Membrane method solid table vinegar concentration device and process

Abstract

The invention discloses a membrane method solid vinegar concentration device which comprises a permeate tank used for storing dialysate; the primary concentration system comprises a circulating tank I, a membrane component I and a pump component I; the secondary concentration system comprises a circulating tank II, a membrane component II and a pump component II; the device is reasonable in structure, acetic acid and water are removed through two-stage concentration, non-volatile acid, polysaccharide and other substances in table vinegar are intercepted as far as possible, and loss of nutritional ingredients in the table vinegar is avoided as far as possible during concentration.

Description

Technical Field

[0001] The invention relates to the technical field of solid vinegar production, and in particular to a membrane solid vinegar concentration device and process. Background Art

[0002] Vinegar brewed by solid-state fermentation contains non-volatile acids, volatile acids and amino acids, reducing sugars and other nutrients. Among them, non-volatile acids and amino acids are the main components that affect the flavor of vinegar. High-quality vinegar needs to have a certain proportion of non-volatile acids. If the proportion of volatile acids is too high, the vinegar will taste sour and irritating. The volatile acid in vinegar is mainly acetic acid.

[0003] In order to increase the yield, the traditional vinegar brewing process adds more water to the solid vinegar embryo after fermentation, which results in low total acid and salt-free solid content of the collected vinegar. At the same time, the proportion of acetic acid in the natural fermentation process is too high, making the vinegar taste thin and the flavor poor. The traditional optimization method is to perform the "drying in the summer and ice removal in the winter" operation on the vinegar, that is, to place the vinegar in a ceramic jar in the open air, use the high temperature in the summer to evaporate the volatile acid and water in the vinegar, and use the principle that acetic acid and water are easy to freeze in the winter to remove the ice on the surface of the jar, so as to concentrate the vinegar. The "drying in the summer and ice removal in the winter" operation requires a lot of space and manpower, and the process is traditional and inefficient, so it is difficult to carry out on a large scale.

[0004] In recent years, some vinegar factories have adopted the method of heating + vacuum decompression evaporation concentration to concentrate vinegar, but this method also has significant disadvantages: 1. While evaporating water and some volatile acids, vacuum concentration will also cause the aroma substances in the vinegar to evaporate, reducing the sensory index of vinegar aroma. 2. This process requires water and volatile acid liquids to evaporate into gas. Due to the existence of phase change, higher energy consumption is required, so the overall cost is high. In response to the above problems, a solution is proposed below. Summary of the invention

[0005] The purpose of the present invention is to provide a membrane solid vinegar concentration device and process, which has the advantages of a vinegar circulation concentration process and equipment with a pump as thrust, no phase change and low energy consumption.

[0006] The above technical objectives of the present invention are achieved through the following technical solutions: A membrane solid vinegar concentration device, comprising a permeate tank, wherein the permeate tank is used to store dialysate; A primary concentration system, the primary concentration system comprises a circulation tank, a membrane assembly and a pump assembly. Two feed pipes are arranged on the top of the circulation tank. The circulation tank is connected to the membrane assembly through a discharge pipe. One end of the membrane assembly and the pump assembly are connected through a drainage pipe. The other end of the pump assembly is connected to the discharge pipe. One end of the membrane assembly away from the circulation tank is connected to a permeate tank through a storage pipe. The circulation tank is connected to the membrane assembly through an external circulation pipe. A secondary concentration system, the secondary concentration system comprises a circulation tank 2, a membrane assembly 2 and a pump assembly 2, the top of the circulation tank 2 is connected to an external circulation pipe 1 through a feed pipe 2, the circulation tank 2 is connected to the membrane assembly 2 through a discharge pipe 2, one end of the membrane assembly 2 and the pump assembly 2 are connected through a discharge pipe 2, the other end of the pump assembly 2 is connected to the discharge pipe 2, the end of the membrane assembly 2 away from the circulation tank 2 is connected to the permeate tank through a storage pipe 2, and the circulation tank 2 is connected to the membrane assembly 2 through the external circulation pipe 2; A cleaning system, the cleaning system includes a cleaning tank and an alkali liquid barrel, the discharge end of the alkali liquid barrel and the discharge end of the cleaning tank are connected to one place through a pipeline, and finally connected to discharge pipe one and discharge pipe two through discharge pipe three, the other ends of the two cleaning pipes at the upper end of the cleaning tank are respectively connected to storage pipe one and storage pipe two, and the other ends of the two exhaust pipes at the upper end of the cleaning tank are respectively connected to feed pipe two and external circulation pipe two.

