JP6942603B2 - Purified sugar manufacturing equipment and manufacturing method - Google Patents

Description

The present invention relates to an apparatus and a method for producing purified sugar.

In the sucrose refining step, a carbonic acid filling step is usually performed in which raw sugar produced from sugar cane or the like is washed, dissolved in warm water, and then impurities are aggregated into fine crystals of calcium carbonate formed by adding lime and carbon dioxide gas. After that, decolorization is performed using activated carbon or an ion exchange resin (see, for example, Patent Document 1) to obtain a sugar solution. This decolorized sugar solution is crystallized to obtain purified sugar.

The carbonic acid saturation step is an important step in removing various impurities, and is considered to be an indispensable step in the purification of sucrose. This carbon dioxide filling step uses a large amount of lime and carbon dioxide. In order to obtain carbon dioxide, it is necessary to burn fuel, which consumes a large amount of energy. Further, although carbon dioxide gas in the exhaust gas of a boiler or the like is normally used, there is a problem that carbon dioxide gas cannot be supplied when the boiler or the like is not in operation. In the carbonic acid satiation process, the cost of coal and a large amount of waste of calcium carbonate including organic substances generated are further problems. From these points, it is desired to omit the carbonation saturation step.

A method using a magnesia adsorbent as an alternative to the carbonic acid saturation step (see, for example, Patent Document 2) is also known, but it is insufficient in removing impurities and decolorizing the raw sugar.

Japanese Unexamined Patent Publication No. 2015-136336 Japanese Unexamined Patent Publication No. 61-274787

An object of the present invention is to provide a refined sugar production apparatus and a production method capable of omitting a carbon dioxide saturation step and obtaining a refined sugar with a quality equal to or higher than that of a purification method including a carbonic acid saturation step. There is.

In the present invention, a filtering means for filtering a solution of raw sugar, an activated charcoal treatment means for treating the obtained filtered liquid with activated charcoal, and an OH-type strongly basic anion exchange resin for treating the obtained activated charcoal liquid are used. And an ion exchange treatment means for desalting with an ion exchange resin containing an H-type weakly acidic cation exchange resin, and a magnesium oxide treatment means for treating the solution with magnesium oxide is provided in front of the filtration means. Further prepared, it is a refined sugar production apparatus that does not perform carbonic acid saturation.

In the purified sugar production apparatus, the magnesium oxide is preferably porous magnesium oxide having a specific surface area of 100 m ² / g or more.

In the purified sugar production apparatus, a weakly acidic cation exchange treatment means for treating the obtained filtrate with a weakly acidic cation exchange resin to adjust the pH to a range of 6 to 8 is further provided after the filtering means. Is preferable.

In the purified sugar production apparatus, 30 to 60 mol% of the functional groups of the weakly acidic cation exchange resin in the weakly acidic cation exchange treatment means may be at least one of sodium form and potassium form. preferable.

Further, in the present invention, a filtration step of filtering a solution of raw sugar, an activated charcoal treatment step of treating the obtained filtered solution with activated charcoal, and an OH-type strongly basic anion using the obtained activated charcoal-treated solution are used. the ion exchange resin containing exchange resin and H-shaped weakly acidic cation exchange resin and an ion exchange treatment step of desalting, only contains, in front of the filtration process, magnesium oxide treating the solution with magnesium oxide It is a method for producing a purified sugar , which further includes a treatment step and does not include a carbon dioxide saturation step.

In the method for producing purified sugar, the magnesium ^{oxide is preferably porous magnesium oxide having a specific surface area of 100 m 2} / g or more.

In the method for producing purified sugar, a weakly acidic cation exchange treatment step of treating the obtained filtrate with a weakly acidic cation exchange resin to adjust the pH to a range of 6 to 8 is further included in the subsequent stage of the filtration step. Is preferable.

In the method for producing a purified sugar, 30 to 60 mol% of the functional group of the weakly acidic cation exchange resin in the weakly acidic cation exchange treatment step is at least one of sodium form and potassium form. preferable.

According to the present invention, the carbonic acid saturation step can be omitted, and the refined sugar can be obtained with a quality equal to or higher than that of the purification method including the carbonic acid saturation step.

