CN101210256A - Method for preparing maltitol - Google Patents
Method for preparing maltitol Download PDFInfo
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- CN101210256A CN101210256A CNA2006101600183A CN200610160018A CN101210256A CN 101210256 A CN101210256 A CN 101210256A CN A2006101600183 A CNA2006101600183 A CN A2006101600183A CN 200610160018 A CN200610160018 A CN 200610160018A CN 101210256 A CN101210256 A CN 101210256A
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- maltose
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Abstract
The invention discloses a method for preparing maltitol, which comprises preparing starch milk from starchy material, preparing maltose from starch milk, preparing maltitol solution from maltose, and concentrating and crystallizing the maltitol solution. During the step of preparing maltitol from maltose, the pH regulator for regulating pH contains magnesium (Mg) element, and during the step of concentrating and crystallizing the maltitol solution, the used crystallization device is a vertical crystallizing tank capable of continuously operating. The inventive method uses magnesium-containing pH regulator to stabilize pH during hydrogenation process, so that the hydrogenation process is easy to control and the obtained maltitol product has high purity. In addition, the inventive method uses vertical crystallizing tank to continuously crystallize maltitol, so as to improve the equipment utilization ratio.
Description
Technical field
The invention belongs to the preparation technology of sugar derivatives, relate in particular to a kind of method for preparing maltose alcohol.
Background technology
Maltose alcohol is made through hydro-reduction by maltose, is a kind of natural low heat value sweeting agent.It has following characteristics: 1) is not is not digested and assimilated in animal body, and the sugariness height, sweet taste is pure, low heat value; 2) non-fermentable, mothproof erosion, anti-going mouldy; 3) viscosity height, heat-resisting acidity is good; 4) moisture retention is good, the food and extend preservation period.There is following problem in present method: the one, and hydro-reduction process pH fluctuation is bigger, wayward; The 2nd, the maltose alcohol Crystallization Procedure is a batch operation, can not move continuously, and plant factor is low.
Summary of the invention
The object of the present invention is to provide a kind of method for preparing maltose alcohol, can stablize hydriding process pH, obtaining highly purified maltose alcohol product, and is continuous production, improves plant factor.
For achieving the above object, the present invention adopts following technical scheme: a kind of method for preparing maltose alcohol, comprise by starchy material produce starch milk, by starch milk make maltose, with maltose make maltitol solution, with the step of maltitol solution condensing crystal, maltose is being made in the step of maltitol solution, regulate the used pH regulator agent of pH and contain element magnesium (Mg), in the step with the maltose solution condensing crystal, used crystallizer is the vertical crystallizer of continuously-running.
Described pH regulator agent is metal magnesium powder or the basic cpd that contains magnesium elements.
Described vertical crystallizer is the vertical continuous crystallisation jar of maltose alcohol.
Starch milk is being made in the step of maltose, earlier starch milk is added enzyme liquefaction: regulate starch concentration to 15-18 mother-in-law U.S., add adjusting PH with base after between the 5.5-5.8, the α-Dian Fenmei that adds 0.1-0.5% calcium chloride, 0.04-0.06%, 105--110 ℃ of steam ejection liquefaction temperature, 135--140 ℃ of second spraying liquefaction temperature; Control liquefaction back DE value is between 3-5, and the BX value is between 23-26; Again with the liquefier saccharification: liquefier is cooled to 60-65 ℃ by the cooling coil pipe, adjust pH is to 5.0-5.5, the βDian Fenmei, the Pullulanase of 0.12-0.2% and the trisaccharide maltose lytic enzyme of 0.15-0.25% that add 0.12-0.18%, keep 58--62 ℃ of temperature, carry out saccharification, saccharification added the middle temperature amylase of 0.015-0.025% after 24 hours, continue saccharification to 48-60 hour, filter and obtain maltose purity at DP
2Fructus Hordei Germinatus liquid glucose more than 88%.
Maltose solution is transferred to concentration 40%, add and contain magnesium (Mg) pH regulator agent regulator solution pH to 8.0-8.7 in right amount, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 120-145 ℃ of control hydrogenation temperature, under hydrogen pressure 8.0-11MPa condition, carried out hydrogenation 60-110 minute, and made the maltitol solution of the sugar alcohol 1-9% (butt) that contains maltose alcohol 85-97% (butt), sorbyl alcohol 2.0-6.0% (butt) and DP 〉=3.