[0007] Preferably, the membrane assembly 1 comprises a heat exchanger 1 and at least three sets of semipermeable membrane groups, a regulating valve and a pressure gauge are arranged between the heat exchanger 1 and the semipermeable membrane group, the semipermeable membrane group comprises a high-pressure membrane shell and a plurality of reverse osmosis membranes located in the high-pressure membrane shell, at least four reverse osmosis membranes are arranged in one of the high-pressure membrane shells, and the three sets of semipermeable membrane groups are connected in sequence by pipelines, and valves are provided at the connections.

[0008] Preferably, the pump assembly 1 comprises a feed pump 1, a high-pressure pump 1 and a circulation pump 1 which are arranged in sequence, and all three pumps are connected to a drain valve. A temperature transmitter is arranged on the side of the feed pump 1 away from the circulation pump 1, pressure gauges are connected to both ends of the circulation pump, one end of the circulation pump is also connected to a pressure transmitter, an end of the circulation pump away from the pressure transmitter is connected to an inner circulation pipe, an inner circulation pipe is provided with an inner circulation valve, and one end of the inner circulation pipe is connected to membrane assembly 1.

[0009] Preferably, the second membrane assembly comprises a second heat exchanger and at least one set of semipermeable membrane groups, and a regulating valve and a pressure gauge are provided between the second heat exchanger and the semipermeable membrane group.

[0010] Preferably, the pump assembly 2 comprises a feed pump 2 and a high-pressure pump 2 which are arranged in sequence, the side of the feed pump 2 away from the high-pressure pump 2 is connected to a temperature transmitter, and the side of the high-pressure pump 2 away from the feed pump 2 is connected to a pressure gauge and a pressure transmitter.

[0011] Preferably, both the discharge pipe 1 and the discharge pipe 2 are connected with a flushing valve and a sewage pipe, the discharge pipe 1 is connected with a concentrate valve, and the discharge pipe 2 is connected with a concentrate valve and a concentrate pump.

