A protein separation, concentration and recovery system

Abstract

The present invention belongs to the technical field of protein recovery, in particular to a protein separation, concentration and recovery system, which comprises: a stock liquid pool, a sedimentation module, a concentration module and a mud storage barrel; the upper layer of stock liquid in the stock liquid pool flows into the sedimentation module for sedimentation, the precipitated protein liquid in the sedimentation module is transported to the mud storage barrel, and the supernatant in the sedimentation module is transported to the concentration module; the concentration module is used to filter small particle proteins in the supernatant, the filtered filtrate is discharged, and the high-concentration protein liquid flows back into the sedimentation module; the concentration module comprises: a concentration pool, wherein a plurality of filter components are provided in the concentration pool, which are used to filter small particle proteins in the supernatant; the present invention first separates large particle proteins through the sedimentation module, and then separates small particle proteins in the supernatant through the concentration module, and the low-concentration protein liquid after separation flows back into the sedimentation module for continued precipitation, thereby completing the recovery of protein in the supernatant.

Description

Technical Field

[0001] The present invention relates to the technical field of protein recovery, in particular to a protein separation, concentration and recovery system. Background Art

[0002] During corn starch processing, corn kernels are soaked in sulfurous acid to break down the germ and bran fibers, then wet-milled to form a mixture of corn protein and starch. Centrifugation produces starch milk and protein slurry (gluten slurry). The starch milk, which still contains protein, must be washed with water and centrifuged again to produce pure starch milk and a supernatant containing small proteins. The protein slurry (gluten slurry) is further concentrated by centrifugation to produce a high-concentration gluten slurry and a supernatant containing small proteins. The above process recovers corn starch and corn protein, respectively. The two supernatants are collectively referred to as the supernatant.

[0003] The traditional method of recovering corn supernatant liquid is to recover protein by precipitation, but the recovery efficiency is low. The clear liquid after precipitation is generally discharged as wastewater. However, the composition of the supernatant liquid is complex, and it contains some small particles of alcohol-soluble protein that cannot be separated by centrifugation. The mass percentage of this particle in this solution is about 0.5-1%. Although it is much lower than the corn protein slurry separated by centrifugation with a content of more than 10%, its protein purity is higher and its value is relatively greater. Moreover, for the large-scale corn processing industry, its cumulative total amount cannot be underestimated. Therefore, recovering corn alcohol-soluble protein in the supernatant liquid has very high social and economic value. Summary of the Invention

[0004] In response to the shortcomings of the existing technology, the present invention provides a protein separation, concentration and recovery system, which is equipped with a concentration module to recover the protein in the supernatant of corn starch, thereby overcoming the shortcomings of the existing technology of directly discharging the supernatant and causing waste of resources.

[0005] In order to achieve the above technical objectives, the specific technical scheme of the present invention is as follows: the present invention proposes a protein separation, concentration and recovery system, comprising: a raw liquid pool, a sedimentation module, a concentration module and a mud storage barrel; the upper raw liquid in the raw liquid pool flows into the sedimentation module for sedimentation, the precipitated protein liquid in the sedimentation module is transported to the mud storage barrel, and the supernatant in the sedimentation module is transported to the concentration module; the concentration module is used to filter the small particle protein in the supernatant, and the filtered filtrate is discharged and the high-concentration protein liquid flows back into the sedimentation module; the concentration module comprises: a concentration pool, and a plurality of groups of filtering components are provided in the concentration pool for filtering the small particle protein in the supernatant; the filtering component comprises a filtrate extraction pipe, a concentrate extraction pipe and a cylindrical filter cartridge, and the output ends of the filter cartridge are connected to the filtrate extraction pipe and the concentrate extraction pipe; the filter cartridge is used to concentrate and filter the supernatant in the concentration pool, and after filtration, the high-concentration protein liquid is extracted through the concentrate extraction pipe and the filtrate is extracted through the filtrate extraction pipe.

[0006] As a preferred technical solution of the present invention, a filter chamber and a filtrate chamber are provided in the filter cartridge, and a water inlet and a concentrated liquid outlet are respectively provided on the filter chamber. The supernatant enters the filter chamber through the water inlet, and a filtrate outlet is provided on the filtrate chamber, wherein the filtrate outlet is connected to the filtrate suction pipe, and the concentrated liquid outlet is connected to the concentrated liquid suction pipe.

