JPH03183500A - Method for purifying sugar liquid - Google Patents
Method for purifying sugar liquidInfo
- Publication number
- JPH03183500A JPH03183500A JP32224589A JP32224589A JPH03183500A JP H03183500 A JPH03183500 A JP H03183500A JP 32224589 A JP32224589 A JP 32224589A JP 32224589 A JP32224589 A JP 32224589A JP H03183500 A JPH03183500 A JP H03183500A
- Authority
- JP
- Japan
- Prior art keywords
- activated carbon
- sugar solution
- treatment
- active carbon
- treated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims description 15
- 239000007788 liquid Substances 0.000 title abstract description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 121
- 239000012528 membrane Substances 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000011148 porous material Substances 0.000 claims abstract description 13
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 12
- 230000003213 activating effect Effects 0.000 claims abstract 3
- 230000001172 regenerating effect Effects 0.000 claims abstract 3
- 238000001179 sorption measurement Methods 0.000 claims description 29
- 239000002253 acid Substances 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 10
- 238000001471 micro-filtration Methods 0.000 claims description 9
- 238000001914 filtration Methods 0.000 abstract description 25
- 238000011282 treatment Methods 0.000 abstract description 11
- 238000010306 acid treatment Methods 0.000 abstract description 5
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 150000001720 carbohydrates Chemical class 0.000 abstract 5
- 229910052799 carbon Inorganic materials 0.000 abstract 5
- 239000000463 material Substances 0.000 abstract 2
- 239000000243 solution Substances 0.000 description 57
- 239000004744 fabric Substances 0.000 description 7
- 238000011049 filling Methods 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- 238000000746 purification Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 238000012360 testing method Methods 0.000 description 4
- 229920002472 Starch Polymers 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 235000019698 starch Nutrition 0.000 description 3
- 239000008107 starch Substances 0.000 description 3
- 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 2
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000004042 decolorization Methods 0.000 description 2
- 238000004332 deodorization Methods 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 239000008103 glucose Substances 0.000 description 2
- 239000003456 ion exchange resin Substances 0.000 description 2
- 229920003303 ion-exchange polymer Polymers 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000006188 syrup Substances 0.000 description 2
- 235000020357 syrup Nutrition 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 229930091371 Fructose Natural products 0.000 description 1
- 239000005715 Fructose Substances 0.000 description 1
- RFSUNEUAIZKAJO-ARQDHWQXSA-N Fructose Chemical compound OC[C@H]1O[C@](O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-ARQDHWQXSA-N 0.000 description 1
- 102000004195 Isomerases Human genes 0.000 description 1
- 108090000769 Isomerases Proteins 0.000 description 1
- 239000005909 Kieselgur Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- GZCGUPFRVQAUEE-SLPGGIOYSA-N aldehydo-D-glucose Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C=O GZCGUPFRVQAUEE-SLPGGIOYSA-N 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000010451 perlite Substances 0.000 description 1
- 235000019362 perlite Nutrition 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Sorption (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、ぶどう糖、異性化糖、水飴等を含有する糖液
の精製方法、特に糖液の清澄度をよくするための脱塩処
理以降の仕上げの精製方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for purifying a sugar solution containing glucose, high fructose sugar, starch syrup, etc., especially after desalination treatment to improve the clarity of the sugar solution. Relating to a method for refining the finish of.
澱粉溶酸を酸あるいは酵素によって処理する液化工程、
糖化工程によって得られるぶどう糖液水飴ｌα、さらに
ぶどう糖液を異性化酵素で異性化させて得られる異性化
糖液等の糖液を製品化する精製方法は、まずイオン交換
樹脂で脱塩し、さらに粉末活性炭で脱色、脱臭処理し、
濃縮缶で適当な濃度に濃縮して製品として、出荷直前に
精密濾過器で除菌濾過を行っている。A liquefaction process in which starch solution is treated with acid or enzymes;
The purification method for commercializing glucose liquid starch syrup lα obtained by the saccharification process and sugar solutions such as isomerized sugar solution obtained by isomerizing the glucose solution with an isomerase is first to desalt it with an ion exchange resin, and then Decolorized and deodorized with powdered activated carbon,
The product is concentrated to an appropriate concentration in a concentrator can, and then sterilized and filtered using a microfilter just before shipping.
