Membrane filtration system for producing high-activity whole milk protein powder

Abstract

The utility model relates to the technical field of milk protein production, in particular to a membrane filtration system for producing high-activity whole milk protein powder, which comprises an ultrafiltration membrane group, a nanofiltration membrane group and a backwashing component, the ultrafiltration membrane group comprises a first ultrafiltration membrane group and a second ultrafiltration membrane group, and the second ultrafiltration membrane group is arranged behind the first ultrafiltration membrane group; the backwashing assembly is arranged between the first ultrafiltration membrane group and the second ultrafiltration membrane group, and an outlet of the backwashing assembly is connected with an inlet of the second ultrafiltration membrane group; the nanofiltration membrane group is arranged behind the second ultrafiltration membrane group. By adopting the membrane filtration system combining the ultrafiltration membrane group and the nanofiltration membrane group, the protein content in the finally produced concentrated protein liquid can be increased, and the backwashing assembly can take away more lactose, so that the protein content is increased, and the protein content in the finally produced concentrated protein liquid reaches 25%.

Description

Technical Field

[0001] The utility model relates to the technical field of milk protein production, in particular to a membrane filtration system for producing high-activity whole milk protein powder. Background Art

[0002] Concentrated milk protein powder (MPC) refers to a dairy product made from raw cow milk (with or without other dairy ingredients added), which is processed through processes such as milk purification, pasteurization, skimming (or not skimming), ultrafiltration and concentration, etc., to remove some of the water, fat, lactose and minerals, and then dried and powdered. It is widely used in products such as yogurt, dairy drinks, neutral milk, baked goods, meat products, sports nutrition foods, etc.

[0003] In order to increase the protein content in the prior art, the production process adopted is: after the raw milk is inspected, it is preheated and centrifuged to obtain skimmed milk; after the skimmed milk is pasteurized, it is transported to an ultrafiltration membrane device and a concentration factor is set, and the temperature of the system is controlled so that the skimmed milk constructs solids in the ultrafiltration membrane device to obtain a concentrated retentate; the concentrated solution is then preheated, further evaporated and concentrated, and then spray-dried to obtain concentrated milk protein powder. For example, the Chinese invention patent with application number CN201811364180.6 discloses a concentrated milk protein liquid and a preparation method thereof, wherein the raw milk is preheated and sterilized; the sterilized raw milk is fed into a centrifuge for milk fat separation to obtain skim milk; the skim milk is pasteurized for the first time; the skim milk that has been pasteurized for the first time is ultrafiltered and concentrated, so that the water, lactose and ash in the skim milk are removed with the permeate to obtain a concentrated liquid; the concentrated liquid is pasteurized for the second time ("post-pasteurization") to obtain the concentrated milk protein liquid; while the ultrafiltration and concentration are being performed, reverse osmosis water can be continuously added to the retentate side for diafiltration to obtain a higher concentration of concentrated liquid. Although the method of combining ultrafiltration with diafiltration in the above method can remove part of the water, lactose and ash in the milk and obtain a milk protein product with a higher protein content to a certain extent, there are still some shortcomings for the application field of high-protein dairy products, such as the protein purity needs to be further improved and the protein activity is insufficient. Summary of the invention

[0004] Based on this, the utility model provides a membrane filtration system for producing high-activity whole milk protein powder, so as to solve the technical problems in the prior art that the protein purity needs to be further improved and the protein activity is insufficient.

[0005] The technical solution of the utility model to solve the above technical problems is as follows:

[0006] A membrane filtration system for producing highly active whole milk protein powder, comprising:

[0007] An ultrafiltration membrane group, the ultrafiltration membrane group comprising a first ultrafiltration membrane group and a second ultrafiltration membrane group, the inlet of the first ultrafiltration membrane group is provided with a first electric valve, the outlet of the first electric valve is provided with a first filter, and the first ultrafiltration membrane group is provided with a first retentate outlet and a first permeate outlet; the inlet of the second ultrafiltration membrane group is connected to the first retentate outlet, the first retentate outlet is provided with a second electric valve, and the second ultrafiltration membrane group is provided with a second retentate outlet and a second permeate outlet;

[0008] A backwash component comprises a backwash water tank and a backwash electric valve, wherein the inlet of the backwash electric valve is connected to the outlet of the backwash water tank, and the outlet of the backwash electric valve is connected to the inlet of the second ultrafiltration membrane group.

