CN1810994A - Crystalline glucose producing process based on whole membrane method - Google Patents
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Abstract
The present invention relates to glucose production, and is one whole membrane method of producing high purity crystalline glucose in relatively low cost. The method includes the following steps: liquefying starch to obtain starch liquid with DE value of 14-25 %; cooling and adding compound amylase to enzymolyze into glucose liquid; microfiltering to obtain dialysate and filter residue; drying the filter residue to produce feed; ultrafiltering the dialysate to obtain ultrafiltrate and ultrafiltered concentrated liquid; nanofiltering the ultrafiltrate to obtain nanofiltrate and nanofiltered concentrated liquid; concentrating the nanofiltrate to obtain concentrated glucose liquid; and spray drying to obtain crystalline glucose product. The nanofiltrate has DX value higher than 99.5 % and the method has no crystallization step and 10 % raised glucose yield. The method can recover starch and polysaccharide and is environment friendly.
Description
Technical field
The present invention relates to a kind of glucose, particularly relate to a kind of manufacture method of the crystalline dextrose based on full embrane method.
Background technology
Glucose (C6H12O6) also claim dextrose, being a kind of important nutritious prod, is the important energy source of organism alive, is prevailing monose and important Essential Chemistry pharmaceuticals, being the integral part of many saccharide compounds, is multiple organic pure and mild antibiotic saccharine material.Evolutions such as acid system, acid-enzyme hydrolysis method, double-enzyme method have been experienced in the production of glucose.Crystalline dextrose starts from nineteen twenty-one with static crystallization process production in the aqueous solution, the production of motion crystallization process starts from nineteen twenty-four, and industrial production oral glucose, injection crystalline dextrose started from after nineteen forty-two.The U.S. in 1940 begins to merge saccharification with sour enzyme and produces high sugariness syrup.The sixties in 20th century, Japan begins the double-enzyme method Mashing process with α-Dian Fenmeiyehua and glucoamylase enzyme glycolysis, and the back is generally adopted by various countries.Along with the development of zymin kind, the technology of being refined sugar by the starch hydrolysis progressively obtains further improving and development, has improved the percent hydrolysis and the Dian Fentang quality product of starch, has satisfied the needs of production and consumption.The later stage eighties 20th century, China is on the basis of the external advanced glucose production process technology of introducing, develop the production technology of successful full-enzyme method, double-enzyme method mashing production glucose, progressively eliminated acid system, acid-enzyme hydrolysis method saccharification technology, improved the yield and quality of glucose.
At present, the method of production high purity glucose is based on the production technique of traditional high-purity crystallized glucose, and its flow process is: starch → liquefaction → saccharification → rotary drum filters (adding diatomite) → activated carbon decolorizing → Plate Filtration → activated carbon decolorizing → Plate Filtration → ion-exchange → evaporation → crystallization → drying.
With the double-enzyme method is example, it is the W-Gum water to be made into 20%～35% starch milk, add α-high temperature liquefying amylase,, be hydrolyzed into DE value (dextrose equivalent value) at 14%～25% saccharan, dextrin etc. through a liquefaction high pressure spraying of injector and the enzyme-added continuous liquefaction reaction of secondary; Through the adding compounded saccharifying enzyme that cools, saccharification liquid DE value is reached more than 98% again; Remove organic impurity and inorganic ion through the enzyme that goes out, decolouring, press filtration and ion-exchange, produce the crystallization DEXTROSE MONOHYDRATE BP through evaporation concentration, crystallisation by cooling, centrifugation and drying again.
This traditional glucose production process exists the technological process of production long, must add diatomite when rotary drum filters, and must adopt activated carbon to carry out adsorption bleaching as sorbent material when decolouring, and consumption of raw and auxiliary materials is big, and production cost is higher, and to defectives such as environment pollute.
