CN102586363A - Maltose production and refining method - Google Patents
Maltose production and refining method Download PDFInfo
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- CN102586363A CN102586363A CN2012100564359A CN201210056435A CN102586363A CN 102586363 A CN102586363 A CN 102586363A CN 2012100564359 A CN2012100564359 A CN 2012100564359A CN 201210056435 A CN201210056435 A CN 201210056435A CN 102586363 A CN102586363 A CN 102586363A
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Abstract
The invention belongs to the technical field of functional sugar production, and particularly discloses a maltose production and refining method. The maltose production and refining method uses an automatically controlled water heater to spray and liquefy starch milk for two times, an automatic enzyme-dosing system to carry out a liquefied liquid saccharification process, and membrane filtration in the process of refining obtained crude syrup into maltose syrup in the end, and the obtained maltose syrup is then refined, purified, concentrated, centrifuged and dried, so that high-purity maltose is obtained. According to the invention, the steps are simple, the operation is easy, the production period is short, the automation degree is high, the production cost can be effectively reduced, and the industrialized production of maltose with a content being more than 90 percent can be realized.
Description
(1) technical field
The invention belongs to technical field of functional sugar production, particularly a kind of production of SANMALT-S and process for purification.
(2) background technology
The maltose molecule formula is C
12H
22O
11H
2O, soluble in water, sugariness is low and gentle, palatability is strong, mouthfeel is good.SANMALT-S has that resistive connection crystalline substance, freezing point are low, moisture retention, endure warm high good characteristic, at aspects such as food service industry such as cold drink, candy, cake, cream based foods as thickening material, softening agent, sweeting agent, application such as anti-browning agent, sanitas.Because SANMALT-S also has the character of Hyposmolality; In human body, not needing pancreas islet just can be absorbed by the body, is sugar products low in calories, can replace glucose to be used for patient's transfusion; Be difficult for causing blood sugar increasing, excellent suitable diabetic subject, intra-operative and patients after surgery.In traditional Chinese medicine, SANMALT-S is used to cure mainly diseases such as empty stomachache, xeropulmonary cough.High malt sugar also has skill to show at light industry in addition, and it can provide high quality raw material for the production of daily necessities (soap, toothpaste, papermaking).
In recent years, because its unique character of SANMALT-S, particularly along with the widespread use of superelevation SANMALT-S; Domestic production technique to SANMALT-S has been carried out a large amount of research; But since (1) common homemade injector cooking effect inadequately evenly, thorough, part is given birth to starch and is got into the saccharification operation on the one hand, cause saccharification after the iodine examination show bluish voilet; For defective; The highest 80-85% that only reaches of maltose content, the opposing party starch of looking unfamiliar gets into the macromole dextrin that generates after the saccharification, brings very big difficulty to decolorization filtering; (2) activated carbon decolorizing poor stability, product yield are low, discharge a large amount of useless charcoals simultaneously, have increased the working cost and local environmental protection difficulty of enterprise; (3) common tubular evaparator heat transfer coefficient is low, and the steam consumption is big, and heating tube is prone to dead pipe phenomenon, has not only reduced heat transfer area, and is prone to cause the corrosion damage of heating tube, has strengthened maintenance cleaning amount.The existence of three big shortcomings just makes that the content of superelevation SANMALT-S is low, production cost is high, is difficult to realize industriallization, thus largely limit promoting the use of of high purity maltose.
(3) summary of the invention
The present invention provides a kind of step is simple, be suitable for industrialized SANMALT-S production and process for purification in order to remedy the deficiency of prior art.