In step with the maltitol solution condensing crystal, will be concentrated into maltose alcohol concentration 75-90% by falling-film evaporator through decolorization filtering and from the Fructus Hordei Germinatus liquid glucose of handing over removal of impurities earlier, then with its from the crystallizer bottom with 3.2-4m
3The flow velocity of/h is sent in the vertical crystallizer, the temperature of vertical crystallizer is 50-65 ℃, starting crystallizer during 4 layers of spiral coil cooling tube of liquid level to the in the crystallizer stirs, nine layers of spiral coil cooling tube are with 80 centimetres of strokes, 2 minutes cycles moved back and forth, simultaneously with the 10-15 kilogram/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours altogether the 200-300 kilogram as crystal seed, after crystallizer advances to expire, stop charging, nine layers of spiral coil cooling tube are lowered the temperature in sequence, material was educated in crystallizer brilliant 30-60 hour, last upper strata greenhouse cooling to 25 ℃, lower floor's temperature of charge is 40 ℃; The maltitol solution that then will keep 50-58 ℃ is with 3.2-4m
3The flow velocity of/h continues charging from the crystallizer bottom, the massecuite major part of advantages of good crystallization is overflowed from the crystallizer top, use the suspended centrifugal of separating factor 1500 to separate 5 minutes from the massecuite that crystallizer top discharge mouth overflows, and clean, obtain the wet sugar alcohol of bulk of moisture 5-8% with less water; The wet sugar alcohol of bulk is pulverized with beater grinder, loose wet sugar alcohol to the mobile drying machine of negative pressure with the gas delivery powder, warm air beating material with 75-85 ℃, upwards blow down at 150-200 millimeter water column pressure hot blast, material is suspended into the other end from inlet, is dried to moisture to enter the dryer cooling section less than 1% material; The material that enters cooling section is blown down to discharge port by 21 ℃ cold wind and is cooled to 30 ℃, can pack, and becomes finished product.
Adopt method of the present invention, owing to used magniferous pH regulator agent, thus stablize hydrogenation pH, make hydrogenation process be easy to control, obtain high purity maltose alcohol product; Next has used vertical continuous crystallisation jar, makes the maltose alcohol crystallization move continuously, has improved plant factor.
Embodiment
Embodiment 1:
Step 1, produce starch milk: after corn purifies by starchy material, the sulfurous acid solution that with content is 0.2-0.5% soaked 70 hours under 50-60 ℃ of condition, remove maize germ through crusher in crushing and eddy flow, after pin mill fiber separation is removed zein and slag crust, promptly make starch milk again.
Step 2, make maltose by starch milk: starch milk adds enzyme liquefaction: regulate starch concentration to 15-18 mother-in-law U.S., add Na
2CO
3After transferring between the pH to 5.5-5.8, add the α-Dian Fenmei of 0.1-0.5% calcium chloride, 0.04-0.06%; During liquefaction, 105--110 ℃ of steam ejection liquefaction temperature, 135--140 ℃ of second spraying liquefaction temperature; Control liquefaction back DE value is between 3-5, and the BX value is between 23-26.
Saccharification: the liquefier that is up to the standards is cooled to 60-65 ℃ by the cooling coil pipe, adjust pH is to 5.0-5.5, the βDian Fenmei, the Pullulanase of 0.12-0.2% and the trisaccharide maltose lytic enzyme of 0.15-0.25% that add 0.12-0.18% keep 58--62 ℃ of temperature, carry out saccharification; After the saccharification 24 hours, add the middle temperature amylase of 0.015-0.025%, continue saccharification to 48-60 hour, detect in the saccharification liquid maltose concentration and carry out the iodine examination,, add the high-temperature of 0.01-0.03% again if the iodine examination is defective, qualified until detecting, this moment, maltose purity was at DP
2More than 88%.Filtration obtains qualified Fructus Hordei Germinatus liquid glucose.