It is a schematic block diagram which shows an example of the purified sugar production apparatus which concerns on embodiment of this invention. It is a schematic block diagram which shows another example of the refined sugar production apparatus which concerns on embodiment of this invention. It is a schematic block diagram which shows another example of the refined sugar production apparatus which concerns on embodiment of this invention.

Embodiments of the present invention will be described below. The present embodiment is an example of carrying out the present invention, and the present invention is not limited to the present embodiment.

An outline of an example of an apparatus for producing purified sugar according to an embodiment of the present invention is shown in FIG. 1, and its configuration will be described. The refined sugar production apparatus 1 includes a filtration apparatus 12 as a filtration means for filtering a solution of raw sugar, an activated carbon treatment apparatus 14 as an activated carbon treatment means for treating the filtrate obtained by the filtration means with activated carbon, and an activated carbon. An ion exchange treatment device 16 is provided as an ion exchange treatment means for desalting the activated carbon treatment liquid obtained by the treatment means with an ion exchange resin. The purified sugar production apparatus 1 is crystallized as a dissolution means for dissolving the raw sugar to obtain a dissolution liquid, and as a crystallization means for crystallizing the ion exchange treatment liquid obtained by the ion exchange treatment means. At least one of the devices 18 may be further provided. Further, a concentrator 20 may be further provided as a concentrating means for concentrating the ion exchange treatment liquid obtained by the ion exchange treatment means to obtain a liquid sugar.

In the purified sugar production apparatus 1 of FIG. 1, the outlet of the dissolution tank 10 and the inlet of the filtration device 12 are connected by a pipe 22, and the outlet of the filtration device 12 and the inlet of the activated carbon treatment apparatus 14 are connected by a pipe 24. The outlet of the activated carbon treatment device 14 and the inlet of the ion exchange treatment device 16 are connected by a pipe 26, the outlet of the ion exchange treatment device 16 and the inlet of the crystallization device 18 are connected by a pipe 28, and the outlet of the crystallization device 18 is connected. A pipe 30 is connected to the pipe 30. The pipe 32 branched from the pipe 28 is connected to the inlet of the concentrator 20, and the pipe 34 is connected to the outlet of the concentrator 20. A storage tank for storing the filtered liquid between the filtration device 12 and the activated carbon treatment device 14, a storage tank for storing the activated carbon treatment liquid between the activated carbon treatment device 14 and the ion exchange treatment device 16, and an ion exchange treatment. A storage tank or the like for storing the ion exchange treatment liquid may be provided between the device 16 and the crystallization device 18.

The method for producing purified sugar and the operation of the device 1 for producing purified sugar according to the present embodiment will be described.

The raw sugar is supplied to the dissolution tank 10, and the raw sugar is dissolved in warm water or the like in the dissolution tank 10 to obtain a dissolution liquid (dissolution step). The dissolution liquid of the raw material sugar is supplied to the filtration device 12 through the pipe 22, and the filtration device 12 performs the filtration treatment of the dissolution liquid (filtration step). The filtrate obtained in the filtration step is supplied to the activated carbon treatment device 14 through the pipe 24, and is treated with activated carbon in the activated carbon treatment device 14 (activated carbon treatment step). The activated carbon treatment liquid obtained in the activated carbon treatment step is supplied to the ion exchange treatment device 16 through the pipe 26, and is desalted by the ion exchange resin in the ion exchange treatment device 16 (ion exchange treatment step). At least a part of the ion exchange treatment liquid obtained in the ion exchange treatment step is supplied to the crystallization device 18 through the pipe 28, and crystallization is performed in the crystallization device 18 (crystallization step). The crystals obtained in the crystallization step are discharged as purified sugar through the pipe 30. On the other hand, a part or all of the ion exchange treatment liquid obtained in the ion exchange treatment step may be supplied to the concentrator 20 through the pipe 32 branched from the pipe 28 and concentrated in the concentrator 20 to be a liquid sugar. (Concentration step). The liquid sugar obtained in the concentration step is discharged through the pipe 34. The liquid sugar obtained in the concentration step may be further sterilized, filtered, or the like, if necessary.