[0012] A processing technology of a membrane solid vinegar concentration device comprises the following steps: S1: Primary concentration, injecting vinegar raw materials and pure water into circulation tank 1, the mixed liquid in circulation tank 1 is sent to membrane module 1, acetic acid and water are permeated through multiple sets of semi-permeable membrane groups, and the remaining substances are intercepted, and the permeate enters the permeate tank; The remaining substances are re-entered into the membrane module 1 through the circulation pump for treatment. This is the internal circulation operation. After several internal circulation operations, the internal circulation valve is closed and the mixed liquid is sent to the external circulation pipe 1 through the high-pressure pump 1 and the feed pump 1. Take samples at the reflux valve. If they do not meet the requirements, they are sent back to the circulation tank through the external circulation valve. Repeat the above operation. This is the external circulation operation. If the requirements are met, the first-stage concentrated liquid is obtained. At this time, the external circulation valve 1 is closed to allow the first-stage concentrated liquid to enter the circulation tank 2 through the feed pipe 2; S2: Secondary concentration: the primary concentrate in the circulation tank 2 is passed into the membrane module 2 through the discharge pipe 2. The membrane module 2 performs permeation concentration on the primary concentrate again. The permeate enters the permeate tank. The concentrated primary concentrate enters the circulation pipe 2 through the high-pressure pump 2 and the feed pump 2. Take a sample of the primary concentrated liquid in the circulation pipe 2. If it does not meet the standard, it will enter the circulation tank 2 again and repeat the above operation. This is the external circulation operation; If the standard is met, a secondary concentrate is obtained, which is discharged and collected through a concentrate valve and a concentrate pump; S3: Cleaning: the pure water in the cleaning tank and the alkali solution in the alkali solution barrel are mixed into a cleaning solution, and the cleaning solution is respectively sent to the discharge pipe 1 and the discharge pipe 2 through the discharge pipe 3. In the primary concentration system, the cleaning liquid first enters into the membrane module 1 to flush several semi-permeable membrane groups, and then the circulation pump 1 performs internal circulation operation to thoroughly clean the membrane module 1. During the cleaning process, the liquid intercepted by the membrane module 1 is discharged through the flushing valve and the sewage pipe set on the discharge pipe 1; the pure water permeated from the membrane module 1 enters into the cleaning pipe and is sent back to the cleaning tank; In the secondary concentration system, the cleaning liquid first enters the membrane module 2 to flush the semipermeable membrane group. During the cleaning process, the liquid intercepted by the membrane module 2 is discharged through the flushing valve and the sewage pipe set on the discharge pipe 2; the pure water permeated from the membrane module 2 enters the cleaning pipe and is sent back to the cleaning tank; During the cleaning process, the gas generated by the reaction is sent into the cleaning tank through the exhaust pipe and discharged through the cleaning tank; The used cleaning liquid in the cleaning tank is discharged through the drain valve and drain pipe at the bottom of the cleaning tank.

[0013] Preferably, the concentration pressure in the primary circulation system is 2.0-2.5 MPa, the concentration ratio is 2.5 times, and the concentration temperature is ≤45°C.

[0014] Preferably, the concentration pressure in the secondary circulation system is 3.0-3.5 MPa, the ultimate pressure is ≤4.0 MPa, the concentration ratio is 2 times, and the concentration temperature is ≤45°C.

[0015] Preferably, the reverse osmosis membrane is a semipermeable membrane with a molecular weight cut-off of 70.

[0016] The beneficial effects of the present invention are as follows: the molecular weight of acetic acid is 60, the molecular weight of water is 18, and the non-volatile acids are mainly lactic acid (molecular weight 90), succinic acid (molecular weight 118), gluconic acid (molecular weight 196), etc. The present application selects a semipermeable membrane with a molecular weight cutoff of 70 to perform a circulating concentration treatment on vinegar, and the acetic acid and water in the vinegar are discharged through the membrane or recovered for other uses, and the non-volatile organic acids and inorganic salts, minerals, sugars, amino acids, proteins and other nutrients in the vinegar are all intercepted; By adjusting the ratio of concentrate and dialysate, that is, adjusting the concentration ratio of vinegar, the vinegar indicators can be flexibly adjusted according to quality requirements. While improving product quality, the advantages of energy saving and consumption reduction are obvious. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a structural schematic diagram of an embodiment.

[0018] Figure numerals: 1. Primary concentration system; 11. Circulation tank one; 111. Feed pipe one; 112. Discharge pipe one; 113. Drain pipe one; 114. External circulation pipe one; 115. Internal circulation pipe; 12. Membrane assembly one; 121. Heat exchanger one; 122. Semipermeable membrane group; 13. Pump assembly one; 2. Secondary concentration system; 21. Circulation tank two; 211. Feed pipe two; 212. Discharge pipe two; 213. Drain pipe two; 214. External circulation pipe two; 22. Membrane assembly two; 23. Pump assembly two; 3. Cleaning system; 31. Cleaning tank; 32. Alkali liquid barrel; 33. Discharge pipe three; 34. Cleaning pipe; 35. Exhaust pipe; 4. Permeate tank. DETAILED DESCRIPTION

[0019] The following is only a preferred embodiment of the present invention, and the protection scope is not limited to this embodiment. All technical solutions under the concept of the present invention should belong to the protection scope of the present invention. The same parts are represented by the same reference numerals.