[0009] The nanofiltration membrane group has an inlet connected to the second retentate outlet, a third electric valve is provided at the inlet of the nanofiltration membrane group, and the nanofiltration membrane group has a third permeate outlet and a third retentate outlet.

[0010] Preferably, the membrane filtration system for producing highly active whole milk protein powder further comprises a permeate recovery device, the inlet of the permeate recovery device being respectively connected to the first permeate outlet, the second permeate outlet and the third permeate outlet for recovering the permeate.

[0011] Preferably, the membrane filtration system for producing highly active whole milk protein powder further comprises a reverse osmosis device, the outlet of the permeate recovery device is connected to the inlet of the reverse osmosis device, and the outlet of the reverse osmosis device is connected to the inlet of the backwash water tank.

[0012] Preferably, in the above-mentioned membrane filtration system for producing highly active whole milk protein powder, a first heat exchange component is also provided at the inlet of the first ultrafiltration membrane group, the first heat exchange component comprises a first heat exchanger and a first temperature measuring device located at the outlet of the first heat exchanger, and the inlet of the first heat exchanger is connected to the outlet of the first electric valve.

[0013] Preferably, in the above-mentioned membrane filtration system for producing highly active whole milk protein powder, a second heat exchange component is also provided at the inlet of the nanofiltration membrane group, the second heat exchange component includes a second heat exchanger and a second temperature measuring device located at the outlet of the second heat exchanger, and the inlet of the second heat exchanger is connected to the outlet of the third electric valve.

[0014] Preferably, in the membrane filtration system for producing highly active whole milk protein powder, the third permeate outlet is provided with a second filter, and the outlet of the second filter is provided with a fourth electric valve.

[0015] Preferably, in the above-mentioned membrane filtration system for producing highly active whole milk protein powder, the first ultrafiltration membrane group includes at least 4 stages of ultrafiltration membrane tubes, each stage of the ultrafiltration membrane tubes includes at least 2 ultrafiltration membrane tubes, each of the ultrafiltration membrane tubes includes at least 3 ultrafiltration membrane cores, the ultrafiltration membrane cores are connected in series, and the ultrafiltration membrane core is a spiral wound membrane.

[0016] Preferably, in the above-mentioned membrane filtration system for producing highly active whole milk protein powder, the second ultrafiltration membrane group includes at least 4 stages of ultrafiltration membrane tubes, each stage of the ultrafiltration membrane tubes includes at least 2 ultrafiltration membrane tubes, each of the ultrafiltration membrane tubes includes at least 3 ultrafiltration membrane cores, the ultrafiltration membrane cores are connected in series, and the ultrafiltration membrane core is a spiral wound membrane.

[0017] Preferably, in the above-mentioned membrane filtration system for producing highly active whole milk protein powder, the nanofiltration membrane group includes at least 5 stages of nanofiltration membrane tubes, each stage of the nanofiltration membrane tubes includes at least 2 nanofiltration membrane tubes, each of the nanofiltration membrane tubes includes at least 2 nanofiltration membrane cores, the nanofiltration membrane cores are connected in series, and the nanofiltration membrane core is a spiral wound membrane.

[0018] Preferably, in the membrane filtration system for producing highly active whole milk protein powder, the first filter is a bag filter with a precision of 400 to 600 meshes; the second filter is a bag filter with a precision of 100 to 200 meshes.

[0019] The technical solution adopted in this application can at least achieve the following beneficial effects:

[0020] The utility model discloses a membrane filtration system for producing high-activity whole milk protein powder, which includes an ultrafiltration membrane group, a backwashing component and a nanofiltration membrane group. The ultrafiltration membrane group includes a first ultrafiltration membrane group and a second ultrafiltration membrane group, wherein the second ultrafiltration membrane group is arranged after the first ultrafiltration membrane group, and the nanofiltration membrane group is arranged after the second ultrafiltration membrane group. The ultrafiltration membrane group can separate low-molecular water, ash and lactose from the milk, and remove lactose and ash while concentrating the protein, thereby determining the concentration ratio; the nanofiltration membrane group can separate water and monovalent minerals from the milk, thereby ensuring the protein retention effect, and making the final protein powder taste more mellow and free of odor; the membrane filtration system combining the ultrafiltration membrane group and the nanofiltration membrane group can increase the protein content in the final concentrated protein solution, so that the protein content in the final concentrated protein solution reaches 25%.

