阅读说明：本技术 一种可工业化生产植物蛋白肽的清洁生产方法 (Clean production method capable of industrially producing vegetable protein peptide ) 是由 于淼 于 2020-08-03 设计创作，主要内容包括：本发明属于谷物类、杂豆类、块茎类深加工领域,尤其是一种可工业化生产植物蛋白肽的清洁生产方法,针对现有的生产周期长、环境不友好、盐含量高、废水处理难度大、运行成本高的问题,现提出如下方案,其包括以下步骤：S1：浸泡磨浆：原料利用碱水,pH=9-11,温度20-50℃,液固比1：2-5,浸泡1-3h,组织松软后,湿法磨浆,80-200目；S2：碱液浸提：将S1中的浆液置于恒温搅拌罐内,温度20℃-50℃,搅拌浸提蛋白成分,2-4h；S3：离心分离；本发明能提高蛋白肽的提取效率,增加产量,降低了高有机物废水排放,减少环境污染,降低企业生产投入成本,具有极为广阔的市场前景。(The invention belongs to the field of deep processing of grains, beans and tubers, in particular to a clean production method capable of industrially producing vegetable protein peptide, aiming at the problems of long production period, environment unfriendliness, high salt content, high wastewater treatment difficulty and high operation cost, the following scheme is proposed, and the method comprises the following steps: s1: soaking and grinding: the raw materials are alkaline water, the pH is =9-11, the temperature is 20-50 ℃, and the liquid-solid ratio is 1: 2-5, soaking for 1-3h, and grinding the soft tissue into 80-200 meshes by a wet method; s2: alkali liquor leaching: placing the slurry in the S1 into a constant-temperature stirring tank, stirring and leaching protein components at the temperature of 20-50 ℃ for 2-4 h; s3: carrying out centrifugal separation; the method can improve the extraction efficiency of the protein peptide, increase the yield, reduce the discharge of high organic matter wastewater, reduce the environmental pollution and reduce the production input cost of enterprises, and has extremely wide market prospect.)

1. A clean production method capable of industrially producing vegetable protein peptide is characterized by comprising the following steps:

s1: soaking and grinding: the raw materials are alkaline water, the pH is =9-11, the temperature is 20-50 ℃, and the liquid-solid ratio is 1: 2-5, soaking for 1-3h, and grinding the soft tissue into 80-200 meshes by a wet method;

s2: alkali liquor leaching: placing the slurry in the S1 into a constant-temperature stirring tank, stirring and leaching protein components at the temperature of 20-50 ℃ for 2-4 h;

s3: centrifugal separation: performing solid-liquid separation on the extracting solution in the S2 through a horizontal spiral centrifuge, returning heavy phase slag to the wet grinding step for repeated extraction once, and allowing light phase liquid to enter the next procedure;

s4: purifying an extracting solution: passing the light phase feed liquid in the S3 through a microfiltration membrane A, wherein the pore diameter range is as follows: 0.010um-0.100um, realizing concentration and purification of alkali-soluble protein components, wherein the part of protein mainly exists in the form of micelle or aggregated protein molecular groups, and is intercepted by a micro-filtration membrane in the filtering process to separate out soluble small-molecular protein, polysaccharide and ash components; and (3) passing the microfiltration membrane permeate through an ultrafiltration membrane, and intercepting the molecular weight: 1000Da-10000Da, intercepting and recovering soluble small molecular protein components, combining with the microfiltration membrane concentrated solution, and discharging the permeated solution to a water treatment process;

s5: and (3) protease hydrolysis: standardizing the concentrated solution in S4, adjusting the concentration to 10-30% with purified water or reuse water and alkali liquor, and adjusting the temperature: 40 ℃ to 55 ℃, pH: 9-11, adding a compound protease preparation according to 0.05% -0.2% of the solid content, stirring and hydrolyzing for 3-6 h;

s6: separation and purification of protein peptide: and (3) passing the protein hydrolysate in the S5 through a microfiltration membrane B, wherein the pore diameter range is as follows: 0.100-0.500 um, separating soluble protein peptide, amino acid and unhydrolyzed insoluble components, drying the unhydrolyzed part to process protein by-products or returning to the previous process for hydrolysis, concentrating the soluble protein peptide part through a nanofiltration membrane until the concentration content of soluble solid matters is 10-20%, and recycling the nanofiltration membrane permeate to the previous alkali extraction process;

s7: and (3) vacuum concentration: further concentrating the protein peptide concentrated solution in the S6 by a vacuum concentration system until the concentration content of soluble solids is 40-50%, and recycling the evaporated condensed water to the previous alkali extraction process;

s8: clarifying and filtering: and (3) filtering and clarifying the concentrated solution in the S7 through a microfiltration membrane C, wherein the pore diameter range is as follows: 0.050um-0.200um, returning the concentrated solution part to the hydrolysis reaction process;

s9: drying and granulating: and (4) drying and granulating the clear permeate liquid described in the S8 by using a spray drying system to obtain a protein peptide powder product.

