CN105316374A - Sugar making method - Google Patents
Sugar making method Download PDFInfo
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- CN105316374A CN105316374A CN201410330383.9A CN201410330383A CN105316374A CN 105316374 A CN105316374 A CN 105316374A CN 201410330383 A CN201410330383 A CN 201410330383A CN 105316374 A CN105316374 A CN 105316374A
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- feed liquid
- saccharification
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- decolouring
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Abstract
The invention discloses a sugar making method. The method comprises the following steps: preparing starch slurry from a starchy raw material, subjecting starch slurry to liquidation and saccharification in sequence to obtain a sugar solution; contacting the sugar solution with active carbon to discolor the sugar solution, then refining the discolored sugar solution by an ion exchange resin, then carrying out heat exchange between refined sugar solution and discolored sugar solution so as to raise the temperature of the refined sugar solution by 10 to 25 DEG C, and finally condensing the refined sugar solution. Through the technical scheme mentioned above, the consumed steam amount in the sugar making technology is largely reduced, and the energy consumption is reduced. Moreover, by adjusting the liquidation technology, the high efficient liquidation of starch slurry with a high dry substance content (32 to 40 wt%) can be achieved, the water consumption in the step of slurry mixing is reduced on the basis that the good effects of liquidation and saccharification are not affected, and the saved water amount is at least 45,000 tons for a production line that consumes 130,000 tons of starchy raw material.
Description
Technical field
The present invention relates to sugaring field, particularly, relate to a kind of wet method method for manufacturing sugar utilizing starchy material.
Background technology
W-Gum is the raw material being widely used in the corn deep processing such as feed, β-amylose industry, and China is starch and β-amylose big producing country, and wherein β-amylose annual production exceedes 6,000,000 tons, and production technique adopts corn wet sugar refining technology mostly.Corn wet sugar refining technology refer to carry out again after corn particle is soaked in water pulling an oar, liquefy, saccharification, separation liquid glucose and sugared slag, decolouring, refining and concentrated technique.Wherein the energy consumption of existing enrichment step consumption is comparatively large, directly affects the production cost of sugar refining technology, is further improved.
Summary of the invention
The object of the invention is the above-mentioned deficiency overcoming prior art, a kind of method for manufacturing sugar that can reduce energy consumption is to a great extent provided.
To achieve these goals, the present inventor has carried out large quantifier elimination, found that, if the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange farthest can recycle heat in sugar refining technology, thus save the quantity of steam needed for technique.Therefore, the invention provides a kind of method of sugaring, the method comprises prepares farinaceous size by starchy material, farinaceous size is carried out successively liquefy and saccharification, obtain liquid glucose, liquid glucose is contacted with gac and decolours, and the feed liquid spent ion exchange resin after decolouring is refined, again the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, with make refining after the temperature of feed liquid raise 10-25 DEG C, then concentrated refining after feed liquid.
By technique scheme, the present invention decreases the quantity of steam that sugar refining technology consumes to a great extent, reduces energy consumption.
And, in the preferred embodiment of the present invention, by adjustment liquefaction process, the efficient liquefaction of the farinaceous size of dry matter content higher (32-40 % by weight) can be realized, the water consumption (for the production line consuming 130,000 tons of starchy materials year, at least saving 4.5 ten thousand tons every year) prepared in farinaceous size (sizing mixing) process is saved under the prerequisite ensureing preferably liquefaction and saccharification result.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
In the present invention, when not doing contrary explanation, term " DE value " refers to that reducing sugar (with glucose meter) accounts for the per-cent of feed liquid dry-matter.
Method for manufacturing sugar provided by the invention comprises prepares farinaceous size by starchy material, farinaceous size is carried out successively liquefy and saccharification, obtain liquid glucose, liquid glucose is contacted with gac and decolours, and the feed liquid spent ion exchange resin after decolouring is refined, again the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, with make refining after the temperature of feed liquid raise 10-25 DEG C (being preferably 11-20 DEG C), then concentrated refining after feed liquid.
According to the preferred embodiment of the present invention, after the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, the temperature of the feed liquid after decolouring reduces 20-35 DEG C.
