CN1233639C - Extraction of soya isoflavone from waste soybean serum - Google Patents
Extraction of soya isoflavone from waste soybean serum Download PDFInfo
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Abstract
The present invention relates to a method for extracting soybean isoflavone from the wastewater of soybean whey, which relates to the technical field of soybean deep processing and wastewater resource recovery. The method comprises: the pretreatment of soybean processing wastewater, such as pH value regulation, centrifugation, prefiltration, microfiltration, etc. is carried out; the crude extract liquid of soybean isoflavone is extracted by primary adsorption; soybean isoflavone with high purify is extracted by secondary adsorption. Experiments prove that the quality and the net content of the obtained product of soybean isoflavone achieve a world advanced level. The present invention has an imple technology, and required devices are all common devices of soybean deep processing industry and water treatment industry; low pole macroporous adsorptive resin is also a commercial product; popularization is easy, and the market prospect is broad; the method can further treat the pollution of soybean whey wastewater, and has obvious economic, environmental and social benefits.
Description
Technical field
The present invention relates to soybean deep processing and waste water reclaiming technical field, particularly from soya whey wastewater, extract the method for soybean isoflavones.
Background technology
The production of present domestic soybean protein isolate mainly is to adopt traditional alkali extraction and acid precipitation technology, and 1 ton of soybean protein isolate of the every production of this technology discharges 40～70m approximately
3Soya whey wastewater, its COD
CrGeneral range be 15000～30000mg/L.It is the anaerobic-aerobic biological treatment that prior art adopts more to the processing of soya whey wastewater, and this traditional technology generally can be with the COD in the soya whey wastewater
CrRemove 80～90%.But this biological treatment treatment effect instability usually is subjected to the restriction of multiple objective factors such as waste water quality, seasonal variation, and investment cost of equipment is higher simultaneously, has also caused the waste of soybean biological active substance in the waste water.
At this problem, the applicant has applied for Chinese invention patent, application number is " utilizing membrane sepn to handle the method for soybean processing waste water " of 01141943.1, and it provides a kind of technology of utilizing membrane separation technique to extract soybean whey protein and soybean oligosaccharide from soya whey wastewater.But this technology does not relate to the technology of extracting soybean isoflavones from soya whey wastewater, and the domestic report of yet not seeing as yet relevant for extraction soybean isoflavones from soya whey wastewater.
Summary of the invention
At above-mentioned problems of the prior art and deficiency, task of the present invention provides a kind of method of extracting soybean isoflavones from soya whey wastewater, it can further realize the recycling treatment of soya whey wastewater, reduces its pollution to environment, increases economic efficiency.
Technical scheme of the present invention realizes with following two kinds of processing methodes:
The step of method one,
1. pre-treatment:
A) with the soya whey wastewater input flocculation jar of soybean protein isolate alkali extraction and acid precipitation technology discharging, flocculate centrifugal by regulating the pH value and adding ionogen; B) will flocculate centrifugate by deep bed filter and micro-strainer filtration, and obtain micro-filtration and see through liquid A1; C) micro-filtration is seen through liquid A1 and concentrate, obtain ultrafiltration and see through liquid B1 and ultrafiltration and concentration liquid C1 by ultra-filtration equipment;
2. one-level adsorbing and extracting soybean isoflavones crude extract:
A) ultrafiltration is seen through liquid B1 under the flow velocity of 1～3BV/h by the low-pole macroporous adsorbent resin, obtain effluent liquid D1 and by the material E1 of absorption with macroporous adsorbent resin; B) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 1～3BV/h, obtains pure water leacheate F1, the reuse after reclaiming ethanol of ethanol leacheate; C) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material E1 wash-out on the macroporous resin under the flow velocity of 1～3BV/h with volume, obtain elutriant G1, be the soybean isoflavones crude extract;
3. secondary absorption is extracted high-purity soybean isoflavone:
A) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant G1 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution H1; B) in concentrated solution H1, add the pure water that is equivalent to 2～4 times of its volumes, obtain secondary absorption stock liquid I1; C) with secondary absorption stock liquid I1 under the flow velocity of 1～3BV/h once more by the low-pole macroporous adsorbent resin, obtain effluent liquid J1 and by the material K1 of absorption with macroporous adsorbent resin; D) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 1～3BV/h; E) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material K1 wash-out on the macroporous resin under the flow velocity of 1～3BV/h with volume, obtain elutriant M1; F) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant M1 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution N1; G) concentrated solution N1 is sterilized, adds pure water and spraying drying, obtain soybean isoflavones product P 1, BV is the resin bed volume.
