CN104844724A - Production method of polydextrose - Google Patents
Production method of polydextrose Download PDFInfo
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- CN104844724A CN104844724A CN201510207073.2A CN201510207073A CN104844724A CN 104844724 A CN104844724 A CN 104844724A CN 201510207073 A CN201510207073 A CN 201510207073A CN 104844724 A CN104844724 A CN 104844724A
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Abstract
The invention belongs to the technical field of polydextrose and particularly relates to a production method of the polydextrose. The production process is greatly simplified, materials are not in contact with the outside world and accordingly the secondary pollution to the finished product and the introduction of impurities due to artificial factors are avoided and reduced and the quality of the product is good, and the production cost is low.
Description
Technical field
The invention belongs to the technical field of poly-dextrose, be specially a kind of production method of poly-dextrose.
Background technology
Poly-dextrose, another name: ID, dextran (Polydextrose), is the polycondensate of the random key of D-Glucose, is combined into master with 1,6-glycosidic link.Shape: for white is to similar white powder or particle, soluble in water, solubleness 70%, the pH of 10% aqueous solution is 2.5 ~ 7.0, without special taste.Poly-dextrose is applied in low calorific food, partly or entirely can substitute sugared and fatty, while reduction food energy, the original local flavor of food and texture can be kept, thus make it the interest that more can cause human consumer, bring gratifying mouthfeel to enjoy.
Poly-dextrose has the unexistent comprehensive nourishing function of general insoluble fibre:
Adjusting blood lipid: water-soluble dietary fibre can cause a skim in small intestine, and swathe part food fat, effectively can limit the absorption of fat in digestive tube, promote the excretion of lipoid cpd, increase satiety, reduce food-intake, thus reach adjusting blood lipid, reduce fat accumulation, the effects such as prevention of obesity.
Reduce cholesterol: the synthesis that can be suppressed cholesterol after poly-dextrose enters enteron aisle by the product that enteric microorganism is degraded, and the meta-bolites bile acide of cholesterol can be adsorbed and excrete, thus reduce cholesterol in human body content, hinder the absorption to cholesterol; The formation of prevention gallbladdergallstonecholetithiasis.
Regulate blood glucose value: poly-dextrose can improve the last susceptibility slightly organized Regular Insulin, reduces the requirement to Regular Insulin, suppresses the secretion of Regular Insulin, hinders the absorption to sugar, thus reaches the object reducing glucose level, prevent diabetes.
Whole intestines effect: poly-dextrose can promote human body enterogastric peristalsis, eliminates constipation, prevention hemorrhoid; Beneficial microorganism growth to be promoted in enteron aisle, reduces pH value in duodenum, create micro-acid environment to stimulate beneficial microorganism as the growth of bifidus bacillus and other milk-acid bacteria, lower the breeding of unwanted bacteria, raising body immunity simultaneously.Reduce the chance that enteron aisle contacts with toxic substance, suppress the absorption of objectionable impurities and promote excretion, reaching the effect of toxin-expelling and face nourishing; Prevention hemorrhoid and colorectal carcinoma; Improve physique.
Help control effect: soluble fiber contributes to the excessive food intake of prevention and fat accumulation.
Antiobesity action: food fibre can reduce food-intake on the one hand, and unnecessary fat and energy is taken away in human body, soluble dietary fibre also can form film on gastrointestinal wall on the other hand, stops the absorption of glucose, hinder nutrient substance to change into heat energy, this just effectively plays effect of fat-reducing.
For in the production technique of poly-dextrose, traditional synthesis, in general, poly-dextrose is by D-glucose monomers, and with under the catalysis of organic acid (as fumaric acid, citric acid etc.), intermolecular dehydration polymerization forms L3.4j, usually the sorbyl alcohol of about 10% weight is added during polymerization, object makes sorbyl alcohol molecule penetrate in polymeric chain, to reduce the viscosity of polymkeric substance, also contributes to improving mouthfeel and color and luster.The molecular-weight average of polymkeric substance depends on time of reaction, polymerization temperature and vacuum tightness, and the object adopting condition of high vacuum degree is that the water molecule energy that polymerization is produced departs from reaction system fast.Polyreaction is carried out under melting state.At present, in the production of poly-dextrose, in product after polymerization, due to containing organic acid and glucose unit molecule dewatered product, so in acid, but the product of neutrality is more suitable for applying in varieties of food items product, so usually will neutralize, temperature because of local in polymerization process traditional is in addition too high, the product (molecular weight >22000) of high molecular can be produced, and cause the coking variable color of glucose molecule, made product remove caramel colour so the solution after neutralization is wanted to filter the high molecular weight component that is insoluble to methyl alcohol and add oxygenant.This technique is due to operation more complicated, and to methanol as solvent be used in last handling process, want evaporating solvent after process and dry to produce organic acid sugar alcohol oxidative decoloration product, because poly-dextrose water-absorbent is extremely strong, viscosity is large, drying operation is quite difficult, and there will be local coking equally time dry, thus the purity of product and color and luster more unstable.