[0021] The flushing component is set at the outlet of the first permeate and the outlet of the flushing component is connected to the inlet of the second ultrafiltration membrane group. Adding wash water (reverse osmosis water) to the retentate of the first ultrafiltration membrane group can take away more lactose, thereby increasing the protein content, and the lower lactose can avoid lactose intolerance. The reverse osmosis device reuses the water obtained after filtering the permeate of the ultrafiltration membrane group and the nanofiltration membrane group for the backwashing component, which can save resources and avoid waste.

[0022] The membrane filtration system for producing highly active whole milk protein powder of the utility model also includes a first heat exchanger and a second heat exchanger, wherein the outlet of the first heat exchanger is connected to the inlet of the first ultrafiltration membrane group; the inlet of the second heat exchanger is connected to the first retentate outlet of the second ultrafiltration membrane group, and the outlet of the second heat exchanger is connected to the inlet of the nanofiltration membrane group. The first heat exchanger is used to control the temperature of the liquid in the ultrafiltration membrane group at 6°C to 10°C, and the second heat exchanger is used to control the temperature of the liquid in the nanofiltration membrane group at 6°C to 10°C, so as to control the reproduction of microorganisms and help to maintain the activity of the protein to the maximum extent. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 Schematic diagram of the structure of the membrane filtration system used to produce high-activity whole milk protein powder.

[0024] In the figure: a first ultrafiltration membrane group 110, a first retentate outlet 111, a first permeate outlet 112, a second ultrafiltration membrane group 120, a second retentate outlet 121, a second permeate outlet 122, a nanofiltration membrane group 200, a third retentate outlet 210, a third permeate outlet 220, a backwashing water tank 310, a backwashing electric valve 320, a first heat exchanger 410, a first temperature measuring device 411, a second heat exchanger 420, a second temperature measuring device 421, a first filter 510, a second filter 520, a first electric valve 610, a second electric valve 620, a third electric valve 630, a fourth electric valve 640, a permeate recovery device 700, a reverse osmosis device 800, and a mixer 900. DETAILED DESCRIPTION

[0025] In order to facilitate the understanding of the present invention, the present invention will be described more comprehensively with reference to the relevant drawings. The drawings provide preferred embodiments of the present invention. However, the present invention can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, the purpose of providing these embodiments is to make the disclosure of the present invention more thoroughly and comprehensively understood.

[0026] It should be noted that when an element is referred to as being "disposed on" another element, it may be directly on the other element or there may be a central element. When an element is considered to be "connected to" another element, it may be directly connected to the other element or there may be a central element at the same time. The terms "vertical", "horizontal", "left", "right", "top", "bottom", "bottom end", "top end" and similar expressions used herein are for illustrative purposes only and do not represent the only implementation method.

[0027] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art in the technical field of the present invention. The terms used herein in the specification of the present invention are only for the purpose of describing specific implementations and are not intended to limit the present invention. The term "and / or" used herein includes any and all combinations of one or more related listed items.

[0028] See also Figure 1 In a specific embodiment of the present application, a membrane filtration system for producing a high-activity whole milk protein powder comprises: an ultrafiltration membrane group, wherein the ultrafiltration membrane group comprises a first ultrafiltration membrane group 110 and a second ultrafiltration membrane group 120, wherein the inlet of the first ultrafiltration membrane group 110 is provided with a first electric valve 610, the outlet of the first electric valve 610 is provided with a first filter 510, and the first ultrafiltration membrane group 110 is provided with a first retentate outlet 111 and a first permeate outlet 112; the inlet of the second ultrafiltration membrane group 120 is connected to the first retentate outlet 111, the first retentate outlet 111 is provided with a second electric valve 620, and the second ultrafiltration membrane group 120 is provided with a first filter 510. The filter membrane group 120 is provided with a second retentate outlet 121 and a second permeate outlet 122; a backwashing assembly, the backwashing assembly includes a backwashing water tank 310 and a backwashing electric valve 320, the inlet of the backwashing electric valve 320 is connected to the outlet of the backwashing water tank 310, and the outlet of the backwashing electric valve 320 is connected to the inlet of the second ultrafiltration membrane group; a nanofiltration membrane group 200, the inlet of the nanofiltration membrane group 200 is connected to the second retentate outlet 121, the inlet of the nanofiltration membrane group 200 is provided with a third electric valve 630, and the nanofiltration membrane group 200 is provided with a third permeate outlet 220 and a third retentate outlet 210. In the prior art, in the process of preparing milk protein powder, the concentration of milk is usually carried out by a membrane concentration method, that is, the pasteurized milk is transported to an ultrafiltration membrane device for concentration, and then the retentate is dried to obtain concentrated milk protein powder. In this method of concentration using only an ultrafiltration membrane device, some monovalent minerals are still present in the retentate, which affects the concentration of protein. Therefore, the embodiment of the present application uses a combination of an ultrafiltration membrane group and a nanofiltration membrane group 200 to concentrate milk to increase the protein content in the concentrated protein liquid.

