CN1390845A - Ion exchange technology in preparing glucose - Google Patents
Ion exchange technology in preparing glucose Download PDFInfo
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- CN1390845A CN1390845A CN 02135121 CN02135121A CN1390845A CN 1390845 A CN1390845 A CN 1390845A CN 02135121 CN02135121 CN 02135121 CN 02135121 A CN02135121 A CN 02135121A CN 1390845 A CN1390845 A CN 1390845A
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- ion exchange
- resin
- column
- liquid glucose
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Abstract
An ion exchange process for preparing glycose features that multiple cationic resin columns are parallelly connected into a group, multiple anionic resin columns are parallelly connected into a group, and both groups are connected via buffer tank and pump. Its advantages are regeneration of any resin column without stopping production, low cost for regeneration and saving resin by 30%.
Description
(1) technical field:
The invention belongs to glucose production process, particularly the ion exchange process in the dextrose production process.
(2) technical background:
Crystalline dextrose generally is raw material with starch, through sizing mixing, liquefaction, saccharification, slagging-off, decolouring, processing from operations such as friendship, crystallization, separation, oven dry.It is one of important source material of industries such as food-processing, medicine, industrial fermentation.
In existing glucose production process, the liquid glucose of starch through sizing mixing, generating after the liquefaction, saccharification behind activated carbon decolorizing, also needs by " ion-exchange " operation, further to remove impurity such as inorganic salt, organic acid and small molecules pigment wherein, liquid glucose is further purified.
" ion-exchange " operation mainly makes liquid glucose finish by cationic resin column and resin anion(R.A) post, in glucose production process, resin cation (R.C.) is generally selected the phenylethylene strong acid type cationic resin for use, and resin anion(R.A) is generally selected macropore phenylethylene weak anion resin for use.
In the existing glucose production process, " ion-exchange " technological process generally is that independent use " sun-the moon " resin column makes up or adopts " sun-the moon-sun-the moon " resin column to carry out the mode that series combination is arranged.Though this class array mode can be finished the further purification work of liquid glucose, exists following deficiency:
1. owing to the difference of anion and cation exchange resin unique characteristics, the terminal point that causes it to reach capacity is not the same, and in above-mentioned series combination, as long as a pillar reaches capacity, promptly need the regeneration together that all stops production, cause the regeneration expense higher like this, the production cycle lengthening influences production efficiency.
2. be cascaded owing to several pillars, resistance is big, and the surging force that liquid glucose forms when flowing through exchange column is big, and is serious to the comminuted destruction that resin itself causes, thereby has also strengthened the cost of changing resin.
(3) summary of the invention:
In order to solve in the existing glucose production above shortcomings in " from handing over " technology, the inventor is under the prerequisite that does not increase the facility investment scale, assembled arrangement mode to yin, yang ion exchange resin post redesigns, having proposed a plurality of cationic resin column parallel connections is one group, the parallel connection of a plurality of resin anion(R.A) post is one group, the permutation and combination method that is connected with infusion pump by the transfer surge tank between two groups.Wherein the quantity of resin column in parallel can be decided according to the needs of liquid glucose treatment capacity.From accompanying drawing 1 as can be seen, (1), (2), (3) are that three parallel connections are one group cationic resin column, (6), (7), (8) are that three parallel connections are that one group negatively charged ion tree refers to post, (4), (5) be respectively transfer surge tank and the infusion pump that connects two groups of yin, yang ion exchange resin posts in parallel, (9) and (10) are the cationic resin column of two parallel connections.Liquid glucose by bleaching process output, at first can enter cation seperation column (1), (2), (3) simultaneously and carry out ion-exchange, enter anion column (6), (7), (8) simultaneously by transfer surge tank (4) and infusion pump (5) then and carry out ion-exchange once more, flow through then cation seperation column (9) and (10), generally after handle cation seperation column (1), (2), (3) and anion column (6), (7), (8), impurity degree of purification in the liquid glucose can reach requirement, and mainly establish for the potential of hydrogen of regulating liquid glucose cation seperation column (9) and (10).
In the design that the present invention proposes, because cation seperation column and anion column are respectively to carry out the parallel connection combination by a plurality of posts, therefore, no matter wherein which pillar reaches capacity, both can it have been blocked separately and regenerate by valve, promptly save the regeneration expense, still can keep working continuously of whole ion exchange system simultaneously.Actual motion shows, design of the present invention compared with prior art, the regeneration expense can save 40%, the recovery cycle of whole ion-exchange process can prolong 20%.In the design of the present invention, transfer surge tank (4) and infusion pump (5) between cationic resin column and resin anion(R.A) post, have been increased, transfer surge tank (4) is hollow jar, its effect is a resistance of alleviating the ion exchange process flow process, thereby also reduced too high mechanical pressure in the liquid glucose transport process to the impact damage of resin itself, thereby prolonged the work-ing life of resin, The actual running results shows, compared with prior art, present design can be saved resin demand 30%.
Because this programme can make from exchanging the journey continous-stable and operate, thereby good purification, the liquid glucose qualification rate can guarantee to reach 100%, and original technology often can only reach 85%.