このうち、脱色、脱臭処理を詳細に述へるとイオン交換
樹脂にて脱塩した糖液を６０°Ｃから８０°Ｃ程度に加
熱し、粉末活性炭を添加し、６０分から９０分撹拌し、
吸着作用を促進する。さらに糖液と粉末活性炭を混合し
た液をフィルタープレス等の構過機で濾過し、清澄な糖
液を得ていた。Of these, the decolorization and deodorization treatments are described in detail. A sugar solution desalted with an ion exchange resin is heated to about 60°C to 80°C, powdered activated carbon is added, and the mixture is stirred for 60 to 90 minutes.
Promotes adsorption action. Furthermore, the mixture of sugar solution and powdered activated carbon was filtered using a filter press or other filtration device to obtain a clear sugar solution.
この場合、当該濾過機は濾布だけの濾過メディアでは濾
布の目詰まりが激しく、実用化するには困難で、通常珪
藻土、パーライト等の濾過助剤を濾布上にケーキ形成さ
せるプリコート操作を行い、糖液と粉末活性炭の混合液
を圧入し、粉末活性炭を除去する。しかし、当該操作の
始めは、粉末活性炭が濾布表面のケーキ層より洩れるた
めに、濾１ｆｆｌ中の粉末活性炭の洩れがなくなるまで
濾液をリサイクルする操作が必要となる。さらに長時間
濾過を行うと、濾布表面のケーキ厚みが増加り、！過の
抵抗が大きくなり糖液の圧入圧を増やさなければならな
い。従って、適当な時期に濾過を停止し、濾過機の濾布
表面のケーキを剥離し、濾布を洗浄する必要がある。In this case, if the filter media is only a filter cloth, the filter cloth will be severely clogged, making it difficult to put it into practical use.Usually, a pre-coating operation is required to form a cake with a filter aid such as diatomaceous earth or perlite on the filter cloth. Then, a mixed solution of sugar solution and powdered activated carbon is injected, and the powdered activated carbon is removed. However, at the beginning of the operation, the powdered activated carbon leaks from the cake layer on the surface of the filter cloth, so it is necessary to recycle the filtrate until the powdered activated carbon in 1ffl of the filter stops leaking. If filtration is continued for an even longer period of time, the thickness of the cake on the surface of the filter cloth will increase. As the resistance increases, the injection pressure of the sugar solution must be increased. Therefore, it is necessary to stop the filtration at an appropriate time, peel off the cake on the surface of the filter cloth of the filter, and wash the filter cloth.
この様に、脱色、脱臭処理は、プリコート操作。In this way, decolorization and deodorization are performed using pre-coat operations.
液酸すサイクル操作、！過操作、ケーキ剥離操作を１サ
イクルとした繁雑な操作となる。Liquid acid cycle operation! This is a complicated operation with one cycle of over-operation and cake-peeling operation.
また、濾過機１台ではプリコート操作時、濾液Ｊサイク
ル操作時、ケーキ剥離操作時は、清澄な糖液は得られず
、製造を中止しなければならな０ため、精製工程を連続
に行えない。このため、濾過機を２台以上設置し、一方
の濾過機で濾過操作を行っている間に、他方の濾過機で
、ケーキ剥離操作、プリコート操作、ｉ！１ｆｆｌリサ
イクル操作を行って、粉末活性炭の混合糖液の濾過準備
を行えば、精製工程で製造を中止せずに、連続的に清澄
な糖液を得られるが、高価な濾過機を２台以上設置する
ために経済的でない。In addition, with a single filtration machine, a clear sugar solution cannot be obtained during precoat operation, filtrate J cycle operation, and cake peeling operation, and production must be stopped, so the purification process cannot be performed continuously. . For this reason, two or more filters are installed, and while one filter is performing the filtration operation, the other filter is performing the cake peeling operation, precoating operation, and i! If you perform the 1ffl recycling operation and prepare the powdered activated carbon mixed sugar solution for filtration, you can continuously obtain a clear sugar solution without stopping the production in the refining process, but it requires two or more expensive filters. Not economical to install.