Heat according to the present invention, the concrete operations of described heat exchange do not specially required, as long as can be made to transmit according to upper type.Usually, can realize heat exchange by interchanger, described interchanger can be various conventional interchanger, and can by commercially available, the such as heat exchanger with oblate of U.S. Brown company.
According to the present invention, the method being prepared farinaceous size by starchy material can be the various methods of this area routine, such as, starchy material can be pulverized (control median size is 10-50 μm) and be mixed to get farinaceous size with water afterwards.Wherein, have no particular limits the concentration of farinaceous size, preferably, in described farinaceous size, the content of dry-matter is 32-40 % by weight, is more preferably 35-40 % by weight.
More preferably, the condition of described liquefaction comprises: the temperature of liquefaction is 105-125 DEG C (being more preferably 110-120 DEG C), and the time of liquefaction is 2-2.5h (being more preferably 2.1-2.4h).The enzymolysis of the farinaceous size to higher concentration (32-40 % by weight) can be realized better by above preferred liquefaction condition, thus under the prerequisite ensureing preferably liquefaction and saccharification result, save the water consumption (for the production line consuming 130,000 tons of starchy materials year, at least saving 4.5 ten thousand tons every year) of sizing mixing in process.
In the present invention, the content and the liquefaction condition that control dry-matter in farinaceous size can be enhanced productivity further in above-mentioned preferable range.The pH value of described farinaceous size can be 5.6-5.8.
According to the present invention, conventional mode can be adopted to liquefy, and such as, the mode of being carried out by farinaceous size liquefying can be: contacted with steam with diastatic mixture by farinaceous size, makes the temperature of mixture rise to 105-125 DEG C.Wherein, water heater can be utilized to carry out the contact of mixture and steam.Liquefy more fully to make starchy material, the mode of being carried out by farinaceous size liquefying can be: contacted with steam with diastatic mixture by farinaceous size, make the temperature of mixture rise to 105-125 DEG C, then by mixture flash distillation to 95-98 DEG C, and maintain 2-2.5h.Flash distillation refer to the saturation water of high pressure enter after in the container of relatively low pressure due to the unexpected reduction of pressure make these saturation waters become a part container pressure under saturated steam and saturation water.The pressure of flash distillation can be-0.06MPa to-0.09MPa.
According to the present invention, the diastatic amount used that liquefies can be selected for the routine of this area, and under preferable case, relative to the dry-matter in farinaceous size per ton, the diastatic amount used that liquefies is 400-450g, is more preferably 420-450g.
Wherein, the amylase that the amylase used that liquefies can adopt for this area routine, as α-amylase, beta-amylase and isoamylase; Also can be fire resistant alpha-diastase.Under preferable case, use fire resistant alpha-diastase and Thermostable α-Amylase, Thermostable α-Amylase has excellent heat resistance, adopt Bacillus licheniformis through deep drainpipe, the operations such as extraction are refining to be formed, can random hydrolysis starch, glycogen and degradation product inside thereof α-Isosorbide-5-Nitrae glucoside bond the viscosity of colloidal starch solution is declined rapidly, produce soluble dextrins and oligosaccharide, excessive hydrolysis can produce a small amount of glucose and maltose.Above-mentioned various amylase all can by commercially available.
In the present invention, for the not special requirement of the mode that farinaceous size is carried out liquefying, the various modes that this area is conventional can be adopted, such as, in farinaceous size, add calcium hydroxide regulates pH to be 5.6-5.8, add α-amylase by feed liquid amount of dry matter again, squeeze into liquefaction injector after stirring with pump, the farinaceous size after enzyme-added and the mass ratio of steam can be 1:0.125-0.15.Wherein, the DE value of liquefier that post liquefaction obtains maintains and is particularly conducive within the scope of the 12-16% of saccharification.
According to the present invention, in order to make starchy material be converted into monose as much as possible, described method also comprises the liquefier obtained by post liquefaction and carries out saccharification.