Above-mentioned steps operating process 3. a) and f) in the ethanol content of the concentrated solution that obtains less than 5%, reduction in bulk is original 1/6～1/4.
The step of method two:
1. pre-treatment:
A) with the soya whey wastewater input flocculation jar of soybean protein isolate alkali extraction and acid precipitation technology discharging, flocculate centrifugal by regulating the pH value and adding ionogen; B) will flocculate centrifugate by deep bed filter and micro-strainer filtration, concentrate by ultra-filtration equipment again, and obtain ultrafiltration and see through liquid A2 and ultrafiltration and concentration liquid B2; C) ultrafiltration is seen through liquid A2 and concentrate, obtain nanofiltration and see through liquid C2 and nanofiltration concentrated solution D2 by nanofiltration device;
2. one-level adsorbing and extracting soybean isoflavones crude extract:
A) in nanofiltration concentrated solution D2, add the pure water that is equivalent to 0.5～3 times of its volume, obtain one-level absorption stock liquid D2-S; B) one-level is adsorbed stock liquid D2-S under the flow velocity of 0.5～1.5BV/h by the low-pole macroporous adsorbent resin, obtain effluent liquid F2 and by the material E2 of absorption with macroporous adsorbent resin; C) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 0.5～1.5BV/h, obtain pure water leacheate F2-N and ethanol leacheate, wherein pure water leacheate F2-N and effluent liquid F2 one are used from the recovery soybean oligosaccharide, the reuse after reclaiming ethanol of ethanol leacheate; D) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material E2 wash-out on the macroporous resin under the flow velocity of 0.5～1.5BV/h with volume, obtain elutriant G2, be the soybean isoflavones crude extract;
3. secondary absorption is extracted high-purity soybean isoflavone:
A) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant G2 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution H2; B) in concentrated solution H2, add the pure water that is equivalent to 2～4 times of its volumes, obtain secondary absorption stock liquid I2; C) with secondary absorption stock liquid I2 under the flow velocity of 0.5～1.5BV/h once more by the low-pole macroporous adsorbent resin, obtain effluent liquid J2 and by the material K2 of absorption with macroporous adsorbent resin; D) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 0.5～1.5BV/h; E) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material K2 wash-out on the macroporous resin under the flow velocity of 0.5～1.5BV/h with volume, obtain elutriant M2; F) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant M2 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution N2; G) concentrated solution N2 is sterilized, adds pure water and spraying drying, obtain soybean isoflavones product P 2, BV is the resin bed volume.
Above-mentioned steps operating process 3. a) and f) in the ethanol content of the concentrated solution that obtains less than 5%, reduction in bulk is original 1/6～1/4.
Adopt the inventive method, can utilize soya whey wastewater to extract soybean isoflavones.Experiment showed, that the soybean isoflavones product quality and the net content that obtain have all reached advanced international standard.Technology of the present invention is simple, and required equipment is the common unit of soybean deep processing industry and water treatment field, and used low-pole macroporous adsorbent resin also is the commercially available prod, is highly susceptible to promoting, and has vast market prospect.The present invention can further administer the pollution of soya whey wastewater, has remarkable economic efficiency, environmental benefit and social benefit.