The present invention realizes through following technical scheme:
A kind of production of SANMALT-S and process for purification are raw material with the milk of starch, comprise the steps:
(1) degree Beaume of adjusting milk of starch is 13 ~ 17, and the pH value is 5.0 ~ 6.0, adds high temperature resistant AMS in Yishui or Liquozyme Supra, and its enzyme-added coefficient is 0.14 ~ 0.19kg/t
(dry starch)
(2) with milk of starch through twice automatically behind the control water heater steam ejection liquefaction, get into laminar flow jar flocculation protein 90 ~ 120min, liquefier is cooled to 55 ~ 65 ℃ rapidly, control liquefier DE value is 2 ~ 8;
(3) the pH value of using the automatic pH of adjusting valve system to regulate cooled liquefier is 4.8 ~ 5.6, in liquefier, adds saccharifying enzyme through adding enzyme system automatically, and enzyme-added coefficient is beta-amylase 1.13 ~ 1.32 kg/t
(dry starch), Pullulanase 1.0 ~ 1.27 kg/t
(dry starch), add trisaccharide maltose enzyme 0.14 ~ 0.19 Kg/t behind 10 ~ 20h again
(dry starch), the control saccharification temperature is 55 ~ 65 ℃, the time is 30 ~ 60h, obtains the raw sugar slurry;
(4) under 40 ~ 60 ℃, be 5 ~ 100,000 membrane filtration with raw sugar slurry through the aperture, flow is 6 ~ 10 m
3/ h obtains maltose syrups;
(5) maltose syrups is removed small-molecule substances such as soluble ion, albumen through ion exchange column, get into chromatographic separation equipment and purify, concentrate through the board-like falling film evaporation system of quadruple effect then, obtain highly purified malt syrup;
(6) highly purified malt syrup gets into crystallization kettle and adds crystal seed, in crystallizer tank behind the growing the grain, carries out the mechanical packaging after centrifugal, oven dry, the screening, finally obtains crystalline-maltose.
The present invention uses automatic control water heater that milk of starch is carried out steam ejection liquefaction twice; Use and add the saccharifying that enzyme system is carried out liquefier automatically; Used membrane filtration in the refining malt syrup process of the raw sugar that obtains at last slurry, the gained malt syrup is re-refined, is concentrated, growing the grain, centrifugal, dry, screen, be packaged to be highly purified crystalline-maltose.
Using automatically, the control water heater carries out steam ejection liquefaction twice; Once be that milk of starch is under the effect of alpha-amylase; After control water heater high temperature liquefies automatically, starch is hydrolyzed into the process of macromolecular substance such as dextrin, be further to reduce viscosity for the second time; Flocculation albumen reaches the effect of the enzyme that goes out simultaneously.
More excellent scheme of the present invention is:
In the step (1), the pH value of milk of starch is 5.6 ~ 5.8, and the glycase of adding is Liquozyme Supra.
In the step (2), during steam ejection liquefaction, temperature is 105 ~ 109 ℃ for the first time, and flow is 17 ~ 20 m
3/ h; Temperature is 130 ~ 140 ℃ for the second time, and flow is 17 ~ 20 m
3/ h.
In the step (2), liquefier is cooled to 59 ~ 63 ℃ rapidly, and control liquefier DE value is 3 ~ 6.
In the step (3), in liquefier, add saccharifying enzyme through adding enzyme system automatically, the beta-amylase of adding is that NOKEZYM SBA, Pullulanase are Promozyme D2, and the trisaccharide maltose enzyme is Maltogenase L, and the control saccharification temperature is 59 ~ 63 ℃.
The present invention uses automatic control water heater to replace the steam ejection liquefaction system to carry out the liquefaction of milk of starch; Because the control water heater has strong shearing force and thorough cooking characteristic automatically; Make liquefaction reach even, thorough boiling gelatinization effect; Make the concentration of sizing mixing promote 2 ~ 3% thereby overcome the viscosity that high dense starch brings, avoided the aging starch phenomenon of using homemade injector to exist; Consider that from the steam consumption aspect the complete blended characteristics of gas-liquid can also improve the transformation efficiency of sugar simultaneously than using homemade injector can practice thrift 20 ~ 30% steam.
The automatic application of regulating the pH value and adding enzyme system; Prevent because of the liquefier long catabiosis that occurs storage period; While has alleviated the work intensity of force largely, thereby makes suitability for industrialized production can obtain the superhigh maltose syrup of maltose content between 90 ~ 93%.
