CN1470176A - Method for treating plant protein whey - Google Patents
Method for treating plant protein whey Download PDFInfo
- Publication number
- CN1470176A CN1470176A CNA021270430A CN02127043A CN1470176A CN 1470176 A CN1470176 A CN 1470176A CN A021270430 A CNA021270430 A CN A021270430A CN 02127043 A CN02127043 A CN 02127043A CN 1470176 A CN1470176 A CN 1470176A
- Authority
- CN
- China
- Prior art keywords
- concentrate
- plant protein
- whey
- processing method
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Peptides Or Proteins (AREA)
- Coloring Foods And Improving Nutritive Qualities (AREA)
Abstract
The invention discloses a plant protein whey processing method, firstly ultra-filtering the concentrated plant protein whey by inorganic ceramic diaphragm, to hold back large-molecular alcohol-soluble protein, the alcohol-soluble protein able to return to the concentrated protein and also able to directly extract the alcohol-soluble protein with specific function; then making depressured concentration on the ultrafiltrate to reclaim the alcohol to obtain the concentrated liquid; and finally purifying the concentrated liquid by solvent and large-aperture resin or directly making acid/enzyme hydrolyzation, and during the hydrolyzing course, adding with acetic ester to carry out alternate/refluent liquid-liquid dynamic extraction, and making depressured concentration on the acetic ester layer to obtain isoflavone ligand with remarkable bioactivity, and refining the water phase to obtain higer-purity oligose.
Description
Technical field
The invention belongs to plant concentration protein production and comprehensive utilization technique field, relate to a kind of processing method of albumen whey, particularly relate to a kind of processing method of plant protein whey.
Background technology
Over year, the development and use of plant protein resource obtain flourish in the whole world surplus in the of nearly ten, and the exploitation vegetable protein becomes the important topic of the current people's of improvement trophic structure for society provides the protein of super quality and competitive price.What intake maximum, biological value were the highest in vegetable protein is soybean protein.Soybean contains the protein more than 36%, and hairtail only contains 18.1%, yellow croaker has only 16.7%, thin pork has only 16.7%, meat has only 12%, chicken has only 24.9%.Soybean is important protein matter source, and it is higher to contain the lysine content that human essential eight seed amino acids, especially children are sought after.Why soy protein products can obtain the development of advancing by leaps and bounds in countries in the world, mainly be to be accompanied by progress of science and technology, people recognize that more and more profoundly protein has the function that other any nutriment all can not replace keeping human survival and development.
Also contain bioactivators such as isoflavones, compound sugar, saponin in the soybean, isoflavones has class estrogen, suppresses breast cancer, anti-oxidant, improve function such as immunity, in recent years, as healthy food batching and medicine, be subjected to international extensive concern.Soyabean oligosaccharides is a kind of emerging functional new sugared source.Soyabean oligosaccharides is the general name of solubility saccharic in the soybean, and it mainly comprises gossypose, stachyose and sucrose.Soyabean oligosaccharides has characteristics such as low sugariness, low heat value, strong curative effect, is the MF of Bifidobacterium (beneficial bacterium) in the human body intestinal canal.Be widely used in beverage, electuary, oral liquid, candy, cake and low heater food and the health products.
Soybean germ is the reproductive organs of soybean, account for 2%～2.5% of soybean gross weight, the constituent uniqueness, wherein isoflavone levels is in the cotyledon 6～10 times, wherein soya bean element (glycitin) and soyasaponins A (soyasaponinA) only are distributed in the plumule of soybean.It is obvious that the isoflavones of soybean cotyledon and plumule is formed difference, do not contain the isoflavones of daizeol (glycitein) in the cotyledon, and key component is about 35: 65 with the ratio that big legumin (daidzein) and daizeol (genistein) calculate.Isoflavone levels reaches 3.33% in the plumule, is 6 times of cotyledon content, and main component is with big legumin (daidzein), and the ratio that daizeol (genistein) and Genistein (genistein) calculate is about 40-55: 30-50: 10-15.
Alcohol processed soybean protein concentrate is the optimum feed stock of production high-quality histone, with the thickness comminuted meat product of histone and meat fusion making as products such as ground meat food, dumpling farcing, ham sausage, quick-frozen foods.FSPC is mainly used in the non-starch additive of meat product industry owing to added soyabean protein powder in the meats such as ham sausage, pork luncheon meat, Western-style ham, can improve goods protein content, just increase the nutritive value of goods.Simultaneously owing to the functional characteristic such as the retentiveness of FSPC, hold oiliness, it can improve the quality and the mouthfeel of meat products.Therefore it becomes indispensable additive in the meat food.