Step 3, maltose is made maltitol solution:
Decolouring, from handing over, concentrating: carry out decolorization filtering to filtering qualified Fructus Hordei Germinatus liquid glucose according to a conventional method, and, the refining Fructus Hordei Germinatus liquid glucose of handling be concentrated into BX75-76 by falling-film evaporator from handing over removal of impurities.
Hydrogenation: the maltose solution that high-purity maltose solution is added water move to concentration 40%, add an amount of magnesium powder regulator solution pH to 8.4, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 130 ℃ of control hydrogenation temperatures, carried out hydrogenation 100 minutes under hydrogen pressure 8.5MPa condition, making contents on dry basis is the maltitol solution of the sugar alcohol 1.2% of maltose alcohol 96%, sorbyl alcohol 2.8% and DP 〉=3.
Step 4, with the maltitol solution condensing crystal:
Secondary decolourization, from handing over, concentrating: according to a conventional method the maltitol solution that makes is carried out decolorization filtering, and from handing over removal of impurities, carry out essence through the nanofiltration membrane of 0.45 μ m again and filter, the refining Fructus Hordei Germinatus liquid glucose of handling is concentrated into maltose alcohol concentration 80% by falling-film evaporator.
Charging: earlier with high 12m, diameter 3.2m volume 113m
3Vertical crystallizer system be adjusted to 53 ℃, with the refining maltitol solution that makes from the crystallizer bottom with 3.5m
3The flow velocity of/h enters crystallizer;
Inoculation: start crystallizer during 4 layers of spiral coil cooling tube of liquid level to the in the crystallizer and stir, nine layers of spiral coil cooling tube moved back and forth with 80 centimetres of strokes, 2 minutes cycles, simultaneously with 10 kilograms/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours totally 200 kilograms as crystal seed.
Educate crystalline substance: crystallizer advance full after, stop charging, nine layers of spiral coil cooling tube are lowered the temperature in sequence, material was educated in crystallizer brilliant 40 hours, last upper strata greenhouse cooling to 25 ℃, lower floor's temperature of charge is 40 ℃.
Continuous crystallisation: the maltitol solution that will keep 53 ℃ is with 3.5m
3The flow velocity of/h continues charging from the crystallizer bottom, and the massecuite major part of advantages of good crystallization is overflowed from the crystallizer top, and small part is recycled to lower floor under stirring and own wt effect become new crystal seed, and crystallisation process is carried out continuously.
Separate: use the suspended centrifugal of separating factor 1500 to separate 5 minutes from the massecuite that crystallizer top discharge mouth overflows, and clean, obtain moisture 6.7% the wet sugar alcohol of bulk with less water.
Pulverize: the wet sugar alcohol of bulk that step 8 makes is pulverized with beater grinder, be beneficial to material and fully contact, improve the efficient of dryer and the productive rate of pulverized sugar finished product with warm air.
Drying: the powder with the preparation of gas delivery step 9 looses wet sugar alcohol to the mobile drying machine of negative pressure, warm air beating material with 80 ℃, upwards blow down at 150-200 millimeter water column pressure hot blast, material is suspended into the other end from inlet, dried to moisture less than 1% material since density diminish, the height that blows afloat increases, and 50 millimeters the baffle plate jumped over enters the dryer cooling section; The material that enters cooling section is blown down to discharge port by 21 ℃ cold wind and is cooled to 30 ℃, can pack.
Pack: be finished product after according to specification requirement the kiln malt sugar alcohol of preparation being packed.
Embodiment 2:
In the present embodiment, the time of soaking corn is 68 hours in the step 1; Hydrogenation stage in the step 3, in maltose solution, add an amount of magnesium powder regulator solution pH to 8.0, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 139 ℃ of control hydrogenation temperatures, carried out hydrogenation 85 minutes under hydrogen pressure 10.2MPa condition, making contents on dry basis is the maltitol solution of the sugar alcohol 8.3% of maltose alcohol 85.8%, sorbyl alcohol 5.9% and DP 〉=3; In step 4, secondary decolourization, from hand over, enriching stage, the refining Fructus Hordei Germinatus liquid glucose of handling is concentrated into maltose alcohol concentration 85%, charging stage by falling-film evaporator, vertical crystallizer system is adjusted to 55 ℃, refining maltitol solution from the crystallizer bottom with 3.5m
3The flow velocity of/h enters crystallizer, inoculation step, with 12 kilograms/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours totally 240 kilograms as crystal seed, educate the brilliant stage, material was educated in crystallizer brilliant 35 hours, the continuous crystallisation stage, the maltitol solution temperature that enters from the crystallizer bottom keeps 55 ℃, at separation phase, obtains moisture 6.5% the wet sugar alcohol of bulk, at drying stage, negative pressure flows in the drying machine with 85 ℃ warm air beating material; Other is identical with embodiment 1.
