An anaerobic membrane bioreactor

Abstract

The present invention relates to the field of anaerobic digestion technology, and more particularly to an anaerobic membrane bioreactor comprising: a reactor body; and a selectively oxygen-permeable micro-aeration membrane assembly; the selectively oxygen-permeable micro-aeration membrane assembly disposed within the reactor body; the selectively oxygen-permeable micro-aeration membrane assembly being connected to an air inlet pipe and an air outlet pipe, respectively; and the air inlet pipe being connected to a micro-aeration pump. The reactor of the present invention solves the problems of high membrane fouling rates and slow dissolution / hydrolysis rates of suspended and macromolecular organic matter in existing reactors by diffusing molecular oxygen into a sludge mixture within the anaerobic membrane bioreactor through the selectively oxygen-permeable micro-aeration membrane assembly.

Description

Technical Field

[0001] The present invention relates to the technical field of anaerobic digestion, in particular to an anaerobic membrane bioreactor. Background Art

[0002] Anaerobic digestion (AD) is a key step in advancing the carbon neutrality strategy because it can reduce organic pollutants, provide methane energy, and recover nitrogen and phosphorus resources. However, AD inevitably faces defects such as low methane yield and low organic matter hydrolysis efficiency. In particular, the dissolution / hydrolysis of organic wastewater containing insoluble / refractory organic wastewater, organic matter and macromolecular solids are becoming the main bottlenecks restricting its anaerobic digestion performance. In recent years, the anaerobic membrane bioreactor (AnMBR) process has been considered to be an effective strategy to stimulate the hydrolysis of some insoluble / refractory organic matter.

[0003] The AnMBR process uses microfiltration / ultrafiltration membrane separation to replace gravity sedimentation coupled with traditional anaerobic digestion. By completely retaining suspended solids and effectively retaining macromolecular organic matter, it achieves complete separation of hydraulic retention time (HRT) from sludge retention time (SRT), and partial separation from suspended and macromolecular organic retention time (ORT, the biochemical reaction time with anaerobic microorganisms). However, AnMBR still faces technical bottlenecks that limit its engineering application, such as membrane fouling caused by organic adsorption, inorganic precipitation, and microbial cell adhesion to the membrane surface in actual wastewater, as well as slow solubility / hydrolysis rates of suspended and macromolecular organic matter. Summary of the Invention

[0004] The object of the present invention is to provide an anaerobic membrane bioreactor, which can reduce the rate of membrane fouling and improve the hydrolysis efficiency of insoluble / poorly soluble organic matter.

[0005] The present invention provides an anaerobic membrane bioreactor, comprising: a reactor body, characterized in that it also comprises: a selective oxygen permeable micro-aeration membrane assembly; the selective oxygen permeable micro-aeration membrane assembly is arranged inside the reactor body; the selective oxygen permeable micro-aeration membrane assembly is respectively connected to an air inlet pipeline and an exhaust pipeline; the air inlet pipeline is connected to a micro-aeration pump.

[0006] Preferably, the selective oxygen permeable micro-aeration membrane assembly is a selective oxygen permeable dense hollow fiber aeration membrane.

[0007] Preferably, it further comprises: an ORP meter; the ORP meter is arranged on the side wall of the reactor body.

[0008] Preferably, a flow meter is provided on the air intake pipe.

[0009] Preferably, a first valve is provided on the intake pipe; and a second valve is provided on the exhaust pipe.

[0010] Preferably, a filter membrane assembly is provided inside the reactor body; the selective oxygen permeable micro-aeration membrane assembly and the filter membrane assembly are arranged side by side relative to each other.

[0011] Preferably, the filter membrane assembly is respectively connected to a water outlet pipeline and a water inlet pipeline; the water outlet pipeline is sequentially connected to a pressure gauge, a third valve, a peristaltic pump, a fourth valve and a measuring cylinder.

[0012] Preferably, a return water pipeline is connected between the peristaltic pump and the fourth valve; the end of the return water pipeline is located above the interior of the reactor body, and a fifth valve is provided on the return water pipeline.

[0013] Preferably, the reactor body also includes: a vacuum biogas circulation pump; the vacuum biogas circulation pump is connected to a biogas circulation inlet pipeline and a biogas circulation outlet pipeline; the end of the biogas circulation inlet pipeline is connected to a filter port located above the interior of the reactor body; the end of the biogas circulation outlet pipeline is provided with a perforated aeration pipe located below the interior of the reactor body.