[0029] Specifically, according to the process flow of preparing milk protein powder, the first ultrafiltration membrane group 110, the backwashing component, the second ultrafiltration membrane group 120, and the nanofiltration membrane group 200 are sequentially arranged, and the working process is as follows: the pasteurized milk is first transported to the first ultrafiltration membrane group 110 for filtration and concentration, and the lactose, water, and ash in the milk are discharged. The retentate contains casein, whey protein, some lactose and ash, and this part of the retentate will be transported to the second ultrafiltration membrane group 120. In order to filter out more lactose, a backwashing component is arranged before the first ultrafiltration membrane group 110 and the second ultrafiltration membrane group 120. The backwashing component transports reverse osmosis water to the retentate output by the first ultrafiltration membrane group 110, and enters the second ultrafiltration membrane group 120 together with the retentate for filtration and compression, and further filters out lactose and part of the ash. At this time, the protein content in the retentate is about 16%. The retentate filtered by the second ultrafiltration membrane group 120 is transported to the second heat exchanger 420, the temperature is controlled at a specified temperature, preferably within 10°C, and then transported to the nanofiltration membrane group 200 to filter out some water and monovalent minerals to obtain a concentrated protein solution. The protein content in the concentrated protein solution after nanofiltration reaches 25%. A first electric valve 610 is provided on the inlet pipeline of the first ultrafiltration membrane group 110. The first electric valve 610 preferably adopts a proportional valve and is electrically connected to the control system. The control system can be used to control the opening of the first electric valve 610, thereby adjusting the flow of milk in the pipeline. A first filter 510 is provided at the outlet of the first electric valve 610. The first filter 510 can be, but not limited to, a Y-type pipeline filter, a bag filter, etc. Preferably, the present application uses a bag filter with a precision of 400 to 600 meshes to remove impurities in milk. Further, a double filter can also be used. The first ultrafiltration membrane group 110 is also provided with a first retentate outlet 111 and a first permeate outlet 112. The permeate mainly contains water, lactose and ash, which is discharged through the first permeate outlet 112 and collected in the permeate recovery device 700. The retentate is transported to the second ultrafiltration membrane group 120 through the first retentate outlet 111 for re-filtration. Similarly, the second ultrafiltration membrane group 120 is also provided with a second retentate outlet 121 and a second permeate outlet 122. The permeate filtered by the second ultrafiltration membrane group 120 is discharged through the second permeate outlet 122 and collected in the permeate recovery device 700. The retentate is transported to the nanofiltration membrane group 200 through the second retentate outlet 121 for filtration and concentration. A second electric valve 620 is provided on the pipeline of the first retentate outlet 111. The second electric valve 620 preferably adopts a proportional valve and is electrically connected to the control system. The opening of the second electric valve 620 can be controlled by the control system.The backwash water tank 310 is used to store backwash water. The outlet of the backwash water tank 310 is connected to a backwash electric valve 320. The outlet of the backwash electric valve 320 is connected to the inlet pipeline of the second ultrafiltration membrane group 120. The backwash electric valve 320 can adjust the flow of the flushing water by adjusting its opening. The backwash electric valve 320 is electrically connected to the control system, and the backwash electric valve 320 can be remotely and automatically controlled by the control system. A third electric valve 630 is provided at the inlet of the nanofiltration membrane group 200. The third electric valve 630 preferably adopts a proportional valve and is electrically connected to the control system. The opening of the third electric valve 630 can be controlled by the control system. The nanofiltration membrane group 200 is provided with a third permeate outlet 220 and a third retentate outlet 210. The retentate filtered and concentrated by the nanofiltration membrane group 200 is a concentrated protein liquid, which flows from the third retentate outlet 210 to the next process equipment, and the permeate is discharged through the third permeate outlet 220.