Description of drawings
Fig. 1 is the workflow diagram of one embodiment of the present invention (method one);
Fig. 2 is the workflow diagram of another embodiment of the present invention (method two).
Embodiment
The present invention is further illustrated below in conjunction with accompanying drawing and concrete embodiment.
Embodiment one, referring to Fig. 1:
Step 1): alkali extraction and acid precipitation technology obtains soya whey wastewater
1. accurately take by weighing defatted soybean meal 370 grams, put into 5000 ml beakers that 4810 milliliters, 50 ℃ deionized waters are housed, be stirred into feed liquid;
2. regulate material liquid pH value to 8.8 with NaOH solution, under 50 ℃, 250rpm, stirred alkaline solution 50 minutes;
3. regulate material liquid pH value to 4.5 with HCl solution, under 40 ℃, 250rpm, stirred acid solution 20 minutes;
4. with feed liquid under 3000rpm centrifugal 5 minutes, obtain 3500 milliliters of soya whey wastewaters;
5. with 1.-4. repetitive operation 3 times of above-mentioned steps, obtain 10.5 liters of soya whey wastewaters altogether, wherein isoflavone content is 110mg/l.
Step 2): pre-treatment
1. with in the soya whey wastewater input flocculation jar, flocculate centrifugal by regulating the pH value and adding ionogen;
2. the centrifugate of will flocculating is filtered by deep bed filter and micro-strainer, obtains micro-filtration and sees through liquid A1;
3. micro-filtration is seen through liquid A1 and concentrate, obtain ultrafiltration and concentration liquid C1 and 8.95 liters of ultrafiltration through liquid B1 by ultra-filtration equipment.
Step 3): one-level adsorbing and extracting soybean isoflavones crude extract
1. under the room temperature ultrafiltration seen through liquid B1 under the flow velocity of 1.25BV/h by the low-pole macroporous adsorbent resin, obtain effluent liquid D1 and by the material E1 of absorption with macroporous adsorbent resin;
2. priority is carried out drip washing to macroporous adsorbent resin with pure water and 8% ethanol that volume is 2BV under the flow velocity of 1.25BV/h, obtains pure water leacheate F1, and the ethanol leacheate can be back to production after reclaiming ethanol;
3. be that 80% ethanol of 2BV will be adsorbed on the material E1 wash-out on the macroporous resin under the flow velocity of 1.25BV/h with volume, obtain 1.1 liters of elutriant G1, be the soybean isoflavones crude extract.
Step 4): secondary absorption is extracted high-purity soybean isoflavone
1. be that 60 ℃, operation negative pressure are under the 0.085MPa elutriant G1 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain 210 milliliters of concentrated solution H1;
2. in concentrated solution H1, add 590 ml pure waters, obtain 800 milliliters of secondary absorption stock liquid I1;
3. under the room temperature, with secondary absorption stock liquid I1 under the flow velocity of 1.25BV/h once more by the low-pole macroporous adsorbent resin, obtain effluent liquid J1 and by the material K1 of absorption with macroporous adsorbent resin;
4. priority is carried out drip washing to macroporous adsorbent resin with pure water and 8% ethanol that volume is 2BV under the flow velocity of 1.25BV/h;
5. be that 80% ethanol of 2BV will be adsorbed on the material K1 wash-out on the macroporous resin under the flow velocity of 1.25BV/h with volume, obtain 150 milliliters of elutriant M1;
6. be that 60 ℃, operation negative pressure are under the 0.085MPa elutriant M1 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain 30 milliliters of concentrated solution N1.
Step 5): obtain the soybean isoflavones product
Concentrated solution N1 is carried out high-temperature short-time sterilization, adds an amount of pure water and spraying drying, obtain 2.3 gram soybean isoflavones product P 1.
