CN104928405A - Technique for extracting glucose from starch saccharified liquid - Google Patents
Technique for extracting glucose from starch saccharified liquid Download PDFInfo
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- CN104928405A CN104928405A CN201510267112.8A CN201510267112A CN104928405A CN 104928405 A CN104928405 A CN 104928405A CN 201510267112 A CN201510267112 A CN 201510267112A CN 104928405 A CN104928405 A CN 104928405A
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K1/00—Glucose; Glucose-containing syrups
- C13K1/06—Glucose; Glucose-containing syrups obtained by saccharification of starch or raw materials containing starch
- C13K1/08—Purifying
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K1/00—Glucose; Glucose-containing syrups
- C13K1/10—Crystallisation
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Abstract
The invention belongs to the field of processing techniques of glucose, and particularly relates to a technique for extracting glucose from a starch saccharified liquid. The technique comprises a concentration procedure, a decolorization procedure, a crystal separation procedure and a drying procedure, which are carried out in sequence. Compared with the prior art, the technique for extracting the glucose from the starch saccharified liquid has the advantages and positive effects that, according to the technique for extracting the glucose from the starch saccharified liquid, the procedures of extracting the glucose from the starch saccharified liquid are enabled to become simple and to be further low in energy consumption by changing a conventional production technique and by utilizing a novel device, and meanwhile, the produced glucose is high-quality and further does not include impurities.
Description
Technical field
The invention belongs to glucose complete processing field, particularly relate to a kind of technique extracting glucose from starch saccharificating liquid.
Background technology
Glucose is also called corn sugar, corn sugar, and even referred to as glucose, be the widest and of paramount importance a kind of monose of distributed in nature, it is a kind of poly-hydroxy aldehyde.Pure glucose is clear crystal, and pleasantly sweet but sweet taste, should be water-soluble not as sucrose, is slightly soluble in ethanol, is insoluble to ether.Aqueous solution optically-active to the right, therefore also known as " dextrose ".Glucose has critical role in field of biology, is the energy derive of viable cell and metabolic intermediate product.Meanwhile, glucose is in candy making industry and field of medicaments extensive application.
The nutrient substance that children's's normal growth is grown is most important with sugar, protein and fat three large key elements.Carbohydrate (carbohydrate) is the main source of supply intimate heat.Glucose is a kind of monose, enters in body and can be used directly.The baby of 1 ~ 6 month, the carbohydrate in food is lactose and a little starch mainly.After 4 months, starch-containing food increases gradually, perfect gradually to the various enzyme systems of pipe intestinal digesting starch when 1 years old, can be hydrolyzed to glucose rapidly, and enter blood at intestinal absorption.Directly can supply energy after absorption, or with the storage of glycogen form, excessive becomes fat.
Long-term, scientific and reasonable taking, self-evident to the raising of a national body constitution, according to Japanese statistics, Japanese teen-age average height increases 14.8cm after World War II, and this is inseparable with their use gluconic acid scientific and reasonable in food, medicine manufacture trace element.In China, the injection of known calglucon, tablet and Zinc Gluuconate Oral Solution all have important physiological function, treatment function.
W-Gum is the important source material extracting glucose, corn starch molecules is formed by connecting by thousands of glucose units (C6H10O5), the technique extracting glucose from starch saccharificating liquid is then extract the final step technique of glucose from corn starch milk, equally, this step process is also related to the quality of glucose finished product.
In order to reduce the by product of glucose, people are in glucose complete processing step, a various solution is proposed, such as, State Intellectual property right publication disclosing a kind of take starch as the method [patent No.: 201410583586.9] of raw material production poly-dextrose, the method that the method adopts in proposition process is by saccharified liquid through decolouring, filtering, from friendship, vacuum concentration, obtained glucose concentrated solution; Glucose concentrated solution is carried out high-temperature vacuum melt polycondensation reaction, obtained poly-dextrose crude product; By poly-dextrose crude product through decolouring, from friendship, chromatographic separation, obtained poly-dextrose liquid; By poly-dextrose liquid through concentrated, dry, obtained poly-dextrose.
Although aforesaid method reduces the by product of glucose to a certain extent, the method complex process, operation inconvenience, meanwhile, due to the consumption of the complexity of operation and then the energy of increase, improve production cost.
Summary of the invention
The present invention is directed to the technical problem such as above-mentioned complex process, operation inconvenience, propose that a kind of technique is simple, handled easily and a kind of technique extracting glucose from starch saccharificating liquid of environmental protection.
