CN106366171B - Pilot production process and production line of white zein - Google Patents
Pilot production process and production line of white zein Download PDFInfo
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- CN106366171B CN106366171B CN201611104803.7A CN201611104803A CN106366171B CN 106366171 B CN106366171 B CN 106366171B CN 201611104803 A CN201611104803 A CN 201611104803A CN 106366171 B CN106366171 B CN 106366171B
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- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K14/00—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
- C07K14/415—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from plants
- C07K14/425—Zeins
Abstract
The invention discloses a production process and a production line of white zein, which are characterized in that corn gluten meal and ethanol aqueous solution are mixed and then subjected to dynamic multistage continuous countercurrent ultrasonic extraction; the extract is firstly filtered by a scraper filter to remove large-particle impurity components such as corn gluten meal and the like in the extracting solution, then filtered by a ceramic membrane to remove filter residues such as pectin fibers and the like in the extracting solution, and then filtered by an ultra-nanofiltration membrane to separate micromolecule substances such as corn yellow pigment and the like from zein; concentrating zein solution by ultrafiltration membrane, recovering ethanol solvent, vacuum concentrating, condensing, recovering ethanol for the second time, and precipitating with water to obtain zein wet powder; drying and crushing the zein wet powder to obtain a white zein product. The white zein produced by the invention has high quality, no solvent residue, green and healthy, improves the added value of the zein powder, and is beneficial to comprehensive development and utilization of the zein powder.
Description
Technical Field
The invention relates to a production process and a production line of white zein, and belongs to the technical field of zein processing.
Background
Zein is the major storage protein in corn and is about 45% of the total protein content of corn. It has unique solubility, is insoluble in water or absolute alcohols, but can be dissolved in alcohol aqueous solution with volume fraction of 60% -95%. Zein can be divided into four classes (α, β, γ, and δ) based on solubility and molecular mass size. Zein consists of specific amino acids, wherein a large number of hydrophobic amino acids exist in the molecule, and amino acids which can be charged, acidic, basic and polar groups are absent, but more sulfur-containing amino acids are contained; the special amino acid composition forms specific functional properties such as strong hygroscopicity, heat resistance, fat resistance and film forming property. The active peptide produced by using the method can be used as an additive of medical products with high protein content and the like, and can be widely applied to industries such as food, medicine, textile, paper making and the like.
However, the existing industrialized zein production mainly uses zein powder as a raw material, aqueous ethanol extraction is mostly adopted, and when zein is extracted, pigment (beta-carotene, lutein, zeaxanthin and the like) and peculiar smell substances in the raw material are dissolved out along with the extraction, so that a zein final product presents yellow color, the chromaticity of the zein final product cannot meet the application requirements of the international market, and the application of the zein in the fields of foods and medicines is limited. In contrast, white zein has a broader market prospect. Another factor limiting the development of food and pharmaceutical grade zein is the large amount of ethanol required to produce zein and the difficulty in recovery, resulting in excessive costs.
At present, related patents and documents report on the production process of white zein, but the white zein stays in a laboratory stage, and pilot-scale and large-scale production are not performed yet. In the earlier laboratory research of our subject group, the method for separating and extracting corn yellow pigment and zein from corn gluten meal by using membrane separation technology (patent CN 201610358358.0) is to mix the crushed corn gluten meal with ethanol water solution and carry out ultrasonic extraction under the light-proof condition; centrifuging after ultrasonic extraction to obtain supernatant; then, performing membrane separation on the supernatant to obtain a corn yellow pigment solution and a zein solution; concentrating the corn yellow pigment solution in vacuum to obtain red oily liquid which is the corn yellow pigment product; washing, precipitating and drying the zein solution to obtain white solid, namely zein. The protein content of the zein product is 90% -93% by mass fraction, which is far higher than the commercial domestic zein product (protein content 83.26%); the zein yield is 40% -46%. The invention further optimizes the conditions of ultrasonic extraction equipment, the membrane aperture and other factors and performs pilot test on the basis of the earlier experimental result of the subject group (patent CN 201610358358.0).