Application number is the method for making that the application for a patent for invention of CN86106624 discloses a kind of crystalline glucose for medicine, its method is to make debranching factor and glucoamylase and starch hydrolyzates effect, obtain containing the above high purity liquid glucose of glucose 97.0% (weight), again that liquid glucose is refining, concentrated, just can make crystalline dextrose, and do not need recrystallize, can make at low cost and do not contain the former high-purity crystallized glucose of heating.Publication number be the application for a patent for invention of CN1715423 disclose a kind of from the crystalline dextrose mother liquor method of separating glucose and function new oligosaccharide, by synthetic resin dedicated, utilize simulated moving bed technology, from the crystalline dextrose mother liquor, separate preparation high purity glucose and functional oligose.Concrete grammar is to be raw material with the crystalline dextrose mother liquor, by simulated moving bed chromatography system, under 35～95 ℃ service temperature, be eluent with water, glucose is separated fully, the component that obtains being rich in the component of glucose and be rich in functional oligose with functional oligose.Publication number is that the application for a patent for invention of CN1398989 discloses the crystallization processes in a kind of glucose production, being characterized in adopting several horizontal crystallizer series connection is one group, implement the horizontal continuous crystallization technology of continuously feeding, continuous discharging, as long as several main parameters indexs such as control material inlet, material outlet temperature, the steady and continuous that gets final product the crystallization control process is operated.
Membrane separation technique is constantly full-fledged in recent years, and this technology use cost aspect descends gradually, and application of membrane separation technology will show good economic benefit in the middle of the production of glucose.When guaranteeing quality product, aspect realizing automatization control and cleaner production, reducing production costs, membrane separation process embodies special advantages, but existing membrane technique utilization all is to adopt a certain membrane process, solve a certain particular problem, do not form complete crystalline dextrose production technique based on full embrane method.
Summary of the invention
The objective of the invention is to the deficiency that exists at existing crystalline dextrose production technique, provide that a kind of Production Flow Chart is short, raw material overall availability height and product purity height, investment is less, production cost is lower based on the manufacture method of the high-purity crystallized glucose of full membrane technique.
Step of the present invention is:
1) starch liquefacation: raw starch is mixed with water, be mixed with the liquid starch material emulsion of producing glucose, contents of starch accounts for 20%～35% of liquid starch material emulsion total mass, sterilize then, be prepared into starch emulsion, in starch emulsion, add a-high temperature liquid amylase again, through a high pressure spraying of liquefaction injector, the enzyme-added continuous liquefaction reaction of secondary is hydrolyzed into the liquefying starch liquid (contain saccharan, dextrin etc.) of dextrose equivalent value (DE value) between 14%～25%;
2) saccharification: the DE value (dextrose equivalent value) that step 1 is prepared the liquefying starch liquid between 14%～25% add compounded saccharifying enzyme after 35-45 ℃ through cooling and under this temperature enzymolysis become glucosylation liquid;
3) micro-filtration filters: glucosylation liquid is filtered by micro-filtration, get the micro-filtration dialyzate and the filter residue of glucose, filter residue is after drying as feed;
4) ultra-filtration filters: the micro-filtration dialyzate is got ultrafiltration dialysis liquid and ultrafiltration and concentration liquid by ultra-filtration filters;
5) nanofiltration separation concentrates: with ultrafiltration dialysis liquid by nanofiltration filter nanofiltration dialyzate and nanofiltration concentrated solution;
6) concentrate: nanofiltration dialyzate simmer down to glucose concentrated solution;
7) spraying drying: with the spray-dried crystalline dextrose finished product that gets of glucose concentrated solution.
In step 1), raw starch is W-Gum, potato starch, Starch rice, tapioca (flour), sweet potato starch etc. or other starch.
In step 2) in, behind enzymolysis 48h, every interval 0.5h or METHOD FOR CONTINUOUS DETERMINATION saccharification liquid DE value when DE value 〉=98%, finish enzymolysis process.
In step 3), micro-filtration filters used microfiltration membrane material selection ceramic membrane or metallic membrane, its molecular weight cut-off is 10000～500000MWCO (aperture is at 0.01～1 μ m), service temperature is 50～90 ℃, operating pressure: entrance pressure is 3.5～7.5bar, going out to press is 1.0～6.0bar, and pressure difference is 1.5～2.5bar.
In step 4), the used mould material of ultrafiltration is selected a kind of in poly (ether-sulfone) ultrafiltration membrane, polysulphones hyperfiltration membrane, polyamide membrane, polyvinylidene fluoride film, polyacrylonitrile film, the composite membrane for use, its molecular weight cut-off is 300～2500MWCO, service temperature is 35～45 ℃, operating pressure: entrance pressure is 12.5～33.5bar, going out to press is 11.5～32.0bar, and pressure difference is 1～1.5bar.