さらに、当該精製工程に粒状活性炭の吸着塔を用いる場
合、吸着塔の単独使用あるいは吸着塔と精密濾過器の組
合せで使用されている。この方式は粉末活性炭による精
製方式に比べて、機器構成数が少ないために経済的であ
るが、次の欠点を有している。Furthermore, when an adsorption tower of granular activated carbon is used in the purification process, the adsorption tower is used alone or in combination with an adsorption tower and a precision filter. Although this method is more economical than the purification method using powdered activated carbon because it requires fewer equipment, it has the following drawbacks.
すなわち、長時間糖液を通液処理すると、粒状活性炭の
吸着能が破過する。この時は古い粒状活性炭を排出し、
新しい粒状活性炭を再充填するか、補充を行う。この状
態で糖液を通液すると、ＰＨの低下、電気伝導度の悪化
が生じる。また、粒状活性炭に付着している微粉の活性
炭が洩れ精密濾過２Ｘの濾過膜を詰まらせる。この場合
の対策として、粒状活性炭の充填後水洗を行って微粉を
除去している。しかしながら、ＰＨの低下と電気伝導度
の悪化は改善されず、このままの状態で長時間おくと再
度青色、にごりが生じ製品とならない。That is, when a sugar solution is passed through the granular activated carbon for a long period of time, the adsorption capacity of the granular activated carbon is exceeded. At this time, discharge the old granular activated carbon,
Refill with new granular activated carbon or top up. If the sugar solution is passed in this state, the pH will drop and the electrical conductivity will deteriorate. Furthermore, the fine activated carbon adhering to the granular activated carbon leaks and clogs the filter membrane of the precision filtration 2X. As a countermeasure in this case, after filling the granular activated carbon, washing with water is performed to remove fine powder. However, the decrease in pH and the deterioration in electrical conductivity were not improved, and if left in this state for a long time, the product would turn blue again and become cloudy, making it impossible to use it as a product.
このため一定量の通液の間処理肢は前工程に戻すか、別
途さらに精製を行っている。For this reason, while a certain amount of liquid is being passed through, the treated limbs are either returned to the previous process or further purified separately.
また、イオン交換による脱塩処理した糖液を精密濾過器
単独で処理する場合、精密濾過膜の細孔を小さくしなけ
れば糖液の清澄度は良くならない。Furthermore, when a sugar solution that has been desalted by ion exchange is processed using a microfilter alone, the clarity of the sugar solution cannot be improved unless the pores of the microfiltration membrane are made smaller.
通常精密濾過膜はカートリッジタイプの使い捨てのもの
か、あるいは逆洗による再生可能な、たとえば焼結金属
によるものであるが、細孔が小さくなれば、カートリッ
ジタイプのものでは、交換頻度か多くなり、ランニング
コストが高くなり、再生可能なものであれば、再生頻度
が多くなり効率的でなく、また設備費も高い。Normally, microfiltration membranes are disposable cartridge-type membranes, or are recyclable by backwashing, for example, made of sintered metal, but as the pores become smaller, cartridge-type membranes have to be replaced more frequently. Running costs are high, and if it is recyclable, it will have to be regenerated more frequently, which is inefficient, and equipment costs are also high.
本発明が解決しようとするのは、従来の粉末活性炭方式
あるいは粒状活性炭方式において、ランニングコスト、
設備費が高く、経済的でなく、繁雑な操作が必要となり
、効率的でなく省人化するのが困難であるという問題で
ある。The present invention aims to solve the problem of running costs,
The problem is that the equipment cost is high, it is not economical, it requires complicated operations, it is not efficient, and it is difficult to save labor.