2. The clean production method of claim 1, wherein in S1, the raw material includes but is not limited to rice, wheat, oat, buckwheat, quinoa, highland barley, corn, potato, sweet potato, soybean, chickpea, pea, and mung bean.

3. The clean production method of claim 1, wherein the alkaline water in S1 is sodium hydroxide or potassium hydroxide.

4. The clean production method of claim 1, wherein in S5, the compound protease preparation includes but is not limited to alkaline protease, neutral protease, and flavourzyme.

5. The clean production method of claim 1, wherein in S1, the raw material is alkaline water, pH =10, temperature is 30 ℃, liquid-solid ratio is 1: 3, soaking for 2 hours, and grinding the soft tissue into 100 meshes by a wet method.

6. The clean production method of vegetable protein peptide as claimed in claim 1, wherein in S2, the alkaline leaching: and (3) placing the slurry in the S1 into a constant-temperature stirring tank, and stirring and leaching the protein component for 3 hours at the temperature of 35 ℃.

7. The clean production method of vegetable protein peptide as claimed in claim 1, wherein in S4, the light phase feed liquid in S3 is passed through microfiltration membrane A, pore size: 0.05um, the concentration and purification of alkali-soluble protein components are realized, the part of protein mainly exists in the form of micelle or aggregated protein molecular groups, and the filtration process is intercepted by a micro-filtration membrane to separate out soluble small molecular protein, polysaccharide and ash components; and (3) passing the microfiltration membrane permeate through an ultrafiltration membrane, and intercepting the molecular weight: 2000Da, intercepting and recovering soluble small molecular protein components, combining the soluble small molecular protein components with the microfiltration membrane concentrated solution, and discharging the permeated solution to the water treatment process.

8. The clean production method of claim 1, wherein in S5, the concentration is adjusted to 15% with clean water or recycled water or lye, and the temperature is as follows: 45 ℃, pH: 10, adding the compound protease preparation according to 0.1 percent of the solid content, stirring and hydrolyzing for 4 hours.

Technical Field

The invention relates to the technical field of deep processing of grains, mixed beans and tubers, in particular to a clean production method capable of industrially producing vegetable protein peptide.

Background

The traditional protein extraction method adopts an alkali dissolution and acid precipitation method, obtains separated protein, and then prepares hydrolyzed protein peptide through hydrolysis of an enzyme preparation, and the production period is long; the environment is not friendly: a large amount of acid and alkali are used in the industrial production process, so that environmental pollution to a certain degree can be caused; large amount of waste water: the traditional industrial production method has the disadvantages of large wastewater discharge amount, high salt content, large wastewater treatment difficulty and high operation cost.

Disclosure of Invention

The invention aims to solve the defects of long production period, unfriendly environment, high salt content, high wastewater treatment difficulty and high operation cost in the prior art, and provides a clean production method capable of industrially producing vegetable protein peptide.

In order to achieve the purpose, the invention adopts the following technical scheme:

a clean production method for industrially producing vegetable protein peptide comprises the following steps:

s1: soaking and grinding: the raw materials are alkaline water, the pH is =9-11, the temperature is 20-50 ℃, and the liquid-solid ratio is 1: 2-5, soaking for 1-3h, and grinding the soft tissue into 80-200 meshes by a wet method;

s2: alkali liquor leaching: placing the slurry in the S1 into a constant-temperature stirring tank, stirring and leaching protein components at the temperature of 20-50 ℃ for 2-4 h;

s3: centrifugal separation: performing solid-liquid separation on the extracting solution in the S2 through a horizontal spiral centrifuge, returning heavy phase slag to the wet grinding step for repeated extraction once, and allowing light phase liquid to enter the next procedure;

s4: purifying an extracting solution: passing the light phase feed liquid in the S3 through a microfiltration membrane A, wherein the pore diameter range is as follows: 0.010um-0.100um, realizing concentration and purification of alkali-soluble protein components, wherein the part of protein mainly exists in the form of micelle or aggregated protein molecular groups, and is intercepted by a micro-filtration membrane in the filtering process to separate out soluble small-molecular protein, polysaccharide and ash components; and (3) passing the microfiltration membrane permeate through an ultrafiltration membrane, and intercepting the molecular weight: 1000Da-10000Da, intercepting and recovering soluble small molecular protein components, combining with the microfiltration membrane concentrated solution, and discharging the permeated solution to a water treatment process;