In step 5), the used mould material of nanofiltration is selected a kind of in polyether sulfone filtering film, polysulfones nanofiltration membrane, polyamide nanofiltration membrane, polyvinylidene difluoride (PVDF) nanofiltration membrane, polyacrylonitrile nanofiltration membrane, the composite nanometer filtering film for use, its molecular weight cut-off is 150～350MWCO, service temperature is 35～45 ℃, operating pressure: entrance pressure is 15.5～45.0bar, going out to press is 14.5～43.5bar, and pressure difference is 1.0～2.0bar.
In step 6), it is 25%～30% that the nanofiltration dialyzate is concentrated into solid content by vacuum concentration or atmospheric evaporation, gets the glucose concentrated solution, and the condition of vacuum concentration is vacuum tightness 35～55mmHg, and thickening temperature is 55～65 ℃.
In step 7), with 25%～30% the glucose concentrated solution spray-driedly handle to such an extent that purity is glucose finished product more than 99.5%, used spray-dryer is the centrifugal spray drier of electrically heated or fuel Heating.
Compare with existing glucose production process, the present invention has following outstanding advantage:
1, saccharification liquid utilization micro-filtration filters, and mainly plays the effect of clarification saccharification liquid, can remove the insoluble particle in the middle of the feed liquid, as materials such as insoluble starch, fat, insoluble proteins, and plays pretreated effect for the ultrafiltration of back.Filter than traditional rotary drum, micro-filtrate membrane filtration need not diatomite and perlite, and filtrate quality is good, and does not have environmental pollution problems.
2, utilize ultrafiltration can remove micro-filtration dialyzate central albumen, pigment, and hold back the assorted sugar of most macromolecule, the composition that sees through ultrafiltration is the assorted sugar of glucose, inorganic salt and minute quantity pigment and small molecules.Replace the effect of the activated carbon decolorizing of traditional processing technology with ultrafiltration.
3, utilize nanofiltration can hold back the central divalence inorganic salt of feed liquid, and pigment and the disaccharides further removed in the middle of the feed liquid are above assorted sugared, especially in the substitutional ion exchange interaction, glucose DX value will be above 99.5% afterwards to guarantee feed liquid to see through nanofiltration, save the crystalline process, shorten production technique, saved crystalline facility investment and working cost, thereby reduced the production cost of crystalline dextrose significantly.
4, the problem that does not have the mother liquor loss; The glucose yield that purity is high improves more than 10%.
5, can reclaim starch, the above polysaccharide material of disaccharides, increase added value.
6, whole process does not have environmental issues such as waste water, refuse.
7, technical process is simplified significantly, for traditional technology, and the one, can save the cost of gac, the 2nd, there is not environmental pollution problems, because it is do not have vacuum, Plate Filtration, crystalline process, simple to operate in addition.
Description of drawings
Fig. 1 is an embodiment of the invention technological process of production block diagram.
Embodiment
Embodiment 1
1, starch liquefacation: raw starch 500Kg is mixed with 1100Kg water, be mixed with 31% starch emulsion, sterilize in 110～115 ℃ then, be prepared into the liquid starch material emulsion of producing glucose.In liquid starch material emulsion, add α-high temperature liquefying amylase,, be hydrolyzed into DE value (dextrose equivalent value) at 14%～25% liquefying starch liquid (containing saccharan, dextrin etc.) through liquefaction a high pressure spraying of injector and the enzyme-added continuous liquefaction reaction of secondary.
2, saccharification: the DE value (dextrose equivalent value) that step 1 is prepared adds compounded saccharifying enzyme after 35～38 ℃ and carry out enzymolysis under this temperature condition through cooling at the liquefying starch liquid between 14%～25% makes the further enzymolysis of liquefying starch liquid become glucose, behind enzymolysis 48h, every 0.5h measures (or METHOD FOR CONTINUOUS DETERMINATION) saccharification liquid DE value, through enzymolysis 52h, the DE value reaches at 98% o'clock, finishes enzymolysis process.
3, micro-filtration filters: the glucose feed liquid of step 2 saccharification gained is filtered by micro-filtration, get the micro-filtration dialyzate 2250Kg and the 246Kg filter residue of glucose, filter residue is after drying as feed.It is that molecular weight cut-off is the ceramic membrane of 120000MWCO that micro-filtration filters used microfiltration membrane material, and processing condition are: service temperature is 50～60 ℃, operating pressure: entrance pressure is 3.5bar, goes out to press to be 1bar, and pressure difference is 2.5bar.