China's alcohol method soybean protein is owing to problems such as comprehensive utilization is poor, and the function modified technical research of protein concentrate is not enough, slower development always.The pure method whey that domestic existing pure method protein concentrate manufacturer produces is through recovery of alcohol distillation, and raffinate has just been discarded, and has following problem in this technology:
1: contain a large amount of protein in the whey, this part albumen is if can fully recycle, and economic benefit can be improved.If but adopted the heating recovery of alcohol distillation, will cause this part protein thermal denaturation just could recycling.
2: sugar is violent with the browning reaction of protein, is unprofitable to the yield of the refining of back segment compound sugar and raising compound sugar.
3: distill sugared concentration height in the after-stage retort, at high temperature produce coking, cause alcohol to reclaim difficulty, thereby the alcohol rate of recovery is low.
4: other high value added product that contains in the whey, can not be fully used as byproducts such as isoflavones.
5: plumule with the solvent hot dipping after the ratio of malonyl glucosides type isoflavones drop to 28%, and the content of corresponding glucosides is elevated to 62% by 23%, show that malonyl glucosides type isoflavones is the main existence form of natural isoflavone, resolve into glucosides after in solvent, being heated.
Based on isoflavone glucoside, the bioavilability of isoflavones is low in the alcohol method soy protein concentrate, and for improving the isoflavones physiological function, it is hydrolyzed to glucoside unit has become a kind of direction.
Soybean comprehensive utilization project is an extremely promising agriculture industrialization project.It not only can drive the adjustment of the structure of agricultural production, and aquaculture, food industry, health products industry, medical industry etc. are all had an immense impact on.It not only has great economic benefit, and has brought great social benefit.It has been listed in one of main composition of 21st century life science development by the U.S..Soybean comprehensive utilization project has more realistic meaning to China, and it will improve the private foster level of Chinese people, promotes relevant industrial and agricultural development and plays an important role, and becomes to have one of project of agriculture industrialization future now most.
Announced a kind of aglycone isoflavones plant protein whey, lactalbumin and preparation method thereof of being rich in for Chinese patent application 94194199.X number; Being rich in aglycone isoflavones vegetable protein serum can followingly obtain: thus change most of at least aglucon isoflavones into the aglycone thing with the whey that β-Portugal's glycosides enzyme of q.s or esterase or acid treatment contain the aglucon isoflavones, obtain being rich in the aglycone whey thus.Chinese patent application discloses a kind of plant protein whey and production method thereof that is rich in Aglucone isoflavone for No. 97122812.4; It is enough to for one section make it that time that transforms takes place by handle whey under uniform temperature and certain pH value, makes the isoflavones conjugate in the plant protein whey be converted into isoflavone glucoside.Make isoflavone glucoside be converted into Aglucone isoflavone is rich in Aglucone isoflavone with production plant protein whey with enzymic catalytic reaction.Therefrom reclaim Aglucone isoflavone lactalbumin material.
Produce the isoflavones aglucon with said method, owing to contain a large amount of albumen in the whey, this part albumen is if can fully recycle, and economic benefit can be improved.In addition, it is violent especially at high temperature to carry out sugared browning reaction with protein as if acid hydrolysis, is unprofitable to the yield of the refining of back segment compound sugar and raising compound sugar.What is more important, along with enzyme or acid-hydrolyzed carrying out, its hydrolysate-isoflavones aglucon increases gradually, tell from reaction system as if untimely, hydrolytic process will descend greatly, and acid or enzyme consumption are increased, hydrolysis slows down, also the biologically active that influences the isoflavones aglucon in various degree.
Summary of the invention
The object of the present invention is to provide a kind of processing method of plant protein whey, it can make plant concentration protein production combine with comprehensive utilization, especially various compositions in the degreasing plumule rationally can be fully utilized, to overcome existing above-mentioned defective in the prior art.
Above-mentioned purpose of the present invention is achieved in that a kind of processing method of plant protein whey, it is characterized in that having following processing step:
Plant protein whey is carried out hyperfiltration treatment with inorganic ceramic membrane, make it separate the back and obtain alcohol soluble protein and membrane filtration liquid.