By the method for producing refined sugar and the apparatus for producing refined sugar according to the present embodiment, the carbon dioxide saturation step can be omitted, and the refined sugar can be obtained with a quality equal to or higher than that of the purification method including the carbonic acid saturation step. can. High-quality refined sugar can be obtained without carbon dioxide saturation, and by not performing carbon dioxide saturation, it is possible to reduce the cost of chemicals such as lime and carbon dioxide, and the production cost such as energy cost. Further, it is possible to produce purified sugar even when the boiler or the like does not operate in the raw sugar factory or the like (for example, the sugar rest period). It is possible to omit the sugar washing process of washing the raw sugar, eliminate the loss due to sugar washing, and improve the refining yield. It is considered that the desalting treatment with an ion exchange resin increases the crystallization efficiency in the crystallization step, improves the yield and quality of the purified sugar, and improves the purification yield.

In the conventional method for purifying sucrose, crystallized purified sugar may be re-dissolved to make it liquid in order to obtain liquid sugar. However, the method for producing purified sugar and the apparatus for producing purified sugar according to the present embodiment. According to the above, since the desalting treatment is carried out by the ion exchange treatment, high quality sucrose can be obtained by concentrating the ion exchange treatment liquid obtained in the ion exchange treatment step.

The raw sugar is produced from sugar cane, sugar beet, etc., and contains sucrose. Sucrose is a disaccharide in which glucose (dextrose) and fructose (fructose) are bound.

In the dissolution step, the raw sugar is dissolved in a solvent such as water in the dissolution tank 10 to obtain a dissolution liquid. If necessary, it may be heated to about 60 to 90 ° C., preferably about 70 to 90 ° C. The melting tank 10 may be provided with a stirring means such as a stirring blade. The solvent such as water may be used, for example, 40 to 100 parts by weight with respect to 100 parts by weight of the raw sugar.

After the dissolution step, if necessary, the pH may be adjusted to the range of 6 to 8 with a pH adjuster (pH adjustment step). As the pH adjuster, for example, an acid such as hydrochloric acid or an alkaline agent such as sodium carbonate may be used. The pH adjustment may be performed in the dissolution tank 10 or the pipe 22, or may be performed in the pH adjustment tank by separately providing a pH adjustment tank between the dissolution tank 10 and the filtration device 12.

In the filtration step, the solution of the raw sugar is filtered to remove insoluble matter. The filtration method is not particularly limited, and for example, the filtration treatment may be performed using a filter precoated with diatomaceous earth, pearlite or the like as a filtration aid. In the filtration step, for example, the solution may be passed through a filter precoated with a filtration auxiliary material such as diatomaceous earth by an upward flow, a downward flow, or a lateral flow.

In the activated carbon treatment step, the filtrate obtained in the filtration step is treated with activated carbon and mainly decolorized. Examples of the activated carbon include granular activated carbon, powdered activated carbon and the like, and it is preferable to use granular activated carbon from the viewpoint of economy, operability and the like. In the activated carbon treatment step, for example, the filtered liquid may be passed through a packed tower filled with granular activated carbon by an upward flow or a downward flow.

The granular activated carbon is an activated carbon having a volume average particle diameter of 200 to 2000 μm. As the granular activated carbon, for example, Diahope MS-10 (manufactured by Calgon Carbon Co., Ltd.), NORIT GAC1240 (manufactured by Cabot Norit Co., Ltd.) and the like can be used.

In the ion exchange treatment step, the activated carbon treatment liquid obtained in the activated carbon treatment step is desalted with an ion exchange resin. In the ion exchange treatment step, decolorization treatment can also be performed.

As the ion exchange resin, a strong basic anion exchange resin such as OH type, a weakly acidic cation exchange resin such as H type, and the like are used. Examples of the treatment method in the ion exchange treatment step include the following methods (1) to (4).
(1) After treatment with a single bed tower of an OH type strongly basic anion exchange resin, treatment is performed with a single bed tower of an H type weakly acidic cation exchange resin.
(2) The treatment is carried out in a mixed bed tower in which an OH-type strong basic anion exchange resin and an H-type weakly acidic cation exchange resin are mixed and filled.
(3) After treating with a single bed tower of OH type strongly basic anion exchange resin, it is treated with a mixed bed tower in which OH type strongly basic anion exchange resin and H type weakly acidic cation exchange resin are mixed and filled. ..
(4) The first column in which an OH-type strong basic anion exchange resin and a sodium (Na) -type or potassium (K) -type cation exchange resin are mixed and filled or made into a multi-layer bed, and an OH-type strong basic anion. The treatment is carried out in a mixed bed tower (second tower) in which the exchange resin and the H-type weakly acidic cation exchange resin are mixed and filled.