4, ultra-filtration filters: the micro-filtration dialyzate that the described micro-filtration of step 3 is filtered gained by ultra-filtration filters get ultrafiltration dialysis liquid and and ultrafiltration and concentration liquid, the used mould material of ultrafiltration is that molecular weight cut-off is the polyvinylidene fluoride (PVDF) ultrafiltration membrane of 2500MWCO, processing condition are: service temperature is 45 ℃, operating pressure: entrance pressure is 15.5bar, go out to press to be 14.5bar, pressure difference is 1.0bar.
5, nanofiltration separation concentrates: with the ultrafiltration dialysis liquid of the described ultra-filtration filters gained of step 4 by nanofiltration filter the nanofiltration glucose dialysis and and the nanofiltration concentrated solution, the used mould material of nanofiltration is that molecular weight cut-off is the polyether sulfone filtering film of 350MWCO, processing condition are: service temperature is 45 ℃, operating pressure: entrance pressure is 45.0bar, go out to press to be 43.5bar, pressure difference is 1.5bar.
6, concentrate: it is 30% that the nanofiltration dialyzate of the glucose of step 5 nanofiltration filtering separation gained is concentrated into solid content by vacuum concentration or atmospheric evaporation, the glucose concentrated solution.The condition of vacuum concentration is vacuum tightness 35mmHg, and thickening temperature is 55 ℃.
7, spraying drying: through the nanofiltration filtering separation concentrate gained 30% the glucose concentrated solution spray-driedly handle to such an extent that purity is glucose finished product more than 99.5%, used spray-dryer is the centrifugal spray drier of electrically heated or fuel Heating, and model is determined according to industrial scale.
Embodiment 2
1, starch liquefacation: raw starch 750Kg is mixed with 1400Kg water, be mixed with 35% starch emulsion, sterilize in 115 ℃ then, be prepared into the liquid starch material emulsion of producing glucose.In liquid starch material emulsion, add α-high temperature liquefying amylase,, be hydrolyzed into DE value (dextrose equivalent value) at 14%～25% saccharan, dextrin etc. through liquefaction a high pressure spraying of injector and the enzyme-added continuous liquefaction reaction of secondary.
2, saccharification: the DE value (dextrose equivalent value) that step 1 is prepared adds compounded saccharifying enzyme after 40～42 ℃ and carry out enzymolysis under this temperature condition through cooling at the liquefying starch liquid between 14%～25% makes the further enzymolysis of liquefying starch liquid become glucose, behind enzymolysis 48h, every 0.5h measures (or METHOD FOR CONTINUOUS DETERMINATION) saccharification liquid DE value, through the 49h enzymolysis, measure the DE value and reach 98%, finish enzymolysis process.
3, micro-filtration filters: the glucose feed liquid of step 2 saccharification gained is filtered by micro-filtration, get the micro-filtration dialyzate 3600Kg and the 393Kg filter residue of glucose, filter residue is after drying as feed.It is that molecular weight cut-off is the metallic membrane of 300000MWCO that micro-filtration filters used microfiltration membrane material, and processing condition are: service temperature is 60～65 ℃, operating pressure: entrance pressure is 7.5bar, goes out to press to be 6.0bar, and pressure difference is 1.5bar.
4, ultra-filtration filters: the micro-filtration dialyzate that the described micro-filtration of step 3 is filtered gained by ultra-filtration filters get ultrafiltration dialysis liquid and and ultrafiltration and concentration liquid, the used mould material of ultrafiltration is that molecular weight cut-off is that polyvinylidene fluoride (PVDF) ultrafiltration membrane, the processing condition of 300MWCO are: service temperature is 45 ℃, operating pressure: entrance pressure is 12.5bar, go out to press to be 11.50bar, pressure difference is 1.0bar.
5, nanofiltration separation concentrates: with the ultrafiltration dialysis liquid of the described ultra-filtration filters gained of step 4 by nanofiltration filter the nanofiltration glucose dialysis and and the nanofiltration concentrated solution, the used mould material of nanofiltration is that molecular weight cut-off is the cellulose acetate nanofiltration membrane of 150MWCO, processing condition are: service temperature is 45 ℃, operating pressure: entrance pressure is 33.5bar, go out to press to be 31.5bar, pressure difference is 2.0bar.