In order to achieve the above object, the technical solution used in the present invention is, the invention provides a kind of technique extracting glucose from starch saccharificating liquid, this technique comprises concentration process, decolorization, Crystallizing process, the drying process of carrying out successively, and wherein said concentration process comprises the following steps:
A, pre-concentration: utilize MVR vaporizer that starch saccharificating liquid is concentrated into concentration about 50%;
B, reconcentration: starch saccharificating liquid pre-concentration being obtained about 50% concentration is transported to triple effect waste heat evaporator and carries out reconcentration, obtains dense syrup;
C, decolouring: in dense syrup, add gac decolour, obtain the dense syrup after decolouring;
D, to stir in the dense syrup delivery surge tank decoloured;
E, by the dense syrup delivery that stirred in crystallizer, add crystal seed simultaneously and mix;
After f, naturally cooling 12h, obtain the massecuite of advantages of good crystallization, then by the massecuite of advantages of good crystallization input whizzer, carry out centrifugation, obtain water-containing crystal glucose and remaining dense syrup;
G, remaining for upper step dense syrup to be added in crystallizer again, add net weight simultaneously and mix crystal seed, after naturally cooling 12h, obtain the massecuite of advantages of good crystallization, then by the massecuite of advantages of good crystallization input whizzer, carry out centrifugation, obtain water-containing crystal glucose and remaining dense syrup;
H, the water-containing crystal glucose obtained after centrifugation is transported in drying unit, carries out drying treatment, obtain the glucose crystallization of water content below 9.0%.
As preferably, described whizzer is top-suspended basket centrifuge.
As preferably, described drying unit is the fixed fluidized bed drying unit of round shape back-mixing bed adverse current.
As preferably, the fixed fluidized bed drying unit of round shape back-mixing bed adverse current comprises fixed fluidized bed drying machine, Vibratingfluidbeddrier and vibrated fluidized bed cooler.
Compared with prior art, advantage of the present invention and positively effect are,
1, the present invention is by changing traditional production technique, utilizes novel equipment to make the process extracting glucose from starch saccharificating liquid become simple and consume energy low, the glucose high-quality of simultaneously producing and not impurity.
2, the present invention utilizes secondary crystal technology, and the effective dense syrup utilized, avoids the waste of dense syrup, and the remaining product of Crystallization Separation, separately can also be used as him, save resource, improve income simultaneously.
Embodiment
In order to more clearly understand above-mentioned purpose of the present invention, feature and advantage, below in conjunction with specific embodiment, the present invention will be further described.It should be noted that, when not conflicting, the feature in the embodiment of the application and embodiment can combine mutually.
Set forth a lot of detail in the following description so that fully understand the present invention, but the present invention can also adopt and be different from other modes described here and implement, and therefore, the present invention is not limited to the restriction of the specific embodiment of prospectus below.
Embodiment 1; The present embodiment improves a kind of process extracting glucose from W-Gum saccharification liquid specifically: mainly comprise concentration process, decolorization, Crystallizing process, the drying process of carrying out successively.
In the present embodiment, first will traditional technology be utilized to go deimpurity W-Gum saccharification liquid to carry out pre-concentration, what method for distinguishing can certainly be used to obtain removes deimpurity W-Gum saccharification liquid, preconcentration steps mainly adopts MVR vaporizer, equipment is provided by Shanghai Xuan Ke company the whole series, the vaporization temperature of MVR vaporizer is lower, and because MVR vaporizer adopts single-effect vacuum evaporation, vaporization temperature is equivalent to the end effect vaporization temperature of multiple-effect falling film vaporizer.The low concentrated very good starch saccharificating liquid to saccharified liquid of vaporization temperature is not deepened substantially in concentration process color.In the present embodiment, saccharified liquid is concentrated into concentration 50%.
When it should be noted that MVR vaporizer for concentrated starch saccharificating liquid, discharge concentration is no more than 55%, because the elevation of boiling point of 55% concentration liquid glucose has reached more than 3 DEG C, the elevation of boiling point is larger, and effective heat transfer temperature difference of evaporation is less.More than 55% sugar concentration continues to rise, and the elevation of boiling point accelerates to rise, and the steam output of MVR vaporizer will decline fast.
Consider the characteristic of MVR vaporizer, therefore must first vacuumize before startup MVR vaporizer, MVR vaporizer runs when vacuum degree deficiency, and its power consumption can rise fast and cause motor to trip, even motor damage time serious.Should also be noted that the motor of MVR vaporizer must not the operation more than 50 hertz, otherwise occur same problem.