The processing method of plant protein whey of the present invention, it is characterized in that with inorganic ceramic membrane carry out hyperfiltration treatment process conditions can for:
Operating temperature: 5-60 ℃, inlet pressure: 0.3-0.8MPa, outlet pressure: 0.05-0.3MPa, flux 0.02-0.8m
3/ m
2H.
This processing method can molecular cut off 1000-20000 alcohol soluble protein, the rejection of protein is 60-93%.
The processing method of plant protein whey of the present invention is characterized in that also having following processing step:
At first membrane filtration liquid is concentrated recovered alcohol through decompression, obtain concentrate;
Then concentrate is carried out acid hydrolysis, in the acid hydrolysis process, add ethyl acetate, carry out the liquid-attitude of the surging extraction of cross-current/counter-current, acid hydrolysis is combined with dynamic extraction, obtain ethyl acetate layer and water;
At last the ethyl acetate layer decompression is concentrated, obtain having the isoflavones aglucon concentrate of notable biological activity, water is obtained the higher compound sugar of purity through making with extra care.
Because acid hydrolysis combines with dynamic extraction, therefore help protecting the biologically active of isoflavones, can accelerate reaction process simultaneously.
The processing method of plant protein whey of the present invention is characterized in that concentrate is carried out also having additional the processing step of concentrate through solvent, macroporous resin purification before the acid hydrolysis.
The processing method of plant protein whey of the present invention is characterized in that acid-hydrolyzed process conditions are:
Acid concentration: 0.1-2mol/l, hydrolysis temperature: 20-80 ℃, hydrolysis time: 0.5-24 hour;
The ethyl acetate addition is a 0.2-2 whey volume doubly, adopts the dynamic liquid-liquid extraction of 1-6 stage countercurrent/cross-flow.
The processing method of plant protein whey of the present invention is characterized in that also having following processing step:
At first membrane filtration liquid is concentrated recovered alcohol through decompression, obtain concentrate;
Then concentrate is carried out enzyme hydrolysis, in the acid hydrolysis process, add ethyl acetate, carry out the liquid-attitude of the surging extraction of cross-current/counter-current, acid hydrolysis is combined with dynamic extraction, obtain ethyl acetate layer and water;
At last the ethyl acetate layer decompression is concentrated, obtain having the isoflavones aglucon concentrate of notable biological activity, water is obtained the higher compound sugar of purity through making with extra care.
Filter penetrating fluid through ultrafiltration, enzyme can be held back reuse, can improve the utilization rate of enzyme to greatest extent.
Identical with above-mentioned acid hydrolysis process, the processing method of plant protein whey of the present invention is characterized in that concentrate is carried out also having additional the processing step of concentrate through solvent, macroporous resin purification before the enzyme hydrolysis.
The processing method of plant protein whey of the present invention is characterized in that the used enzyme of enzyme hydrolysis process is: biological pectase, industrial amylase, lactase, lactonase etc.;
The ethyl acetate addition is a 0.2-2 whey volume doubly, adopts the dynamic liquid-liquid extraction of 1-6 stage countercurrent/cross-flow.
The processing method of plant protein whey of the present invention, when the used enzyme of enzyme hydrolysis process was the Amylase AG 300L of letter (NOVOZYMES) company of Novi, enzyme hydrolysis condition was concentration of substrate 2-30g/l, reaction time 20-50 minute, pH5-8, temperature 5-45 ℃.
The processing method of plant protein whey of the present invention, when the used enzyme of enzyme hydrolysis process was the Lactozym of letter (NOVOZYMES) company of Novi, enzyme hydrolysis condition was concentration of substrate 2-30g/l, reaction time 20-50 minute, pH2-6, temperature 25-80 ℃.
Below, in conjunction with specific embodiments and relevant drawings the present invention is described in further detail.
Description of drawings
Fig. 1 is the flow chart of the dynamic cross-current/counter-current extraction of acid hydrolysis of the present invention;
Fig. 2 is the flow chart of the dynamic cross-current/counter-current extraction of enzyme hydrolysis of the present invention.
The specific embodiment
With reference to Fig. 1, it is the flow chart of the dynamic cross-current/counter-current extraction of acid hydrolysis of the present invention.