[0030] In a preferred embodiment, the membrane filtration system for producing highly active whole milk protein powder further includes a permeate recovery device 700, the inlet of which is connected to the first permeate outlet 112, the second permeate outlet 122 and the third permeate outlet 220, respectively, for recovering the permeate. The permeate filtered by the ultrafiltration membrane group mainly contains water, lactose and ash, and the permeate filtered by the nanofiltration membrane group 200 mainly contains water and monovalent minerals. These permeates are discharged from the ultrafiltration membrane group and the nanofiltration membrane group 200 and then transported to the permeate recovery device 700 for recovery. The permeate recovery device 700 is a container for collecting and holding the permeate, which can be a water tank, a water storage tank, a recovery kettle or other containers.

[0031] In order to effectively utilize the permeate recovered by the permeate recovery device 700, in another specific embodiment of the present application, a reverse osmosis device 800 is further included, wherein the outlet of the permeate recovery device 700 is connected to the inlet of the reverse osmosis device, and the permeate outlet of the reverse osmosis device 800 is connected to the inlet of the backwash water tank 310, so that the water obtained after filtration by the reverse osmosis device 800 is reused for the backwash component, which can save resources and avoid waste; the retentate outlet of the reverse osmosis device 800 discharges the milk permeate concentrate, which can be used to make milk permeate powder.

[0032] Furthermore, a first heat exchange component is also provided at the inlet of the first ultrafiltration membrane group 110, and the first heat exchange component includes a first heat exchanger 410 and a first temperature measuring device 411 located at the outlet of the first heat exchanger 410, and the inlet of the first heat exchanger 410 is connected to the outlet of the first electric valve 610. In order to adjust the milk filtered by the first filter 510 to the specified process temperature, the first heat exchanger 410 and the first temperature measuring device 411 located at the outlet of the first heat exchanger 410 are provided at the inlet of the first ultrafiltration membrane group 110, and the inlet of the first heat exchanger 410 is connected to the outlet of the first electric valve 610. The first heat exchanger 410 controls the temperature of the milk at a predetermined temperature, preferably 6°C to 10°C. The first temperature measuring device 411 can be a temperature measuring element such as a temperature sensor, but is not limited to it. The first temperature measuring device 411 is electrically connected to the control system, and is used to detect the temperature of the milk in the pipeline, and transmit the temperature signal to the control system. The control system controls the first heat exchanger 410, thereby achieving instant regulation of the temperature of the milk.

[0033] Furthermore, a second heat exchange component is provided at the inlet of the nanofiltration membrane group 200 , and the second heat exchange component includes a second heat exchanger 420 and a second temperature measuring device 421 located at the outlet of the second heat exchanger 420 , and the inlet of the second heat exchanger 420 is connected to the outlet of the third electric valve 630 . Before the retentate filtered by the second ultrafiltration membrane group 120 is transported to the nanofiltration membrane group 200, the retentate needs to be adjusted to a specified process temperature. Therefore, a second heat exchanger 420 and a second temperature measuring device 421 located at the outlet of the second heat exchanger 420 are arranged at the inlet of the nanofiltration membrane group 200. The inlet of the second heat exchanger 420 is connected to the outlet of the third electric valve 630, and is used to control the temperature of the retentate filtered by the second ultrafiltration membrane group 120 to a predetermined temperature, preferably within 30°C. The second temperature measuring device 421 can adopt but is not limited to temperature measuring elements such as temperature sensors. The second temperature measuring device 421 is electrically connected to the control system, and is used to detect the temperature of the retentate in the pipeline and transmit the temperature signal to the control system. The control system controls the second heat exchanger 420, thereby achieving real-time regulation of the retentate temperature.