Wherein, have no particular limits the condition of described saccharification, the temperature of described saccharification is preferably 60-70 DEG C.The pH value of described saccharification is preferably 4.2-4.4.The time of described saccharification is preferably 36-48h.The consumption of saccharification saccharifying enzyme used can be the saccharifying enzyme consumption of this area routine, and preferably, relative to the dry-matter in farinaceous size per ton, the amount of saccharification saccharifying enzyme used is 550-650g.
Wherein, saccharifying enzyme is also known as starch α-Isosorbide-5-Nitrae-glucuroide, and this enzyme acts on the non reducing end of starch molecule, in units of glucose, acts on the α-Isosorbide-5-Nitrae-glycosidic link in starch molecule successively, generates glucose.Product after saccharifying enzyme acts on amylopectin has glucose and the oligosaccharides with α-1,6-glycosidic link; Acting on the product after amylose starch is all almost glucose.Described saccharifying enzyme can by commercially available.
To the not special requirement of the mode of described saccharification, can carry out with reference to the usual manner of this area, such as, gained liquefier be added in saccharifying tank, add saccharifying enzyme and stir, generally DE value be reached 98-98.8% as saccharification terminal.
According to the present invention, in order to realize decolouring better, before decolouring, the feed liquid that can also obtain saccharification carries out solid-liquid separation (as press filtration), then the liquid phase obtained (liquid glucose) is decoloured.The concrete operations of decolouring can for the conventional decoloring method adopted in sugar refining technology, and kind and the consumption of gac are well known to those skilled in the art, and such as, the consumption (weight) of gac can be 0.5-1g/100g feed liquid; The temperature of decolouring can be 75-85 DEG C, and the time can be 15-30min.Decolouring is preferably carried out under the condition stirred.If decolorizing effect is bad, can also carry out secondary decolourization, those skilled in the art can carry out selection and judge to this, do not repeat them here.
In method of the present invention, liquid glucose still containing part inorganic salt and organic impurity, therefore adopts ion exchange resin to refine, plays the effect of ion-exchange and absorption after decolouring.The ability specific activity charcoal that ion exchange resin removes deproteinize, amino acid, hydroxymethylfurfural and coloring matter etc. is strong.Through the liquid glucose of ion exchange resin treatment, ash content can be reduced to original 1/10, and remove thoroughly coloring matter, thus, not only product clarity is good, and is long placed in also nondiscoloration, is conducive to the preservation of product.Ion exchange resin is divided into Zeo-karb and two kinds, anionite-exchange resin, and the technique generally applied at present is " sun-cloudy-sun-cloudy " 4 filter beds, and namely 2 pairs of cationic, anionic exchange resin filter bed series connection use.The concrete use of ion exchange resin is conventionally known to one of skill in the art, does not repeat them here.
According to the present invention, described starchy material can for well known in the art various may be used for enzymolysis, fermentation containing the raw material of starch, such as, can be selected from corn, potato class, wheat and Chinese sorghum one or more.
Below will be described the present invention by embodiment.In following examples, the maize raw material of starchy material for by the mean particle size obtained after corn (moisture content is 13 % by weight) pulverizing being 10 microns of use; The step of decolouring is: gac (the specific surface area 1000m adding 0.5g/100g liquid glucose in liquid glucose
2/ g, granularity are less than 50 μm), cross after 80 DEG C of stirring in water bath decolouring 20min and filter gac; The refining Zeo-karb used is 732 storng-acid cation exchange resins, anionite-exchange resin is D311 weak base anion-exchange resin, feed liquid is successively by the ion exchange resin filter bed that " sun-cloudy-sun-cloudy " connects, and the flow rate control of feed liquid is 2BV/h; The measuring method reference standard QB/T2319-1997 of transmittance, instrument is spectrum SP-752 ultraviolet-visible pectrophotometer (Shanghai Spectrum Apparatus Co., Ltd.), and transmittance is higher, and illustrate that the turbidity of liquid glucose is lower, liquid glucose is purer; DE value adopts fehling reagent titration detection method to record.In following examples, the experimental technique of unreceipted actual conditions, conveniently condition is carried out.