Wherein the content of soybean isoflavones is 42.67% in the product P 1, Soyasaponin content is 21.78%, soybean protein content is 20.99%, soybean oligosaccharide content is to include vegetable fibre, inorganic salt, phytic acid etc. in 11.88%, remaining 2.67% the composition.The rate of recovery of soybean isoflavones is 50%～55% in the whole technology, wherein the rate of recovery of soybean isoflavones is about 80% in the resin absorption process, but the soybean isoflavones that is lost in ultra-filtration process can enter in the soybean whey protein product, and the soybean isoflavones that is lost in the resin absorption process can enter in the soybean oligosaccharide product, and promptly soybean isoflavones has obtained effective utilization basically fully.
Embodiment two, referring to Fig. 2:
Step 1): alkali extraction and acid precipitation technology obtains soya whey wastewater
With the method for embodiment one, use bigger Glass Containers instead, repetitive operation repeatedly obtains 50 liters of soya whey wastewaters altogether.
Step 2): pre-treatment
1. with in the soya whey wastewater input flocculation jar, flocculate centrifugal by regulating the pH value and adding ionogen;
2. the centrifugate of flocculating is filtered by deep bed filter and micro-strainer, concentrates by ultra-filtration equipment again, obtains ultrafiltration and concentration liquid A2 and ultrafiltration and sees through liquid B2;
3. ultrafiltration is seen through liquid A2 and concentrate, obtain nanofiltration and see through liquid C2 and 6.01 liters of nanofiltration concentrated solution D2 by nanofiltration device.
Step 3): one-level adsorbing and extracting soybean isoflavones crude extract
1. the pure water that adds 5.09 liters in nanofiltration concentrated solution D2 obtains 12 liters of one-level absorption stock liquid D2-S;
2. under the room temperature one-level adsorbed stock liquid D2-S under the flow velocity of 0.75BV/h by the low-pole macroporous adsorbent resin, obtain effluent liquid F2 and by the material E2 of absorption with macroporous adsorbent resin;
3. priority is carried out drip washing to macroporous adsorbent resin with pure water and 8% ethanol that volume is 2BV under the flow velocity of 0.75BV/h, obtains pure water leacheate F2-N, and the ethanol leacheate can be back to production after reclaiming ethanol;
4. be that 80% ethanol of 2BV will be adsorbed on the material E2 wash-out on the macroporous resin under the flow velocity of 0.75BV/h with volume, obtain 1.7 liters of elutriant G2, be the soybean isoflavones crude extract.
Step 4): secondary absorption is extracted high-purity soybean isoflavone
1. be that 60 ℃, operation negative pressure are under the 0.085MPa elutriant G2 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain 330 milliliters of concentrated solution H2;
2. in concentrated solution H2, add 1000 ml pure waters, obtain 1.33 liters of secondary absorption stock liquid I2;
3. under the room temperature, with secondary absorption stock liquid I2 under the flow velocity of 0.75BV/h once more by the low-pole macroporous adsorbent resin, obtain effluent liquid J2 and by the material K2 of absorption with macroporous adsorbent resin:
4. priority is carried out drip washing to macroporous adsorbent resin with pure water and 8% ethanol that volume is 2BV under the flow velocity of 0.75BV/h;
5. be that 80% ethanol of 2BV will be adsorbed on the material K2 wash-out on the macroporous resin under the flow velocity of 0.75BV/h with volume, obtain 250 milliliters of elutriant M2;
6. be that 60 ℃, operation negative pressure are under the 0.085MPa elutriant M2 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain 50 milliliters of concentrated solution N2.
Step 5): obtain the soybean isoflavones product
Concentrated solution N2 is carried out high-temperature short-time sterilization, adds an amount of pure water and spraying drying, obtain 7.6 gram soybean isoflavones product P 2.