(4) description of drawings:
Accompanying drawing 1 is the process flow diagram of the ion exchange column permutation and combination method of design of the present invention
(5) embodiment:
Liquid glucose after last operation filter cleaner and the decolouring is transported in the ion exchange process flow process of the present invention's design, pass through in parallel cation seperation column (1), (2), (3)---transfer surge tank (4) and infusion pump (5)---successively and pass through anion column (6), (7), (8) in parallel flow through then adjustable column (cation seperation column) (9), (10) again, be transported to down and go on foot the condensing crystal operation.
Its main technique operation controlled variable is as follows:
The sugar concentration that enters from the preface of handing over is 35-45%
Feeding temperature is 40-50 ℃
The controlled variable index of discharge port liquid glucose is PH3.5-4.5
Specific conductivity＜50us/cm
Transmittance＞90%
Resin column regenerated method and prior art are similar in this technology, as column outlet liquid glucose index specific conductivity＞50us/cm, PH＜3.5 or＞4.5, look is seen when undesirable, promptly should regenerate.
Claims (2)
1. the ion exchange process in the glucose production is characterized in that a plurality of positively charged ions trees are referred to that the post parallel connection is one group, and the parallel connection of a plurality of resin anion(R.A) post is one group, the permutation and combination method that is connected with infusion pump by the transfer surge tank between two groups.
2. ion exchange process as claimed in claim 1 is characterized in that processing parameter is as follows:
Charging sugar concentration 35-45%
40-50 ℃ of charging liquid glucose temperature
Discharging liquid glucose PH3.5-4.5
Specific conductivity＜50us/cm
Transmittance＞90%
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02135121XA CN1162439C (en) | 2002-06-18 | 2002-06-18 | Ion exchange technology in preparing glucose |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02135121XA CN1162439C (en) | 2002-06-18 | 2002-06-18 | Ion exchange technology in preparing glucose |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1390845A true CN1390845A (en) | 2003-01-15 |
| CN1162439C CN1162439C (en) | 2004-08-18 |
Family
ID=4748036
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB02135121XA Expired - Fee Related CN1162439C (en) | 2002-06-18 | 2002-06-18 | Ion exchange technology in preparing glucose |
Country Status (1)
| Country | Link |
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| CN (1) | CN1162439C (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100540683C (en) * | 2004-03-19 | 2009-09-16 | 奥加诺株式会社 | The process for purification of sugar soln and refining plant |
| CN102102116A (en) * | 2010-12-21 | 2011-06-22 | 山东省鲁洲食品集团有限公司 | Method for preparing high-purity crystalline dextrose from maize peel acid hydrolysis residues |
| CN102559940A (en) * | 2011-12-31 | 2012-07-11 | 三达膜科技（厦门）有限公司 | Separation and purification method of glucose |
| CN102586492A (en) * | 2011-12-31 | 2012-07-18 | 三达膜科技（厦门）有限公司 | Method for removing impurities from saccharification solution in glucose production process |
| CN102586361A (en) * | 2011-12-31 | 2012-07-18 | 三达膜科技（厦门）有限公司 | Manufacturing method of glucose |
| CN103540690A (en) * | 2013-09-29 | 2014-01-29 | 山东西王糖业有限公司 | PH regulation method in high fructose corn syrup production process |
| CN103657146A (en) * | 2013-12-02 | 2014-03-26 | 上海好成食品发展有限公司 | Ion exchange method during sugar refining and system thereof |
-
2002
- 2002-06-18 CN CNB02135121XA patent/CN1162439C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100540683C (en) * | 2004-03-19 | 2009-09-16 | 奥加诺株式会社 | The process for purification of sugar soln and refining plant |
| CN102102116A (en) * | 2010-12-21 | 2011-06-22 | 山东省鲁洲食品集团有限公司 | Method for preparing high-purity crystalline dextrose from maize peel acid hydrolysis residues |
| CN102102116B (en) * | 2010-12-21 | 2013-01-02 | 山东省鲁洲食品集团有限公司 | Method for preparing high-purity crystalline dextrose from maize peel acid hydrolysis residues |
| CN102559940A (en) * | 2011-12-31 | 2012-07-11 | 三达膜科技（厦门）有限公司 | Separation and purification method of glucose |
| CN102586492A (en) * | 2011-12-31 | 2012-07-18 | 三达膜科技（厦门）有限公司 | Method for removing impurities from saccharification solution in glucose production process |
| CN102586361A (en) * | 2011-12-31 | 2012-07-18 | 三达膜科技（厦门）有限公司 | Manufacturing method of glucose |
| CN102559940B (en) * | 2011-12-31 | 2014-08-06 | 三达膜科技（厦门）有限公司 | Separation and purification method of glucose |
| CN102586492B (en) * | 2011-12-31 | 2015-04-22 | 三达膜科技（厦门）有限公司 | Method for removing impurities from saccharification solution in glucose production process |
| CN103540690A (en) * | 2013-09-29 | 2014-01-29 | 山东西王糖业有限公司 | PH regulation method in high fructose corn syrup production process |
| CN103540690B (en) * | 2013-09-29 | 2015-09-02 | 山东西王糖业有限公司 | PH regulator method in high fructose syrup production process |
| CN103657146A (en) * | 2013-12-02 | 2014-03-26 | 上海好成食品发展有限公司 | Ion exchange method during sugar refining and system thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1162439C (en) | 2004-08-18 |
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Granted publication date: 20040818 Termination date: 20170618 |