Embodiment 1
In starchy material, add water move to dry matter content is 35 % by weight, add calcium hydroxide and regulate pH=6.0, add α-amylase (dry-matter per ton adds the α-amylase of 420g), liquefaction injector is squeezed into pump after stirring, farinaceous size after enzyme-added and the mass ratio of steam are 1:0.13, the temperature of liquefaction is 115 DEG C, and the time of liquefaction is 2.3h, and the DE value of the liquefier of acquisition is 14%.
The liquefier obtained by post liquefaction adds saccharifying tank, at 60 DEG C, and pH value 4.4 times, add saccharifying enzyme (4060 compounded saccharifying enzymes that Genencor Company produces, dry-matter per ton adds the saccharifying enzyme of 550g), stir 48h, namely arrive saccharification terminal (DE value is 98.3%).
The saccharified liquid obtained after saccharification is carried out press filtration, obtain the liquid glucose that transmittance is 98%, liquid glucose is contacted with gac and decolours, and the feed liquid spent ion exchange resin after decolouring is refined, then the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, with make refining after the temperature of feed liquid raise 11 DEG C, after heat exchange, the temperature of the feed liquid after decolouring reduces by 20 DEG C, then concentrates the feed liquid after refining, and the amount of the concentrated steam consumed is 0.357g/g starchy material.
Embodiment 2
In starchy material, add water move to dry matter content is 40 % by weight, add calcium hydroxide and regulate pH=6.0, add α-amylase (dry-matter per ton adds the α-amylase of 450g), liquefaction injector is squeezed into pump after stirring, farinaceous size after enzyme-added and the mass ratio of steam are 1:0.13, the temperature of liquefaction is 120 DEG C, and the time of liquefaction is 2.1h, and the DE value of the liquefier of acquisition is 16%.
The liquefier obtained by post liquefaction adds saccharifying tank, at 70 DEG C, and pH value 4.2 times, add saccharifying enzyme (4060 compounded saccharifying enzymes that Genencor Company produces, dry-matter per ton adds the saccharifying enzyme of 600g), stir 36h, namely arrive saccharification terminal (DE value is 98.6%).
The saccharified liquid obtained after saccharification is carried out press filtration, obtain the liquid glucose that transmittance is 98.5%, liquid glucose is contacted with gac and decolours, and the feed liquid spent ion exchange resin after decolouring is refined, then the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, with make refining after the temperature of feed liquid raise 20 DEG C, after heat exchange, the temperature of the feed liquid after decolouring reduces by 35 DEG C, then concentrates the feed liquid after refining, and the amount of the concentrated steam consumed is 0.350g/g starchy material.
Embodiment 3
In starchy material, add water move to dry matter content is 38 % by weight, add calcium hydroxide and regulate pH=6.0, add α-amylase (dry-matter per ton adds the α-amylase of 430g), liquefaction injector is squeezed into pump after stirring, farinaceous size after enzyme-added and the mass ratio of steam are 1:0.13, the temperature of liquefaction is 110 DEG C, and the time of liquefaction is 2.4h, and the DE value of the liquefier of acquisition is 12%.
The liquefier obtained by post liquefaction adds saccharifying tank, at 62 DEG C, and pH value 4.3 times, add saccharifying enzyme (4060 compounded saccharifying enzymes that Genencor Company produces, dry-matter per ton adds the saccharifying enzyme of 650g), stir 40h, namely arrive saccharification terminal (DE value is 98.5%).
The saccharified liquid obtained after saccharification is carried out press filtration, obtain the liquid glucose that transmittance is 99%, liquid glucose is contacted with gac and decolours, and the feed liquid spent ion exchange resin after decolouring is refined, then the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, with make refining after the temperature of feed liquid raise 18 DEG C, after heat exchange, the temperature of the feed liquid after decolouring reduces by 30 DEG C, then concentrates the feed liquid after refining, and the amount of the concentrated steam consumed is 0.353g/g starchy material.
Embodiment 4
Refine sugar according to the method for embodiment 3, unlike, the content adding water move to dry-matter in starchy material is 30 % by weight, and the DE value of the liquefier of acquisition is 17%, DE value after saccharification is 96.8%, and the transmittance recording the liquid phase (liquid glucose) that press filtration obtains is 96%.