[0020] like Figure 1 As shown, a membrane solid vinegar concentration device includes a permeate tank 4, a primary concentration system 1, a secondary concentration system 2 and a cleaning system 3.

[0021] The primary concentration system 1 includes a circulation tank 11, a membrane assembly 12 and a pump assembly 13. Two feed pipes 111 are provided on the top of the circulation tank 11. The two feed pipes 111 respectively add pure water and vinegar raw materials to be processed into the circulation tank 11, and the pure water and the vinegar raw materials form a mixed liquid in the circulation tank 11.

[0022] The circulation tank 11 is connected to the membrane assembly 12 through the discharge pipe 112. By opening the feed valve on the discharge pipe 112, the mixed liquid in the circulation tank 11 will enter the membrane assembly 12. The membrane assembly 12 includes a heat exchanger 121 and at least three sets of semipermeable membrane groups 122. Three sets of semipermeable membrane groups 122 are used in this design. The mixed liquid first enters the heat exchanger for cooling, and then enters the three sets of semipermeable membrane groups 122 in turn. A regulating valve and a pressure gauge are provided between the heat exchanger 121 and the semipermeable membrane group 122, which can regulate the flow rate and flow of the mixed liquid entering the semipermeable membrane group 122.

[0023] The semipermeable membrane group 122 includes a high-pressure membrane shell and a plurality of reverse osmosis membranes located in the high-pressure membrane shell. At least four reverse osmosis membranes are arranged in one high-pressure membrane shell. The reverse osmosis membrane is a semipermeable membrane with a molecular weight cutoff of 70. In this design, the 8040 type material-specific sanitary RO membrane in the DOW membrane is used, which can permeate water molecules and acetic acid molecules and intercept non-volatile organic acids and inorganic salts, minerals, sugars, amino acids, proteins and other nutrients.

[0024] In this design, the three sets of semipermeable membrane groups 122 are sequentially connected by pipelines, and valves are provided at the connection points. Opening the valves can allow the liquids in the three sets of semipermeable membrane groups 122 to circulate with each other without penetration, which is convenient for cleaning.

[0025] The end of the membrane assembly 12 away from the circulation tank 11 is connected to the permeate tank 4 through a storage tube 1. After being processed by three sets of semipermeable membrane groups 122, the seeped water and acetic acid will enter the permeate tank 4, and the retained mixed liquid will enter the pump assembly 13 through a discharge pipe 113.

[0026] The pump assembly 13 includes a feed pump 1, a high-pressure pump 1 and a circulation pump 1 which are arranged in sequence. The mixed liquid first contacts the circulation pump 1. The circulation pump 1 can make two choices, one is to perform internal circulation operation on the mixed liquid, and the other is to send the mixed liquid back to the discharge pipe 112 through the feed pump 1 and the high-pressure pump 1. A temperature transmitter is arranged on the side of the feed pump 1 away from the circulation pump 1. Pressure gauges are connected to both ends of the circulation pump. A pressure transmitter is also connected to one end of the circulation pump, so that the pressure and temperature of the mixed liquid here can be monitored.

[0027] This design will first take 3 to 5 internal circulations for the mixed liquid, and then send it to the discharge pipe 112. During the internal circulation operation, the internal circulation valve set on the internal circulation pipe 115 is opened, one end of the internal circulation pipe 115 is connected to one of the semipermeable membrane groups 122, and the circulation pump 1 sends the mixed liquid into the semipermeable membrane group 122, and the valve between the semipermeable membrane groups 122 is opened to allow the mixed liquid to enter the first set of semipermeable membrane groups 122, and then the valve is closed to allow it to pass through the three sets of semipermeable membrane groups 122 again. After repeating the operation, a large part of the water and acetic acid in the mixed liquid can be removed.