Embodiment 3: in the present embodiment, the time of soaking corn is 60 hours in the step 1; Hydrogenation stage in the step 3, in maltose solution, add an amount of magnesium oxide regulator solution pH to 8.2, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 125 ℃ of control hydrogenation temperatures, carried out hydrogenation 110 minutes under hydrogen pressure 9.0MPa condition, making contents on dry basis is the maltitol solution of the sugar alcohol 3.2% of maltose alcohol 94.3%, sorbyl alcohol 2.5% and DP 〉=3; In step 4, secondary decolourization, from hand over, enriching stage, the refining Fructus Hordei Germinatus liquid glucose of handling is concentrated into maltose alcohol concentration 75%, charging stage by falling-film evaporator, vertical crystallizer system is adjusted to 50 ℃, refining maltitol solution from the crystallizer bottom with 3.5m
3The flow velocity of/h enters crystallizer, inoculation step, with 15 kilograms/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours totally 300 kilograms as crystal seed, educate the brilliant stage, material was educated in crystallizer brilliant 60 hours, the continuous crystallisation stage, the maltitol solution temperature that enters from the crystallizer bottom keeps 50 ℃, at separation phase, obtains moisture 5% the wet sugar alcohol of bulk, at drying stage, negative pressure flows in the drying machine with 85 ℃ warm air beating material; Other is identical with embodiment 1.
Embodiment 4: in the present embodiment, the time of soaking corn is 80 hours in the step 1; Hydrogenation stage in the step 3, in maltose solution, add an amount of magnesium oxide regulator solution pH to 8.7, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 135 ℃ of control hydrogenation temperatures, carried out hydrogenation 110 minutes under hydrogen pressure 10.5MPa condition, making contents on dry basis is the maltitol solution of the sugar alcohol 3.7% of maltose alcohol 92.6%, sorbyl alcohol 3.7% and DP 〉=3; In step 4, secondary decolourization, from hand over, enriching stage, the refining Fructus Hordei Germinatus liquid glucose of handling is concentrated into maltose alcohol concentration 90%, charging stage by falling-film evaporator, vertical crystallizer system is adjusted to 58 ℃, refining maltitol solution from the crystallizer bottom with 3.5m
3The flow velocity of/h enters crystallizer, inoculation step, with 12 kilograms/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours totally 240 kilograms as crystal seed, educate the brilliant stage, material was educated in crystallizer brilliant 45 hours, the continuous crystallisation stage, the maltitol solution temperature that enters from the crystallizer bottom keeps 55 ℃, at separation phase, obtains moisture 7% the wet sugar alcohol of bulk, at drying stage, negative pressure flows in the drying machine with 85 ℃ warm air beating material; Other is identical with embodiment 1.
Embodiment 5: in the present embodiment, the time of soaking corn is 80 hours in the step 1; Hydrogenation stage in the step 3, in maltose solution, add an amount of magnesium oxide regulator solution pH to 8.5, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 135 ℃ of control hydrogenation temperatures, carried out hydrogenation 110 minutes under hydrogen pressure 10.5MPa condition, making contents on dry basis is the maltitol solution of the sugar alcohol 3.7% of maltose alcohol 92.6%, sorbyl alcohol 3.7% and DP 〉=3; In step 4, secondary decolourization, from hand over, enriching stage, the refining Fructus Hordei Germinatus liquid glucose of handling is concentrated into maltose alcohol concentration 80%, charging stage by falling-film evaporator, vertical crystallizer system is adjusted to 65 ℃, refining maltitol solution from the crystallizer bottom with 3.5m
3The flow velocity of/h enters crystallizer, inoculation step, with 13 kilograms/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours totally 260 kilograms as crystal seed, educate the brilliant stage, material was educated in crystallizer brilliant 50 hours, the continuous crystallisation stage, the maltitol solution temperature that enters from the crystallizer bottom keeps 55 ℃, at separation phase, obtains moisture 8% the wet sugar alcohol of bulk, at drying stage, negative pressure flows in the drying machine with 80 ℃ warm air beating material; Other is identical with embodiment 1.