Embodiment 5
Refine sugar according to the method for embodiment 3, unlike, the temperature controlling liquefaction is 130 DEG C, and the DE value of the liquefier of acquisition is 19%, and the DE value after saccharification is 95%, and the transmittance recording the liquid phase (liquid glucose) that press filtration obtains is 89%.
Embodiment 6
Refine sugar according to the method for embodiment 3, unlike, the time controlling liquefaction is 3h, and the DE value of the liquefier of acquisition is 20%, and the DE value after saccharification is 94%, and the transmittance recording the liquid phase (liquid glucose) that press filtration obtains is 93.4%.
Comparative example 1
Refine sugar according to the method for embodiment 3, unlike, do not carry out heat exchange, the amount of the concentrated steam consumed is 0.375g/g starchy material.
As can be seen from the result of above embodiment, method of the present invention can reduce energy consumption to a great extent.Especially, the result of comparing embodiment 3 and embodiment 4-6 can be found out, control the content of dry-matter in farinaceous size and liquefaction condition in preferable range of the present invention, the higher farinaceous size of dry matter content can be processed under the prerequisite ensureing preferably liquefaction and saccharification result, save the water consumption of sizing mixing in process, and be conducive to the energy consumption reducing the steps such as subsequent concentration, and DE value and the transmittance of liquid glucose can be improved further, namely realize the object of enhancing productivity.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (9)
1. the method for a sugaring, it is characterized in that, the method comprises prepares farinaceous size by starchy material, farinaceous size is carried out successively liquefy and saccharification, obtain liquid glucose, liquid glucose is contacted with gac and decolours, and the feed liquid spent ion exchange resin after decolouring is refined, again the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, with make refining after the temperature of feed liquid raise 10-25 DEG C, then concentrated refining after feed liquid.
2. method according to claim 1, wherein, carries out heat exchange by the feed liquid after the feed liquid after refining and decolouring, with make refining after the temperature of feed liquid raise 11-20 DEG C.
3. method according to claim 1, wherein, after the feed liquid after the feed liquid after refining and decolouring is carried out heat exchange, the temperature of the feed liquid after decolouring reduces 20-35 DEG C.
4. according to the method in claim 1-3 described in any one, wherein, with the dry weight basis of starchy material, the concentration of described farinaceous size is 32-40 % by weight, and the condition of described liquefaction comprises: the temperature of liquefaction is 105-125 DEG C, and the time of liquefaction is 2-2.5h.
5. method according to claim 4, wherein, in described farinaceous size, the content of dry-matter is 35-40 % by weight.
6. method according to claim 4, wherein, the temperature that the condition of described liquefaction comprises liquefaction is 110-120 DEG C, and the time of liquefaction is 2.1-2.4h.
7. method according to claim 1, wherein, relative to the dry-matter in farinaceous size per ton, the diastatic amount used that liquefies is 400-450g.
8. method according to claim 1, wherein, the condition of described saccharification comprises: the temperature of saccharification is 60-70 DEG C, the pH value of saccharification is 4.2-4.4, the time of saccharification is 36-48h, and relative to the dry-matter in farinaceous size per ton, the amount of saccharification saccharifying enzyme used is 550-650g.
9. method according to claim 1, wherein, described starchy material be selected from corn, potato class, wheat and Chinese sorghum one or more.
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| CN201410330383.9A CN105316374A (en) | 2014-07-11 | 2014-07-11 | Sugar making method |
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| CN111139319A (en) * | 2020-02-11 | 2020-05-12 | 浙江华康药业股份有限公司 | System and method for reducing content of 5-hydroxymethylfurfural in high fructose corn syrup |
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| CN111139319A (en) * | 2020-02-11 | 2020-05-12 | 浙江华康药业股份有限公司 | System and method for reducing content of 5-hydroxymethylfurfural in high fructose corn syrup |
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| CN114287519A (en) * | 2021-11-23 | 2022-04-08 | 江西正邦农业科学院 | Preparation method and application of oligosaccharide chelate |
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