[0028] After that, the mixed liquid enters the discharge pipe 112. At this time, the mixed liquid in the discharge pipe 112 no longer enters the membrane module 12, but enters the circulation pipe 1 connecting the discharge pipe 112 and the circulation tank 11. A sampling valve is provided on the circulation pipe 1, and the concentrated liquid can be sampled through the sampling valve. If the concentration standard of the first stage is not reached, the mixed liquid enters the circulation tank 11 again, and the above operation is repeated. This is the external circulation operation.

[0029] If the first stage concentration standard is reached, a primary concentrated liquid is obtained, which can be fed into the secondary circulation system through the second feed pipe 211.

[0030] The secondary concentration system 2 includes a circulation tank 21, a membrane assembly 22 and a pump assembly 23. One end of a feed pipe 211 is connected to the circulation tank 21, and the primary concentrate enters the circulation tank 21. The circulation tank 21 is connected to the membrane assembly 22 through a discharge pipe 212. After the feed valve is opened, the primary concentrate enters the membrane assembly 22.

[0031] The membrane assembly 22 includes a heat exchanger 2 and at least one set of semipermeable membrane groups 122. After the primary concentrate is cooled by the heat exchanger, it enters the semipermeable membrane group 122. In this design, only one set of semipermeable membrane group 122 is set in the membrane assembly 22. The liquid intercepted by the semipermeable membrane group 122 enters the pump assembly 23 through the drain pipe 213, and the liquid permeating the semipermeable membrane group 122 enters the permeated liquid tank 4. A regulating valve and a pressure gauge are provided between the heat exchanger 2 and the semipermeable membrane group 122 to adjust the flow rate and flow rate of the primary concentrate.

[0032] The pump assembly 23 includes a feed pump 2 and a high-pressure pump 2 which are arranged in sequence. A temperature transmitter is connected to the side of the feed pump 2 away from the high-pressure pump 2, and a pressure gauge and a pressure transmitter are connected to the side of the high-pressure pump 2 away from the feed pump 2, so that the pressure and temperature of the primary concentrated liquid can be monitored.

[0033] The circulation tank 21 is connected to the membrane assembly 22 through the external circulation pipe 214. The primary concentrated liquid flowing out of the pump assembly 23 will enter the external circulation pipe 214 and be sampled through the sampling valve arranged therein. If the standard of the second stage concentration is not reached, the treated primary concentrated liquid will enter the circulation tank 21 again for external circulation operation.

[0034] If the standard of the second stage concentration is reached, the concentrate is discharged through the concentrate valve and concentrate pump provided on the second feed pipe 211 and collected.

[0035] The cleaning system 3 includes a cleaning tank 31 and an alkali liquid barrel 32. The discharge end of the alkali liquid barrel 32 is connected to the discharge end of the cleaning tank 31 through a pipeline, and finally connected to the discharge pipe 1 112 and the discharge pipe 2 212 through the discharge pipe 3 33. The other ends of the two cleaning pipes 34 at the upper end of the cleaning tank 31 are respectively connected to the storage pipe 1 and the storage pipe 2, and the other ends of the two exhaust pipes 35 at the upper end of the cleaning tank 31 are respectively connected to the feed pipe 2 211 and the external circulation pipe 2 214.

[0036] Both the feed pipe 1 111 and the feed pipe 2 211 are connected with a flushing valve and a sewage pipe, and the feed pipe 1 111 is connected with a concentrate valve.