Use membrane filtration to replace activated carbon decolorizing, simplify production technique, shorten the production cycle, need not to add flocculating aids, improve filtrating quality and syrup yield.Consider from the cost aspect; Produce statistics malt syrup per ton and need consume about 0.86kg gac; Per kilogram is by 60 yuan of calculating; The gac expense that annual output 40000t SANMALT-S is used to decolour is 206.4 ten thousand, only considers enterprise cost, year about 2,000,000 yuan expense of saving behind the use membrane filtration from the gac aspect.Consider from filtrating quality aspect; Former saccharification liquid printing opacity is 45.3%; Printing opacity is 96.7% behind membrane filtration, and this explanation membrane filtration has not only been removed the macromolecular substance in the saccharification liquid, has also removed small-molecule substances such as most dextrin, soluble proteins; Improve the resin service efficiency and increase resin work-ing life, reduced the acid and alkali consumption in the regenerative process simultaneously.
Use the board-like falling film evaporation concentration systems of quadruple effect heat transfer coefficient high, the steam consumption is low, the backwater ratio is big, and the weight of equipment of unit heat-transfer surface is light, and the weight of equipment of common shell and tube evaporator unit heat transfer area is 70.9Kg/m
2, plate-type down-film evaporator then is 35.3Kg/m
2, improved steam utilization widely, further reduced the cost of enterprise.
Step of the present invention is simple, and processing ease is with short production cycle; Level of automation is high, can effectively reduce production costs, and realizes that the suitability for industrialized production maltose content reaches more than 90%; Also, finally just can make the crystalline-maltose of purity more than 99.8% just because of improvement of the present invention.
(4) embodiment
Embodiment 1:
Starch slurry regulates that degree Beaume is 14, pH value 5.6, adding Liquozyme Supra0.12 Kg/t
(dry starch), stir.
The U.S. controls the water heater steam ejection liquefaction, 105 ℃ of temperature, flow 17m automatically through the first time
3/ h.Be cooled to 94 ℃, behind the insulation 120min, the U.S. controls water heater injection, 125 ℃ of temperature, flow 17m automatically for the second time
3/ h.
Be cooled to 59 ℃, pH value 4.8 is regulated in robotization, adds enzyme system automatically and adds beta-amylase NOKEZYM SBA 1.13 Kg/t
(dry starch), Promozyme D2 1.27 Kg/t
(dry starch)Add Maltogenase L 0.14 Kg/t behind the 15h again
(dry starch)Saccharification react is to 40h, and the maltose content of saccharification this moment liquid is 90.01% superhigh maltose syrup.
Embodiment 2:
Starch slurry regulates that degree Beaume is 17, pH value 5.8, adding Liquozyme Supra0.14 Kg/t
(dry starch), stir.
The U.S. controls the water heater steam ejection liquefaction, 109 ℃ of temperature, flow 20m automatically through the first time
3/ h.Be cooled to 98 ℃, behind the insulation 90min, the U.S. controls water heater injection, 140 ℃ of temperature, flow 20m automatically for the second time
3/ h.
Be cooled to 63 ℃, pH value 5.6 is regulated in robotization, adds enzyme system automatically and adds beta-amylase NOKEZYM SBA 1.32 Kg/t
(dry starch), Promozyme D2 1.0 Kg/t
(dry starch)Add Maltogenase L 0.19 Kg/t behind the 15h again
(dry starch)Saccharification react is to 60h, and the maltose content of saccharification this moment liquid is 92.28% superhigh maltose syrup.
Embodiment 3:
Starch slurry regulates that degree Beaume is 15, pH value 5.7, adding Liquozyme Supra0.13 Kg/t
(dry starch), stir.