The pilot test is to make the scientific research result meet the market and industrialization requirements, reduce the transformation risk, and improve the transformation rate. The process aims at verifying, improving and perfecting laboratory achievements or theoretical achievements, eliminating various uncertainty factors, obtaining reliability data, parameters and intermediate product quality controllable inspection standards of related technologies and equipment of products, matching the reliability data, parameters and intermediate product quality controllable inspection standards with other related technologies, conforming to production reality and conforming to social requirements, so that new technologies are compliant to production, and new products are successfully brought to markets. Pilot test is an essential link for converting scientific and technological achievements into productivity, and success or failure of achievement industrialization mainly depends on success or failure of pilot test, so pilot test is important. For food-grade and pharmaceutical-grade zein with high requirements on production technology and product quality, a pilot-scale production line should be established, which has extremely important effect and significance for large-scale production of zein.
Disclosure of Invention
The invention aims at solving the problems of high cost, yellow color of products and the like in the prior art for producing zein, and provides a production process for white zein which ethanol is recycled for the second time and the production cost is low;
another object of the present invention is to provide a production line of white zein, so as to realize the large-scale production of white zein.
The invention provides a production process of white zein, which comprises the steps of mixing zein powder with ethanol water solution, and carrying out dynamic multistage continuous countercurrent ultrasonic extraction under a dark condition; the extract is firstly filtered by a duplex scraper filter to remove large-particle impurity components such as corn gluten meal and the like in the extract solution, then filtered by a ceramic membrane to remove filter residues such as pectin fibers and the like in the extract solution, and then filtered by an ultrafiltration membrane to separate corn yellow pigment, small molecular substances and zein to obtain zein solution; concentrating zein solution by ultrafiltration membrane, recovering ethanol solvent, vacuum concentrating, condensing, recovering ethanol, and precipitating with water to obtain zein wet powder; drying the zein wet powder in vacuum, crushing and vacuum packaging to obtain a white zein product.
60-95% of ethanol aqueous solution by volume, and the solid-liquid ratio of the corn protein powder to the ethanol aqueous solution is 1:3-1:25 kg/L.
The continuous countercurrent ultrasonic extraction process comprises the following steps: dynamic three-stage continuous countercurrent ultrasonic extraction is adopted, the extraction temperature is controlled to be 30-60 ℃, the ultrasonic frequency is 10-30 KHz, and the extraction time is 15-120 min; the stirring speed is 30-150 rpm.
The primary filtration process of the duplex scraper type filter comprises the following steps: the mesh number of the filter screen is 60-120 meshes, the filter pressure is-0.02-0.1 MPa, and the stirring speed is 70-120 revolutions per minute.
The ceramic membrane filtration process comprises the following steps: the pore diameter of the ceramic membrane is 50-100 um, the pressure is 0-10 bar, and the temperature is 20-100 ℃.
The ultrafiltration membrane filtration process comprises the following steps: the aperture of the ultrafiltration membrane is 10kDa to 80kDa, the pressure is 0 to 40bar, and the temperature is 20 ℃ to 100 ℃.
The ultrafiltration membrane protein concentration process comprises the following steps: the aperture of the ultrafiltration membrane is 360Da, the pressure range is 0-40 bar, the temperature is 20-40 ℃,
the vacuum concentration process comprises the following steps: concentrating at 30-45 ℃ and under the pressure of-0.02-0.1 MPa for 10-180 min until the alcohol concentration of the concentrate is 40%, and adding water to separate out zein.
The drying process comprises the following steps: the drying temperature is 30-60 ℃, the pressure is 0.2-0.9 kPa, and the drying time is 60-360 min.
The crushing process comprises the following steps: and crushing the zein powder into 100-200 meshes of zein powder at the temperature of 20-50 ℃.
Vacuum packaging: the packaging temperature is 20-50 ℃, the vacuum pressure is 0.1 Pa-0.1 MPa, the vacuumizing time is 1-30 s, the heat sealing temperature is 70-90 ℃, and the heat sealing time is 1-10 s.
The production process of the corresponding white zein comprises a feeding system, an extraction system, a filtering system, a concentration system, vacuum drying equipment, a pulverizer and a vacuum packaging machine. The structure of each system and the connection and cooperation between the systems will be described in detail.
