CN1049666A - Extract the novel process of stevioside with ordinary resin - Google Patents
Extract the novel process of stevioside with ordinary resin Download PDFInfo
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- CN1049666A CN1049666A CN 90103875 CN90103875A CN1049666A CN 1049666 A CN1049666 A CN 1049666A CN 90103875 CN90103875 CN 90103875 CN 90103875 A CN90103875 A CN 90103875A CN 1049666 A CN1049666 A CN 1049666A
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- stevioside
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- ordinary resin
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- desalination
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Abstract
The present invention is a kind of novel process with ordinary resin extraction stevioside, the real food chemical field that belongs to, and existing technology with resin extraction stevioside comprises operations such as cured leaf immersion, purification, filtration, absorption, desalination, decolouring, thickening filtration drying.The present invention is a kind of novel process of extracting stevioside with ordinary resin, it is characterized in that cured leaf screens the sand clod before soaking, removes surperficial ash content, a certain proportion of prescription is adopted in rinsing, flocculation, particularly desalination, the decolouring two operations soft, therefore it is pure white to adopt ordinary resin to obtain color and luster equally, be of high quality the product that cost is low.
Description
The true food chemical field of the present invention.
The technical process of producing stevioside at present both at home and abroad mainly is the cured leaf immersion and heats 65 ℃, use calcium oxide (or Tai-Ace S 150 or ferrous sulfate) to force to purify again, Plate Filtration, absorption, desalination, the decolouring of employing characteristic resin then, concentrate, once more Plate Filtration, spraying drying, go out finished product.The content of its glucoside of glucoside that this kind technical process is produced has only below 85%, ash content but accounts for 0.2%, and need with the characteristic strongly basic anion decolorizing resins such as 280 types that cost an arm and a leg, market is in short supply, therefore exist quality product not high, required auxiliary material is difficult to buy problems such as disposable input cost height.
Purpose of the present invention, before soaking, cured leaf on the basis of ordinary process flow process takes to filter out the sand clod, remove a series of physical cleaning measures such as the cold soft water immersion of surface dirt, and adopt the inexpensive common strongly basic anion decolorizing resin of easily purchasing, by concentrate for twice, special process such as vacuum filtration, produce and contain the glucoside amount more than 98%, ash content is at 0.05-0.06%, and sugariness is at the pure white stevioside of the high color and luster of the quality standard more than 200 times.
The present invention uses air float separator (Fig. 2) to carry out dedusting impurity elimination (a) with the novel process that ordinary resin extracts stevioside in the leaching stage (A) before, rinsing then, precipitation, recovery (b).Carry out cold soft water immersion earlier and forced to stir (A1) in the leaching stage (A), and under 75 ℃ of temperature, force to purify (A with a certain proportion of Tai-Ace S 150 and calcium oxide
1), carry out Plate Filtration (B), absorption (C), for the first time concentrated (D), desalination (E), three grades of decolourings (F) then, carry out concentrating (G), vacuum filtration (H), spraying drying (L) second time, going out finished product (P), again as Fig. 1.
The present invention extracts stevioside with ordinary resin novel process the leaching stage (A) before, select for use air float separator (Fig. 2) to carry out dedusting impurity elimination (a), and rinsing, precipitation, recovery (b) have been removed the impurity thing like this, have been avoided the impurity thing to enter next operation.Adopt simultaneously and reclaim rinsing post precipitation washing lotion, prevented that the part glucoside runs off along with rinsing.Used in soaking, forcing to stir is cold soft water, prevented from so at high temperature the non-effective ingredient of dissolved to sneak in the liquid glucose, when forcing to purify (A2), Tai-Ace S 150 by a certain percentage and calcium oxide mix use, therefore the amount of sulfur acid aluminium and calcium oxide is than the technology minimizing 30% of other single use Tai-Ace S 150 (or ferrous sulfate, or calcium oxide) in the liquid glucose after purifying.Carried out concentrating for the first time (G) before in desalination (E), so separated the alcoholic content in the liquid glucose, the effect of desalination (E) has greatly been improved, its electric conductivity drops to 100 μ S by 300 μ S of existing technology.In decolouring (F), there is not alcohol in because of liquid glucose, and owing to passed through dedusting impurity elimination (a), and rinsing, precipitation, recovery operations such as (b), removed in the liquid glucose 97% impurity (except that chlorophyll), and existing technology can only be removed 83.4% impurity (except that chlorophyll), therefore can use the inexpensive common strong alkali negatively charged ion decolorizing resin of easily purchasing, its decolorizing effect is very high, and the ash content of product 0.2% drops to 0.05-0.06% by what existing technology was produced.Concentrate the back for the second time and adopt vacuum filtration (H) method, thereby leach the micro-resin of discharging, improved the purity of product with liquid glucose.