[0037] A processing technology of a membrane solid vinegar concentration device comprises the following steps: S1: Primary concentration, injecting vinegar raw materials and pure water into circulation tank 1, the mixed liquid in circulation tank 1 is sent to membrane module 1, acetic acid and water are permeated through multiple sets of semi-permeable membrane groups, and the remaining substances are intercepted, and the permeate enters the permeate tank; The remaining substances are re-entered into the membrane module 1 through the circulation pump for treatment. This is the internal circulation operation. After several internal circulation operations, the internal circulation valve is closed and the mixed liquid is sent to the external circulation pipe 1 through the high-pressure pump 1 and the feed pump 1. Take samples at the reflux valve. If they do not meet the requirements, they are sent back to the circulation tank through the external circulation valve. Repeat the above operation. This is the external circulation operation. If the requirements are met, the first-stage concentrated liquid is obtained. At this time, the external circulation valve 1 is closed to allow the first-stage concentrated liquid to enter the circulation tank 2 through the feed pipe 2; S2: Secondary concentration: the primary concentrate in the circulation tank 2 is passed into the membrane module 2 through the discharge pipe 2. The membrane module 2 performs permeation concentration on the primary concentrate again. The permeate enters the permeate tank. The concentrated primary concentrate enters the circulation pipe 2 through the high-pressure pump 2 and the feed pump 2. Take a sample of the primary concentrated liquid in the circulation pipe 2. If it does not meet the standard, it will enter the circulation tank 2 again and repeat the above operation. This is the external circulation operation; If the standard is met, a secondary concentrate is obtained, which is discharged and collected through a concentrate valve and a concentrate pump; S3: Cleaning: the pure water in the cleaning tank and the alkali solution in the alkali solution barrel are mixed into a cleaning solution, and the cleaning solution is respectively sent to the discharge pipe 1 and the discharge pipe 2 through the discharge pipe 3. In the primary concentration system, the cleaning liquid first enters into the membrane module 1 to flush several semi-permeable membrane groups, and then the circulation pump 1 performs internal circulation operation to thoroughly clean the membrane module 1. During the cleaning process, the liquid intercepted by the membrane module 1 is discharged through the flushing valve and the sewage pipe set on the feed pipe 1; the pure water permeated from the membrane module 1 enters into the cleaning pipe and is sent back to the cleaning tank; In the secondary concentration system, the cleaning liquid first enters the membrane module 2 to flush the semipermeable membrane group. During the cleaning process, the liquid intercepted by the membrane module 2 is discharged through the flushing valve and the drain pipe set on the feed pipe 2; the pure water permeated from the membrane module 2 enters the cleaning pipe and is sent back to the cleaning tank; During the cleaning process, the gas generated by the reaction is sent into the cleaning tank through the exhaust pipe and discharged through the cleaning tank; The used cleaning liquid in the cleaning tank is discharged through the drain valve and drain pipe at the bottom of the cleaning tank.

[0038] In this design, the concentration pressure in the primary circulation system is 2.0-2.5 MPa, the concentration ratio is 2.5 times, and the concentration temperature is ≤45°C. The concentration pressure in the secondary circulation system is 3.0-3.5 MPa, the ultimate pressure is ≤4.0 MPa, the concentration ratio is 2 times, and the concentration temperature is ≤45°C.

[0039] The reverse osmosis membrane in this design uses a spiral membrane to concentrate the vinegar stock solution and discharge the permeate containing acetic acid and water. The spiral membrane can intercept non-volatile acids, polysaccharides and other substances in the vinegar as much as possible, mainly passing acetic acid and water, and then concentrating the vinegar, which can avoid the loss of nutrients as much as possible while concentrating.