Ensuing reconcentration step needs by MVR vaporizer pre-concentration to concentration about 50%, then sends to triple effect waste heat evaporator and be concentrated to crystallization desired concn further.Triple effect waste heat evaporator can use the steam flashed off in liquefying starch breast process in traditional technology to be thermal source, and its temperature is about 90 ~ 93 DEG C, and after reconcentration step terminates, will obtain concentration is the dense syrup of 68-72%.
Decolorization process is the procedure added in order to ensure the finished product, its need add gac very low, be about amount of dry matter ten thousand/to very much son three.The useless charcoal that dense syrup decolorization produces still has certain decolorizing ability, if can ensure fresh change, can continue to use.
After dense syrup decolorization is completed, next be exactly the step of Crystallization Separation, Crystallization Separation step mainly adopts secondary grading crystallization processes in the present embodiment, first be that the 68-72% dense syrup pump that decolours is squeezed in the first surge tank with the flow velocity of 36385kg/h by concentration, after stirring lower blade in dense syrup submergence first surge tank, start the agitator in the first surge tank and set temperature is 96 DEG C, when liquid level reaches 60% of the first surge tank, opening the first surge tank outlet valve and arranging flow is 25m
3/ h, after being filtered, syrup delivery enters in the second surge tank by ejector priming, after stirring lower blade in dense syrup submergence second surge tank, start agitator in the second surge tank and set temperature is 53 DEG C, when liquid level reaches the second surge tank 30%, opening the second surge tank outlet valve and arranging flow is 25m
3/ h, after being filtered, dense syrup enters in the 3rd surge tank by ejector priming, after stirring lower blade in dense syrup submergence the 3rd surge tank, start the agitator in the 3rd surge tank and set temperature is 45 DEG C, when liquid level reaches 50%, opening the 3rd surge tank outlet valve and arranging flow is 50m
3/ h, after being filtered, close the first surge tank outlet valve and ejector priming to charging in crystallizer.In combinations kind tank, crystal seed is added with worm conveyor, after the quantity of crystal seed is qualified (in the present embodiment, said quantity is qualified refers to that crystal seed reaches the proportioning with dense syrup, and proportioning is digital known by those skilled in the art, therefore in the present embodiment, no longer mention), with 15m
3/ h flow enters crystallizer, with 45m
3the syrup of/h flow mixes under the effect of crystallizer agitator, and Temperature fall 12 hours, when rate to be crystallized reaches requirement, separates massecuite, and remaining material, adds crystal seed and repeat above-mentioned crystallization processes, reach the object of two-stage crystallization.
Consider that from improving the quality of products crystallization adopts 40 cubes of horizontal decrease temperature crystalline machines.Horizontal crystallizer, compared with the vertical cooling crystallizer of continuous crystallisation, has crystal grain packed uniform and percent crystallization in massecuite (xln dry account for the total dry of massecuite only than) high advantage, adopts the top-suspended basket centrifuge of Guangxi Su Shi group in the present embodiment.
The massecuite of advantages of good crystallization enters whizzer, under the influence of centrifugal force, high-purity crystallized glucose is wherein deposited in the basket of whizzer, still dissolves glucose in the solution and a small amount of assorted sugar is glucose mother liquid (or claiming grape molasses) after whizzer throws away.Glucose mother liquid should make rational arrangement according to its purity.
Ensuing drying step mainly by obtain after Crystallization Separation moisture crystalline dextrose send into the fixed fluidized bed drying machine of round shape back-mixing bed adverse current that pressure is 3.5kpa, temperature is 80 DEG C and (adopt the method that the present embodiment provides, according to strict step, general obtained for water content be the crystalline dextrose of 14%), be characterized in hot blast and the complete counter current contact of material, the moisture of 90-95% can be dried; Send into through the dried crystalline dextrose of fixed fluidized bed drying machine the Vibratingfluidbeddrier that pressure is 350pa, temperature is 43 DEG C, under the effect of vibratory screening apparatus, screen out comprised moisture; Send into normal pressure through the dried crystalline dextrose of Vibratingfluidbeddrier, temperature is the vibrated fluidized bed cooler of 13 DEG C, obtains the finished product through cooling.
In the present embodiment, the temperature provided, pressure and PH scope all often many experiments record, and when specifically using, temperature range deviation ± 5 DEG C, pressure divergence ± 100pa or 0.5kpa, pH value deviation ± 0.5 all should be the claimed content of the present invention.