[0007] As a preferred technical solution of the present invention, a plurality of hollow filter membranes are provided in the filter chamber for filtering the supernatant, and the upper end of the hollow filter membrane is set as an open structure and the lower end is set as a closed structure.

[0008] As a preferred technical solution of the present invention, the upper end of the hollow filter membrane is cast on the top of the filter chamber and extends into the filtrate chamber, and the lower end of the hollow filter membrane swings freely in the filter chamber.

[0009] As a preferred technical solution of the present invention, the filter chamber is provided with an aeration inlet, through which gas enters the filter chamber and is extracted together with the high-concentration protein liquid through the concentrated liquid outlet.

[0010] As a preferred technical solution of the present invention, the surface pore size of the hollow filter membrane ranges from 20 nm to 50 nm.

[0011] As a preferred technical solution of the present invention, the surface of the hollow filter membrane is provided with hydroxyl groups and carboxyl groups, and the contact angle between the surface of the hollow filter membrane and water is less than 60 degrees.

[0012] As a preferred technical solution of the present invention, it also includes a filter press module, and the high-concentration protein in the mud storage barrel is transported to the filter press module. The high-concentration protein liquid is pressed into a protein mud cake for recovery through the filter press module, and the filtrate is returned to the original liquid pool.

[0013] The beneficial effects of the present invention are:

[0014] 1. The present invention is provided with a sedimentation module and a concentration module. The sedimentation module first separates the large particle protein, and then the small particle protein in the supernatant is separated by the concentration module. The low-concentration protein liquid after separation flows back into the sedimentation module for further precipitation. The high-concentration protein after precipitation is pressed into a filter cake by the filter press module to complete the protein recovery in the supernatant.

[0015] 2. The concentration module of the present invention is provided with multiple groups of filtering components, each of which is provided with a filter cartridge, a filtrate extraction tube and a concentrate extraction tube. A plurality of hollow filter membranes are provided in the filter cartridge. The hollow filter membrane has a high protein recovery rate and a fast recovery efficiency, thereby being able to recover the maximum amount of protein molecules in the supernatant. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 This is a schematic diagram of a protein separation, concentration and recovery system proposed by the present invention.

[0017] Figure 2 This is a schematic structural diagram of the concentration module proposed in the present invention.

[0018] Figure 3 Schematic diagram of the structure of the filter assembly of the present invention.

[0019] Figure 4 This is a schematic cross-sectional view of the filter cartridge proposed in the present invention.

[0020] In the figure: 1. Raw liquid tank; 2. Sedimentation module; 3. Concentration module; 31. Concentration tank; 32. Filter assembly; 321. Filter cartridge; 3211. Filtrate chamber; 3212. Concentrate outlet; 3213. Filtered liquid outlet; 3214. Aeration inlet; 3215. Water inlet; 3216. Filter chamber; 3217. Hollow filter membrane; 322. Filtered liquid extraction pipe; 323. Concentrated liquid extraction pipe; 4. Mud storage tank; 5. Filter press module. DETAILED DESCRIPTION

[0021] The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all the embodiments.

[0022] Example 1: This example discloses a protein separation, concentration and recovery system. Figure 1 As shown, it includes: a raw liquid pool 1, a sedimentation module 2, a concentration module 3, a mud storage barrel 4 and a filter press module 5; after the corn is separated, the upper raw liquid is collected in the raw liquid pool 1, and the upper raw liquid in the raw liquid pool 1 flows into the sedimentation module 2 for sedimentation, wherein the sedimentation module 2 is an inclined plate sedimentation tank or an inclined tube sedimentation tank, and large particles of protein sink to the bottom of the sedimentation module 2 to form a high-concentration precipitated protein liquid, and the precipitated protein liquid is transported to the mud storage barrel 4 to form a high-concentration protein, and the small particles of protein in the sedimentation module 2 are transported to the concentration module 3 along with the supernatant; the concentration module 3 then filters the small particle protein in the supernatant, and the filtered filtrate is directly After discharge and filtration, small particle proteins adhere together to form large particle flocs, and the large particle flocs form a high-concentration protein liquid with the liquid in the concentration module and flow back into the sedimentation module 2. The large particle flocs and the large particle protein are settled together to form a cycle; wherein, the high-concentration protein in the mud storage barrel 4 is transported to the filter press module 5, and the filter press module 5 adopts a frame plate filter press. The high-concentration protein is pressed into a protein mud cake by the filter press module 5 for recovery, and the filtrate filtered out is returned to the stock liquid pool 1. The filtrate contains a small amount of protein molecules and enters the sedimentation module again for sedimentation, thereby achieving maximum recovery of protein in the upper stock liquid.