The feeding system comprises a solvent blending tank, wherein a solvent filter is arranged at the inlet of the solvent blending tank, and the ethanol solution added into the solvent blending tank is filtered. An on-line solvent concentration measuring instrument and a solvent rheometer are arranged in the solvent blending tank, the on-line solvent concentration measuring instrument is used for measuring the concentration of the solvent ethanol in the solvent blending tank, and the solvent rheometer is used for measuring the volume quantity of the solvent added into the extraction circulation tank from the solvent blending tank. The solvent in the solvent blending tank is pumped into the extraction system by the solvent blending tank through a centrifugal pump.
The extraction system comprises a countercurrent extraction tank, wherein a stirring device is arranged in the countercurrent extraction tank, and an ultrasonic reactor communicated with the countercurrent extraction tank is arranged outside the countercurrent extraction tank, so that countercurrent extraction is carried out under ultrasonic conditions. The ultrasonic reactor may be a focused ultrasonic reactor. In order to improve extraction efficiency, the countercurrent extraction tank adopts three stages of continuous countercurrent extraction tanks, each stage of countercurrent extraction tank is communicated through a thick slurry diaphragm pump, and the last stage of countercurrent extraction tank is connected with a filtering system through the thick slurry diaphragm pump.
The filtering system sequentially comprises seven parts, namely a scraper filter, a coarse filtrate temporary storage tank, a ceramic membrane filter, a ceramic membrane filtrate temporary storage tank, an ultra-nanofiltration membrane filter and an ultra-nanofiltration filtrate protein temporary storage tank; wherein the scraper type filter is a two-joint scraper type filter, and a liquid outlet of the scraper type filter is pumped into the rough filtrate temporary storage tank through a thick slurry diaphragm pump; pumping the liquid of the rough filtrate temporary storage tank into a ceramic membrane filter through a thick slurry diaphragm pump; pumping filtrate of the ceramic membrane filter into a ceramic membrane filtrate temporary storage tank through a high-pressure centrifugal pump; the bottom of the ceramic membrane liquid filtration temporary storage tank is connected with the material inlet end of the ultra-nanofiltration membrane filter through a valve and a pipeline, and the solution at the material inlet end of the ultra-nanofiltration membrane filter is pumped into the ultra-nanofiltration membrane element through a thick slurry diaphragm pump, so that the feed liquid is filtered by a feed liquid inlet membrane; pumping the solution at the outlet end of the permeate of the ultrafiltration membrane filter into an ultrafiltration filtrate pigment temporary storage tank through a high-pressure centrifugal pump, and pumping the solution at the outlet end of the concentrate of the feed liquid of the ultrafiltration membrane filter into an ultrafiltration filtrate protein temporary storage tank through a thick slurry diaphragm pump; the bottom of the ultrafiltrate protein temporary storage tank is connected with the ultrafiltrate protein concentration equipment through a valve and a pipeline.
The concentration system comprises seven parts, namely a supernano filtrate protein concentration device, a protein concentrate temporary storage tank, a solvent recovery temporary storage tank, a scraper vacuum concentration device, a spiral wound pipe condenser, an ethanol recovery temporary storage tank and a protein precipitation device; the solution at the outlet end of the permeate of the ultra-nanofiltration filtrate protein concentration equipment is pumped into a solvent recovery temporary storage tank through a high-pressure centrifugal pump, and the solution at the outlet end of the feed liquid outlet membrane concentrate is pumped into a protein concentrate temporary storage tank through a thick slurry diaphragm pump; pumping the protein liquid in the protein concentrate temporary storage tank into scraper vacuum concentration equipment through a thick slurry diaphragm pump; the bottom of the scraper vacuum concentration device is connected with the protein precipitation device through a thick slurry diaphragm pump, the top of the scraper vacuum concentration device is connected with a spiral winding pipe condenser through a pipeline, and ethanol recovered by the spiral winding pipe condenser is pumped into an ethanol recovery temporary storage tank through a high-pressure centrifugal pump.