Of these, the treatment method (4) is preferable from the viewpoint of the quality of the treatment liquid and the like. When the filtered solution of the magnesium oxide-treated solution is subjected to a weakly acidic cation exchange treatment as in the purified sugar production apparatus 5 of FIG. 3, which will be described later, the treatment method of (3) may be used.

Examples of the OH-type strongly basic anion exchange resin include an acrylic-based OH-type strongly basic anion exchange resin and a styrene-based OH-type strongly basic anion exchange resin. Examples of acrylic OH-type strongly basic anion exchange resins include Amberlite (registered trademark, the same applies hereinafter) IRA958, IRA458RF (manufactured by Dow Chemical Co., Ltd.), PUROLITE (registered trademark, the same applies hereinafter) A860, A850 (Purolite). (Manufactured by the company) and the like. Among the acrylic OH-type strong basic anion exchange resins, the gel type resin is particularly advantageous because it has a large exchange capacity and the amount of sucrose solution that can be treated is large. Examples of the gel-type acrylic strongly basic anion exchange resin include Amberlite IRA458RF (manufactured by Dow Chemical Co., Ltd.) and PUROLITE A850 (manufactured by Purolite Co., Ltd.).

Examples of the styrene-based OH-type strongly basic anion exchange resin include Amberlite IRA900J, IRA402, IRA402BL (manufactured by Dow Chemical Corporation), PUROLITE A500S (manufactured by Purolite Co., Ltd.), Diaion (registered trademark, the same applies hereinafter) SA10A, Examples include PA308 (manufactured by Mitsubishi Chemical Corporation).

Examples of the H-type weakly acidic cation exchange resin include Amberlite IRC76, Dowex (registered trademark, the same applies hereinafter) MAC-3 (manufactured by Dow Chemical Corporation), PUROLITE C115E (manufactured by Purolite), Diaion WK10, WK11 (manufactured by Purolite). Mitsubishi Chemical Corporation) and the like.

The Na-type or K-type cation exchange resin may be a strongly acidic cation exchange resin or a weakly acidic cation exchange resin. Examples of the Na-type strong acid cation exchange resin include Amberlite IR120B Na, IR124 Na, 200CT Na, 252 Na, Amberlex 100 (manufactured by Dow Chemical Corporation), Diaion SK1B, PK216 (manufactured by Mitsubishi Chemical Corporation), and PUROLITE. Examples include C100E (manufactured by Purolite). Alternatively, a known H-type strong acid cation exchange resin converted into a Na-type or K-type strong acid cation exchange resin by regenerating it with a regenerating agent such as NaOH or KOH may be used. Similarly, a known H-type weakly acidic cation exchange resin may be converted into a Na-type or K-type weakly acidic cation exchange resin by regenerating it with a regenerating agent such as NaOH or KOH.

In the crystallization step, at least a part of the ion exchange treatment liquid obtained in the ion exchange treatment step is crystallized to obtain purified sugar. Crystallization is carried out, for example, by heating and concentrating the ion exchange treatment liquid at 40 to 80 ° C. under reduced pressure. Usually, sucrose crystal nuclei are added during concentration.

In the concentration step, a part or all of the ion exchange treatment liquid obtained in the ion exchange treatment step is concentrated to obtain a liquid sugar. Concentration is performed, for example, by heating and concentrating the ion exchange treatment liquid at 40 to 80 ° C.

According to the method for producing purified sugar according to the present embodiment, for example, a color value of 600 I. U.S. From the above raw sugars, the color value was set to 30 I. U.S. To the following, preferably 20 I. U.S. Purified sugar reduced to the following can be obtained.

In the method for producing purified sugar and the apparatus for producing purified sugar according to the present embodiment, a magnesium oxide treatment means may be provided in the first stage of the filtration treatment step by the filtration means, and the solution of the raw sugar may be treated with magnesium oxide. ..

In addition to the configuration of the purified sugar producing apparatus 1 of FIG. 1, the purified sugar producing apparatus 3 of FIG. As a magnesium oxide treatment means for treating magnesium oxide, a magnesium oxide treatment device 36 is further provided. In the purified sugar production apparatus 3 of FIG. 2, the outlet of the dissolution tank 10 and the inlet of the magnesium oxide treatment device 36 are connected by a pipe 38, and the outlet of the magnesium oxide treatment device 36 and the inlet of the filtration device 12 are connected by a pipe 40. It is connected.