[0034] Further, the third permeate outlet 220 of nanofiltration membrane group 200 is provided with second filter 520, and the outlet of second filter 520 is provided with the fourth electric valve 640. The retentate after ultrafiltration membrane group filtration filters out some water and monovalent minerals through nanofiltration membrane group 200, and obtains concentrated protein liquid, and the permeate is discharged by the third permeate outlet 220 that nanofiltration membrane group 200 is provided with, and concentrated protein liquid is delivered to second filter 520 by the third retentate outlet 210, and second filter 520 can adopt but not limited to Y-type pipeline filter, bag filter etc., as preferably, the present application selects bag filter with precision of 100 purpose, prevents foreign matter etc. from entering pipeline and polluting concentrated protein liquid. The outlet of second filter 520 is provided with the fourth electric valve 640, and the fourth electric valve 640 preferentially adopts proportional valve, is electrically connected with control system. The concentrated protein liquid after second filter 520 filtration is delivered to next process equipment through the fourth electric valve 640.

[0035] In the membrane filtration system of the present application, the concentration factor, i.e., the cutoff liquid: permeate is (1.2 to 6.0):1, and the concentration factor is achieved through proportional valve control, that is, the concentration factor is controlled by the opening ratio of the first electric valve 610, the second electric valve 620, the third electric valve 630 and the fourth electric valve 640.

[0036] In a preferred embodiment, the first ultrafiltration membrane group 110 includes at least 4 ultrafiltration membrane tubes, each of which includes at least 2 ultrafiltration membrane tubes, each of which includes at least 3 ultrafiltration membrane cores, which are connected in series, and the ultrafiltration membrane cores are spiral membranes. The second ultrafiltration membrane group 120 includes at least 4 ultrafiltration membrane tubes, each of which includes at least 2 ultrafiltration membrane tubes, each of which includes at least 3 ultrafiltration membrane cores, which are connected in series, and the ultrafiltration membrane cores are spiral membranes. The number and connection method of membrane tubes directly affect the filtration effect. If there are too few membrane tubes, there will be more impurities in the retentate, which will reduce the protein content in the retentate accordingly; if there are too many membrane tubes, the filtration time will be long and the filtration efficiency will be low. In order to meet the actual working conditions and achieve good filtration efficiency and high protein content, the number and connection method of the ultrafiltration membrane tubes in this scheme are a preferred method, which can be adjusted appropriately according to the actual working conditions. The ultrafiltration membrane tube is a spiral wound membrane, which has a large membrane area and a correspondingly strong production capacity. In the use environment of this scheme, a standard size sanitary spiral wound membrane is selected.

[0037] Further, the nanofiltration membrane group 200 includes at least 5 levels of nanofiltration membrane tubes, each level of the nanofiltration membrane tubes includes at least 2 nanofiltration membrane tubes, each nanofiltration membrane tube includes at least 2 nanofiltration membrane cores, the nanofiltration membrane cores are connected in series, and the nanofiltration membrane cores are spiral membranes. The number and connection method of the membrane tubes directly affect the filtration effect. If there are too few membrane tubes, there will be more impurities in the retentate, which will correspondingly reduce the protein content in the retentate; if there are too many membrane tubes, the filtration time will be long and the filtration efficiency will be low. In order to meet the actual working conditions and achieve good filtration efficiency and high protein content, the number and connection method of the nanofiltration membrane tubes in this scheme are a better way, which can be adjusted appropriately according to the actual working conditions. Among them, the nanofiltration membrane tube is a spiral membrane, which has a large membrane area and a correspondingly strong production capacity. In the use environment of this scheme, a standard size sanitary spiral membrane is selected.

[0038] In actual use, since the retentate from the first ultrafiltration membrane group 110 and the reverse osmosis water from the backwashing assembly are jointly transported to the second ultrafiltration membrane group 120 to filter out more lactose, a mixer 900 can also be set at the entrance of the second ultrafiltration membrane group 120 to facilitate the retentate and the backwashing water to be fully mixed, so as to achieve the purpose of more sufficient filtration compression. Since the role of the nanofiltration membrane group 200 is to filter the retentate after the ultrafiltration membrane group is filtered again, filtering out the water and monovalent minerals therein, the membrane pore diameter of the ultrafiltration membrane tube is larger than the diameter of the nanofiltration membrane pore.