Summary of the invention
The object of the invention is to for the more unstable problem of the purity of current product, the polymerization degree and color and luster, and a kind of production method of poly-dextrose is provided, enormously simplify production sequence, material does not contact the external world, avoid and reduce the introducing of secondary pollution that human factor brings finished product and impurity, the quality of product is better, and production cost is also lower.
Technical scheme of the present invention is:
A production method for poly-dextrose, comprise batching, polymerization, end reaction, decolouring, membrane sepn, ion-exchange, concentrated, spraying dry, concrete production stage is as follows:
(1) prepare burden: accurately take glucose, sorbyl alcohol, citric acid, drop into reactor;
(2) be polymerized: the material prepared is added in reactor, first open after stirring reinforced, mixing speed 10r/min, start vacuum pump, vacuum tightness >=-0.095MPa, intensification 180-200 DEG C, polymerization process, according to the current conditions adjustment mixing speed of motor, adopts variable-frequency motor, reaction 4h; Be provided with autoclave whipping appts in described reactor, this autoclave whipping appts comprises rotating shaft, and one end of this rotating shaft connects motor, and the other end of this rotating shaft is provided with agitating vane;
(3) terminate reaction: the 80 DEG C of salt-free water adding charged material weight 2.5 times after reaction terminates be cooled to less than 100 DEG C for subsequent use, make feed liquid poly-dextrose content at 28-32%;
(4) decolour: drop into medicinal active carbon decoloring, by the throwing carbon amounts of material liquid volume 0.2%, 80 DEG C of insulation 30min, mixing speed 20r/min, removes gac with full-automatic fragrant special decarburizing machine, with salt-free washing carbon 3 times, retain clear liquid, feed liquid specification of quality: transmittance >=95%;
(5) membrane sepn: feed liquid step (4) obtained, by nanofiltration membrane separation purifying, obtains nanofiltration concentrated solution, with the salt-free washing concentrated solution 3 times of concentrated solution 3 times of volumes, retaining molecular weight is 600-800Da.Retain concentrated solution, the recycling of nanofiltration clear liquid, after this step, in membrane sepn feed liquid, the molecular weight of oligosaccharide reaches 700-20000;
(6) ion-exchange: according to the requirement of quality product PH height, by the H of membrane sepn feed liquid successively by having regenerated
+and OH
-type ion exchange column, feeding temperature 30-50 DEG C, crossing column flow rate is 1 times of resin volume; (7) concentrated: the feed liquid after ion-exchange is concentrated through dual-effect concentrator;
(8) spraying dry: the feed liquid that dual-effect concentrator is concentrated squeezes into drying process, open air intake, exhaust fan, stablize drying tower system negative pressure at-0.1--0.4MPa, open heating system progressively about intensification dehumidification system to 100 DEG C, open clarifixator to boost to 25MPa and start feed, Controlling System Ya Li≤20MPa, air draft stablizes 90-120 DEG C, controls the standard that temperature of outgoing air to product moisture suits the requirements;
(9) pack: the material of gas delivery is entered automatic packing machine packing, sealing, cover outer bag after screening, metal detection, cyclonic separation is introduced after being sieved by the material of the king-tower of drying tower and micro mist tower, under connect and automatically pack weigher, send into district to be checked by travelling belt.
Feature of the present invention also has:
Method of the present invention, produces the poly-dextrose of 700-20000 molecular weight.
Described step (4) decolouring: the condition of transmittance is feed liquid content when being 30%, at the transmittance that 440nm records.
For in step (2) polymerization, stopped reaction after current of electric reaches 30A.
For in step (6) ion-exchange, root feed liquid quality standard: according to quality product requirement; Conductance≤80us/cm-
1; Transmittance>=98%.