本発明は、上記事情に鑑みてなされたもので、その目的
とするところは、糖液の仕上げの精製工程で、高品質の
糖液を効率的、経済的かつ連続的に製造することができ
る糖液の精製方法を提供することにある。The present invention was made in view of the above circumstances, and its purpose is to efficiently, economically, and continuously produce high-quality sugar solution in the finishing purification process of sugar solution. The object of the present invention is to provide a method for purifying sugar solution.
上記目的を達成するために、本発明の請求項１は、活性
炭の吸着能力の賦活、あるいは再生処理をした後、さら
に塩酸等の酸処理を行い、水洗後５００ ℃以上１２０
０℃以下で熱処理を行った粒状活性炭を用いて、糖液中
の異物を除去して精製するものである。In order to achieve the above object, claim 1 of the present invention provides that after the adsorption capacity of activated carbon is activated or regenerated, it is further treated with an acid such as hydrochloric acid, and after washing with water, the temperature
It uses granular activated carbon that has been heat-treated at 0°C or lower to remove foreign substances from the sugar solution and purify it.
また、本発明の請求項２は、請求項１で処理した糖液を
、さらに１０μ夏以下０．４５μ１以上の細孔を有する
精密濾過膜を装着している精密濾過器に通して、糖液中
の異物を除去して精製するものである。In addition, claim 2 of the present invention provides that the sugar solution treated in claim 1 is further passed through a precision filter equipped with a precision filtration membrane having pores of 10 μm or less and 0.45 μ1 or more. It is purified by removing foreign substances inside.
さらに、本発明の請求項３は、請求項１で処理した糖Ｗ
ｔを、さらに液中で浸漬されると精密濾過膜と岐の間の
界面に電位差が生じる精密濾過器に通して、糖液中の異
物を除去して精製するものである。Furthermore, claim 3 of the present invention provides sugar W treated according to claim 1.
The sugar solution is further purified by passing it through a microfilter that creates a potential difference at the interface between the microfiltration membrane and the sugar solution when immersed in the solution, thereby removing foreign substances from the sugar solution.
本発明者らは、上記従来の粒状活性炭処理した糖液のＰ
Ｈ低下、電気伝導度の悪化の原因を究明解析した。すな
わち、この現象は粒状活性炭の賦活又は再生処理をされ
た後に、活性炭中の灰分含有量を減少させるために行う
塩酸等の酸処理に起因するものである。酸は活性炭中の
細孔に吸着されており、この酸は多量の水で洗浄しても
取り除かれず、ロータリーキルン、多段炉等で５００
℃以上１２００°Ｃ以下で熱処理されて初めて取り除か
れる。The present inventors have discovered that the P of the sugar solution treated with the conventional granular activated carbon is
The cause of the decrease in H and deterioration of electrical conductivity was investigated and analyzed. That is, this phenomenon is caused by acid treatment such as hydrochloric acid, which is performed to reduce the ash content in the activated carbon after the granular activated carbon has been activated or regenerated. The acid is adsorbed in the pores in the activated carbon, and this acid cannot be removed even by washing with a large amount of water, and is
It can only be removed after being heat-treated at temperatures between 1200°C and above.
そして、当該熱処理した粒状活性炭を熱水中に浸漬し、
細孔中の空気を脱気し、粒状活性炭に付着している微粉
を洗浄除去する。次いで、この粒状活性炭を吸着塔に充
填する。粒状活性炭の輸送はポンプ、空気圧で行うより
吸着塔上部の活性炭洗浄槽から重力で落下させた方が、
輸送の破砕が少なく望ましい。吸着塔に充填された粒状
活性炭は水または糖液で逆洗膨張展開させる。この膨張
展開率は静置層の３０％以上８０％以下とする。Then, the heat-treated granular activated carbon is immersed in hot water,
The air in the pores is degassed and the fine powder adhering to the granular activated carbon is washed and removed. Next, this granular activated carbon is packed into an adsorption tower. It is better to transport granular activated carbon by dropping it by gravity from the activated carbon cleaning tank at the top of the adsorption tower than by using pumps or air pressure.