[0040] The specific embodiments described above further illustrate the technical problems, technical solutions and beneficial effects solved by the present invention. It should be understood that the above are only specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A membrane solid vinegar concentration device, characterized in that: include a permeate tank (4), wherein the permeate tank (4) is used to store dialysate; A primary concentration system (1), the primary concentration system (1) comprising a circulation tank (11), a membrane assembly (12) and a pump assembly (13), two feed pipes (111) are arranged on the top of the circulation tank (11), the circulation tank (11) is connected to the membrane assembly (12) via a discharge pipe (112), one end of the membrane assembly (12) and the pump assembly (13) are connected via a discharge pipe (113), the other end of the pump assembly (13) is connected to the discharge pipe (112), the end of the membrane assembly (12) away from the circulation tank (11) is connected to a permeate tank (4) via a storage pipe (1), and the circulation tank (11) is connected to the membrane assembly (12) via an external circulation pipe (114); A secondary concentration system (2), the secondary concentration system (2) comprising a second circulation tank (21), a second membrane assembly (22) and a second pump assembly (23), the top of the second circulation tank (21) being connected to an external circulation pipe (114) via a second feed pipe (211), the second circulation tank (21) being connected to the second membrane assembly (22) via a second discharge pipe (212), one end of the second membrane assembly (22) and the second pump assembly (23) being connected via a second discharge pipe (213), the other end of the second pump assembly (23) being connected to the second discharge pipe (212), the end of the second membrane assembly (22) away from the second circulation tank (21) being connected to a permeate tank (4) via a second storage pipe, the second circulation tank (21) being connected to the second membrane assembly (22) via a second external circulation pipe (214); A cleaning system (3), the cleaning system (3) comprising a cleaning tank (31) and an alkali liquid barrel (32), the discharge end of the alkali liquid barrel (32) and the discharge end of the cleaning tank (31) being connected to one point through a pipeline, and finally connected to a discharge pipe one (112) and a discharge pipe two (212) through a discharge pipe three (33), the other ends of two cleaning pipes (34) at the upper end of the cleaning tank (31) being connected to a storage pipe one and a storage pipe two, respectively, and the other ends of two exhaust pipes (35) at the upper end of the cleaning tank (31) being connected to a feed pipe two (211) and an external circulation pipe two (214), respectively.

2. A membrane solid vinegar concentration device according to claim 1, characterized in that: The membrane assembly 1 (12) comprises a heat exchanger 1 (121) and at least three sets of semipermeable membrane groups (122), a regulating valve and a pressure gauge are arranged between the heat exchanger 1 (121) and the semipermeable membrane group (122), the semipermeable membrane group (122) comprises a high-pressure membrane shell and a plurality of reverse osmosis membranes located in the high-pressure membrane shell, at least four reverse osmosis membranes are arranged in one of the high-pressure membrane shells, and the three sets of semipermeable membrane groups (122) are connected in sequence through pipelines, and valves are arranged at the connections.

3. A membrane solid vinegar concentration device according to claim 1, characterized in that: The pump assembly 1 (13) comprises a feed pump 1, a high-pressure pump 1 and a circulation pump 1 which are arranged in sequence, and the three pumps are all connected to a discharge valve. A temperature transmitter is arranged on the side of the feed pump 1 away from the circulation pump 1, and pressure gauges are connected to both ends of the circulation pump. One end of the circulation pump is also connected to a pressure transmitter. The end of the circulation pump away from the pressure transmitter is connected to an internal circulation pipe (115), and an internal circulation valve is arranged on the internal circulation pipe (115). One end of the internal circulation pipe (115) is connected to the membrane assembly 1 (12).

4. A membrane solid vinegar concentration device according to claim 2, characterized in that: The second membrane assembly (22) comprises a second heat exchanger and at least one set of semipermeable membrane groups (122), and a regulating valve and a pressure gauge are provided between the second heat exchanger and the semipermeable membrane group (122).

5. A membrane solid vinegar concentration device according to claim 1, characterized in that: The pump assembly 2 (23) comprises a feed pump 2 and a high-pressure pump 2 which are arranged in sequence, wherein the side of the feed pump 2 away from the high-pressure pump 2 is connected to a temperature transmitter, and the side of the high-pressure pump 2 away from the feed pump 2 is connected to a pressure gauge and a pressure transmitter.