In concentrated for step (7), dual-effect concentrator operation parameter: steam: 0.4-0.7MPa; Vacuum a: effect :-0.05--0.08MPa, two effects :-0.08--0.095MPa; Temperature a: effect: 80-98 DEG C, two effects: 50-70 DEG C.
In concentrated for step (7), obtain the feed liquid degree Beaume concentrated after process: 45-50
ob
e.
For in step (1) batching, glucose: sorbyl alcohol: citric acid part by weight is 150:18:1.
The present invention improves processing condition and adjusts, and the positively effect specifically brought is as follows:
A () adopts the reaction system of stirring, in technique before, because the reaction system of melting state is along with the carrying out of reaction, viscosity is increasing, so reaction is carried out in static container.Because whole reaction process is not stirred, so inevitably because of component (water-insoluble) and the coking phenomenon (product color is poor) of the higher generation high molecular of local temperature.This patent adopts the autoclave whipping appts that can stir high viscosity reaction mixture, and adopt the variable-frequency motor that agitation speed can change with viscosity (resistance), thus whole reaction process held stationary is made to carry out equably, because vacuum tightness during polymerization is high, temperature of reaction is low, do not produce the component (water-insoluble) of ultra-high molecular weight, so just need not through separating step (by dissolution with solvents in old technology, cross the method filtering insolubles and be separated).
The pH value of (b) ion exchange resin telomerized polymer
The present invention adopts the combination of ion exchange resin to regulate pH, namely needs high pH feed liquid to adopt advanced positive post to enter cloudy post again, needs the feed liquid of low pH to adopt advanced cloudy post, then enter the way of positive post, and the mode finally returning stream at cloudy post or positive post is adjusted to the pH value of needs.Effectively prevent and add other materials that alkali brings and the too high difficult problem of feed liquid specific conductivity caused.
C () adopts sophisticated equipment to avoid the introducing of secondary pollution and impurity
Full-automatic fragrant special decarburizing machine is have employed in production process, pH value resin moderated, the application of membrane separation plant, gas delivery, device of full automatic packaging, material is made not contact the external world, avoid and reduce the introducing of secondary pollution that human factor brings finished product and impurity, improve quality and the quality of product.
D () adopts advanced fully-automatic packaging system
Drying process have employed advanced air-flow materials-handling technology, introduces cyclonic separation after being sieved by the material of the king-tower of drying tower and micro mist tower, under connect and automatically pack weigher, send into district to be checked by travelling belt.The unmanned contact with material of whole production process, namely reduces labour intensity, turn avoid secondary pollution.And traditional production technique is sieved by dried material descendant's work point dress, manual weighing, artificial sealing, hand haulage.
Beneficial effect of the present invention is:
The reactor that processing method of the present invention adopts and autoclave stir, add the adjustment of upconverter and temperature, improve the polymerization degree, decrease the generation of pigment and other impurity, the advanced special decarburizing machine of full-automatic sweet smell, unique pH regulator mode are selected, fully-automatic packaging production line, decreases the touch opportunity of people and material, and production method is obviously better than old technology production method.
Table 1 product primary quality measure
Accompanying drawing explanation
Fig. 1 is the structural representation of autoclave whipping appts;
Fig. 2 is another structural representation of autoclave whipping appts;
Fig. 3 is the equipment component syndeton schematic diagram of packaging step.
Wherein, 1 is motor, and 2 is rotating shaft, and 3 is blade, and 4 is drying tower, and 5 is vibratory screening apparatus, and 6 is micro mist tower, and 7 is weigher, and 8 is cyclonic separator, and 9 is travelling belt, and 10 is sealing machine, and 11 is clean area.
Embodiment
Below by specific embodiment, technical scheme of the present invention is described in detail.
A production method for high purity, high-polymerization degree poly-dextrose, method of the present invention, produces the poly-dextrose of 700-20000 molecular weight.