The U.S. controls the water heater steam ejection liquefaction, 107 ℃ of temperature, flow 18m automatically through the first time
3/ h.Be cooled to 96 ℃, behind the insulation 100min, the U.S. controls water heater injection, 135 ℃ of temperature, flow 18m automatically for the second time
3/ h.
Be cooled to 61 ℃, pH value 5.3 is regulated in robotization, adds enzyme system automatically and adds beta-amylase NOKEZYM SBA 1.22 Kg/t
(dry starch), Promozyme D2 1.18 Kg/t
(dry starch)Add Maltogenase L 0.17 Kg/t behind the 15h again
(dry starch)Saccharification react is to 55h, and the maltose content of saccharification this moment liquid is 93.75% superhigh maltose syrup.
Above-mentioned malt syrup is handled through membrane filtration and is removed macromolecular substance and impurity etc., flow 8 m
3/ h; Ion exchange resin obtains high-purity maltose syrup after removing salt ion plasma type material.Get into chromatographic separation equipment and purify, obtain highly purified malt syrup.Be concentrated into 65-75% through the board-like falling film evaporation system of quadruple effect, make highly purified malt syrup.
After highly purified malt syrup gets into crystallization kettle and adds crystal seed, crystallizer tank growing the grain, carry out the mechanical packaging after centrifugal, oven dry, the screening, finally obtain crystalline-maltose purity more than 99.8%.
Claims (5)
1. the production of a SANMALT-S and process for purification are raw material with the milk of starch, it is characterized by, and comprise the steps:
(1) degree Beaume of adjusting milk of starch is 13 ~ 17, and the pH value is 5.0 ~ 6.0, adds high temperature resistant AMS in Yishui or Liquozyme Supra, and its enzyme-added coefficient is 0.14 ~ 0.19kg/t
(dry starch)
(2) with milk of starch through twice automatically behind the control water heater steam ejection liquefaction, get into laminar flow jar flocculation protein 90 ~ 120min, liquefier is cooled to 55 ~ 65 ℃ rapidly, control liquefier DE value is 2 ~ 8;
(3) the pH value of using the automatic pH of adjusting valve system to regulate cooled liquefier is 4.8 ~ 5.6, in liquefier, adds saccharifying enzyme through adding enzyme system automatically, and enzyme-added coefficient is beta-amylase 1.13 ~ 1.32 kg/t
(dry starch), Pullulanase 1.0 ~ 1.27 kg/t
(dry starch), add trisaccharide maltose enzyme 0.14 ~ 0.19 Kg/t behind 10 ~ 20h again
(dry starch), the control saccharification temperature is 55 ~ 65 ℃, the time is 30 ~ 60h, obtains the raw sugar slurry;
(4) under 40 ~ 60 ℃, be 5 ~ 100,000 membrane filtration with raw sugar slurry through the aperture, flow is 6 ~ 10 m
3/ h obtains maltose syrups;
(5) maltose syrups is removed small-molecule substances such as soluble ion, albumen through ion exchange column, get into chromatographic separation equipment and purify, concentrate through the board-like falling film evaporation system of quadruple effect then, obtain highly purified malt syrup;
(6) highly purified malt syrup gets into crystallization kettle and adds crystal seed, in crystallizer tank behind the growing the grain, carries out the mechanical packaging after centrifugal, oven dry, the screening, finally obtains crystalline-maltose.
2. the production of SANMALT-S according to claim 1 and process for purification, it is characterized in that: in the step (1), the pH value of milk of starch is 5.6 ~ 5.8, and the glycase of adding is Liquozyme Supra.
3. the production of SANMALT-S according to claim 1 and process for purification is characterized in that: in the step (2), during steam ejection liquefaction, temperature is 105 ~ 109 ℃ for the first time, and flow is 17 ~ 20 m
3/ h; Temperature is 130 ~ 140 ℃ for the second time, and flow is 17 ~ 20 m
3/ h.
4. the production of SANMALT-S according to claim 1 and process for purification, it is characterized in that: in the step (2), liquefier is cooled to 59 ~ 63 ℃ rapidly, and control liquefier DE value is 3 ~ 6.