[0023] like Figure 2-3As shown, the concentration module 3 includes: a concentration tank 31, the bottom of the concentration tank 31 is bucket-shaped, and multiple groups of filter components 32 are provided in the concentration tank 31 for filtering small particle proteins in the supernatant; the filter component 32 includes a filtrate suction pipe 322, a concentrate suction pipe 323 and a cylindrical filter cartridge 321, and the output ends of the filter cartridge 321 are connected to the filtrate suction pipe 322 and the concentrate suction pipe 323, and the filtrate suction pipe 322 and the concentrate suction pipe 323 are both connected to an external water pump, which is powered by the water pump; wherein, the filter cartridge 321 is used to concentrate and filter the supernatant in the concentration tank 31, and after filtration, the high-concentration protein liquid is extracted through the concentrate suction pipe 323 and the filtrate is extracted through the filtrate suction pipe 322, and the high-concentration protein liquid is transported to the sedimentation module 2 for further precipitation, and the filtrate is directly discharged after being extracted.

[0024] like Figure 4 As shown, the filter cartridge 321 is provided with a filter chamber 3216 and a filtrate chamber 3211. The filtrate chamber 3211 is provided above the filter chamber 3216. The filter chamber 3216 is provided with a plurality of hollow filter membranes 3217 for filtering the supernatant. The cross section of the hollow filter membrane 3217 is circular. The surface of the hollow filter membrane 3217 is provided with hydroxyl and carboxyl groups. The contact angle between the surface of the hollow filter membrane 3217 and water is less than 60 degrees, which prevents protein adhesion and contamination, and avoids the hollow filter membrane The pore size of the surface of 3217 is blocked, the upper end of the hollow filter membrane 3217 is set as an open structure and the lower end is set as a closed structure. The upper end of the hollow filter membrane 3217 is cast on the top of the filter chamber 3216 and extends into the filtrate chamber 3211, and the lower end of the hollow filter membrane 3217 is free to swing in the filter chamber 3216. The method of sealing the hollow filter membrane 3217 can use a hot melt pressure sealing method, or a method of dripping PVDF organic solution and then soaking in water to solidify; wherein, The hollow filter membrane 3217 is about 1 meter long and has a surface pore size of 20-50 nm. The hollow filter membrane 3217 can withstand water temperatures of no less than 55°C. The filter chamber 3216 is provided with a water inlet 3215 and a concentrate outlet 3212, and the filtrate chamber 3211 is provided with a filtrate outlet 3213. The filtrate outlet 3213 is connected to the filtrate extraction pipe 322, and the concentrate outlet 3212 is connected to the concentrate extraction pipe 323. The supernatant The supernatant enters the filter chamber 3216 through the water inlet 3215, and flows from bottom to top in the filter chamber 3216. During the flow, the supernatant is filtered by the hollow filter membrane 3217. After filtration, the filtrate enters the filtrate chamber 3211 from the upper opening of the hollow filter membrane 3217. Small particle protein adheres to the surface of the hollow filter membrane 3217 to form larger flocs, which are regularly extracted from the concentrated liquid outlet 3212 through the concentrated liquid extraction tube 323.

[0025] Preferably, the filter chamber 3216 is provided with an aeration inlet 3214, which is connected to an external air pipe. The gas enters the filter chamber 3216 through the aeration inlet 3214 and is extracted together with the high-concentration protein liquid through the concentrate outlet 3212. The protein content of the liquid entering the sedimentation module 2 after the supernatant is concentrated is not less than 2%, and is finally discharged into the mud storage barrel 4. Finally, the liquid containing high-concentration protein particles in the mud storage barrel 4 is pumped into the plate and frame filter press and pressed into a mud cake, and the protein separation, concentration and recovery process is completed.