Claims (6)
1. method for preparing maltose alcohol, comprise by starchy material produce starch milk, by starch milk make maltose, with maltose make maltitol solution, with the step of maltitol solution condensing crystal, it is characterized in that: maltose is being made in the step of maltitol solution, regulate the used pH regulator agent of pH and contain element magnesium (Mg), in the step with the maltose solution condensing crystal, used crystallizer is the vertical crystallizer of continuously-running.
2. the method for preparing maltose alcohol as claimed in claim 1 is characterized in that: described pH regulator agent is metal magnesium powder or the basic cpd that contains magnesium elements.
3. the method for preparing maltose alcohol as claimed in claim 1 is characterized in that: described vertical crystallizer is the vertical continuous crystallisation jar of maltose alcohol.
4. the method for preparing maltose alcohol as claimed in claim 1, it is characterized in that: starch milk is being made in the step of maltose, earlier starch milk is added enzyme liquefaction: regulate starch concentration to 15-18 mother-in-law U.S., add adjusting PH with base after between the 5.5-5.8, the α-Dian Fenmei that adds 0.1-0.5% calcium chloride, 0.04-0.06%, 105--110 ℃ of steam ejection liquefaction temperature, 135--140 ℃ of second spraying liquefaction temperature; Control liquefaction back DE value is between 3-5, and the BX value is between 23-26; Again with the liquefier saccharification: liquefier is cooled to 60-65 ℃ by the cooling coil pipe, adjust pH is to 5.0-5.5, the βDian Fenmei, the Pullulanase of 0.12-0.2% and the trisaccharide maltose lytic enzyme of 0.15-0.25% that add 0.12-0.18%, keep 58--62 ℃ of temperature, carry out saccharification, saccharification added the middle temperature amylase of 0.015-0.025% after 24 hours, continue saccharification to 48-60 hour, filter and obtain maltose purity at DP
2Fructus Hordei Germinatus liquid glucose more than 88%.
5. the method for preparing maltose alcohol as claimed in claim 4, it is characterized in that: maltose solution is transferred to concentration 40%, add and contain magnesium (Mg) pH regulator agent regulator solution pH to 8.0-8.7 in right amount, add an amount of hydrogenation catalyst nickel-aluminum-molybdenum catalyzer, 120-145 ℃ of control hydrogenation temperature, under hydrogen pressure 8.0-11MPa condition, carried out hydrogenation 60-110 minute, and made the maltitol solution of the sugar alcohol 1-9% (butt) that contains maltose alcohol 85-97% (butt), sorbyl alcohol 2.0-6.0% (butt) and DP 〉=3.