It is desirable because there is less crushing during transportation. The granular activated carbon packed in the adsorption tower is backwashed and expanded with water or sugar solution. The rate of expansion and development is 30% or more and 80% or less of the stationary layer.
逆洗膨張展開させ静置させると粒状活性炭の層は沈降速
度の粒径による差に従って、小さい粒子から大きい粒子
へ順序よく整置する。この結果吸着塔での糖ｌ＆中の浮
遊物等の懸濁物の捕集能力が増す。When the granular activated carbon is left to stand after being backwashed, expanded, and developed, the layers of granular activated carbon are arranged in an orderly manner from small to large particles according to the difference in sedimentation speed depending on the particle size. As a result, the adsorption tower's ability to collect suspended matter such as suspended matter in sugar 1& is increased.
さらに当該吸着塔で粒状活性炭処理した糖液を１０μｌ
以下の細孔を有する精密濾過膜または液中に浸漬すると
当該濾過膜と液の間の界面に電位差が生じる精密濾過器
で濾過処理を行うと、吸着処理した糖液よりさらに清澄
度の良いものが得られ、また精密濾過器の単独処理より
精密濾過膜の濾過連成時間がのび、ランニングコストが
安くなり、かつ糖液の負荷変動に対し製品の清澄度が影
響されず、高品質の糖液が製造できる。Furthermore, 10 μl of sugar solution treated with granular activated carbon in the adsorption tower
When filtration is carried out using a precision filtration membrane with the following pores or a precision filtration device that creates a potential difference at the interface between the filtration membrane and the liquid when immersed in the liquid, the clarity is even better than that of the adsorption-treated sugar solution. In addition, the combined filtration time of the microfiltration membrane is longer than that of a microfilter alone, reducing running costs, and the clarity of the product is not affected by changes in the sugar solution load, resulting in high quality sugar. liquid can be produced.
以下、第１図に基づいて本発明の一実施例を説明する。 Hereinafter, one embodiment of the present invention will be described based on FIG.
第１図において符号ｌは脱塩された糖液であり、これを
熱処理した粒状活性炭を充填したｔｆｌ１２，３．４に
通液させる。ここで、上記粒状活性炭は、吸着能力の賦
活、あるいは再生処理をした後に、塩酸等の酸処理を行
い、水洗後５００′Ｃ以上１２００℃以下で熱処理を行
い、さらに、熱水中で脱気、洗浄して得られたものであ
る。そして、吸着塔２，３．４を通過した糖液５は精密
濾過器６にて糖液５の中の微細なコロイダル物質。In FIG. 1, reference numeral 1 indicates a desalted sugar solution, which is passed through TFL12, 3.4 filled with heat-treated granular activated carbon. Here, the above-mentioned granular activated carbon is subjected to an acid treatment such as hydrochloric acid after activation or regeneration treatment of its adsorption capacity, followed by heat treatment at 500'C or more and 1200C or less after washing with water, and then degassing in hot water. , obtained by washing. The sugar solution 5 that has passed through the adsorption towers 2 and 3.4 is filtered through a precision filter 6 to remove fine colloidal substances in the sugar solution 5.
活性炭等の浮遊物質をカートリッジが持っている電位差
を利用して濾過精製する。Floating substances such as activated carbon are filtered and purified using the potential difference that the cartridge has.