6. A membrane solid vinegar concentration device according to claim 1, characterized in that: The discharge pipe 1 (112) and the discharge pipe 2 (212) are both connected to a flushing valve and a sewage pipe, the discharge pipe 1 (112) is connected to a concentrated liquid valve, and the discharge pipe 2 (212) is connected to a concentrated liquid valve and a concentrated liquid pump.

7. The processing technology of a membrane solid vinegar concentration device according to any one of claims 1 to 6, characterized in that: The following steps are included: S1: Primary concentration, injecting vinegar raw materials and pure water into circulation tank 1, the mixed liquid in circulation tank 1 is sent to membrane module 1, acetic acid and water are permeated through multiple sets of semi-permeable membrane groups, and the remaining substances are intercepted, and the permeate enters the permeate tank; The remaining substances are re-entered into the membrane module 1 through the circulation pump for treatment. This is the internal circulation operation. After several internal circulation operations, the internal circulation valve is closed and the mixed liquid is sent to the external circulation pipe 1 through the high-pressure pump 1 and the feed pump 1. Take samples at the reflux valve. If they do not meet the requirements, they are sent back to the circulation tank through the external circulation valve. Repeat the above operation. This is the external circulation operation. If the requirements are met, the first-stage concentrated liquid is obtained. At this time, the external circulation valve 1 is closed to allow the first-stage concentrated liquid to enter the circulation tank 2 through the feed pipe 2; S2: Secondary concentration: the primary concentrate in the circulation tank 2 is passed into the membrane module 2 through the discharge pipe 2. The membrane module 2 performs permeation concentration on the primary concentrate again. The permeate enters the permeate tank. The concentrated primary concentrate enters the circulation pipe 2 through the high-pressure pump 2 and the feed pump 2. Take a sample of the primary concentrated liquid in the circulation pipe 2. If it does not meet the standard, it will enter the circulation tank 2 again and repeat the above operation. This is the external circulation operation; If the standard is met, a secondary concentrate is obtained, which is discharged and collected through a concentrate valve and a concentrate pump; S3: Cleaning: the pure water in the cleaning tank and the alkali solution in the alkali solution barrel are mixed into a cleaning solution, and the cleaning solution is respectively sent to the discharge pipe 1 and the discharge pipe 2 through the discharge pipe 3. In the primary concentration system, the cleaning liquid first enters into the membrane module 1 to flush several semi-permeable membrane groups, and then the circulation pump 1 performs internal circulation operation to thoroughly clean the membrane module 1. During the cleaning process, the liquid intercepted by the membrane module 1 is discharged through the flushing valve and the sewage pipe set on the discharge pipe 1; the pure water permeated from the membrane module 1 enters into the cleaning pipe and is sent back to the cleaning tank; In the secondary concentration system, the cleaning liquid first enters the membrane module 2 to flush the semipermeable membrane group. During the cleaning process, the liquid intercepted by the membrane module 2 is discharged through the flushing valve and the sewage pipe set on the discharge pipe 2; the pure water permeated from the membrane module 2 enters the cleaning pipe and is sent back to the cleaning tank; During the cleaning process, the gas generated by the reaction is sent into the cleaning tank through the exhaust pipe and discharged through the cleaning tank; The used cleaning liquid in the cleaning tank is discharged through the drain valve and drain pipe at the bottom of the cleaning tank.

8. The processing technology of a membrane solid vinegar concentration device according to claim 7 is characterized in that: The concentration pressure in the primary circulation system is 2.0-2.5 MPa, the concentration ratio is 2.5 times, and the concentration temperature is ≤45°C.

9. A membrane solid vinegar concentration device and process according to claim 7, characterized in that: The concentration pressure in the secondary circulation system is 3.0-3.5 MPa, the ultimate pressure is ≤4.0 MPa, the concentration ratio is 2 times, and the concentration temperature is ≤45°C.

10. A membrane solid vinegar concentration device and process according to claim 7, characterized in that: The reverse osmosis membrane is a semipermeable membrane with a molecular weight cut-off of 70.

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