1: at first the pure method protein concentrate of soybean (soybean germ) whey is carried out hyperfiltration treatment, processing method adopts can carry out hyperfiltration treatment by molecular cut off 1000-20000 inorganic ceramic membrane,
The process conditions of hyperfiltration treatment:
Operating temperature: 5-60 ℃, inlet pressure: 0.3-0.8MPa, outlet pressure: 0.05-0.3MPa, flux 0.02-0.8m
3/ m
2H,
Through after the hyperfiltration treatment, obtain alcohol soluble protein and film penetrating fluid, independent processing can be recycled or do to alcohol soluble protein, and the film penetrating fluid concentrates recovered alcohol through decompression, obtains the concentrate of penetrating fluid;
2: concentrate can adopt macroreticular resin, and methods such as solvent extraction are further purified isoflavones or compound sugar, or directly carries out dynamic extraction;
3: the acid hydrolysis condition is acid concentration: 0.1-2mol/l, hydrolysis temperature: 20-80 ℃, and hydrolysis time: 0.5-24 hour, in the acid hydrolysis process, add ethyl acetate, the ethyl acetate addition is a 0.2-2 film infiltration concentrate volume doubly, adopts the dynamic liquid-liquid extraction of 1-6 stage countercurrent/cross-flow
Carrying out along with hydrolysis, the isoflavones aglucon increases gradually, because the isoflavones aglucon is very little in aqueous phase solubility, ethyl acetate mutually in solubility big, make final reacting product change over to rapidly ethyl acetate mutually in, accelerate reaction process like this, reduced sour consumption, acidolysis is combined with dynamic extraction, help protecting the biologically active of isoflavones;
4: after dynamically hydrolysis was finished, standing demix concentrated the ethyl acetate layer decompression, reclaims ethyl acetate, obtains isoflavones aglucon concentrate, but the ethyl acetate reuse continues dynamic extraction;
5: water adds the alkali neutralization, and desalination removes to concentrate refining compound sugar then.
The macroreticular resin that is adopted in the purification step of present embodiment can be nonpolar, low pole and polar macroporous resin such as DM130, XAD-4, DA-201 etc., solvent can be n-butanol, ether, acetone etc. respectively, and the acid of being adopted in the acid hydrolysis step of present embodiment can be hydrochloric acid, sulfuric acid etc.
With reference to Fig. 2, it is the flow chart of the dynamic cross-current/counter-current extraction of enzyme hydrolysis of the present invention.
1: at first the pure method protein concentrate of soybean (soybean germ) whey is carried out hyperfiltration treatment, processing method adopts can carry out hyperfiltration treatment by molecular cut off 1000-20000 inorganic ceramic membrane,
Process conditions:
Operating temperature: 5-60 ℃, inlet pressure: 0.3-0.8MPa, outlet pressure: 0.05-0.3MPa, flux 0.02-0.8m
3/ m
2H,
Through after the hyperfiltration treatment, obtain alcohol soluble protein and film penetrating fluid, independent processing can be recycled or do to alcohol soluble protein, and the film penetrating fluid concentrates recovered alcohol through decompression, obtains the concentrate of penetrating fluid;
2: concentrate can adopt macroreticular resin, and methods such as solvent extraction are further purified isoflavones or compound sugar, or directly carries out dynamic extraction;
3: can carry out enzyme hydrolysis preferably enzyme biological pectase is arranged, industrial amylase, lactase, lactonase etc., when the used enzyme of enzyme hydrolysis process is the AmylaseAG 300L of letter (NOVOZYMES) company of Novi, enzyme hydrolysis condition is concentration of substrate 2-30g/l, reaction time 20-50 minute, pH5-8, temperature 5-45 ℃; And when the used enzyme of enzyme hydrolysis process is the Lactozym of letter (NOVOZYMES) company of Novi, enzyme hydrolysis condition is concentration of substrate 2-30g/l, reaction time 20-50 minute, pH2-6, temperature 25-80 ℃, in the enzyme hydrolysis process, add ethyl acetate, the ethyl acetate addition is a 0.2-2 film infiltration concentrate volume doubly, adopt the dynamic liquid-liquid extraction of 1-6 stage countercurrent/cross-flow
Carrying out along with hydrolysis, the isoflavones aglucon increases gradually, because the isoflavones aglucon is very little in aqueous phase solubility, ethyl acetate mutually in solubility big, make final reacting product change over to rapidly ethyl acetate mutually in, accelerate reaction process like this, reduced enzyme dosage, enzymolysis is combined with dynamic extraction, help protecting the biologically active of isoflavones;
4: after dynamically hydrolysis was finished, standing demix concentrated the ethyl acetate layer decompression, reclaims ethyl acetate, obtains isoflavones aglucon concentrate, and ethyl acetate can be used, and continues dynamic extraction;
5: water can be held back reuse with enzyme through the ultrafiltration filter, can improve the utilization rate of enzyme to greatest extent, and ultrafiltration membrane permeate liquid is removed refining compound sugar.