Detect: detect according to standards of pharmacopoeia for the medicinal DEXTROSE MONOHYDRATE BP using present method to produce
Through inspection, the medicinal DEXTROSE MONOHYDRATE BP using present method to produce meets state-promulgated pharmacopoeia standard, and is better than the medicinal DEXTROSE MONOHYDRATE BP of produced in conventional processes.
The above; it is only preferred embodiment of the present invention; it is not restriction the present invention being made to other form; the Equivalent embodiments that any those skilled in the art may utilize the technology contents of above-mentioned announcement to be changed or be modified as equivalent variations is applied to other field; but everyly do not depart from technical solution of the present invention content; according to any simple modification, equivalent variations and remodeling that technical spirit of the present invention is done above embodiment, still belong to the protection domain of technical solution of the present invention.
Claims (6)
1. from starch saccharificating liquid, extract a technique for glucose, it is characterized in that, this technique comprises concentration process, decolorization, Crystallizing process, the drying process of carrying out successively, and wherein said concentration process comprises the following steps:
A, pre-concentration: utilize MVR vaporizer that starch saccharificating liquid is concentrated into concentration about 50%;
B, reconcentration: starch saccharificating liquid pre-concentration being obtained about 50% concentration is transported to triple effect waste heat evaporator and carries out reconcentration, obtains dense syrup.
Described Crystallizing process comprises the following steps:
C, first to stir in the dense syrup delivery surge tank decoloured;
D, by the dense syrup delivery that stirred in crystallizer, add crystal seed simultaneously and mix.
After e, naturally cooling 12h, obtain the massecuite of advantages of good crystallization, then by the massecuite of advantages of good crystallization input whizzer, carry out centrifugation, obtain water-containing crystal glucose and remaining dense syrup;
F, remaining dense syrup to be added in crystallizer again, to repeat Step d and step e.
2. a kind of technique extracting glucose from starch saccharificating liquid according to claim 1, is characterized in that, described whizzer is top-suspended basket centrifuge.
3. a kind of technique extracting glucose from starch saccharificating liquid according to claim 1, is characterized in that, described decolorization is powder activity carbon decoloring.
4. a kind of technique extracting glucose from starch saccharificating liquid according to claim 1, it is characterized in that, described drying process comprises the following steps:
G, the water-containing crystal glucose obtained after Crystallization Separation is transported in drying unit, carries out drying treatment, obtain the glucose crystallization of water content below 9.0%.
5. a kind of technique extracting glucose from starch saccharificating liquid according to claim 4, is characterized in that, described drying unit is the fixed fluidized bed drying unit of round shape back-mixing bed adverse current.
6. a kind of technique extracting glucose from starch saccharificating liquid according to claim 5, it is characterized in that, the fixed fluidized bed drying unit of described round shape back-mixing bed adverse current comprises fixed fluidized bed drying machine, Vibratingfluidbeddrier and vibrated fluidized bed cooler.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102703547A (en) * | 2012-06-14 | 2012-10-03 | 万福生科(湖南)农业开发股份有限公司 | Method for producing glucose bulk drug for injection by using rice |
| CN103450287A (en) * | 2013-09-24 | 2013-12-18 | 山东华义玉米科技有限公司 | Glucose mother liquor recycling process |
| CN103725731A (en) * | 2013-12-30 | 2014-04-16 | 河南飞天农业开发股份有限公司 | Crystalline dextrose special for sodium gluconate and preparation method of crystalline dextrose |
| CN103865968A (en) * | 2012-12-16 | 2014-06-18 | 西王药业有限公司 | Process for improving quality of anhydrous glucose and glucose monohydrate products |
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- 2015-05-22 CN CN201510267112.8A patent/CN104928405A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102703547A (en) * | 2012-06-14 | 2012-10-03 | 万福生科(湖南)农业开发股份有限公司 | Method for producing glucose bulk drug for injection by using rice |
| CN103865968A (en) * | 2012-12-16 | 2014-06-18 | 西王药业有限公司 | Process for improving quality of anhydrous glucose and glucose monohydrate products |
| CN103450287A (en) * | 2013-09-24 | 2013-12-18 | 山东华义玉米科技有限公司 | Glucose mother liquor recycling process |
| CN103725731A (en) * | 2013-12-30 | 2014-04-16 | 河南飞天农业开发股份有限公司 | Crystalline dextrose special for sodium gluconate and preparation method of crystalline dextrose |
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Application publication date: 20150923 |