[0026] Example 2: The recovery system of Example 1 of the present invention was used to conduct an experiment on the upper layer of raw liquid in the process of a corn starch production enterprise. The upper layer of raw liquid was filtered using a hollow filter membrane 3217 with a pore size of 50 nm. Equal weights of the upper layer of raw liquid (the total dry matter content of the upper layer of raw liquid was about 1.9-2.4%, of which alcohol-soluble proteins accounted for 0.3-1%; carbohydrates accounted for 0.5-0.8%, and the remainder was fat, salt, lactic acid, amino acids, etc.) and the filtrate were taken, and dried to obtain dry matter. Multiple groups of experiments were conducted to detect the dry matter content percentage and obtain M in and M out , the difference M p =M in -M out (M p The experimental data of multiple groups of experiments are shown in Table 1 below. Table 1 shows the experimental data of the recovery of alcohol-soluble proteins:

[0027] Table 1

[0028] Serial number <![CDATA[Original liquid dry matter M in (%)]]> <![CDATA[Filtered liquid dry matter M out (%)]]> <![CDATA[Recovery amount M p (%)]]> 1 3.1 2.3 0.8 2 2.75 2.11 0.64 3 2.7 2.47 0.23 4 3.06 2.74 0.32 5 2.61 2.26 0.35 6 2.98 2.09 0.89 7 2.9 2.2 0.7 8 2.92 2.18 0.74 9 2.51 2.07 0.44 10 3.1 2.7 0.4 11 3.4 2.3 1.1 12 3.41 2.4 1.01 13 3.47 2.59 0.88 14 3 2.7 0.3 15 3 2.6 0.4 16 3 2.3 0.7 17 3.27 2.96 0.31 18 3.01 2.7 0.31 19 2.8 2.4 0.4 20 3.4 3 0.4 21 3.8 2.7 1.1 22 2.4 2 0.4 23 2.3 2 0.3 24 2.3 1.7 0.6 25 2.2 1.7 0.5 26 2.3 1.9 0.4 27 2.3 1.6 0.7 28 2.4 2 0.4 29 2.3 1.6 0.7 30 2.4 2 0.4 31 2.35 2.12 0.23 32 3.5 2.7 0.8 33 3.3 2.5 0.8 34 3.07 2.56 0.51 35 3 2.5 0.5 36 3.1 2.3 0.8 37 2.4 1.6 0.8 38 2.7 2.2 0.5 39 2.34 2.07 0.27 40 2.6 2.1 0.5

[0029] It can be obtained by calculation from Table 1 above that the recovery rate M of alcohol-soluble protein using the recovery system of the present invention is p The average value is about 0.56%, which is equivalent to about 5.6 kg of alcohol-soluble protein being recovered from every ton of upper liquid, which not only solves the problem of resource waste, but also solves the problem of environmental pollution.

[0030] Example 3: The recovery system of Example 2 of the present invention is used to filter the upper liquid using a hollow filter membrane 3217 with a pore size of 50 nm. Then, equal weights of the upper liquid and the filtrate are taken and filtered repeatedly until a filter cake is formed and the filtered water is clear. Multiple groups of experiments are performed, and the filter cake after the upper liquid is dried and the weight W is recorded. in Filter the filtrate and dry the filter cake to record the weight W f , the recovery rate is Rec, where , the experimental data are shown in Table 2 below, which is the experimental data of the recovery rate of alcohol-soluble protein:

[0031] Table 2

[0032] Serial number <![CDATA[Weight (g / ml) of prolamine in the stock solution W in > <![CDATA[Weight (g / ml) of gliadin in the filtrate W f > <![CDATA[Recovery rate R ec (W in -W f ) / W in *100%]]> 1 0.0305 0.0029 99.62 2 0.248 0.0081 96.73 3 0.0316 0.0102 98.71 4 0.0502 0.0206 98.36 5 0.0986 0.0073 99.70 6 0.0498 0.004 99.68 7 0.0453 0.0065 99.43 8 0.032 0.0099 98.76 9 0.0597 0.0069 99.54 10 0.0552 0.0229 98.34 11 0.0772 0.0063 99.67 12 0.0213 0.0284 94.67 13 0.0456 0.0063 99.45 14 0.0341 0.0032 99.62 15 0.03217 0.004 99.55 16 0.0596 0.0066 99.56 17 0.0586 0.0039 99.73 18 0.0328 0.013 98.41 19 0.0497 0.0083 99.33 20 0.0268 0.0035 99.48 21 0.0244 0.0034 99.44 22 0.025 0.0041 99.34 23 0.0264 0.0102 98.45 24 0.0323 0.0103 98.72 25 0.0331 0.0102 98.77 26 0.0217 0.0064 98.82 27 0.0188 0.0037 99.21

[0033] It can be calculated from Table 2 above that the average recovery rate of alcohol-soluble proteins in the upper liquid by the recovery system of the present invention is about 99%, and the protein recovery efficiency is extremely high.