5. the production of SANMALT-S according to claim 1 and process for purification; It is characterized in that: in the step (3); In liquefier, add saccharifying enzyme through adding enzyme system automatically; The beta-amylase that adds is that NOKEZYM SBA, Pullulanase are Promozyme D2, and the trisaccharide maltose enzyme is Maltogenase L, and the control saccharification temperature is 59 ~ 63 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100564359A CN102586363A (en) | 2012-03-06 | 2012-03-06 | Maltose production and refining method |
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|---|---|---|---|
| CN2012100564359A CN102586363A (en) | 2012-03-06 | 2012-03-06 | Maltose production and refining method |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105925642A (en) * | 2016-06-14 | 2016-09-07 | 湖南汇升生物科技有限公司 | Method of industrial production for trehalose by way of microbial fermentation |
| CN107043796A (en) * | 2017-05-18 | 2017-08-15 | 南京林业大学 | A kind of method for preparing malt syrup |
| CN107447058A (en) * | 2017-09-26 | 2017-12-08 | 精晶药业股份有限公司 | A kind of preparation method of crystalline maltose |
| CN107739744A (en) * | 2017-10-30 | 2018-02-27 | 无锡甜丰食品有限公司 | A kind of filtering preparation method of malt syrup |
| CN108676827A (en) * | 2018-05-30 | 2018-10-19 | 湖南汇升生物科技有限公司 | A method of producing injection maltose bulk pharmaceutical chemicals |
| CN108754035A (en) * | 2018-04-19 | 2018-11-06 | 华南师范大学 | A kind of method that sweet potato prepares maltose from hydrolysis |
| CN109234338A (en) * | 2018-09-08 | 2019-01-18 | 肇庆焕发生物科技有限公司 | A kind of production method of high purity crystal maltitol malt syrup |
| CN110938714A (en) * | 2019-12-03 | 2020-03-31 | 山东福田药业有限公司 | Production method of high-purity crystal maltose |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105925642A (en) * | 2016-06-14 | 2016-09-07 | 湖南汇升生物科技有限公司 | Method of industrial production for trehalose by way of microbial fermentation |
| CN105925642B (en) * | 2016-06-14 | 2019-08-13 | 湖南汇升生物科技有限公司 | With the method for microbe fermentation method industrialized production trehalose |
| CN107043796A (en) * | 2017-05-18 | 2017-08-15 | 南京林业大学 | A kind of method for preparing malt syrup |
| CN107043796B (en) * | 2017-05-18 | 2018-11-09 | 南京林业大学 | A method of preparing malt syrup |
| CN107447058A (en) * | 2017-09-26 | 2017-12-08 | 精晶药业股份有限公司 | A kind of preparation method of crystalline maltose |
| CN107739744A (en) * | 2017-10-30 | 2018-02-27 | 无锡甜丰食品有限公司 | A kind of filtering preparation method of malt syrup |
| CN108754035A (en) * | 2018-04-19 | 2018-11-06 | 华南师范大学 | A kind of method that sweet potato prepares maltose from hydrolysis |
| CN108754035B (en) * | 2018-04-19 | 2022-04-12 | 华南师范大学 | Method for preparing maltose by sweet potato self-hydrolysis |
| CN108676827A (en) * | 2018-05-30 | 2018-10-19 | 湖南汇升生物科技有限公司 | A method of producing injection maltose bulk pharmaceutical chemicals |
| CN109234338A (en) * | 2018-09-08 | 2019-01-18 | 肇庆焕发生物科技有限公司 | A kind of production method of high purity crystal maltitol malt syrup |
| CN110938714A (en) * | 2019-12-03 | 2020-03-31 | 山东福田药业有限公司 | Production method of high-purity crystal maltose |
| CN110938714B (en) * | 2019-12-03 | 2023-08-15 | 山东福田药业有限公司 | Production method of high-purity crystalline maltose |
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Application publication date: 20120718 |