In the purified sugar production apparatus 3 of FIG. 2, the raw sugar is supplied to the dissolution tank 10, and the raw sugar is dissolved in warm water or the like in the dissolution tank 10 to obtain a dissolution liquid (dissolution step). The solution of the raw sugar is supplied to the magnesium oxide treatment device 36 through the pipe 38, and the magnesium oxide treatment of the solution is performed in the magnesium oxide treatment device 36 (magnesium oxide treatment step). The magnesium oxide-treated liquid obtained in the magnesium oxide treatment step is supplied to the filtration device 12 through the pipe 40, and the magnesium oxide-treated liquid is filtered in the filtration device 12 (filtration step). After the filtration step, if necessary, the pH may be adjusted to the range of 6 to 8 with a pH adjuster (pH adjustment step). As the pH adjuster, for example, an acid such as hydrochloric acid or an alkaline agent such as sodium carbonate may be used. The pH adjustment may be performed in the pipe 24, or may be performed in the pH adjustment tank by separately providing a pH adjustment tank between the filtration device 12 and the activated carbon treatment device 14. After that, in the same manner as in the refined sugar production apparatus 1 of FIG. 1, an activated carbon treatment step, an ion exchange treatment step, a crystallization step, and a concentration step if necessary are performed.

By performing the magnesium oxide treatment, impurities are further removed even when the quality of the raw sugar is low (for example, a color value of 1000 IU or more), and a high quality purified sugar can be obtained. When the quality of the raw sugar is high (for example, the color value is less than 800 IU), the magnesium oxide treatment may not be performed.

Examples of magnesium oxide include powdered magnesium oxide and porous magnesium oxide, and it is preferable to use porous magnesium oxide. The specific surface area of the porous magnesium oxide ^{is preferably 100 m 2} / g or more, and more preferably 120 m ² / g or more. If the specific surface area of magnesium oxide ^{is less than 100 m 2} / g, the effect of removing impurities may be low. The upper limit of the specific surface area of magnesium oxide is the higher as long as it can be produced and the strength can be maintained.

In the latter stage of the filtration step by the filtration means, a weakly acidic cation exchange treatment means may be provided, and the filtrate obtained in the filtration step may be treated with a weakly acidic cation exchange resin to adjust the pH to the range of 6 to 8. (Weakly acidic cation exchange treatment means).

The refined sugar production apparatus 5 of FIG. 3 is obtained in a filtration step in the latter stage of the filtration apparatus 12, that is, between the filtration apparatus 12 and the activated carbon treatment apparatus 14, in addition to the configuration of the refined sugar production apparatus 3 of FIG. A weakly acidic cation exchange treatment device 42 is further provided as a weakly acidic cation exchange treatment means for treating the obtained filtrate with a weakly acidic cation exchange resin to adjust the pH to a range of 6 to 8. In the purified sugar production apparatus 5 of FIG. 3, the outlet of the filtration apparatus 12 and the inlet of the weakly acidic cation exchange processing apparatus 42 are connected by a pipe 44, and the outlet of the weakly acidic cation exchange processing apparatus 42 and the activated charcoal processing apparatus 14 are connected. Is connected to the entrance of the pipe 46 by a pipe 46. A storage tank for storing the filtrate between the filtration device 12 and the weakly acidic cation exchange treatment device 42, and a weakly acidic cation exchange treatment liquid between the weakly acidic cation exchange treatment device 42 and the activated charcoal treatment device 14. A storage tank or the like for storing the water may be provided. In addition to the configuration of the purified sugar production device 1 in FIG. 1, a weakly acidic cation is used to transfer the filtrate obtained in the filtration step to the latter stage of the filtration device 12, that is, between the filtration device 12 and the activated carbon treatment device 14. A weakly acidic cation exchange treatment device 42 may be further provided as a weakly acidic cation exchange treatment means for treating with an exchange resin and adjusting the pH to a range of 6 to 8.