[0014] Preferably, a sample inlet is provided on the top of the reactor body.

[0015] Beneficial effects:

[0016] The technical solution of the present invention diffuses molecular oxygen into the sludge mixed liquid in the anaerobic membrane bioreactor through a selective oxygen-permeable micro-aeration membrane assembly, thereby improving the particle size of sludge particles and thereby reducing the membrane fouling rate. Moreover, it can improve the activity of facultative anaerobic bacteria in the anaerobic membrane bioreactor system, solving the problem of slow dissolution / hydrolysis rate of suspended and macromolecular organic matter in existing reactors. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the specific embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0018] Figure 1 A schematic structural diagram of the anaerobic membrane bioreactor provided by the present invention;

[0019] Figure 2This is a graph showing changes in protein group content in Example 2 of the present invention, wherein no micro-aeration refers to an AD experiment without micro-aeration conditions performed before the micro-aeration group, micro-aeration refers to an AD experiment without micro-aeration conditions performed in the micro-aeration group, and no micro-aeration (2) refers to an AD experiment without micro-aeration conditions performed after the micro-aeration group.

[0020] Figure 3 This is a graph showing changes in TCOD and SCOD content in the proteome in Example 2 of the present invention;

[0021] Figure 4 This is a graph showing changes in polysaccharide content in the starch group in Example 2 of the present invention;

[0022] Figure 5 This is a graph showing changes in TCOD and SCOD content in the starch group in Example 2 of the present invention;

[0023] Figure 6 This is the critical flux test of the proteome in Example 3 of the present invention under the condition of no micro-aeration;

[0024] Figure 7 This is the critical flux test of the proteome under micro-aeration conditions in Example 3 of the present invention;

[0025] Figure 8 This is the critical flux test result of the starch group without micro-aeration in Example 3 of the present invention;

[0026] Figure 9 This is the critical flux test of the starch group under micro-aeration conditions in Example 3 of the present invention;

[0027] Figure 10 This is the particle size distribution test of the proteomic sludge mixture in Example 3 of the present invention;

[0028] Figure 11 This is the particle size distribution test of the starch group sludge mixture in Example 3 of the present invention;

[0029] Figure 12 A physical picture of the selective oxygen permeable micro-aeration membrane assembly provided by the present invention;

[0030] Figure 13 A schematic diagram of the structure of a selective oxygen permeable micro-aeration membrane assembly provided by the present invention;

[0031] Figure 14 A schematic diagram of the membrane structure design of the selective oxygen permeable micro-aeration membrane assembly provided by the present invention;

[0032] Figure 15 This is a scanning electron microscope image of the membrane structure cross-section of the selective oxygen permeable micro-aeration membrane assembly provided by the present invention.

[0033] Explanation of the accompanying symbols: 1. Inlet; 2. Water outlet pipe; 3. Pressure gauge; 4. Third valve; 5. Peristaltic pump; 6. Fourth valve; 7. Measuring cylinder; 8. Fifth valve; 9. Reactor body; 10. Filter membrane assembly; 11. Perforated aeration tube; 12. Selective oxygen permeability micro-aeration membrane assembly; 121. Support core; 122. Hollow fiber; 123. Biomembrane; 124. Membrane fiber diameter; 125. Air inlet; 126. First exhaust port; 127. Second exhaust port; 13. Biogas circulation outlet pipe; 14. Biogas circulation inlet pipe; 15. Vacuum biogas circulation pump; 16. Flow meter; 17. Micro-aeration pump; 18. ORP meter; 19. Exhaust pipe; 20. Filter port; 21. Methane measurement system. DETAILED DESCRIPTION

[0034] The following will clearly and completely describe the technical solutions of the present invention in conjunction with the embodiments. Obviously, the embodiments described are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0035] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise" and the like to indicate directions or positional relationships based on the directions or positional relationships shown in the accompanying drawings, and 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 direction, be constructed and operate in a specific direction, and therefore should not be understood as limiting the present invention.

[0036] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the said features. In the description of the present invention, "multiple" means two or more, unless otherwise clearly and specifically defined. In addition, the terms "installed", "connected", and "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be a communication between the two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to the specific circumstances.

[0037] Example 1

[0038] like Figure 1 As shown, this embodiment provides an anaerobic membrane bioreactor, including: a reactor body 9, and also including: a selective oxygen permeable micro-aeration membrane assembly 12; the selective oxygen permeable micro-aeration membrane assembly 12 is arranged inside the reactor body 9; the selective oxygen permeable micro-aeration membrane assembly 12 is respectively connected to an air inlet pipe and an exhaust pipe 19; the air inlet pipe is connected to the micro-aeration pump 17.