[0034] Finally, it should be noted that in the description of the present invention, it should be noted that the terms "vertical", "up", "down", "horizontal", etc., indicating orientations or positional relationships, are based on the orientations or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation. Therefore, they cannot be understood as limiting the present invention.

[0035] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art will be able to modify the technical solutions described in the aforementioned embodiments or replace some of the technical features therein with equivalents. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present invention shall be included within the scope of protection of the present invention.

Claims

1. A protein separation, concentration and recovery system, characterized in that: include: Raw liquid tank (1), sedimentation module (2), concentration module (3) and sludge storage tank (4); The upper layer of the raw liquid in the raw liquid pool (1) flows into the sedimentation module (2) for sedimentation, the precipitated protein liquid in the sedimentation module (2) is transported to the mud storage barrel (4), and the supernatant in the sedimentation module (2) is transported to the concentration module (3); The concentration module (3) is used to filter the small particle protein in the supernatant, and the filtered filtrate is discharged and the high-concentration protein solution flows back into the sedimentation module (2); The concentration module (3) comprises: a concentration tank (31), wherein a plurality of filter components (32) are provided in the concentration tank (31) for filtering small particle proteins in the supernatant; the filter components (32) comprise a filtrate extraction pipe (322), a concentrate extraction pipe (323), and a cylindrical filter cartridge (321), wherein the output ends of the filter cartridge (321) are connected to the filtrate extraction pipe (322) and the concentrate extraction pipe (323); The filter cartridge (321) is used to concentrate and filter the supernatant in the concentration tank (31); after filtration, the high-concentration protein liquid is extracted through the concentrated liquid extraction pipe (323), and the filtrate is extracted through the filtrate extraction pipe (322); The filter cartridge (321) is provided with a filter chamber (3216) and a filtrate chamber (3211), the filter chamber (3216) being provided with a water inlet (3215) and a concentrated liquid outlet (3212), respectively; supernatant liquid enters the filter chamber (3216) through the water inlet (3215), and the filtrate chamber (3211) is provided with a filtrate outlet (3213), wherein the filtrate outlet (3213) is connected to a filtrate extraction pipe (322), and the concentrated liquid outlet (3212) is connected to a concentrated liquid extraction pipe (323); A plurality of hollow filter membranes (3217) are provided in the filter chamber (3216) for filtering the supernatant. The upper end of the hollow filter membrane (3217) is configured as an open structure, and the lower end is configured as a closed structure.

2. A protein separation, concentration and recovery system according to claim 1, characterized in that: The upper end of the hollow filter membrane (3217) is cast on the top of the filter chamber (3216) and extends into the filtrate chamber (3211), and the lower end of the hollow filter membrane (3217) swings freely in the filter chamber (3216).

3. A protein separation, concentration and recovery system according to claim 2, characterized in that: The filter chamber (3216) is provided with an aeration inlet (3214), through which gas enters the filter chamber (3216) and is extracted together with the high-concentration protein liquid through the concentrated liquid outlet (3212).

4. A protein separation, concentration and recovery system according to claim 3, characterized in that: The surface pore size of the hollow filter membrane (3217) ranges from 20 nm to 50 nm.

5. A protein separation, concentration and recovery system according to claim 4, characterized in that: The surface of the hollow filter membrane (3217) is provided with hydroxyl groups and carboxyl groups, and the contact angle between the surface of the hollow filter membrane (3217) and water is less than 60 degrees.

6. A protein separation, concentration and recovery system according to claim 5, characterized in that: It also includes a filter press module (5), wherein the high-concentration protein in the mud storage barrel (4) is transported to the filter press module (5), and the high-concentration protein liquid is pressed into a protein mud cake through the filter press module (5) for recovery, and the filtrate is returned to the original liquid pool (1).

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