[0039] The technical features of the above embodiments may be combined arbitrarily. To make the description concise, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0040] The above-mentioned embodiments only express several implementation methods of the utility model, and the description is relatively specific and detailed, but it cannot be understood as limiting the scope of the utility model patent. It should be pointed out that for ordinary technicians in this field, several modifications and improvements can be made without departing from the concept of the utility model, which all belong to the protection scope of the utility model. Therefore, the protection scope of the utility model patent shall be based on the attached claims.

Claims

1. A membrane filtration system for producing highly active whole milk protein powder, characterized in that: include: An ultrafiltration membrane group, the ultrafiltration membrane group comprising a first ultrafiltration membrane group and a second ultrafiltration membrane group, the inlet of the first ultrafiltration membrane group is provided with a first electric valve, the outlet of the first electric valve is provided with a first filter, and the first ultrafiltration membrane group is provided with a first retentate outlet and a first permeate outlet; the inlet of the second ultrafiltration membrane group is connected to the first retentate outlet, the first retentate outlet is provided with a second electric valve, and the second ultrafiltration membrane group is provided with a second retentate outlet and a second permeate outlet; A backwashing assembly, the backwashing assembly comprising a backwashing water tank and a backwashing electric valve, the inlet of the backwashing electric valve is connected to the outlet of the backwashing water tank, and the outlet of the backwashing electric valve is connected to the inlet of the second ultrafiltration membrane group; The nanofiltration membrane group has an inlet connected to the second retentate outlet, a third electric valve is provided at the inlet of the nanofiltration membrane group, and the nanofiltration membrane group has a third permeate outlet and a third retentate outlet.

2. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: It also includes a permeate recovery device, the inlet of which is respectively connected to the first permeate outlet, the second permeate outlet and the third permeate outlet for recovering the permeate.

3. The membrane filtration system for producing high-activity whole milk protein powder according to claim 2, characterized in that: It also includes a reverse osmosis device, the outlet of the permeate recovery device is connected to the inlet of the reverse osmosis device, and the outlet of the reverse osmosis device is connected to the inlet of the backwash water tank.

4. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: A first heat exchange component is also provided at the inlet of the first ultrafiltration membrane group. The first heat exchange component includes a first heat exchanger and a first temperature measuring device located at the outlet of the first heat exchanger. The inlet of the first heat exchanger is connected to the outlet of the first electric valve.

5. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: A second heat exchange component is also provided at the inlet of the nanofiltration membrane group. The second heat exchange component includes a second heat exchanger and a second temperature measuring device located at the outlet of the second heat exchanger. The inlet of the second heat exchanger is connected to the outlet of the third electric valve.

6. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: The third permeate outlet is provided with a second filter, and the outlet of the second filter is provided with a fourth electric valve.

7. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: The first ultrafiltration membrane group includes at least 4 levels of ultrafiltration membrane tubes, each level of the ultrafiltration membrane tubes includes at least 2 ultrafiltration membrane tubes, each of the ultrafiltration membrane tubes includes at least 3 ultrafiltration membrane cores, the ultrafiltration membrane cores are connected in series, and the ultrafiltration membrane cores are spirally wound membranes.

8. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: The second ultrafiltration membrane group includes at least 4 levels of ultrafiltration membrane tubes, each level of the ultrafiltration membrane tubes includes at least 2 ultrafiltration membrane tubes, each of the ultrafiltration membrane tubes includes at least 3 ultrafiltration membrane cores, the ultrafiltration membrane cores are connected in series, and the ultrafiltration membrane cores are spirally wound membranes.

9. The membrane filtration system for producing high-activity whole milk protein powder according to claim 1, characterized in that: The nanofiltration membrane group includes at least 5 stages of nanofiltration membrane tubes, each stage of the nanofiltration membrane tubes includes at least 2 nanofiltration membrane tubes, each of the nanofiltration membrane tubes includes at least 2 nanofiltration membrane cores, the nanofiltration membrane cores are connected in series, and the nanofiltration membrane cores are spiral membranes.

10. The membrane filtration system for producing high-activity whole milk protein powder according to claim 6, characterized in that: The first filter is a bag filter with a precision of 400 to 600 meshes; the second filter is a bag filter with a precision of 100 to 200 meshes.

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