CN101381417B - Refining technique method in malt amylin production process - Google Patents

Abstract

The invention discloses a refining process method for the productionof maltodextrin. The technical proposal of the method is as follows: the prior ion exchange refining system is adjusted, and a macroporous nonpolar adsorption resin column is added behind an adjustment column to form an ion exchange and adsorption resin refining system; a decolorized sugar solution directly enters the adsorption resin column through an ion exchange column for further removal of impurities and peculiar smell, and then is sent to a concentration and drying system to be processed into a dextrine product. The light transmittance of the sugar solution treated by adopting the technical proposal is improved to 96.2 percent from the prior 92.2 percent, and is improved by 3. 28 percent; the chroma is improved to a value less than 15Hz from a value which is averagely less than 40Hz; the white content is improved to 92.5 percent from average 89 percent; and particularly the odor of the product is apparently improved, is reduced to a light odor or no odor from the prior strong acid and base odor and burned odor, and achieves the requirement of customers.

Description

Refining technique in the malt amylin production process

Technical field:

The invention belongs to the maltodextrin production field, relate to the process for refining of maltodextrin.

Background technology:

Maltodextrin is one of product of starch deep processing, it is to be raw material with the starch slurry, the product between starch and Dian Fentang that makes through control low degree enzymolysis, maltodextrin is widely used in industries such as candy, beverage, food, medicine, makeup, also can be applied in other Industrial processes as dispersion agent, stablizer.

Existing dextrin product serves as main production with the GB product standard, also require to control in its production process to satisfy GB, but along with the raising of users such as food, beverage to specification of quality, the index of grading whiteness, peculiar smell, the ash of original product standard can not satisfy user's requirement, needs further to improve the specification of quality of product.

Summary of the invention:

In order to produce high-level dextrin product, must the process for refining in the existing dextrin production process be improved, with the standard of improving the quality of products, satisfy the specification of quality of high-end customer.

The inventor finds through the substantive test analysis, and the peculiar smell of dextrin product comes from the peculiar smell that starch production process and dextrin go out and produce in the enzyme operation, wherein also comprises the peculiar smell that brings in anion-cation exchange resin.The refining system of " cationic exchange coloum-anion-exchange column-adjustable column " formula of prior art can't be removed the peculiar smell problem.

In order to remove the peculiar smell in the former dextrin production process, and further improve the index such as whiteness, colourity of dextrin product, the invention provides a kind of new dextrin refining technique, the technical scheme of this method is that former ion-exchange refining system is adjusted, behind adjustable column, macropore nonpolar adsorption resin post constitutes ion-exchange and polymeric adsorbent refining system; Liquid glucose after the decolouring behind ion exchange column, directly enters adsorption resin column, further removes impurity and peculiar smell, send concentrated, dehumidification system to be processed as the dextrin product then.

General macroporous adsorbent resin all has certain taste removal effect, but its effect has suitable difference, the inventor filters out two kinds of resins of DA201-C-II and XAD16, as the preferred taste removal polymeric adsorbent that uses in the processing method of the present invention after the concrete kind of polymeric adsorbent has been carried out conscientiously estimating.

Below be the performance test experiment of two kinds of polymeric adsorbents:

Taste removal polymeric adsorbent kind:

The XAD16 ROHM AND HAAS provides;

DA201-C-II Jiangsu Su Qing provides.

Outward appearance:

The XAD16 oyster white is granular, and particle is less, and particle diameter is even

DA201-C-II brown is granular, and particle is less, and particle diameter is even

Activation and desorption method:

The XAD16 activation was used the 1%NaOH solution soaking 10 hours, used deionized water rinsing to neutral.Desorb uses 1%NaOH solution flushing (2 times of resin volumes of speed per hour) to liquid with no taste to flow out, and re-uses deionized water rinsing to neutral.

DA201-C-II activation was used the 1%NaOH+1%NaCl solution soaking 10 hours, used deionized water rinsing to neutral.Desorb uses 1%NaOH+1%NaCl solution flushing (2 times of resin volumes of speed per hour) to liquid with no taste to flow out, and re-uses deionized water rinsing to neutral.

Detection method: static adsorptive method, dynamic adsorption method

Detect and use feed liquid: electricity is led 230 μ s/cm, dry 42%.

Test-results:

Table 1 Static Adsorption adsorptive capacity relatively

Model	The resin volume	The feed liquid adsorptive capacity
			XAD16	100ml	3700ml
DA201—C—II	100ml	4300ml

Annotate: resin absorption is at room temperature carried out.

The dynamic adsorption test result:

Dynamic adsorption fashionable dress post amount is 300ml, and the high 30cm of post, 2 times of resin volumes of input speed per hour expect that temperature is a room temperature.Circulation twice, twice adsorptive capacity is as follows.

Table 2 dynamic adsorption adsorptive capacity relatively

Model	Feed liquid adsorptive capacity 1	Feed liquid adsorptive capacity 2
			XAD16	2300ml	730ml
DA201—C—II	2500ml	1990ml

Annotate: symbol 1,2 expression cycle index; Resin absorption is at room temperature carried out.

Table 3 dynamic adsorption water consumption relatively

Model	Alkali lye consumption 1	Alkali lye consumption 2	Wash water consumption 1	Wash water consumption 2
					XAD16	380ml	1170ml	1500ml	660ml
DA201-C-II	600ml	1300ml	2000ml	2100ml

Annotate: symbol 1,2 expression cycle index; Resin absorption is at room temperature carried out.