Macroreticular resin that is adopted in the purification step of present embodiment and solvent also can be nonpolar, low pole and polar macroporous resin such as DM130, XAD-4, and DA-201 etc., solvent can be n-butanol, ether, acetone etc. respectively.
The production technology of plant protein whey can adopt existing manufacturing technique usually in the above-described embodiments, for example: at first produce low temperature (plumule) dregs of rice, leach with alcohol then, obtain pure method soy-bean whey, last protein concentrate.
Process conditions: alcohol concentration: 60-75%; Solid-to-liquid ratio: 1: 3-1: 6; (if interrupted extraction needs 2-4 time)
Extraction temperature: 40-55 ℃; Extraction time: 40 minutes-3 hours.
The pure method soy-bean whey main component that obtains by said method please see the following form:
| Ethanol content | Crude protein | Ash content | Total reducing sugar | General flavone, saponin |
| ??60-75％ | ??1-6％ | ????0.3-1％ | ????1-2.5％ | ??0.1-1％ |
Though the removal method of alcohol soluble protein has heating in the whey, isoelectric point method, flocculence etc., heating can make sugar violent with the browning reaction of protein, and the serious sex change of albumen, and albumen can not be recycled; Isoelectric point method can only be removed the heavy albumen of acid in the soybean, and this is very limited; And adopting flocculants such as zinc acetate, copper sulphate, milk of lime to handle, running cost is higher, also can introduce a large amount of ions in liquid glucose, has increased the weight of the compound sugar difficulty of post-processing.
Therefore having adopted membrane separation technique, membrane separation technique in the present invention is a kind of filtering technique of chemical process, the same with common isolated by filtration process, requires to have at least in the separated mixture a kind of component can unhinderedly pass through film.Other component is being blocked in various degree then.The film separation process has following characteristics: membrane separation process is the separation of pure physical property, promptly requires separated component neither to have thermodynamic (al) variation, does not also have chemistry or biological variation.Therefore, can reclaim and utilize a certain component in the mixture at least in principle; Membrane separation process constitutes with kit form, therefore, can adapt to the demand of different production capacity.
Ultrafiltration must be selected the membrane material and the molecular cut off that suit, and for alcoholic extract, ultrafiltration has two requirements, at first must this kind membrane material can ethanol-tolerant, variation physics or chemistry can not take place because of the erosion of alcohol; Secondly used molecular cut off must be held back big molecules such as protein as far as possible, sees through little molecules such as compound sugar, and the big water flux of trying one's best also must be arranged simultaneously, and only in this way, ultrafiltration could effective and economic use.
The selection of membrane material:, find in process of the test that when using PS membrane, film has shrinkage phenomenon owing to contain alcohol in this system, and after ultrafiltration finishes, can not recover, illustrate that film is destroyed.When adopting cellulose acetate film, the easy polluted membrane of protein surface, not easy cleaning.According to the demand of separating, synthetic solid film can be by organic or inorganic material manufacturing.
According to the demand of separating, synthetic solid film can be by organic or inorganic material manufacturing.Asymmetric ceramic membrane is made of two-layer at least, constitutes by three layers at least in some cases.The purpose of this class dissymmetrical structure is to constitute a kind of flawless separating layer, reduces the flowed friction of film simultaneously again, and ensures the mechanical strength of film.The thickness of carrier layer is several millimeters, has the coarse texture of aperture 1-10 μ m; The thickness in intermediate layer placed on it is 10-100 μ m, and the aperture is 50-100nm.Real separating layer is very thin, and thickness is about 1 μ m, aperture 2-50nm.The advantage of inoranic membrane has: the no problem of aging of heat endurance (2) resistance to chemical attack (3) that (1) is high, long service life (4) but back flush (5) separation extreme and selectivity are controllable.