Illustrate and at first the sweet Stevia cured leaf is dropped into one of most preferred embodiment of the present invention-extract the novel process of stevioside winnowing machine (Fig. 2) and carry out dedusting impurity elimination (a) with ordinary resin.Winnowing machine (Fig. 2) mainly is made up of back material baffle (6), 120 purpose separated material guiding principles (7) and discharge door (8), discharge door (9), discharge door (10) and slag notch (11), the ash output hole (12) of the preceding material baffle (5) of opening for feed (1), 4.0kW gas blower (2), large dial wheel (3), small driving wheel (4), uniform ∮ 5mm aperture, uniform ∮ 3mm aperture.Through selection by winnowing, most stevia rebaudianum cured leaf is emitted from discharge door (8), and diameter is discharged from slag notch (11) greater than 5mm and heavier sand clod simultaneously.Diameter is less than 5mm, emit from discharge door (9) by material baffle (5) greater than the stevia rebaudianum cured leaf of 3mm.Diameter is emitted from discharge door (10) by material baffle (6) less than the stevia rebaudianum cured leaf of 3mm, and dust is discharged from ash output hole (12) by separated material guiding principle (7).Stevia rebaudianum cured leaf through dedusting impurity elimination (a) is put into rinsing bath, rinsing bath is of a size of 5000 * 1200 * 1000mm, is provided with 12 groups of shift forks that are contained on the same axle in it.Folium Chrysanthemi stirs rinsing fully in rinsing bath, it is in 1000 liters the settling tank, to carry out 48 hours natural sedimentation that the water after the rinsing is input to volume, discharges throw out, the water behind the reclaiming clean (b).Soak with normal temperature soft water then, force to stir (A1), stir needed 4 times repeatedly at every turn in 2 hours.After discharging waste residue the treating pond of liquid glucose input 2500 * 1500 * 1500mm is forced to purify (A2), its method is by liquid glucose: Tai-Ace S 150: the mixed of unslaked lime=1: 0.0035: 0.01, under 75 ℃ of temperature, dissolve, flocculate, left standstill then 4 hours, its impurity is fully precipitated.Liquid glucose after the pressure purification (A2) is input to xmys450 template frame filter carries out Plate Filtration (B).Liquid glucose behind the Plate Filtration (B) (transparency of liquid glucose reaches 98%, does not have throw out after the boiling) is cooled to normal temperature, and is input in the adsorption column and adsorbs (C).Adsorption column is of a size of ∮ 400 * 3000mm, and the volume of the AB-8 macroporous adsorbent resin in the adsorption column of packing into equals adsorption column volumetrical 1/3rd.Liquid glucose flows out by the AB-8 macroporous adsorbent resin with the speed of 11 liters of per minutes.Absorption (C) back cleans resin surface with soft water, positive and negative several, be washed till out saliva as clear as crystal till.From resin column adding 70 degree alcohol suitable for reading water is ejected then, pleasantly sweet or stop to emit liquid when alcoholic content is arranged from export effusive liquid, soaked 30 minutes, and carried out wash-out with alcohol with the flow velocity of 4 liters of per minutes again, ethanol concn to be exported is lower than and stops wash-out when inlet ethanol concn 5 is spent.The mixed solution of liquid glucose and alcohol is input to 1000L type concentrating under reduced pressure jar, at negative pressure 700mm/Hg, carry out under 75 ℃ of states of temperature concentrating (D) first time, liquid glucose is separated with alcohol, liquid glucose is passed to shell and tube cooler is cooled to 18 ℃, and the steaming that adds 3 times of liquid glucose amounts stays water to dilute.Liquid glucose after the dilution is input in B1 ∮ 300 * 2000mm type desalting column and carries out desalination (E), and 732 type resin cation (R.C.) volumes in the salt plug of packing into equal desalting column volumetrical 3/4ths.The flow velocity that the liquid glucose per minute is 11 liters flows out by 732 type resin cation (R.C.)s, import successively in three identical ∮ 300 * 3000mm resin anion(R.A) decolorizing column through