吸着塔２，３．４の粒状活性炭は一定量の通液量で破過
するが、吸着塔２，３．４の破過は同時に生じない。従
って、吸着塔２の活性炭充填時は糖ｉ（ｌ Ｉは配管７
を経由して吸着塔３．４に連成される。また、吸着塔３
の活性炭充填時は糖液ｌは吸着塔２を通液した後、配管
８を経由して吸着塔４に通液される。さらに、吸着塔４
の活性炭充填時は糖液ｌは吸着塔２，３を連成した後、
配管９を経由して精密濾過器６に送られる。The granular activated carbon in the adsorption towers 2 and 3.4 breaks through when a certain amount of liquid passes through the adsorption towers, but the breakthrough in the adsorption towers 2 and 3.4 does not occur at the same time. Therefore, when filling the adsorption tower 2 with activated carbon, sugar i (l I is the pipe 7
It is coupled to adsorption tower 3.4 via. In addition, adsorption tower 3
When charging the activated carbon, the sugar solution 1 passes through the adsorption tower 2 and then passes through the adsorption tower 4 via the piping 8. Furthermore, adsorption tower 4
When charging activated carbon, sugar solution l is coupled to adsorption towers 2 and 3, and then
It is sent to the precision filter 6 via piping 9.
以下、従来方法及び本発明の方法について具体的に実施
した結果を詳述する。まず、従来方法を下記に示す。Hereinafter, the results of concrete implementation of the conventional method and the method of the present invention will be described in detail. First, the conventional method is shown below.
（１）内径１７ｘｘのガラスのカラムに粒状活性炭を５
５ｃｃ充填し糖液を連成させた結果を第１表に示す。(1) 5 granular activated carbon in a glass column with an inner diameter of 17xx
Table 1 shows the results of filling 5 cc and coupling the sugar solution.
活性炭は充填量の１０倍の水で通水洗浄を行った。尚、
結果は通液量が充填量の１４倍通連成である。Activated carbon was washed by passing water through it with 10 times the amount of water filled. still,
As a result, the amount of liquid passed was 14 times the amount of filling.
（以下余白） 第 １ 表 タイプＡ活性炭は酸処理を行っている。(Margin below) No. 1 table Type A activated carbon is acid treated.
タイプＢ活性炭は酸処理を行っていない。Type B activated carbon is not acid treated.
タイプへの活性炭処理液はＰ Ｈ、電導度とも満足され
る液は得られない。It is not possible to obtain a solution that satisfies both the pH and conductivity of the activated carbon treatment solution for the type.
タイプＢの活性炭では処理液のＰ Ｈ低下はほとんとな
いが電導度について満足すべき処理液は得られない。With type B activated carbon, there is almost no decrease in the pH of the treatment solution, but a treatment solution that is satisfactory in terms of conductivity cannot be obtained.
次に、本発明の実施例について示す。Next, examples of the present invention will be described.
（２−１）上記（１）と同様の条件において、熱処理し
た粒状活性炭を充填し通液した結果を第２表に示す。(2-1) Table 2 shows the results of filling and passing heat-treated granular activated carbon under the same conditions as in (1) above.
なお、水洗条件は上記（１）と同じである。Note that the water washing conditions are the same as in (1) above.
第 ２ 表 結果はＰＨと電導度において改善された。Table 2 The results were improved in PH and conductivity.
（２−２）内径４Ｃ）ｖのガラスのカラムに熱処理した
粒状活性炭を３２３ｃｃ充填し連続試験を行った。(2-2) A continuous test was conducted by filling 323 cc of heat-treated granular activated carbon into a glass column with an inner diameter of 4C)v.
活性炭は１５分間５０％の層膨張率にて展開させて逆洗
し、さらに３６倍量の水で洗浄した。この結果を第３表
に示す。The activated carbon was developed for 15 minutes at a bed expansion rate of 50%, backwashed, and further washed with 36 times the amount of water. The results are shown in Table 3.
（以下余白）
連続試験においてもＰ Ｈ、電導度において熱処理した
粒状活性炭の効果は持続した。しかし着色度においては
改善されなかった。(Left below) Even in continuous tests, the effects of heat-treated granular activated carbon on PH and conductivity persisted. However, the degree of coloration was not improved.
（３）そこで、発明者らは上記（ｉｔ）、（２２）の処
理液の着色度が糖液のコロイダル物質。(3) Therefore, the inventors developed a colloidal substance in which the degree of coloring of the treatment liquid in (it) and (22) above is that of a sugar solution.