The aperture of milipore filter is generally in (10-100) * 10
-10M, but milipore filter usually not with its pore size as index, and to hold back relative molecular weight as index.So-called " relative molecular mass cutoff value " refers to that rejection reaches the relative molecular weight that minimum more than 90% is trapped material, from experimental result, operating temperature: 5-60 ℃, inlet pressure: 0.3-0.8MPa, outlet pressure: 0.05-0.3MPa, molecular cut off 1000-20000, rate and protein retention 60-93%; Flux 0.02-0.8m
3/ m
2H.
The dynamic liquid-liquid extraction of hydrolysis and adverse current/cross-flow:
Plumule with the solvent hot dipping after the ratio of malonyl glucosides type isoflavones drop to 28%, and the content of corresponding glucosides is elevated to 62% by 23%, shows that malonyl glucosides type isoflavones is the main existence form of natural isoflavone, resolves into glucosides after being heated in solvent.The variation of isoflavones structure differs greatly the composition of the isoflavones in the different bean foods, in the alcohol method soy protein concentrate based on isoflavone glucoside, the bioavilability of isoflavones, for improving the isoflavones physiological function, it is hydrolyzed to glucoside unit has become a kind of direction.Acidolysis is combined with dynamic extraction, help protecting the biologically active of isoflavones, can accelerate reaction process simultaneously.
Acidolysis condition: acid concentration: 0.1-2mol/l, hydrolysis temperature: 20-80 ℃, hydrolysis time 0.5-24 hour;
Enzyme has biological pectase preferably, (the Amylase AG 300L as NOVOZYMES company should condition be concentration of substrate 2-30g/l to industrial amylase, reaction time 20-50 minute, pH5-8, temperature 5-45 ℃), lactase is (as the Lactozym of NOVOZYMES company, suitable condition is concentration of substrate 2-30g/l, reaction time 20-50 minute, and pH2-6, temperature 25-80 ℃), lactonase etc.
The flow process of the multistage cross flow extraction of adopting in the present invention and the flow process that multi-stage countercurrent leaches all can adopt traditional technical scheme, do not give unnecessary details at this.
Owing to adopted membrane separation technique in the present invention, it is the separation of pure physical property, promptly requires separated component neither to have thermodynamic (al) variation, does not also have chemistry or biological variation.Therefore, can reclaim and utilize a certain component in the mixture at least in principle; Membrane separation process constitutes with kit form, therefore, can adapt to the demand of different production capacity.
Because acid hydrolysis combines with dynamic extraction, therefore help protecting the biologically active of isoflavones, can accelerate reaction process simultaneously.
Owing to be to filter penetrating fluid by ultrafiltration, therefore enzyme can be held back reuse, can improve the utilization rate of enzyme to greatest extent.
The above only is specific embodiments of the invention, but technical characterictic of the present invention is not limited to the specific embodiment lifted, these specific embodiments be not with since limit the present invention, every any similar variation in technical conceive scope of the present invention, all be contained in the category of the present invention, for example: inorganic membrane filtration and dynamic hydrolysis are equally applicable to the processing of the heavy method protein isolate whey of the molten acid of alkali; Employed extractant also can also be selected ether etc. for use except ethyl acetate in adverse current/cross-flow dynamic fluid flow liquid extraction process.Therefore any person skilled in the art person is in the field of the invention, can think easily and variation or modify all be encompassed in protection scope of the present invention.
Claims (10)
1, a kind of processing method of plant protein whey is characterized in that having following processing step:
Plant protein whey is carried out hyperfiltration treatment with inorganic ceramic membrane, make it separate the back and obtain alcohol soluble protein and membrane filtration liquid.
2, the processing method of plant protein whey as claimed in claim 1 is characterized in that the process conditions of carrying out hyperfiltration treatment with inorganic ceramic membrane are:
Operating temperature: 5-60 ℃, inlet pressure: 0.3-0.8MPa, outlet pressure: 0.05-0.3MPa, flux 0.02-0.8m
3/ m
2H.
3, the processing method of plant protein whey as claimed in claim 1 or 2 is characterized in that also having following processing step:
At first membrane filtration liquid is concentrated recovered alcohol through decompression, obtain concentrate;
Then concentrate is carried out acid hydrolysis, in the acid hydrolysis process, add ethyl acetate, carry out the liquid-attitude of the surging extraction of cross-current/counter-current, acid hydrolysis is combined with dynamic extraction, obtain ethyl acetate layer and water;
At last the ethyl acetate layer decompression is concentrated, obtain having the isoflavones aglucon concentrate of notable biological activity, water is obtained the higher compound sugar of purity through making with extra care.