Comprise batching, polymerization, end reaction, decolouring, membrane sepn, ion-exchange, concentrated, spray drying step, concrete production stage is as follows:
(1) prepare burden: accurately take glucose, sorbyl alcohol, citric acid, glucose: sorbyl alcohol: citric acid part by weight is 150:18:1, drop into reactor;
(2) be polymerized: the material prepared is added in reactor, first open after stirring reinforced, mixing speed 10r/min, start vacuum pump, vacuum tightness >=-0.095MPa, intensification 180-200 DEG C, polymerization process adjusts rotating speed according to current of electric situation variator, stopped reaction after current of electric reaches 30A; Be provided with autoclave whipping appts in described reactor, this autoclave whipping appts comprises rotating shaft 2, and one end of this rotating shaft connects motor 1, and the other end of this rotating shaft is provided with agitating vane 3;
(3) terminate reaction: the 80 DEG C of salt-free water adding charged material weight 2.5 times after reaction terminates make feed liquid poly-dextrose content at 28-32%, be cooled to less than 100 DEG C for subsequent use;
(4) decolour: drop into medicinal active carbon decoloring, by the throwing carbon amounts of material liquid volume 0.2%, 80 DEG C of insulation 30min, mixing speed 20r/min, removes gac by fully-closed stainless steel filtering system, with salt-free washing carbon 3 times, retain clear liquid, feed liquid specification of quality after removing gac: transmittance >=95%, condition is feed liquid content when being 30%, at the transmittance that 440nm records;
(5) membrane sepn: feed liquid step (4) obtained is by nanofiltration membrane separation purifying, obtain nanofiltration concentrated solution, with the salt-free washing concentrated solution 3 times of concentrated solution 3 times of volumes, retaining molecular weight is 600-800Da, obtain membrane sepn feed liquid, the recycling of nanofiltration clear liquid, after this step, in membrane sepn feed liquid, the molecular weight of oligosaccharide reaches 700-20000;
(6) ion-exchange: according to the requirement of quality product PH height, membrane sepn feed liquid is passed through H successively
+and OH
-type ion exchange column, feeding temperature 30-50 DEG C, crossing column flow rate is 1 times of resin volume; Root feed liquid quality standard: according to quality product requirement; Conductance≤80us/cm-
1; Transmittance>=98%;
(7) concentrated: the feed liquid after ion-exchange is concentrated through dual-effect concentrator; Dual-effect concentrator operation parameter: steam: 0.4-0.7MPa; Vacuum a: effect :-0.05--0.08MPa, two effects :-0.08--0.095MPa; Temperature a: effect: 80-98 DEG C, two effects: 50-70 DEG C; Concentrated feed liquid degree Beaume: 45-50
ob
e;
(8) spraying dry: the feed liquid that dual-effect concentrator is concentrated squeezes into drying process, open air intake, exhaust fan, stablize drying tower system negative pressure at-0.1--0.4MPa, open heating system progressively intensification dehumidification system to 90-110 DEG C, open clarifixator to boost to 25MPa and start feed, Controlling System Ya Li≤20MPa, air draft stablizes 90-120 DEG C, controls the standard that temperature of outgoing air to product moisture suits the requirements;
(9) pack: the material of gas delivery is entered automatic packing machine packing, sealing, cover outer bag after screening, metal detection, by tape transport to district to be checked.
(9) pack: the material of gas delivery is entered automatic packing machine packing, sealing, cover outer bag after screening, metal detection, the material of the king-tower of drying tower 4 and micro mist tower 6 is crossed vibratory screening apparatus 5 and sieves rear introducing cyclonic separator 8, under connect automatically packaging weigher 7, sealing machine 10, send into district to be checked by travelling belt 9, whole operating in clean area 11 is carried out.