6, concentrate: it is 25% that the nanofiltration dialyzate of the glucose of step 5 nanofiltration filtering separation gained is concentrated into solid content by vacuum concentration or atmospheric evaporation, the glucose concentrated solution.The condition of vacuum concentration is vacuum tightness 55mmHg, and thickening temperature is 65 ℃.
7, spraying drying: through the nanofiltration filtering separation concentrate gained 30% the glucose concentrated solution spray-driedly handle to such an extent that purity is glucose finished product more than 99.5%, used spray-dryer is the electrically heated centrifugal spray drier.
Embodiment 3
1, starch liquefacation: raw starch 500Kg is mixed with 1100Kg water, be mixed with 31% starch emulsion, sterilize in 115 ℃ then, be prepared into the liquid starch material emulsion of producing glucose.Adding-high temperature liquefying amylase in liquid starch material emulsion through liquefaction a high pressure spraying of injector and the enzyme-added continuous liquefaction reaction of secondary, is hydrolyzed into DE value (dextrose equivalent value) at 14%～25% saccharan, dextrin etc.
2, saccharification: the DE value (dextrose equivalent value) that step 1 is prepared adds compounded saccharifying enzyme after 42～45 ℃ and carry out enzymolysis under this temperature condition through cooling at the liquefying starch liquid between 14%～25% makes the further enzymolysis of liquefying starch liquid become glucose, behind enzymolysis 48h, every 0.5h measures (or METHOD FOR CONTINUOUS DETERMINATION) saccharification liquid DE value, during 61h, measure the DE value and reach at 98% o'clock, finish enzymolysis process.
3, micro-filtration filters: the glucose feed liquid of step 2 saccharification gained is filtered by micro-filtration, get the micro-filtration dialyzate 2240Kg and the 253Kg filter residue of glucose, filter residue is after drying as feed.It is that molecular weight cut-off is the ceramic membrane of 5000000MWCO that micro-filtration filters used microfiltration membrane material, and processing condition are: service temperature is 80～90 ℃, operating pressure: entrance pressure is 4.0bar, goes out to press to be 2.0bar, and pressure difference is 2.0bar.
4, ultra-filtration filters: the micro-filtration dialyzate that the described micro-filtration of step 3 is filtered gained by ultra-filtration filters get ultrafiltration dialysis liquid and and ultrafiltration and concentration liquid, the used mould material of ultrafiltration is that molecular weight cut-off is that polyvinylidene fluoride (PVDF) ultrafiltration membrane, the processing condition of 1000MWCO are: service temperature is 40 ℃, operating pressure: entrance pressure is 33.5bar, go out to press to be 32.0bar, pressure difference is 1.5bar.
5, nanofiltration separation concentrates: with the ultrafiltration dialysis liquid of the described ultra-filtration filters gained of step 4 by nanofiltration filter nanofiltration glucose dialysis and nanofiltration concentrated solution, the used mould material of nanofiltration is that molecular weight cut-off is the cellulose acetate rolling nanofiltration membrane core of 200MWCO, processing condition are: service temperature is 45 ℃, operating pressure: entrance pressure is 15.5bar, go out to press to be 14.5bar, pressure difference is 1.0bar.
6, concentrate: it is 28% that the nanofiltration dialyzate of the glucose of step 5 nanofiltration filtering separation gained is concentrated into solid content by vacuum concentration or atmospheric evaporation, the glucose concentrated solution.The condition of vacuum concentration is vacuum tightness 45mmHg, and thickening temperature is 60 ℃.
7, spraying drying: through the nanofiltration filtering separation concentrate gained 30% the glucose concentrated solution spray-driedly handle to such an extent that purity is glucose finished product more than 99.5%, used spray-dryer is the centrifugal spray drier of fuel Heating.