4, the processing method of plant protein whey as claimed in claim 3 is characterized in that concentrate is carried out also having additional the processing step of concentrate through solvent, macroporous resin purification before the acid hydrolysis.
5, the processing method of plant protein whey as claimed in claim 4 is characterized in that acid-hydrolyzed process conditions are:
Acid concentration: 0.1-2mol/l, hydrolysis temperature: 20-80 ℃, hydrolysis time: 0.5-24 hour;
The ethyl acetate addition is a 0.2-2 whey volume doubly, adopts the dynamic liquid-liquid extraction of 1-6 stage countercurrent/cross-flow.
6, the processing method of plant protein whey as claimed in claim 1 or 2 is characterized in that also having following processing step:
At first membrane filtration liquid is concentrated recovered alcohol through decompression, obtain concentrate;
Then concentrate is carried out enzyme hydrolysis, in the acid hydrolysis process, add ethyl acetate, carry out the liquid-attitude of the surging extraction of cross-current/counter-current, acid hydrolysis is combined with dynamic extraction, obtain ethyl acetate layer and water;
At last the ethyl acetate layer decompression is concentrated, obtain having the isoflavones aglucon concentrate of notable biological activity, water is obtained the higher compound sugar of purity through making with extra care.
7, the processing method of plant protein whey as claimed in claim 6 is characterized in that concentrate is carried out also having additional the processing step of concentrate through solvent, macroporous resin purification before the enzyme hydrolysis.
8, the processing method of plant protein whey as claimed in claim 7 is characterized in that the used enzyme of enzyme hydrolysis process is: biological pectase, industrial amylase, lactase, lactonase etc.;
The ethyl acetate addition is a 0.2-2 whey volume doubly, adopts the dynamic liquid-liquid extraction of 1-6 stage countercurrent/cross-flow.
9, the processing method of plant protein whey as claimed in claim 8 is characterized in that the used enzyme of enzyme hydrolysis process is Amylase AG 300L, and enzyme hydrolysis condition is concentration of substrate 2-30g/l, reaction time 20-50 minute, and pH5-8, temperature 5-45 ℃.
10, the processing method of plant protein whey as claimed in claim 8 is characterized in that the used enzyme of enzyme hydrolysis process is Lactozym, and enzyme hydrolysis condition is concentration of substrate 2-30g/l, reaction time 20-50 minute, and pH2-6, temperature 25-80 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021270430A CN100362932C (en) | 2002-07-26 | 2002-07-26 | Method for treating plant protein whey |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021270430A CN100362932C (en) | 2002-07-26 | 2002-07-26 | Method for treating plant protein whey |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1470176A true CN1470176A (en) | 2004-01-28 |
| CN100362932C CN100362932C (en) | 2008-01-23 |
Family
ID=34143454
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021270430A Expired - Fee Related CN100362932C (en) | 2002-07-26 | 2002-07-26 | Method for treating plant protein whey |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100362932C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102702274A (en) * | 2012-06-12 | 2012-10-03 | 华东理工大学 | Method for preparing high-purity soybean oligosaccharide from soybean whey wastewater |
| CN103988972A (en) * | 2014-05-26 | 2014-08-20 | 福建省微生物研究所 | Desalting and protein recovering method of salted egg white |
| CN104115990A (en) * | 2014-06-17 | 2014-10-29 | 哈尔滨旭康农业高科技有限公司 | Preparation method and high-quality water-soluble soybean protein mixed powder prepared by same |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2592769B1 (en) * | 1986-01-10 | 1990-10-12 | Agronomique Inst Nat Rech | PROCESS FOR OBTAINING A MATERIAL ENRICHED IN BETA CASEIN, APPARATUS FOR THE IMPLEMENTATION OF THIS PROCESS, AND APPLICATION OF THE PRODUCTS OBTAINED BY THIS PROCESS AS FOODS, FOOD SUPPLEMENTS OR ADDITIVES IN THE FOOD AND PHARMACEUTICAL INDUSTRY OR IN THE PREPARATION OF PEPTID PHYSIOLOGICAL ACTIVITY |
-
2002
- 2002-07-26 CN CNB021270430A patent/CN100362932C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102702274A (en) * | 2012-06-12 | 2012-10-03 | 华东理工大学 | Method for preparing high-purity soybean oligosaccharide from soybean whey wastewater |