the liquid glucose of desalination (E) and to carry out three grades of decolourings, the volume of the strong alkali resin anion(R.A) of NK polystyrene in the negatively charged ion decolorizing column of packing into equals negatively charged ion decolorizing column volumetrical 3/4ths, and liquid glucose flows out with the flow velocity of 6 liters of per minutes.Carry out concentrating (G) second time in the liquid glucose input 1000L concentrating under reduced pressure jar after decolouring (F), at negative pressure 700mm/Hg, under 90 ℃ of conditions of temperature, the water content that liquid glucose is concentrated in the liquid glucose accounts for 30%.Liquid glucose behind the general for the second time concentrated (G) is input to and carries out vacuum filtration (H) in the vacuum filtration jar (Fig. 3).Vacuum filtration jar (Fig. 3) is ∮ 600 * 500mm stainless steel Cylinder, the top center place is provided with square-shaped hopper (3-1), square-shaped hopper (3-1) is connected with tank body (3-2) place of opening the door, top, its joining place lays through disinfectant 200 order industrial filter cloths (3-4) and two-layer qualitative filter paper at a slow speed (3-5), tank body (3-2) top place is provided with the vacuum pumping hole (3-3) of ∮ 25mm, the tank base center is provided with the leakage fluid dram (3-6) of ∮ 25mm, liquid glucose adds square-shaped hopper (3-1) back and by vacuum pumping hole (3-3) air pressure in the tank body (3-2) is reduced to 700mm/Hg, liquid glucose considers cloth (3-4) by industry and two-layer qualitative filter paper at a slow speed (5) enters in the tank body (3-2), emit by leakage fluid dram (3-6) at last, and reclaim micro-resin.Liquid glucose behind the vacuum filtration (H) carries out spraying drying (L) again, goes out finished product (P).
Description of drawings
Fig. 1, technological process of production figure
A, dedusting impurity elimination A
1, soak, force to stir
B, rinsing, precipitation reclaim A
2, force to purify
A, leaching stage B, Plate Filtration
C, absorption F
3, three grades of decolourings
D, for the first time concentrated G, concentrated for the second time
E, desalination H, vacuum filtration
F, decolouring L, spraying drying
F
1, one-level decolouring P, finished product
F
2, two-level decolour
Fig. 2 winnowing machine
2-1, opening for feed 2-10, discharge door
2-2, gas blower 2-12, ash output hole
2-3, large dial wheel
2-5, preceding material baffle Fig. 3, vacuum filtration jar
2-7, separated material guiding principle 3-1, square-shaped hopper
2-9, discharge port 3-2, tank body
2-11, cleanout door 3-3, vacuum pumping hole
2-4, small driving wheel 3-4, industrial filter cloth
2-6, back material baffle 3-5, two-layer qualitative filter paper at a slow speed
2-8, discharge door 3-6, leakage fluid dram
Claims (6)
1, the present invention extracts the novel process of stevioside with ordinary resin, belong to the food chemical field, comprise that cured leaf soaks (A1), forces to purify (A2), Plate Filtration (B), absorption (C), desalination (E), decolouring (F), concentrate, Plate Filtration and spraying drying flow processs such as (L).The present invention is characterized in that cured leaf soaks (A1) and carries out dedusting impurity elimination (a), rinsing, precipitation, recovery (b) before, adopts cold soft water when cured leaf soaks (A1).Carry out concentrating the first time (P) before in desalination (E), in decolouring (E) technology, adopt the strong alkali resin anion(R.A) of common NK polystyrene, concentrate (P) for the second time and adopt vacuum filtration (H) method.
2, as the described novel process with ordinary resin extraction stevioside of claim (1), its feature is that also its winnowing machine of winnowing machine (Fig. 2) (Fig. 2) that dedusting impurity elimination (a) is adopted is provided with large dial wheel (3), small driving wheel (4), preceding material baffle (5), back material baffle (6) and separated material guiding principle (7).The aperture of the preceding uniform ∮ 5mm of material baffle (5), the uniform ∮ 3mm of back material baffle (6) aperture, separated material guiding principle (7) is 120 orders.