活性炭に起因する微粉炭と推定し、以下の試験を行った
。熱処理した粒状活性炭を通液させた糖液をミクロンサ
イズの細孔を持った濾過膜で濾過処理した。この結果を
第４表、第５表に示す。The following tests were conducted assuming that the pulverized coal was caused by activated carbon. A sugar solution passed through heat-treated granular activated carbon was filtered through a filter membrane with micron-sized pores. The results are shown in Tables 4 and 5.
第 ４ 表
第
表
細孔サイズを小さく
していけば糖液の清澄度は改
善される。しかしながら、通常当該精密濾過膜は使い棄
てであり、細孔が小さくなるに従っ“Ｃ単価も高くなり
、０．４５μ１未満の精密濾過膜を工業的に使用するに
は経済的でない。Table 4 The clarity of the sugar solution can be improved by reducing the pore size. However, such microfiltration membranes are usually disposable, and as the pores become smaller, the C unit price also increases, making it uneconomical to industrially use microfiltration membranes with a diameter of less than 0.45 μl.
（４）上記（３）における濾過試験において、界面に電
位差が生じる濾過膜を用いて濾過した。(4) In the filtration test in (3) above, filtration was performed using a filtration membrane that generated a potential difference at the interface.
第 ６ 表
※ｌ：界面に電位差を生じない濾過膜、※２・界面に電
位差が生じる濾過膜、※３．界面に電位差が※２の濾過
膜の約２培土じる濾過膜
糖液中の小さい粒子、又はコロイダル物質か静電気吸着
と細孔によるフィルトレーンヨンによって着色度が大巾
に改善され高品質の糖液が得られた。Table 6 *1: Filtration membranes that do not create a potential difference at the interface, *2. Filtration membranes that create a potential difference at the interface, *3. The degree of coloration is greatly improved by small particles in the sugar solution or colloidal substances, or by electrostatic adsorption and pores of the filtration membrane, which has a potential difference at the interface. A liquid was obtained.
このように、本発明によれば、活性炭の充填時も製造中
止させず、高品質の糖液が連続的かつ経済的に製造でき
る。As described above, according to the present invention, high-quality sugar solution can be produced continuously and economically without stopping production even when filling activated carbon.
以上説明したように、本発明の請求項１は、活性炭の吸
着能力の賦活、あるいは再生処理をした後、さらに塩酸
等の酸処理を行い、水洗後５００°Ｃ以上１２００″Ｃ
以下で熱処理を行った粒状活性炭を用いて、糖液中の異
物を除去して精製するものであるから、粒状活性炭を熱
処理することによって、粒状活性炭から酸を取り除き、
糖液のＰＨ。As explained above, claim 1 of the present invention is to activate or regenerate the adsorption capacity of activated carbon, and then to perform acid treatment such as hydrochloric acid, and after washing with water, to
Since the heat-treated granular activated carbon is used to remove foreign substances from the sugar solution and purify it, by heat-treating the granular activated carbon, the acid is removed from the granular activated carbon.
PH of sugar solution.
電導度を改善することができる。Conductivity can be improved.
また、粉状活性炭処理した糖液を、１０μ次以下０．４
５μ肩以上の細孔を有する精密濾過膜。In addition, the sugar solution treated with powdered activated carbon is
A precision filtration membrane with pores of 5μ or more.
あるいは液中に浸漬すると、当該濾過膜と液との間の界
面に電位差を生じる精密濾過器で濾過処理することによ
り、吸着処理した糖液よりさらに清澄度の良いものが得
られ、かつ精密濾過器の単独処理より、精密濾過膜の濾
過通液時間がのび、ランニングコストが安くなり、かつ
糖液の負荷変動に対して製品の清澄度が影響されず、高
品質の糖液が製造できる。Alternatively, by filtration using a precision filter that creates a potential difference at the interface between the filtration membrane and the solution when immersed in the solution, a sugar solution with better clarity than adsorption treatment can be obtained, and the precision filtration Compared to single-unit processing, the filtration time through the microfiltration membrane is longer, running costs are lower, and the clarity of the product is not affected by sugar solution load fluctuations, making it possible to produce high-quality sugar solution.