| CN102702274B (en) * | 2012-06-12 | 2015-01-28 | 华东理工大学 | Method for preparing high-purity soybean oligosaccharide from soybean whey wastewater |
| CN103988972A (en) * | 2014-05-26 | 2014-08-20 | 福建省微生物研究所 | Desalting and protein recovering method of salted egg white |
| CN103988972B (en) * | 2014-05-26 | 2016-01-20 | 福建省微生物研究所 | A kind of method of salted egg albumen desalination and recovery albumen |
| CN104115990A (en) * | 2014-06-17 | 2014-10-29 | 哈尔滨旭康农业高科技有限公司 | Preparation method and high-quality water-soluble soybean protein mixed powder prepared by same |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100362932C (en) | 2008-01-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105476030A (en) | Multi-functional composite oligopeptide nutrition powder | |
| CN109251954B (en) | Production method of sea cucumber polypeptide | |
| CN108822163B (en) | Comprehensive cyclic production method of D-glucosamine hydrochloride | |
| CN101096697B (en) | Industrial production method of ovum protein polypeptide from fowl ovum by enzymatical process | |
| CN103265614A (en) | Method for extracting soy protein, oligosaccharide and isoflavone from soybean wastewater by one-step process | |
| CN1300135C (en) | Method for preparing soybean isoflavone, soybean spanin, oligosaccharide and soybean concentrated protein | |
| CN1344565A (en) | Fucoidin ester as antiviral immunoregulator and its prepn | |
| CN1985852A (en) | Process of extracting sea cucumber polyose and other active components from boiled sea cucumber juice | |
| CN103849671A (en) | Method of preparing antioxidative peptide by enzymolysis of byproducts in mackerel can processing | |
| CN1132830C (en) | Method for extracting protein, short peptide, nucleic acid, isoflavone, saponin and oligosaccharide by using high and low temperature soybean cake | |
| CN1259130A (en) | Preparation of isoflavones from legumes | |
| CN113512108B (en) | Marine fish skin collagen oligopeptide and preparation method and application thereof | |
| CN100362932C (en) | Method for treating plant protein whey | |
| CN108913499A (en) | A kind of tartary buckwheat extract and preparation method thereof, application and health liquor | |
| CN1531863A (en) | Novel method for producing inulin using heliangine or cicheriin as raw material | |
| CN112342259A (en) | Method for extracting soybean polypeptide from soybean whey wastewater | |
| CN111418700A (en) | Tuna peptide, extraction method thereof and application of tuna peptide as antihypertensive agent | |
| CN110669813A (en) | Yak rib small molecule peptide and extraction method thereof | |
| CN100351388C (en) | Method for producing soybean isoflavones aglycone using glucosidase and membrane technology | |
| KR100901379B1 (en) | Method for separation and purification of corosolic acid from corosolic acid-containing materials | |
| CN1210287C (en) | Method for producing sialic acid | |
| CN102618611A (en) | Method for preparing corn oligopeptide by using membrane integration technology | |
| CN112176017A (en) | Method for efficiently extracting protein peptide from sea cucumber intestines | |
| CN112592780A (en) | Yellow serofluid beer and preparation method thereof | |
| CN1261586C (en) | Method for preparing aglycon of soybean isoflavone glycoside base by enzymatic method hydrolyzing soybean |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: SANHE HUIFU GRAIN AND OIL GROUP CO., LTD. Free format text: FORMER OWNER: HUIFU GRAIN-OIL FOOD PROCESSING CO., LTD., SANHE CITY Effective date: 20050708 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20050708 Address after: 065201 Yanjiao economic and Technological Development Zone, Hebei, Sanhe Applicant after: Sanhe Hopefull Grain & Oil Group Co., Ltd. Address before: 065201 Yanjiao economic and Technological Development Zone, Hebei, Sanhe Applicant before: Huifu Grain-Oil Food Processing Co., Ltd., Sanhe City |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Sanhe Hopefull Biotechnology Co., Ltd. Assignor: Sanhe Hopefull Grain & Oil Group Co., Ltd. Contract record no.: 2011990001022 Denomination of invention: Method for treating plant protein whey Granted publication date: 20080123 License type: Exclusive License Open date: 20040128 Record date: 20111103 |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080123 Termination date: 20170726 |