In the purified sugar manufacturing apparatus 5 of FIG. 3, the raw sugar is supplied to the dissolution tank 10, and the raw sugar is dissolved in warm water or the like in the dissolution tank 10 to obtain a dissolution liquid (dissolution step). The solution of the raw sugar is supplied to the magnesium oxide treatment device 36 through the pipe 38, and the magnesium oxide treatment of the solution is performed in the magnesium oxide treatment device 36 (magnesium oxide treatment step). The magnesium oxide-treated liquid obtained in the magnesium oxide treatment step is supplied to the filtration device 12 through the pipe 40, and the magnesium oxide-treated liquid is filtered in the filtration device 12 (filtration step). The filtrate obtained in the filtration step is supplied to the weakly acidic cation exchange treatment device 42 through the pipe 44, and the weakly acidic cation exchange treatment of the filtrate is performed in the weakly acidic cation exchange treatment device 42 (weakly acidic cations). Ion exchange processing process). The weakly acidic cation exchange treatment liquid obtained in the weakly acidic cation exchange treatment step is supplied to the activated carbon treatment apparatus 14 through the pipe 46, and the activated carbon treatment of the weakly acidic cation exchange treatment liquid is performed in the activated carbon treatment apparatus 14 ( Activated carbon treatment process). After that, the ion exchange treatment step, the crystallization step, and if necessary, the concentration step are performed in the same manner as in the purified sugar production apparatus 1 of FIG.

By performing a weakly acidic cation exchange treatment on the magnesium oxide-treated solution, the pH can be easily adjusted to the range of 6 to 8, and since no acid is added, there is an advantage that the salt concentration in the sugar solution does not increase. Further, hardness components such as Mg and Ca in the sugar solution are exchanged for Na and K, and scaling to equipment in the subsequent process can be suppressed.

Examples of the weakly acidic cation exchange resin include Amberlite IRC76, Dowex (registered trademark, the same applies hereinafter) MAC-3 (manufactured by Dow Chemical Co., Ltd.), PUROLITE C115E (manufactured by Purolite Co., Ltd.), Diaion WK10, WK11 (Mitsubishi Chemical Co., Ltd.). H-type weakly acidic cation exchange resin such as (manufactured by the company) can be used.

It is preferable that 30 to 60 mol% of the functional group of the weakly acidic cation exchange resin used in the weakly acidic cation exchange processing apparatus 42 is at least one of sodium form and potassium form, and 40 to 50 mol%. Is more preferably at least one of the sodium and potassium forms. The remaining functional groups are H-type. When 30 to 60 mol% of the functional group of the weakly acidic cation exchange resin is at least one of the sodium form and the potassium form, it becomes easy to adjust the pH of the magnesium oxide treatment solution in the range of 6 to 8. .. If less than 30 mol% of the functional groups of the weakly acidic cation exchange resin are at least one of the sodium and potassium forms, the pH can be less than 6, and more than 60 mol% of the sodium and potassium forms. At least one of the forms may have a pH greater than 8.

In the latter stage of the ion exchange treatment step by the ion exchange treatment means, a second activated carbon treatment means may be provided to treat the ion exchange treatment liquid with activated carbon (second activated carbon treatment step). Examples of the activated carbon used in the second activated carbon treatment step include granular activated carbon and powdered activated carbon, and it is preferable to use granular activated carbon. In the second activated carbon treatment step, for example, the ion exchange treatment liquid may be passed through a packed bed filled with granular activated carbon by an upward flow and a downward flow. By treating the ion exchange treatment liquid with activated carbon, impurities can be further removed and the color value can be further reduced.

Hereinafter, the present invention will be described in more detail with reference to Examples and Comparative Examples, but the present invention is not limited to the following Examples.

<Examples 1 to 3>
Using the raw sugars of the quality shown in Table 1, the purification treatment was carried out using the refined sugar production apparatus 1 shown in FIG.

The raw sugar was dissolved in warm water at 70 ° C. and sodium carbonate was added to adjust the pH to 7.5. Filtration treatment was performed using diatomaceous earth, and the liquid was passed through a column packed with granular activated carbon (Diahope MS-10, manufactured by Calgon Carbon Co., Ltd.). Regarding the obtained activated carbon treatment liquid, OH type strongly basic anion exchange resin (Amberlite IRA458RF, manufactured by Dow Chemical Co., Ltd.) and sodium (Na) type or potassium (K) type cation exchange resin (Amberlex 100, Dow Chemical Co., Ltd.) OH type strongly basic anion exchange resin (IRA900J, manufactured by Dow Chemical Co., Ltd.) and H type weakly acidic cation exchange resin (Amberlite IRC76, manufactured by Dow Chemical Co., Ltd.) ) Was mixed and filled in a mixed bed tower (second tower) for desalting.