Claims (8)
1. a production method for poly-dextrose, comprise batching, polymerization, end reaction, decolouring, membrane sepn, ion-exchange, concentrated, spraying dry, concrete production stage is as follows:
(1) prepare burden: accurately take glucose, sorbyl alcohol, citric acid, drop into reactor;
(2) be polymerized: the material prepared is added in reactor, first open after stirring reinforced, mixing speed 10r/min, start vacuum pump, vacuum tightness >=-0.095MPa, intensification 180-200 DEG C, polymerization process, according to the current conditions adjustment mixing speed of motor, adopts variable-frequency motor, reaction 4h; Be provided with autoclave whipping appts in described reactor, this autoclave whipping appts comprises rotating shaft, and one end of this rotating shaft connects motor, and the other end of this rotating shaft is provided with agitating vane;
(3) terminate reaction: the 80 DEG C of salt-free water adding charged material weight 2.5 times after reaction terminates be cooled to less than 100 DEG C for subsequent use, make feed liquid poly-dextrose content at 28-32%;
(4) decolour: drop into medicinal active carbon decoloring, by the throwing carbon amounts of material liquid volume 0.2%, 80 DEG C of insulation 30min, mixing speed 20r/min, removes gac with full-automatic fragrant special decarburizing machine, with salt-free washing carbon 3 times, retain clear liquid, feed liquid specification of quality: transmittance >=95%;
(5) membrane sepn: feed liquid step (4) obtained, by nanofiltration membrane separation purifying, obtains nanofiltration concentrated solution, with the salt-free washing concentrated solution 3 times of concentrated solution 3 times of volumes, retaining molecular weight is 600-800Da;
Retain concentrated solution, the recycling of nanofiltration clear liquid, after this step, in membrane sepn feed liquid, the molecular weight of oligosaccharide reaches 700-20000;
(6) ion-exchange: according to the requirement of quality product PH height, by the H of membrane sepn feed liquid successively by having regenerated
+and OH
-type ion exchange column, feeding temperature 30-50 DEG C, crossing column flow rate is 1 times of resin volume; (7) concentrated: the feed liquid after ion-exchange is concentrated through dual-effect concentrator;
(8) spraying dry: the feed liquid that dual-effect concentrator is concentrated squeezes into drying process, open air intake, exhaust fan, stablize drying tower system negative pressure at-0.1--0.4MPa, open heating system progressively about intensification dehumidification system to 100 DEG C, open clarifixator to boost to 25MPa and start feed, Controlling System Ya Li≤20MPa, air draft stablizes 90-120 DEG C, controls the standard that temperature of outgoing air to product moisture suits the requirements;
(9) pack: the material of gas delivery is entered automatic packing machine packing, sealing, cover outer bag after screening, metal detection, cyclonic separation is introduced after being sieved by the material of the king-tower of drying tower and micro mist tower, under connect and automatically pack weigher, send into district to be checked by travelling belt.
2. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, produces the poly-dextrose of 700-20000 molecular weight.
3. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, described step (4) decolouring: the condition of transmittance is feed liquid content when being 30%, at the transmittance that 440nm records.
4. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, in step (2) polymerization, and stopped reaction after current of electric reaches 30A.
5. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, in step (6) ion-exchange, and root feed liquid quality standard: according to quality product requirement; Conductance≤80us/cm-
1; Transmittance>=98%.
6. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, in concentrated for step (7), and dual-effect concentrator operation parameter: steam: 0.4-0.7MPa; Vacuum a: effect :-0.05--0.08MPa, two effects :-0.08--0.095MPa; Temperature a: effect: 80-98 DEG C, two effects: 50-70 DEG C.
7. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, in concentrated for step (7), obtains the feed liquid degree Beaume concentrated: 45-50 after process
ob
e.
8. the production method of a kind of poly-dextrose according to claim 1, is characterized in that, in step (1) batching, and glucose: sorbyl alcohol: citric acid part by weight is 150:18:1.
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|---|---|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108117611A (en) * | 2017-12-28 | 2018-06-05 | 保龄宝生物股份有限公司 | The production method of low reduced sugar polydextrose |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101508740A (en) * | 2009-03-23 | 2009-08-19 | 保龄宝生物股份有限公司 | Process for preparing poly-glucose |
| CN102429148A (en) * | 2011-11-11 | 2012-05-02 | 山东龙力生物科技股份有限公司 | Preparation method of high-purity polydextrose with controllable molecular weight |
| CN103483463A (en) * | 2012-06-12 | 2014-01-01 | 保龄宝生物股份有限公司 | Production method of polydextrose |
| CN104211830A (en) * | 2014-08-27 | 2014-12-17 | 陕西盛迈石油有限公司 | Preparation method of polydextrose |
-
2015
- 2015-04-28 CN CN201510207073.2A patent/CN104844724A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101508740A (en) * | 2009-03-23 | 2009-08-19 | 保龄宝生物股份有限公司 | Process for preparing poly-glucose |
| CN102429148A (en) * | 2011-11-11 | 2012-05-02 | 山东龙力生物科技股份有限公司 | Preparation method of high-purity polydextrose with controllable molecular weight |
| CN103483463A (en) * | 2012-06-12 | 2014-01-01 | 保龄宝生物股份有限公司 | Production method of polydextrose |
| CN104211830A (en) * | 2014-08-27 | 2014-12-17 | 陕西盛迈石油有限公司 | Preparation method of polydextrose |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108117611A (en) * | 2017-12-28 | 2018-06-05 | 保龄宝生物股份有限公司 | The production method of low reduced sugar polydextrose |
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Application publication date: 20150819 |
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