In summary, compared with the prior art, the invention has the following characteristics:
1. the dynamic multistage continuous countercurrent ultrasonic extraction technology and the membrane separation technology are combined to produce the zein, and the produced zein product has white color and high quality, so that the zein is not limited by the color, can be widely applied to the food and medicine industries, obviously improves the added value of the zein powder, and is beneficial to the comprehensive development and utilization of the zein powder;
2. the invention discloses a pilot-scale production line of white zein, which fills the blank of the production line of white zein. The production line carries out secondary recovery on the used solvent ethanol, realizes the recycling of the solvent, avoids the pollution of the solvent to the environment, reduces the production cost of zein, and simultaneously ensures that no solvent residue exists in the zein powder product, thereby being green and healthy.
Drawings
FIG. 1 is a structural layout of a pilot plant line feed system and extraction system of the present invention;
FIG. 2 is a structural layout of a three-stage continuous countercurrent extraction tank of the extraction system of the pilot production line of the present invention;
FIG. 3 is a schematic diagram of a doctor blade filter and a temporary coarse filtrate tank in a pilot line filtration system according to the present invention;
FIG. 4 is a structural layout of a ceramic membrane filter and a ceramic membrane filtrate temporary storage tank in a pilot production line filtration system of the invention;
FIG. 5 is a structural layout of an ultrafiltration membrane filter, an ultrafiltrate protein temporary storage tank and an ultrafiltrate pigment temporary storage tank in a pilot production line filtration system of the present invention;
FIG. 6 is a schematic diagram of the structure layout of the ultrafiltrate protein concentration device, the ultrafiltrate protein concentrate temporary storage tank and the solvent recovery temporary storage tank in the pilot production line concentration system of the present invention;
FIG. 7 is a schematic diagram of a scraper vacuum concentrating apparatus, a spiral wound tube condenser, an ethanol recovery temporary storage tank and a protein precipitation apparatus in a concentrating system of a pilot plant line according to the present invention.
Detailed Description
The pilot plant production process and production line of the white zein of the present invention are further described below by way of specific examples.
Example 1
(1) Solvent blending tank and solvent blending
The solvent filter is installed at the inlet of the solvent blending tank 1, and the ethanol solution added into the solvent blending tank is filtered. An on-line solvent concentration measuring instrument and a solvent rheometer are arranged in the solvent blending tank, the on-line solvent concentration measuring instrument is used for measuring the concentration of the solvent ethanol in the solvent blending tank, and the solvent rheometer is used for measuring the volume quantity of the solvent added into the extraction circulation tank from the solvent blending tank. The solvent in the solvent blending tank is pumped into the extraction system through the centrifugal pump 2.
And (3) solvent preparation: ethanol and water are added into a solvent blending tank, and an ethanol water solution is blended into a solution with the volume percentage of 80 percent.
(2) Three-stage continuous countercurrent extraction tank and extraction process thereof
The countercurrent extraction tank adopts a three-stage continuous countercurrent extraction tank 3, each stage of countercurrent extraction tank is communicated through a thick slurry diaphragm pump 6, and the last stage of countercurrent extraction tank is connected with the filtering system through the thick slurry diaphragm pump. A stirring device 4 is arranged in each stage of countercurrent extraction tank, and an ultrasonic reactor 5 communicated with the countercurrent extraction tank is arranged outside the countercurrent extraction tank, so that countercurrent extraction is carried out under ultrasonic conditions. The ultrasonic reactor may be a focused ultrasonic reactor.
Each stage of extraction process comprises the following steps: 15kg of corn gluten meal is added into a countercurrent extraction tank, and then 225L of 80% ethanol water solution is pumped in according to the solid-to-liquid ratio of the corn gluten meal to the ethanol solution of 1:15 kg/L. Then starting an energy-accumulating ultrasonic reactor for stirring and extracting, and carrying out ultrasonic extraction under the light-shielding closed condition, wherein the extraction temperature is 45 ℃, the ultrasonic frequency is 19.73KHz, and the extraction time is 60min; the stirring rate was 50 rpm.