Wherein the content of soybean isoflavones is 47.65% in the product P 2, Soyasaponin content is 22.59%, soybean protein content is 12.73%, soybean oligosaccharide content is to include vegetable fibre, inorganic salt, phytic acid etc. in 15.23%, remaining 1.80% the composition.The rate of recovery of soybean isoflavones is about 66% in the whole technology, and the purity of soybean isoflavones product P 2 has also obtained raising to a certain degree than product P 1, and the soybean isoflavones that is lost will mainly enter in soybean whey protein and the soybean oligosaccharide product.Ethanol content is less than 5% in the concentrated solution that obtains in the operating process of described step 4), and reduction in bulk is original 1/6～1/4.
Adopt the present invention, ultrafiltration and concentration liquid C1 that obtains from above-mentioned method one and the ultrafiltration and concentration liquid B2 that obtains from method two can be used for extracting soybean whey protein; The one-level absorption effluent liquid D1 and the pure water leacheate F1 that will obtain from method one merge, and the one-level absorption effluent liquid F2 and the pure water leacheate F2-N that perhaps will obtain from method two merge, and can be used for extracting soybean oligosaccharide.
Claims (4)
1. a method of extracting soybean isoflavones from soya whey wastewater is characterized in that comprising the steps,
1. pre-treatment:
A) with the soya whey wastewater input flocculation jar of soybean protein isolate alkali extraction and acid precipitation technology discharging, flocculate centrifugal by regulating the pH value and adding ionogen; B) will flocculate centrifugate by deep bed filter and micro-strainer filtration, and obtain micro-filtration and see through liquid A1; C) micro-filtration is seen through liquid A1 and concentrate, obtain ultrafiltration and see through liquid B1 and ultrafiltration and concentration liquid C1 by ultra-filtration equipment;
2. one-level adsorbing and extracting soybean isoflavones crude extract:
A) ultrafiltration is seen through liquid B1 under the flow velocity of 1～3BV/h by the low-pole macroporous adsorbent resin, obtain effluent liquid D1 and by the material E1 of absorption with macroporous adsorbent resin; B) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 1～3BV/h, obtains pure water leacheate F1, the reuse after reclaiming ethanol of ethanol leacheate; C) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material E1 wash-out on the macroporous resin under the flow velocity of 1～3BV/h with volume, obtain elutriant G1, be the soybean isoflavones crude extract;
3. secondary absorption is extracted high-purity soybean isoflavone:
A) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant G1 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution H1; B) in concentrated solution H1, add the pure water that is equivalent to 2～4 times of its volumes, obtain secondary absorption stock liquid I1; C) with secondary absorption stock liquid I1 under the flow velocity of 1～3BV/h once more by the low-pole macroporous adsorbent resin, obtain effluent liquid J1 and by the material K1 of absorption with macroporous adsorbent resin; D) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 1～3BV/h; E) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material K1 wash-out on the macroporous resin under the flow velocity of 1～3BV/h with volume, obtain elutriant M1; F) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant M1 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution N1; G) concentrated solution N1 is sterilized, adds pure water and spraying drying, obtain soybean isoflavones product P 1, BV is the resin bed volume.
2. according to the described method of from soya whey wastewater, extracting soybean isoflavones of claim 1, it is characterized in that, the operating process 3. of described step a) and f) in the ethanol content of the concentrated solution that obtains less than 5%, reduction in bulk is original 1/6～1/4.