Brix (%), pH, conductivity (μS / cm), ash content (%), and color value (I.U.) of each liquid were measured at the dissolution liquid, the activated carbon treatment inlet, the activated carbon treatment outlet, and the ion exchange treatment outlet. bottom. Brix (%) representing the sugar content was measured using a digital refractometer (manufactured by Atago, RX-5000i). The pH was measured using a pH measuring device (manufactured by TOA-DKK, HM-26S). The conductivity (μS / cm) was measured using a conductivity measuring device (manufactured by Yokogawa Electric, SC-72). The ash content (%) was calculated by the ICUMSA method from the measured value of conductivity. The color value (I.U.) was calculated by measuring the absorbance of the sugar solution using a spectrophotometer (U-3010, manufactured by Hitachi, Ltd.) according to the ICUMSA method. The results are shown in Tables 2, 3 and 4, respectively.

<Comparative example 1>
Using the raw sugar of Example 1 shown in Table 1, purification treatment was carried out by a method of desalting and decoloring with an ion exchange resin including a conventional carbonic acid saturation step. The results are shown in Table 5, respectively.

As described above, the method and apparatus of the examples made it possible to omit the carbonic acid saturation step, and it was possible to obtain the refined sugar with a quality equal to or higher than that of the purification method including the carbonic acid saturation step.

<Reference experiments 1-3>
Magnesium oxide powder (UC-95ST, manufactured by Ube Material Industries Ltd.), magnesium hydroxide powder (UD-650-1, manufactured by Ube Material Industries Ltd.), porous magnesium oxide (UCM-150, manufactured by Ube Material Industries Ltd.) ) Was used to bring it into contact with the solution of the raw sugar, and the effect of reducing the color value was confirmed (reference experiment 1).

(experimental method)
Using a solution prepared by adding warm water at 70 ° C to the raw sugar of Example 2 in Table 1, 1000 mg / L of each additive was added, and the mixture was stirred at 70 ° C for 1 minute and then filtered using diatomaceous earth. , Sodium carbonate was added to adjust the pH to 7.0, and then the color value was measured. The results are shown in Table 6.

By using magnesium oxide powder or porous magnesium oxide, the color value of the solution of raw sugar can be reduced, and in particular, by using porous magnesium oxide, the color value of the solution of raw sugar is significantly reduced. We were able to.

<Example 4>
Using the raw sugar of Example 2 in Table 1, a purification treatment was carried out using the refined sugar production apparatus 3 shown in FIG.

The raw sugar is dissolved in warm water at 70 ° C., 250 mg / L of porous magnesium oxide (UCM-150, manufactured by Ube Material Industries Ltd.) is added, the mixture is stirred at 70 ° C. for 1 minute, and then filtered using diatomaceous earth. , Hydrochloric acid was added to adjust the pH to 7.5. The liquid was passed through a column packed with granular activated carbon (Diahope MS-10). The obtained activated carbon treatment liquid was desalted with an ion exchange resin in the same manner as in Example 2.

In the same manner as in Example 2, after neutralization of the solution and the magnesium oxide step treatment liquid (activated carbon treatment inlet), at the activated carbon treatment outlet and the ion exchange treatment outlet, Brix (%), pH, conductivity (μS / cm), The ash content (%) and the color value (IU) were measured. The results are shown in Table 7, respectively.

Comparing the results of Example 4 (Table 7) with the results of Example 2 (Table 3), it was found that the use of porous magnesium oxide significantly reduced the color value of the solution of the raw sugar. ..

<Example 5>
Using the raw sugar of Example 2 in Table 1, a purification treatment was carried out using the refined sugar production apparatus 5 shown in FIG.

The raw sugar is dissolved in warm water at 70 ° C., 250 mg / L of porous magnesium oxide (UCM-150, manufactured by Ube Material Industries Ltd.) is added, the mixture is stirred at 70 ° C. for 1 minute, and then filtered using diatomaceous earth. rice field. The obtained filtrate was passed through a column packed with a weakly acidic cation exchange resin having 50% of functional groups in the form of sodium with a sodium hydroxide solution to obtain a weakly acidic cation exchange treatment solution. The obtained weakly acidic cation exchange treatment liquid was passed through a column packed with granular activated carbon (Diahope MS-10). The obtained activated carbon treatment liquid was desalted with an ion exchange resin in the same manner as in Example 2.