(3) Scraper type filter and primary filter
The extracting solution of the continuous countercurrent ultrasonic extracting tank is subjected to coarse filtration by adopting a two-connected scraper type filter 7 so as to remove large-particle impurity components such as corn gluten meal and the like in the extracting solution. Filtrate at the liquid outlet of the scraper type filter is pumped into a rough filtrate temporary storage tank 8 through a thick slurry diaphragm pump 6.
Primary filtration: the number of the filter meshes of the scraper type filter is 80 meshes, the filtering pressure is-0.085 MPa, and the scraper speed of the scraper type filter is 90 revolutions per minute.
(4) Ceramic membrane filter and filtration
The liquid in the temporary storage tank of the coarse filtrate is filtered by a ceramic membrane filter 9 to remove impurities such as fiber, pectin and the like in the extraction solution. The liquid in the rough filtration temporary storage tank 8 is pumped into a ceramic membrane filter 9 through a thick slurry diaphragm pump 6 for filtration. Filtrate is pumped into the ceramic membrane filtrate temporary storage tank 10 by a high pressure centrifugal pump.
And (3) ceramic membrane filtration: the ceramic membrane filtration has a membrane pore size of 50um, a pressure of 2bar and a temperature of 24 ℃.
(5) Ultrafiltration membrane filter and filtration
The liquid in the ceramic membrane filter temporary storage tank 10 is filtered by adopting an ultrafiltration membrane filter 11, so that the pigment and zein are separated. And opening a valve at the bottom of the ceramic membrane liquid filtration temporary storage tank 10 to enable liquid in the ceramic membrane liquid filtration temporary storage tank to enter the ultrafiltration membrane filter 11 for filtration. The liquid at the permeate outlet end of the ultrafiltration membrane filter 11 is pumped into an ultrafiltration filtrate pigment temporary storage tank 13 through a centrifugal pump 2; the liquid at the outlet end of the concentrated liquid of the liquid outlet membrane of the ultra-nanofiltration membrane filter 11 is pumped into an ultra-nanofiltration filtrate protein temporary storage tank 12 through a thick liquid diaphragm pump 6. The bottom of the ultrafiltrate protein temporary storage tank 12 is connected with the ultrafiltrate protein concentration device 14 through a valve and a pipeline.
Ultra-nanofiltration filtration: the membrane pore size of the ultra-nanofiltration separation device was 10kDa, the pressure was 8bar and the temperature was 36 ℃.
(6) Protein concentration equipment for super-nano filtrate, protein concentration and ethanol recovery
The zein solution in the ultrafiltrate protein temporary storage tank 12 is concentrated using the ultrafiltrate protein concentration device 14. The valve at the bottom of the ultrafiltrate protein holding tank 12 is opened to allow zein solution to enter the ultrafiltrate concentration device 14. The permeate outlet end of the ultra-nanofiltration liquid protein concentration device 11 is pumped into a solvent recovery temporary storage tank 16 through a centrifugal pump 2 for recovery, and the liquid at the permeate outlet end of the permeate outlet membrane concentrate is pumped into a protein concentrate temporary storage tank 15 through a thick slurry membrane pump 6.
Protein concentration and ethanol recovery: the membrane aperture of the ultra-nanofiltration protein concentration equipment is 360Da, the pressure is 8bar, the temperature is 26 ℃, the zein is concentrated, and meanwhile, the ethanol is recovered.
(7) Scraper vacuum concentration equipment and vacuum concentration of protein
The liquid in the protein concentrate temporary storage tank 15 is vacuum-concentrated by a scraper vacuum concentration device 17. The protein liquid in the protein concentrate temporary storage tank 15 is pumped into the scraper vacuum concentration equipment 17 through the thick slurry diaphragm pump 6, the top of the scraper vacuum concentration equipment 17 is connected with the spiral winding pipe condenser 18 through a pipeline, and the ethanol recovered by the spiral winding pipe condenser is pumped into the ethanol recovery temporary storage tank 19 for recycling through the centrifugal pump 2 after being cooled.
Concentrating: the temperature is 35 ℃, the pressure is-0.085 MPa, the time is 60min, and the concentrated solution is pumped into protein precipitation equipment when the alcohol concentration in the concentrated solution is 40 percent.