3. a method of extracting soybean isoflavones from soya whey wastewater is characterized in that comprising the steps,
1. pre-treatment:
A) with the soya whey wastewater input flocculation jar of soybean protein isolate alkali extraction and acid precipitation technology discharging, flocculate centrifugal by regulating the pH value and adding ionogen; B) will flocculate centrifugate by deep bed filter and micro-strainer filtration, concentrate by ultra-filtration equipment again, and obtain ultrafiltration and see through liquid A2 and ultrafiltration and concentration liquid B2; C) ultrafiltration is seen through liquid A2 and concentrate, obtain nanofiltration and see through liquid C2 and nanofiltration concentrated solution D2 by nanofiltration device;
2. one-level adsorbing and extracting soybean isoflavones crude extract:
A) in nanofiltration concentrated solution D2, add the pure water that is equivalent to 0.5～3 times of its volume, obtain one-level absorption stock liquid D2-S; B) one-level is adsorbed stock liquid D2-S under the flow velocity of 0.5～1.5BV/h by the low-pole macroporous adsorbent resin, obtain effluent liquid F2 and by the material E2 of absorption with macroporous adsorbent resin; C) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 0.5～1.5BV/h, obtain pure water leacheate F2-N and ethanol leacheate, wherein pure water leacheate F2-N and effluent liquid F2 one are used from the recovery soybean oligosaccharide, the reuse after reclaiming ethanol of ethanol leacheate; D) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material E2 wash-out on the macroporous resin under the flow velocity of 0.5～1.5BV/h with volume, obtain elutriant G2, be the soybean isoflavones crude extract;
3. secondary absorption is extracted high-purity soybean isoflavone:
A) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant G2 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution H2; B) in concentrated solution H2, add the pure water that is equivalent to 2～4 times of its volumes, obtain secondary absorption stock liquid I2; C) with secondary absorption stock liquid I2 under the flow velocity of 0.5～1.5BV/h once more by the low-pole macroporous adsorbent resin, obtain effluent liquid J2 and by the material K2 of absorption with macroporous adsorbent resin; D) priority is carried out drip washing to macroporous adsorbent resin with pure water and 5%～20% ethanol that volume is 1.5～3BV under the flow velocity of 0.5～1.5BV/h; E) be that 70%～90% ethanol of 1.5～3BV will be adsorbed on the material K2 wash-out on the macroporous resin under the flow velocity of 0.5～1.5BV/h with volume, obtain elutriant M2; F) be that 50～75 ℃, operation negative pressure are under 0.08～0.095MPa elutriant M2 to be carried out concentrating under reduced pressure to reclaim ethanol in Heating temperature, obtain concentrated solution N2; G) concentrated solution N2 is sterilized, adds pure water and spraying drying, obtain soybean isoflavones product P 2, BV is the resin bed volume.
4. the method for extracting soybean isoflavones from soya whey wastewater according to claim 3 is characterized in that, the operating process 3. of described step a) and f) in the ethanol content of the concentrated solution that obtains less than 5%, reduction in bulk is original 1/6～1/4.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03137102 CN1233639C (en) | 2003-06-04 | 2003-06-04 | Extraction of soya isoflavone from waste soybean serum |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03137102 CN1233639C (en) | 2003-06-04 | 2003-06-04 | Extraction of soya isoflavone from waste soybean serum |
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| CN1552703A CN1552703A (en) | 2004-12-08 |
| CN1233639C true CN1233639C (en) | 2005-12-28 |
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100393710C (en) * | 2005-11-03 | 2008-06-11 | 深圳清华大学研究院 | Method for extracting soybean isoflavone from soybean whey liquid |
| CN102002029B (en) * | 2010-11-06 | 2012-01-11 | 黑龙江八一农垦大学 | Method for separating and extracting isoflavone by simulated moving bed adsorption |
| CN103265614A (en) * | 2013-05-28 | 2013-08-28 | 宜宾学院 | Method for extracting soy protein, oligosaccharide and isoflavone from soybean wastewater by one-step process |
| CN110551094A (en) * | 2019-06-17 | 2019-12-10 | 山东禹王生态食业有限公司 | Method for extracting soybean isoflavone aglycone from soybean milk water |
| CN110204523B (en) * | 2019-06-17 | 2021-05-11 | 山东师范大学 | Preparation method of pure glycitein |
| CN111944010B (en) * | 2020-08-20 | 2023-05-09 | 运城学院 | Extraction equipment and method for soybean protein, isoflavone and oligosaccharide in bean product wastewater |
| CN113355372A (en) * | 2021-06-10 | 2021-09-07 | 苏州金记食品有限公司 | Process for purifying soybean whey and extracting soybean isoflavone aglycone |
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