第１図は本発明の一実施例を示す糖酸精製工程の最終仕
上工程を説明する説明図である。
１・・・脱塩された糖ｌ夜（原液）、２，３．４・・・
吸着塔、５・・・糖液、６・・・精密濾過器。FIG. 1 is an explanatory diagram illustrating the final finishing step of the sugar acid purification step showing one embodiment of the present invention. 1... Desalted sugar (undiluted solution), 2, 3.4...
Adsorption tower, 5...sugar solution, 6... precision filter.
Claims (3)
た後、さらに塩酸等の酸処理を行い、水洗後５００℃以
上１２００℃以下で熱処理を行った粒状活性炭を用いて
、糖液中の異物を除去して精製することを特徴とする糖
液の精製方法。(1) After activating or regenerating the adsorption capacity of activated carbon, it is further treated with an acid such as hydrochloric acid, washed with water, and then heat-treated at a temperature of 500°C or more and 1200°C or less. A method for purifying a sugar solution, characterized by purifying it by removing.
０．４５μｍ以上の細孔を有する精密濾過膜を装着して
いる精密濾過器に通して、糖液中の異物を除去して精製
することを特徴とする糖液の精製方法。(2) The sugar solution treated according to claim 1 is further purified by passing it through a microfilter equipped with a microfiltration membrane having pores of 10 μm or less and 0.45 μm or more to remove foreign substances in the sugar solution. A method for purifying a sugar solution, characterized by:
れると精密濾過膜と液の間の界面に電位差が生じる精密
濾過器に通して、糖液中の異物を除去して精製すること
を特徴とする糖液の精製方法。(3) The sugar solution treated in claim 1 is further passed through a microfilter that creates a potential difference at the interface between the microfiltration membrane and the solution when immersed in the solution to remove foreign substances in the sugar solution. A method for purifying a sugar solution, characterized by purifying it.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP01322245A JP3117979B2 (en) | 1989-12-12 | 1989-12-12 | Sugar solution purification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP01322245A JP3117979B2 (en) | 1989-12-12 | 1989-12-12 | Sugar solution purification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03183500A true JPH03183500A (en) | 1991-08-09 |
| JP3117979B2 JP3117979B2 (en) | 2000-12-18 |
Family
ID=18141526
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP01322245A Expired - Lifetime JP3117979B2 (en) | 1989-12-12 | 1989-12-12 | Sugar solution purification method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3117979B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0591900A (en) * | 1991-01-16 | 1993-04-16 | Natl Starch & Chem Investment Holding Corp | Treatment of polysaccharide with column carbon |
| JP2010233576A (en) * | 2003-03-05 | 2010-10-21 | Nippon Beet Sugar Mfg Co Ltd | Process for purifying difructose dianhydride iii crystal |
| JP2010284133A (en) * | 2009-06-15 | 2010-12-24 | Nippon Rensui Co Ltd | Method for producing purified sugar solution |
| WO2019189650A1 (en) * | 2018-03-29 | 2019-10-03 | 東レ株式会社 | Method for producing glucose syrup and method for producing chemical product |
-
1989
- 1989-12-12 JP JP01322245A patent/JP3117979B2/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0591900A (en) * | 1991-01-16 | 1993-04-16 | Natl Starch & Chem Investment Holding Corp | Treatment of polysaccharide with column carbon |
| JP2010233576A (en) * | 2003-03-05 | 2010-10-21 | Nippon Beet Sugar Mfg Co Ltd | Process for purifying difructose dianhydride iii crystal |
| JP2010284133A (en) * | 2009-06-15 | 2010-12-24 | Nippon Rensui Co Ltd | Method for producing purified sugar solution |
| WO2019189650A1 (en) * | 2018-03-29 | 2019-10-03 | 東レ株式会社 | Method for producing glucose syrup and method for producing chemical product |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3117979B2 (en) | 2000-12-18 |
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