pre-treat it with softening and decolorization, and then concentrate it in a multi-effect can. A method for producing sugar from a beet sugar concentrate, which comprises desalting by dialysis, adjusting the pH with an OH-type anion exchange resin, and decolorizing with a Cl-type anion exchange resin.
が４０〜６０の範囲にある濃縮液を用いることを特徴と
する特許請求の範囲第１項に記載のビート糖濃縮液から
の砂糖の製造方法。(2) Solid content of the above beet sugar concentrate (hereinafter referred to as Bx)
The method for producing sugar from a beet sugar concentrate according to claim 1, characterized in that a concentrate having a beet sugar concentration of 40 to 60 is used.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23271888A JPH0280000A (en) | 1988-09-19 | 1988-09-19 | Production of sugar from beet sugar concentrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP23271888A JPH0280000A (en) | 1988-09-19 | 1988-09-19 | Production of sugar from beet sugar concentrate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0280000A true JPH0280000A (en) | 1990-03-20 |
Family
ID=16943698
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP23271888A Pending JPH0280000A (en) | 1988-09-19 | 1988-09-19 | Production of sugar from beet sugar concentrate |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0280000A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6372049B1 (en) * | 1997-06-02 | 2002-04-16 | Centre for the Advancement of New Technologies “CANTEC” | Method of producing sugar syrup from sugar-containing raw materials |
| JP2009520484A (en) * | 2005-12-21 | 2009-05-28 | ダニスコ・シュガー・アクティーゼルスカブ | How to recover brown food grade sugar products from sugar beet solution |
| CN103328656A (en) * | 2011-01-21 | 2013-09-25 | 大塚制药株式会社 | Method for inhibiting the growth of thermotolerant acidophilic bacteria |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5077552A (en) * | 1973-11-20 | 1975-06-24 | ||
| JPS5747498A (en) * | 1980-09-01 | 1982-03-18 | Nissin Sugar Mfg | Purifying of sugar solution |
-
1988
- 1988-09-19 JP JP23271888A patent/JPH0280000A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5077552A (en) * | 1973-11-20 | 1975-06-24 | ||
| JPS5747498A (en) * | 1980-09-01 | 1982-03-18 | Nissin Sugar Mfg | Purifying of sugar solution |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6372049B1 (en) * | 1997-06-02 | 2002-04-16 | Centre for the Advancement of New Technologies “CANTEC” | Method of producing sugar syrup from sugar-containing raw materials |
| JP2009520484A (en) * | 2005-12-21 | 2009-05-28 | ダニスコ・シュガー・アクティーゼルスカブ | How to recover brown food grade sugar products from sugar beet solution |
| CN103328656A (en) * | 2011-01-21 | 2013-09-25 | 大塚制药株式会社 | Method for inhibiting the growth of thermotolerant acidophilic bacteria |
| CN103328656B (en) * | 2011-01-21 | 2015-05-27 | 大塚制药株式会社 | Method for inhibiting the growth of thermotolerant acidophilic bacteria |
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