Effect is described and test result analysis:

1. the discharging liquid glucose after the absorption does not have pungent smell, and is respond well, should increase the taste removal resin absorption post of one or more parallel connections behind adjustable column.

2. resin property descends very soon after two circulations, leads too high relevantly with the electricity of polymeric adsorbent charging liquid glucose, leads 230 μ s/cm owing to detect with the liquid glucose electricity, and too high electricity is led absorption and the regeneration that has had a strong impact on polymeric adsorbent.

Therefore, except that the polymeric adsorbent kind of preferred properties excellence, should control the electricity that reduces feed liquid and lead in operating process, the flavor polymeric adsorbent is taken off in protection.

Through the repetition test screening, the inventor determines that the process conditions of adsorption resin column is as follows in the process for refining of the present invention:

Enter the sugar concentration of adsorption resin column: 33%-35%; Specific conductivity :≤50 μ s/cm; Flow: the 1.5-2 of resin volume doubly/per hour; The cycle of operation: treatment capacity is 80-100 a times of resin volume; PH value: 5.0-7.0.

Wherein, to enter the method for liquid glucose specific conductivity≤50 μ s/cm of adsorption resin column as follows in control:

1. strengthen monitoring, discharging liquid glucose (promptly entering the feed liquid of the adsorption resin column) specific conductivity that keeps ion exchange resin column otherwise is regenerated below 50 μ s/cm immediately;

2. the cycle of operation of resin anion(R.A) was reduced to 14 hours by 16 hours;

3. in the ion exchange resin regeneration process, the electricity of strict control resin sluice water is led, and makes resin regeneration thorough; Change the regeneration washing condition of resin anion(R.A), with the wash-down water flow velocity by 25m ³/ h brings up to 35m ³/ h;

The regeneration condition of polymeric adsorbent:

1. regeneration opportunity: when the discharging liquid glucose pH value behind the taste removal resin drops to below 5.0 or peculiar smell is arranged, need regeneration in time;

2. desorption and regeneration method: the mixed solution that utilizes the sodium chloride solution of 2% sodium hydroxide solution and 8%, pass through resin bed with the following current of 1-1.5BV/h flow velocity, tasteless to flowing liquid, use deionized water rinsing then, with the following current of 2-3BV/h flow velocity by resin bed, to washing till water outlet reaches neutrality.

The invention has the beneficial effects as follows:, improved 3.28% owing to adopted transmittance that technique scheme handles liquid glucose on average to bring up to 96.2% by former 92.2%; Colourity is by on average bringing up to less than 15Hz less than 40Hz; Whiteness brings up to 92.5% by average 89%; Particularly product odour is significantly improved, and is relieved to the light or substantially tasteless of flavor by original strong acid-base flavor, burnt burning, has reached requirement of client, for enterprise has increased benefit.

Description of drawings:

Fig. 1 is maltodextrin ion exchange resin and absorption taste removal resin purification schema.

Among the figure: 1-96C cation exchange resin column, 2-120 resin anion(R.A) exchange column, 3-96C adjustable column, 4-adsorption resin column.

Embodiment

Now will use the test result of ion-exchange of the present invention and polymeric adsorbent refining system and process for refining working method purified 12 batch of material liquid to disclose as follows:

Effect comparison table before and after the taste removal resin purification:

Claims (4)

1. the refining technique in the malt amylin production process is characterized in that former ion-exchange refining system is adjusted, and behind adjustable column, increases macropore nonpolar adsorption resin post, constitutes ion-exchange and polymeric adsorbent refining system; Liquid glucose after the decolouring behind ion exchange column, directly enters adsorption resin column, further removes impurity and peculiar smell, send concentrated, dehumidification system to be processed as the dextrin product then.

2. the refining technique in the malt amylin production process according to claim 1 is characterized in that the process conditions of adsorption resin column in the described process for refining is as follows:

Enter the sugar concentration of adsorption resin column: 33%-35%; Specific conductivity :≤50 μ s/cm; Flow: the 1.5-2 of resin volume doubly/per hour; The cycle of operation: treatment capacity is 80-100 a times of resin volume; PH value: 5.0-7.0.

3. as the refining technique in the malt amylin production process as described in the claim 2, it is as follows to it is characterized in that said control enters the method for the liquid glucose specific conductivity of adsorption resin column≤50 μ s/cm:

1. strengthen monitoring, the discharging liquid glucose specific conductivity that keeps ion exchange resin column otherwise is regenerated below 50 μ s/cm immediately;

2. the cycle of operation of the resin anion(R.A) in the former ion-exchange refining system was reduced to 14 hours by 16 hours;

3. in the ion exchange resin regeneration process, the electricity of strict control resin sluice water is led, and makes resin regeneration thorough; Change the regeneration washing condition of the resin anion(R.A) in the former ion-exchange refining system, with the wash-down water flow velocity by 25m ³/ h brings up to 35m ³/ h.

4. the refining technique in the malt amylin production process according to claim 1 is characterized in that the regeneration condition of adsorption resin column in the described process for refining is as follows:

1. regeneration opportunity: when the discharging liquid glucose pH value behind the taste removal resin drops to below 5.0 or peculiar smell is arranged, need regeneration in time;

2. desorption and regeneration method: the mixed solution that utilizes the sodium chloride solution of 2% sodium hydroxide solution and 8%, pass through resin bed with the following current of 1-1.5BV/h flow velocity, tasteless to flowing liquid, use deionized water rinsing then, with the following current of 2-3BV/h flow velocity by resin bed, to washing till water outlet reaches neutrality.