(8) Vacuum drying
Drying zein wet powder at 50deg.C under 0.2kPa for 120min to obtain 5.925kg.
(9) Crushing
Pulverizing zein powder at 30deg.C to 120 mesh zein powder.
(10) Vacuum package
Vacuum packaging zein powder at room temperature under vacuum pressure of 0.1Pa for 2s at 70deg.C for 5s.
The zein yield produced by the production line and the process is 39.5%, the protein content is 89.25%, the chroma L value is 56.25 (L value is black and white) through detection, the a value is 3.28 (a value is red and green), and the b value is 3.65 (b value is blue and yellow).
Example 2
The structure and arrangement of the production line are the same as in example 1. The specific production process is controlled as follows:
(1) And (3) solvent preparation: ethanol and water are added into a solvent blending tank, and an ethanol water solution is blended into a solution with the volume percentage of 90 percent.
(2) Extracting: 15kg of corn gluten meal is added into a countercurrent extraction tank, and then 120L of ethanol water solution is pumped according to the solid-to-liquid ratio of the corn gluten meal to the ethanol solution of 1:8 kg/L. Then starting an energy-accumulating ultrasonic reactor for stirring and extracting, and carrying out ultrasonic extraction under the light-shielding closed condition, wherein the extraction temperature is 50 ℃, the ultrasonic frequency is 25KHz, and the extraction time is 45min; the stirring rate was 100 rpm.
(3) Primary filtration: the extract was pumped into a scraper filter of a separation system, the mesh size of the filter screen was 60 mesh, the filtration pressure was-0.1 MPa, and the scraper rate of the scraper filter was 120 rpm.
(4) And (3) ceramic membrane filtration: the ceramic membrane filtration has a membrane pore size of 80um, a pressure of 1.5bar and a temperature of 26 ℃.
(5) Ultra-nanofiltration filtration: the membrane pore size of the ultra-nanofiltration separation device was 15kDa, the pressure was 5bar and the temperature was 38 ℃.
(6) Protein concentration and ethanol recovery: the membrane aperture of the ultra-nanofiltration protein concentration equipment is 360Da, the pressure is 5bar, the temperature is 28 ℃, and the ethanol recovery is carried out.
(7) Concentrating: concentrating the ultra-nanofiltration filtrate in a scraper vacuum concentrating device at 45deg.C under-0.02 MPa for 30 min, and pumping into a protein precipitation device when the alcohol concentration in the concentrated solution is 40%, and precipitating to obtain zein wet powder by adding water into the protein precipitation device. And recovering the ethanol obtained by concentration.
(8) And (3) drying: the drying temperature is 45 ℃, the pressure is 0.5kPa, and the drying time is 180 minutes, thus obtaining 5.37kg of white zein dry powder.
(9) Crushing: pulverizing zein powder at 35deg.C to 150 mesh zein powder.
(10) And (3) packaging: vacuum packaging zein powder at room temperature under vacuum pressure of 0.5Pa for 10s at 80deg.C for 10s.
The zein yield produced by the production line and the process is 35.8%, the protein content is 91.65%, the chroma L value is 50.32 (L value is black and white) through detection, the a value is 4.86 (a value is red and green), and the b value is 8.92 (b value is blue and yellow).
Example 3
The structure and arrangement of the production line are the same as in example 1. The specific production process is controlled as follows:
(1) And (3) solvent preparation: ethanol and water are added into a solvent blending tank, and an ethanol water solution is blended into a solution with the volume percentage of 85 percent.
(2) Extracting: 15kg of corn gluten meal is added into a countercurrent extraction tank, and then 150L of ethanol water solution is pumped according to the solid-to-liquid ratio of the corn gluten meal to the ethanol solution of 1:10 kg/L. Then starting an energy-accumulating ultrasonic reactor for stirring and extracting, and carrying out ultrasonic extraction under the light-shielding closed condition, wherein the extraction temperature is 40 ℃, the ultrasonic frequency is 15KHz, and the extraction time is 90min; the stirring rate was 80 rpm.
(3) Primary filtration: the extract was pumped into a scraper filter of a separation system with a mesh number of 100 mesh, a filtration pressure of-0.02 MPa and a scraper rate of 100 rpm.