Brix (%), pH, conductivity (μS / cm), ash content in the solution, the weakly acidic cation exchange treatment liquid (activated carbon treatment inlet), the activated carbon treatment outlet, and the ion exchange treatment outlet in the same manner as in Example 2. (%) And color value (IU) were measured. The results are shown in Table 8.

By treating the magnesium oxide treatment liquid with a weakly acidic cation exchange resin, the pH could be easily adjusted to the range of 6 to 8.

<Example 6>
In the same manner as in Example 5, a weakly acidic cation exchange resin in which 20 mol%, 40 mol%, 60 mol%, and 80 mol% of the functional groups were made into sodium forms of the obtained filtrate with a sodium hydroxide solution, respectively. Was passed through a column packed with a weakly acidic cation exchange treatment solution to obtain a weakly acidic cation exchange treatment solution. The pH of the obtained weakly acidic cation exchange treatment liquid is shown in Table 9, respectively.

As described above, the pH of the magnesium oxide treatment solution is adjusted to the range of 6 to 8 by having 30 to 60 mol% of the functional groups of the weakly acidic cation exchange resin being at least one of the sodium form and the potassium form. It will be easier to do.

1,3,5 Purified sugar production equipment, 10 dissolution tanks, 12 filtration equipment, 14 activated charcoal processing equipment, 16 ion exchange processing equipment, 18 crystallization equipment, 20 concentrators, 22, 24, 26, 28, 30, 32 , 34, 38, 40, 44, 46 Piping, 36 Magnesium oxide treatment equipment, 42 Weakly acidic cation exchange treatment equipment.

Claims (8)

Filtration means for filtering the solution of raw sugar and
Activated carbon treatment means for treating the obtained filtrate with activated carbon,
An ion exchange treatment means for desalting the obtained activated charcoal treatment liquid with an ion exchange resin containing an OH-type strong basic anion exchange resin and an H-type weakly acidic cation exchange resin.
Equipped with a,
A magnesium oxide treatment means for treating the solution with magnesium oxide is further provided before the filtration means.
A device for producing purified sugar, which is characterized by not performing carbonic acid saturation. The device for producing purified sugar according to claim 1.
An apparatus for producing purified sugar, wherein the magnesium oxide is a porous magnesium oxide having a specific surface area of 100 m ^{2 / g or more.} The device for producing purified sugar according to claim 1 or 2.
The production of purified sugar is further provided with a weakly acidic cation exchange treatment means for treating the obtained filtrate with a weakly acidic cation exchange resin to adjust the pH to a range of 6 to 8 after the filtration means. Device. The device for producing purified sugar according to claim 3.
An apparatus for producing a purified sugar, wherein 30 to 60 mol% of the functional group of the weakly acidic cation exchange resin in the weakly acidic cation exchange treatment means is at least one of a sodium form and a potassium form. .. A filtration process that filters the solution of the raw sugar
An activated carbon treatment step in which the obtained filtrate is treated with activated carbon,
An ion exchange treatment step of desalting the obtained activated charcoal treatment solution with an ion exchange resin containing an OH-type strong basic anion exchange resin and an H-type weakly acidic cation exchange resin.
Only including,
A magnesium oxide treatment step of treating the solution with magnesium oxide is further included before the filtration step.
A method for producing purified sugar, which does not include a carbonic acid saturation step. The method for producing purified sugar according to claim 5.
A method for producing purified sugar, wherein the magnesium oxide is a porous magnesium oxide having a specific surface area of 100 m ^{2 / g or more.} The method for producing a purified sugar according to claim 5 or 6.
The production of purified sugar further comprises a weakly acidic cation exchange treatment step of treating the obtained filtrate with a weakly acidic cation exchange resin to adjust the pH to a range of 6 to 8 after the filtration step. Method. The method for producing purified sugar according to claim 7.
A method for producing a purified sugar, wherein 30 to 60 mol% of the functional group of the weakly acidic cation exchange resin in the weakly acidic cation exchange treatment step is at least one of a sodium form and a potassium form. ..

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