[0039] In this embodiment, a selective oxygen permeable micro-aeration membrane assembly 12 is introduced into the anaerobic membrane bioreactor to provide a trace amount of oxygen to stimulate the activity of facultative anaerobic bacteria, thereby increasing the efficiency of organic matter dissolution / hydrolysis and improving the characteristics of the sludge mixed liquor, thereby optimizing the membrane fouling potential.

[0040] like Figures 12 to 15 As shown, in this embodiment, an air inlet 125, a first exhaust port 126 and a second exhaust port 127 are provided at the upper end of the selective oxygen permeable micro-aeration membrane assembly 12; wherein, the air inlet 125 is connected to the air inlet pipeline; the first exhaust port 126 and the second exhaust port 127 are respectively connected to the exhaust pipeline 19. When in use, any one of the first exhaust port 126 and the second exhaust port 127 is opened and the other is closed; when the exhaust port in use is blocked, nitrogen cannot be discharged, accumulates in the membrane cavity, and aeration cannot be performed. At this time, the other exhaust port can be switched in time without affecting the operation of the equipment.

[0041] In this embodiment, the selective oxygen permeable micro-aeration membrane assembly 12 includes, from inside to outside, a supporting core 121 , hollow fibers 122 , and a biological membrane 123 . The diameter 124 of the membrane fibers of the selective oxygen permeable micro-aeration membrane assembly 12 is approximately 0.7 mm.

[0042] The selective oxygen permeable micro-aeration membrane assembly 12 can be used to pass oxygen in the air into the reactor, thereby preventing other gases in the air except oxygen from entering the reactor, especially nitrogen in the air, which can inhibit the formation of methane and reduce the methane yield.

[0043] In this embodiment, the selective oxygen permeable micro-aeration membrane assembly 12 is a selective oxygen permeable dense hollow fiber aeration membrane assembly. The working principle is to utilize the synergistic effect between the selective gas permeable membrane and the attached growth type biofilm. The gas permeable membrane is used to transfer oxygen to the biofilm attached to the surface of the gas permeable membrane. At the same time, matrices such as ammonia and organic matter diffuse from the sewage into the biofilm. The MABR aerobic biofilm (with nitrifying bacteria as the dominant bacteria) installed in the anoxic tank and the denitrifying bacteria suspended in the anoxic zone realize synchronous nitrification and denitrification (SND) to enhance the removal of ammonia nitrogen and total nitrogen in the sewage.

[0044] It is understood that the specific shape, size, and number of the selective oxygen permeable micro-aeration membrane assemblies 12 in this embodiment can be flexibly configured according to actual needs and are not limited to a specific form. For example, the selective oxygen permeable micro-aeration membrane assemblies 12 in this embodiment can be arranged in multiple groups, and these multiple groups can be arranged around the filter membrane assembly 10 to better stimulate the activity of facultative anaerobic bacteria. Furthermore, the inlet lines of the multiple groups of selective oxygen permeable micro-aeration membrane assemblies 12 can be connected to the same main inlet line, and the outlet lines of the multiple groups of selective oxygen permeable micro-aeration membrane assemblies 12 can be connected to the same main inlet line. Of course, the main inlet line can also be connected to an exhaust gas treatment device. Furthermore, the selective oxygen permeable micro-aeration membrane assemblies 12 can be arranged vertically or horizontally, or the selective oxygen permeable micro-aeration membrane assemblies 12 surrounding the assemblies can be arranged at an angle, with all selective oxygen permeable micro-aeration membrane assemblies 12 tilted toward the filter membrane assembly 10. It can be seen that there are many ways to modify or replace this embodiment, which will not be described in detail here.

[0045] This embodiment further includes an ORP meter 18, which is mounted on the side wall of the reactor body 9. The membrane micro-aeration dosage is adjusted by the actual ORP value (ensuring ORP is between -300-0 mv) instead of the dissolved oxygen adjustment, and ORP is more sensitive to the oxygen introduced.

[0046] In this embodiment, a flow meter 16 is provided in the air intake pipeline.

[0047] In this embodiment, a first valve is provided on the intake pipe; and a second valve is provided on the exhaust pipe 19 .