6. the method for preparing maltose alcohol as claimed in claim 5, it is characterized in that: in step the maltitol solution condensing crystal, to be concentrated into maltose alcohol concentration 75-90% by falling-film evaporator through decolorization filtering and from the Fructus Hordei Germinatus liquid glucose of handing over removal of impurities earlier, then with its from the crystallizer bottom with 3.2-4m
3The flow velocity of/h is sent in the vertical crystallizer, the temperature of vertical crystallizer is 50-65 ℃, starting crystallizer during 4 layers of spiral coil cooling tube of liquid level to the in the crystallizer stirs, nine layers of spiral coil cooling tube are with 80 centimetres of strokes, 2 minutes cycles moved back and forth, simultaneously with the 10-15 kilogram/hour speed at the uniform velocity add from the crystallizer top exsiccant crystal maltitol 20 hours altogether the 200-300 kilogram as crystal seed, after crystallizer advances to expire, stop charging, nine layers of spiral coil cooling tube are lowered the temperature in sequence, material was educated in crystallizer brilliant 30-60 hour, last upper strata greenhouse cooling to 25 ℃, lower floor's temperature of charge is 40 ℃; The maltitol solution that then will keep 50-58 ℃ is with 3.2-4m
3The flow velocity of/h continues charging from the crystallizer bottom, the massecuite major part of advantages of good crystallization is overflowed from the crystallizer top, use the suspended centrifugal of separating factor 1500 to separate 5 minutes from the massecuite that crystallizer top discharge mouth overflows, and clean, obtain the wet sugar alcohol of bulk of moisture 5-8% with less water; The wet sugar alcohol of bulk is pulverized with beater grinder, loose wet sugar alcohol to the mobile drying machine of negative pressure with the gas delivery powder, warm air beating material with 75-85 ℃, upwards blow down at 150-200 millimeter water column pressure hot blast, material is suspended into the other end from inlet, is dried to moisture to enter the dryer cooling section less than 1% material; The material that enters cooling section is blown down to discharge port by 21 ℃ cold wind and is cooled to 30 ℃, can pack, and becomes finished product.
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|---|---|---|---|
| CNA2006101600183A CN101210256A (en) | 2006-12-30 | 2006-12-30 | Method for preparing maltitol |
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| CNA2006101600183A CN101210256A (en) | 2006-12-30 | 2006-12-30 | Method for preparing maltitol |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101684504B (en) * | 2008-09-26 | 2013-10-30 | 保龄宝生物股份有限公司 | Preparation method of superhigh maltose syrup |
| CN106755212A (en) * | 2016-12-08 | 2017-05-31 | 安徽睿知信信息科技有限公司 | A kind of preparation method of maltitol |
| CN109053368A (en) * | 2018-09-21 | 2018-12-21 | 安阳市豫鑫木糖醇科技有限公司 | A method of in xylose solution plus magnesium powder adjusts pH value |
| CN109234338A (en) * | 2018-09-08 | 2019-01-18 | 肇庆焕发生物科技有限公司 | A kind of production method of high purity crystal maltitol malt syrup |
| CN109336939A (en) * | 2018-12-01 | 2019-02-15 | 浙江华康药业股份有限公司 | A kind of hydrogenation process of sugar alcohol |
| CN112679557A (en) * | 2020-12-30 | 2021-04-20 | 回头客食品集团股份有限公司 | Production process of maltitol for food |
| CN112707942A (en) * | 2020-12-29 | 2021-04-27 | 山东福田药业有限公司 | Method for reducing sorbitol content in liquid maltitol |
| CN114369689A (en) * | 2021-12-31 | 2022-04-19 | 山东福田药业有限公司 | Crystalline maltose and preparation method thereof |
-
2006
- 2006-12-30 CN CNA2006101600183A patent/CN101210256A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101684504B (en) * | 2008-09-26 | 2013-10-30 | 保龄宝生物股份有限公司 | Preparation method of superhigh maltose syrup |
| CN106755212A (en) * | 2016-12-08 | 2017-05-31 | 安徽睿知信信息科技有限公司 | A kind of preparation method of maltitol |
| CN109234338A (en) * | 2018-09-08 | 2019-01-18 | 肇庆焕发生物科技有限公司 | A kind of production method of high purity crystal maltitol malt syrup |
| CN109053368A (en) * | 2018-09-21 | 2018-12-21 | 安阳市豫鑫木糖醇科技有限公司 | A method of in xylose solution plus magnesium powder adjusts pH value |
| CN109336939A (en) * | 2018-12-01 | 2019-02-15 | 浙江华康药业股份有限公司 | A kind of hydrogenation process of sugar alcohol |
| CN112707942A (en) * | 2020-12-29 | 2021-04-27 | 山东福田药业有限公司 | Method for reducing sorbitol content in liquid maltitol |
| CN112679557A (en) * | 2020-12-30 | 2021-04-20 | 回头客食品集团股份有限公司 | Production process of maltitol for food |
| CN114369689A (en) * | 2021-12-31 | 2022-04-19 | 山东福田药业有限公司 | Crystalline maltose and preparation method thereof |
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Application publication date: 20080702 |