(4) And (3) ceramic membrane filtration: the ceramic membrane filtration has a membrane pore size of 100um, a pressure of 1bar and a temperature of 28 ℃.
(5) Ultra-nanofiltration filtration: the membrane pore size of the ultra-nanofiltration separation device was 10kDa, the pressure range was 8bar and the temperature was 36 ℃.
(6) Protein concentration and ethanol recovery: the membrane aperture of the ultra-nanofiltration protein concentration equipment is 360Da, the pressure is 8bar, the temperature is 27 ℃, and the ethanol recovery is carried out.
(7) Concentrating: concentrating the ultra-nanofiltration filtrate in a scraper vacuum concentrating device at 40deg.C under-0.1 MPa for 45min, and pumping into a protein precipitation device when the alcohol concentration in the concentrated solution is 40%, and precipitating to obtain zein wet powder by adding water into the protein precipitation device. And recovering the ethanol obtained by concentration.
(8) And (3) drying: the drying temperature was 40℃and the pressure was 0.8kPa, and the drying time was 150 minutes.
(9) Crushing: pulverizing zein powder at 30deg.C to 120 mesh zein powder.
(10) And (3) packaging: vacuum packaging zein powder at room temperature under vacuum pressure of 0.5Pa for 10s at 90deg.C for 2s.
The zein yield produced by the production line and the process is 36.2%, the protein content is 90.53%, the chroma L value is 48.65 (L value is black and white) through detection, the a value is 2.15 (a value is red and green), and the b value is 5.87 (b value is blue and yellow).
All electrical equipment such as motors, diaphragm slurry pumps, centrifugal pumps and the like in the production line are required to be explosion-proof.
Claims (2)
1. A process for preparing white zein includes such steps as mixing corn protein powder with aqueous solution of alcohol, and ultrasonic extracting in multistage continuously and counter-current mode; the extract is firstly filtered by a scraper filter to remove large particle impurity components in the extracting solution, then filtered by a ceramic membrane to remove pectin fibers in the extracting solution, and then filtered by an ultrafiltration membrane to separate corn yellow pigment and micromolecular substances from zein, thus obtaining zein liquid; concentrating zein solution by ultrafiltration membrane, recovering ethanol solvent, vacuum concentrating, condensing, recovering ethanol, and precipitating with water to obtain zein wet powder; drying, crushing and vacuum packaging the zein wet powder to obtain a white zein product;
the dynamic multistage continuous countercurrent ultrasonic extraction process comprises the following steps: dynamic three-stage continuous countercurrent ultrasonic extraction is adopted, the extraction temperature is 30-60 ℃, the ultrasonic frequency is 10-30 KHz, and the extraction time is 15-120 min; the stirring speed is 30-150 rpm;
the primary filtration process comprises the following steps: the mesh number of the scraper type filter is 60-120 meshes, the filtering pressure is-0.02-0.1 MPa, and the stirring speed is 70-120 revolutions per minute;
the ceramic membrane filtration process comprises the following steps: the pore diameter of the ceramic membrane is 50-100 um, the pressure is 0-10 bar, and the temperature is 20-100 ℃;
the ultrafiltration membrane filtration process comprises the following steps: the aperture of the ultrafiltration membrane is 10 kDa-80 kDa, the pressure is 0-40 bar, and the temperature is 20-100 ℃;
the ultrafiltration membrane concentration process comprises the following steps: the aperture of the ultrafiltration membrane is 360Da, the pressure range is 0-40 bar, and the temperature is 20-40 ℃;
the vacuum concentration process comprises the following steps: concentrating at 30-45 ℃ and under the pressure of-0.02-0.1 MPa for 10-180 min until the alcohol concentration in the concentrate is 40%, pumping the zein concentrate into protein precipitation equipment, and adding water into the protein precipitation equipment to separate out zein wet powder; and recovering the ethanol obtained by concentrating and condensing.
2. The process for producing white zein according to claim 1, wherein: 60-95% of ethanol aqueous solution by volume, and the solid-liquid ratio of the corn protein powder to the ethanol aqueous solution is 1:3-1:25 kg/L.
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