3, as the described novel process with ordinary resin extraction stevioside of claim (1), its feature also is to carry out concentrating the first time (D) before in desalination (E) under 75 ℃ of temperature, negative pressure 700mm/Hg.
4, as the described novel process of extracting stevioside with ordinary resin of claim (1), when also being decolouring (F), its feature adopts the strong alkali resin anion(R.A) of NK vinylbenzene, strong its amount of alkali resin anion(R.A) of NK vinylbenzene in the decolorizing column of packing into equals decolorizing column volumetrical 1/3, and liquid glucose is with the velocity flow mistake of 4 liters of per minutes.
5, as the described novel process with ordinary resin extraction stevioside of claim (1), its feature also is to concentrate for the second time (G) back and adopts vacuum filtration (H) method, and its negative pressure is 700mm/Hg.
6, such as claim (1), (5) described vacuum filtration (H) employing through disinfectant 200 order industrial filter cloths (3-4) and two-layer qualitative filter paper at a slow speed (3-5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90103875 CN1024348C (en) | 1990-05-23 | 1990-05-23 | Process for extracting stevioside from ordinary resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90103875 CN1024348C (en) | 1990-05-23 | 1990-05-23 | Process for extracting stevioside from ordinary resin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1049666A true CN1049666A (en) | 1991-03-06 |
| CN1024348C CN1024348C (en) | 1994-04-27 |
Family
ID=4878293
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 90103875 Expired - Fee Related CN1024348C (en) | 1990-05-23 | 1990-05-23 | Process for extracting stevioside from ordinary resin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1024348C (en) |
Cited By (32)
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| CN1081648C (en) * | 1997-09-10 | 2002-03-27 | 中国石化齐鲁石油化工公司 | Method for producing heat-resistant copolymerized resin |
| CN101503435B (en) * | 2009-03-26 | 2011-07-06 | 李善汪 | Method for purifying stevioside by secondary ion exchange |
| CN102161684A (en) * | 2011-03-07 | 2011-08-24 | 天津港源生物制品集团有限公司 | Method for extracting stevia rebaudiana sugar by using mixed flocculant |
| US8257948B1 (en) | 2011-02-17 | 2012-09-04 | Purecircle Usa | Method of preparing alpha-glucosyl Stevia composition |
| US8299224B2 (en) | 2009-10-15 | 2012-10-30 | Purecircle Sdn Bhd | High-purity Rebaudioside D |
| US8318459B2 (en) | 2011-02-17 | 2012-11-27 | Purecircle Usa | Glucosyl stevia composition |
| US8334006B2 (en) | 2005-10-11 | 2012-12-18 | Purecircle Sdn Bhd | Process for manufacturing a sweetener and use thereof |
| US8337927B2 (en) | 2005-10-11 | 2012-12-25 | Purecircle Sdn Bhd | Process for manufacturing a sweetener and use thereof |
| US8790730B2 (en) | 2005-10-11 | 2014-07-29 | Purecircle Usa | Process for manufacturing a sweetener and use thereof |
| US9752174B2 (en) | 2013-05-28 | 2017-09-05 | Purecircle Sdn Bhd | High-purity steviol glycosides |
| US9771434B2 (en) | 2011-06-23 | 2017-09-26 | Purecircle Sdn Bhd | Products from stevia rebaudiana |
| CN107474086A (en) * | 2016-06-07 | 2017-12-15 | 上海达盛食品有限公司 | The technique for extracting stevioside |
| US9877501B2 (en) | 2011-06-03 | 2018-01-30 | Purecircle Sdn Bhd | Stevia composition |
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-
1990
- 1990-05-23 CN CN 90103875 patent/CN1024348C/en not_active Expired - Fee Related
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| CN101503435B (en) * | 2009-03-26 | 2011-07-06 | 李善汪 | Method for purifying stevioside by secondary ion exchange |
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Also Published As
| Publication number | Publication date |
|---|---|
| CN1024348C (en) | 1994-04-27 |
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