s5: and (3) protease hydrolysis: standardizing the concentrated solution in S4, adjusting the concentration to 10-30% with purified water or reuse water and alkali liquor, and adjusting the temperature: 40 ℃ to 55 ℃, pH: 9-11, adding a compound protease preparation according to 0.05% -0.2% of the solid content, stirring and hydrolyzing for 3-6 h;

s6: separation and purification of protein peptide: and (3) passing the protein hydrolysate in the S5 through a microfiltration membrane B, wherein the pore diameter range is as follows: 0.100-0.500 um, separating soluble protein peptide, amino acid and unhydrolyzed insoluble components, drying the unhydrolyzed part to process protein by-products or returning to the previous process for hydrolysis, concentrating the soluble protein peptide part through a nanofiltration membrane until the concentration content of soluble solid matters is 10-20%, and recycling the nanofiltration membrane permeate to the previous alkali extraction process;

s7: and (3) vacuum concentration: further concentrating the protein peptide concentrated solution in the S6 by a vacuum concentration system until the concentration content of soluble solids is 40-50%, and recycling the evaporated condensed water to the previous alkali extraction process;

s8: clarifying and filtering: and (3) filtering and clarifying the concentrated solution in the S7 through a microfiltration membrane C, wherein the pore diameter range is as follows: 0.050um-0.200um, returning the concentrated solution part to the hydrolysis reaction process;

s9: drying and granulating: and (4) drying and granulating the clear permeate liquid described in the S8 by using a spray drying system to obtain a protein peptide powder product.

Preferably, in S1, the raw materials include, but are not limited to, rice, wheat, oat, buckwheat, quinoa, highland barley, corn, potato, sweet potato, soybean, chickpea, pea, and mung bean.

Preferably, in S1, the alkaline water is prepared from sodium hydroxide or potassium hydroxide and purified water or recycled water.

Preferably, in S5, the complex protease preparation includes, but is not limited to, alkaline protease, neutral protease, and flavourzyme.

Preferably, in S1, the raw material is alkaline water, and the pH =10, the temperature is 30 ℃, and the liquid-solid ratio is 1: 3, soaking for 2 hours, and grinding the soft tissue into 100 meshes by a wet method.

Preferably, in the S2, the alkali solution leaching: and (3) placing the slurry in the S1 into a constant-temperature stirring tank, and stirring and leaching the protein component for 3 hours at the temperature of 35 ℃.

Preferably, in S4, the light phase feed liquid in S3 is passed through a microfiltration membrane a, with a pore size: 0.05um, the concentration and purification of alkali-soluble protein components are realized, the part of protein mainly exists in the form of micelle or aggregated protein molecular groups, and the filtration process is intercepted by a micro-filtration membrane to separate out soluble small molecular protein, polysaccharide and ash components; and (3) passing the microfiltration membrane permeate through an ultrafiltration membrane, and intercepting the molecular weight: 2000Da, intercepting and recovering soluble small molecular protein components, combining the soluble small molecular protein components with the microfiltration membrane concentrated solution, and discharging the permeated solution to the water treatment process.

Preferably, in S5, the concentration is adjusted to 15% with purified or recycled water or lye, and the temperature: 45 ℃, pH: 10, adding the compound protease preparation according to 0.1 percent of the solid content, stirring and hydrolyzing for 4 hours.

Compared with the prior art, the invention has the beneficial effects that:

the production efficiency is improved: the steps of acid precipitation and cleaning in the traditional process of 'alkali dissolution and acid precipitation' for protein extraction are omitted, the extraction and hydrolysis of the protein are combined into one process, and the production period is greatly shortened;

the product yield is improved: substrates acted by protease in the hydrolysis procedure in the scheme are all protein components of an alkali-soluble part, the hydrolysis efficiency is higher than that of the traditional method for directly hydrolyzing protein, and especially, the yield of the hydrolyzed protein is improved more obviously by using raw materials containing gluten and other water-insoluble proteins with higher proportion; materials obtained in the steps of alkali extraction, concentration, filtration and the like are returned to the previous working procedure for recycling;

energy conservation and emission reduction: the discharged water is the permeated water filtered by the ultrafiltration membrane, and compared with the discharged water of the traditional alkali-dissolving acid-precipitating method, the content of organic matters in the water is greatly reduced, and the sewage treatment cost is saved; the recycling of the nanofiltration membrane permeate and the evaporation condensate reduces the water consumption and the production cost;

the method can improve the extraction efficiency of the protein peptide, increase the yield, reduce the discharge of high organic matter wastewater, reduce the environmental pollution and reduce the production input cost of enterprises, and has extremely wide market prospect.

Drawings

FIG. 1 is a process flow chart of a clean production method for industrially producing vegetable protein peptide according to the present invention.

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.