Claims (10)
1, based on the crystalline dextrose manufacture method of full embrane method, it is characterized in that the steps include:
1) starch liquefacation: raw starch is mixed with water, be mixed with the liquid starch material emulsion of producing glucose, contents of starch accounts for 20%～35% of liquid starch material emulsion total mass, sterilize then, be prepared into starch emulsion, in starch emulsion, add α-high temperature liquid amylase again, through a high pressure spraying of liquefaction injector, the enzyme-added continuous liquefaction reaction of secondary is hydrolyzed into the liquefying starch liquid of dextrose equivalent value between 14%～25%;
2) saccharification: the dextrose equivalent value that step 1 is prepared the liquefying starch liquid between 14%～25% add compounded saccharifying enzyme after 35～45 ℃ through cooling and under this temperature enzymolysis become glucosylation liquid;
3) micro-filtration filters: the glucose feed liquid is filtered by micro-filtration, get the micro-filtration dialyzate and the filter residue of glucose, filter residue is after drying as feed;
4) ultra-filtration filters: the micro-filtration dialyzate is got ultrafiltration dialysis liquid and ultrafiltration and concentration liquid by ultra-filtration filters;
5) nanofiltration separation concentrates: with ultrafiltration dialysis liquid by nanofiltration filter nanofiltration dialyzate and nanofiltration concentrated solution;
6) concentrate: nanofiltration dialyzate simmer down to glucose concentrated solution;
7) spraying drying: with the spray-dried crystalline dextrose finished product that gets of glucose concentrated solution.
2, the crystalline dextrose manufacture method based on full embrane method as claimed in claim 1 is characterized in that described raw starch is selected from W-Gum, potato starch, Starch rice, tapioca (flour), sweet potato starch or other starch.
3, the crystalline dextrose manufacture method based on full embrane method as claimed in claim 1 is characterized in that in step 2) in, behind enzymolysis 48h, every interval 0.5h or METHOD FOR CONTINUOUS DETERMINATION saccharification liquid dextrose equivalent value when dextrose equivalent value 〉=98%, finish enzymolysis process.
4, the crystalline dextrose manufacture method based on full embrane method as claimed in claim 1 is characterized in that in step 3), and micro-filtration filters used microfiltration membrane material and is selected from ceramic membrane or metallic membrane, and its molecular weight cut-off is 10000～500000MWCO.
5, as claim 1 or 4 described crystalline dextrose manufacture method based on full embrane method, it is characterized in that in step 3) the filtering service temperature of micro-filtration is 50～90 ℃, operating pressure: entrance pressure is 3.5～7.5bar, going out to press is 1.0～6.0bar, and pressure difference is 1.5～2.5bar.
6, the crystalline dextrose manufacture method based on full embrane method as claimed in claim 1, it is characterized in that in step 4), the used mould material of ultrafiltration is selected from a kind of in poly (ether-sulfone) ultrafiltration membrane, polysulphones hyperfiltration membrane, polyamide membrane, polyvinylidene fluoride film, polyacrylonitrile film, the composite membrane, and its molecular weight cut-off is 300～2500MWCO.
7, as claim 1 or 6 described crystalline dextrose manufacture method based on full embrane method, it is characterized in that in step 4) the service temperature of ultrafiltration is 35～45 ℃, operating pressure: entrance pressure is 12.5～33.5bar, going out to press is 11.5～32.0bar, and pressure difference is 1～1.5bar.
8, the crystalline dextrose manufacture method based on full embrane method as claimed in claim 1, it is characterized in that in step 5), the used mould material of nanofiltration is selected from a kind of in polyether sulfone filtering film, polysulfones nanofiltration membrane, polyamide nanofiltration membrane, polyvinylidene difluoride (PVDF) nanofiltration membrane, polyacrylonitrile nanofiltration membrane, the composite nanometer filtering film, and its molecular weight cut-off is 150～350MWCO.
9, as claim 1 or 8 described crystalline dextrose manufacture method based on full embrane method, it is characterized in that in step 5) the service temperature of nanofiltration is 35～45 ℃, operating pressure: entrance pressure is 15.5～45.0bar, going out to press is 14.5～43.5bar, and pressure difference is 1.0～2.0bar.
10, the crystalline dextrose manufacture method based on full embrane method as claimed in claim 1, it is characterized in that in step 6), it is 25%～30% that the nanofiltration dialyzate is concentrated into solid content by vacuum concentration or atmospheric evaporation, get the glucose concentrated solution, the condition of vacuum concentration is vacuum tightness 35～55mmHg, and thickening temperature is 55～65 ℃.
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Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS56144100A (en) * | 1980-04-10 | 1981-11-10 | Kuraray Co | High purification of starch converting saccharide liquid |
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