[0048] In this embodiment, a filtration membrane assembly 10 is provided inside the reactor body 9 ; and a selective oxygen permeable micro-aeration membrane assembly 12 is arranged side by side with the filtration membrane assembly 10 .

[0049] In this embodiment, the filter membrane assembly 10 is connected to a water outlet pipe 2 and a water inlet pipe respectively; the water outlet pipe 2 is sequentially connected to a pressure gauge 3, a third valve 4, a peristaltic pump 5, a fourth valve 6 and a measuring cylinder 7.

[0050] In this embodiment, a return water pipeline is connected between the peristaltic pump 5 and the fourth valve 6 ; the end of the return water pipeline is located above the interior of the reactor body 9 , and a fifth valve 8 is provided on the return water pipeline.

[0051] In this embodiment, the reactor body 9 also includes: a vacuum biogas circulation pump 15; the vacuum biogas circulation pump 15 is connected to a biogas circulation inlet pipe 14 and a biogas circulation outlet pipe 13; the end of the biogas circulation inlet pipe 14 is connected to a filter port 20 located above the interior of the reactor body 9; the end of the biogas circulation outlet pipe 13 is provided with a perforated aeration pipe 11 located below the interior of the reactor body 9.

[0052] In this embodiment, a sample inlet 1 is provided on the top of the reactor body 9 .

[0053] In this embodiment, the present invention further comprises: a methane measuring system 21 , which is connected to the reactor body 9 through a pipeline.

[0054] The working principle and process of the anaerobic membrane bioreactor are as follows:

[0055] The outlet pipe 2, pressure gauge 3, third valve 4, peristaltic pump 5, fourth valve 6, measuring cylinder 7, fifth valve 8, and filter membrane assembly 10 are used to test membrane flux and critical flux to evaluate the membrane fouling potential: the sludge mixture is sucked into the inner cavity of the filter membrane assembly 10 by the peristaltic pump 5 and then flows along the outlet pipe 2, pressure gauge 3, third valve 4, peristaltic pump 5, fourth valve 6, and measuring cylinder 7 to test the flux of the filter membrane assembly 10 and record the pressure value; the critical flux of the filter membrane assembly 10 is tested along the outlet pipe 2, pressure gauge 3, third valve 4, peristaltic pump 5, and fifth valve 8.

[0056] The perforated aeration pipe 11, the biogas circulation outlet pipe 13, the biogas circulation inlet pipe 14, the vacuum biogas circulation pump 15, and the filter port 20 are used for biogas circulation aeration: after the biogas is sucked out through the filter port 20, it passes through the biogas circulation inlet pipe 14, the vacuum biogas circulation pump 15, the biogas circulation outlet pipe 13, and the perforated aeration pipe 11 to perform biogas aeration circulation to completely mix the sludge.

[0057] The reactor body 9, the selective oxygen permeable micro-aeration membrane assembly 12, the flow meter 16, the micro-aeration pump 17, the ORP meter 18, and the exhaust pipe 19 are used for micro-aeration of the anaerobic system: membrane micro-aeration is performed through the micro-aeration pump 17, the flow meter 16, the selective oxygen permeable micro-aeration membrane assembly 12, and the exhaust pipe 19. Oxygen penetrates into the reactor body 9 through the selective oxygen permeable micro-aeration membrane assembly 12, and other gases (nitrogen, etc.) in the air source except oxygen are discharged through the exhaust pipe 19, avoiding the interference of nitrogen sources in the air on methane generation. The aeration amount is monitored by the ORP meter 18 to prevent excessive aeration.

[0058] Example 2

[0059] In this embodiment, bacterial peptone and insoluble starch were selected as carbon sources and injected into a pre-temporarily acclimated AnMBR at a chemical oxygen demand (COD) dose of 4 g / L. NH4Cl and Na2HPO4 were used as nitrogen and phosphorus sources, respectively, to ensure that COD:N:P in the reactor body 9 was 200:5:1. NaHCO3 and COD were used in a ratio of 1:1 to keep the pH value in the reactor body 9 stable to prevent excessive acidification due to VFA accumulation. The culture solution was added into the reactor body 9 from the sampling port 1 for batch experiments.

[0060] Batch anaerobic digestion experiments were conducted in two parts according to different organic carbon sources:

[0061] Proteome: Using dissolved macromolecular proteins as carbon source, the effects of three stages (no micro-aeration, micro-aeration, and no micro-aeration (2)) on the solubility / hydrolysis of organic matter were investigated by measuring the content change trend of macromolecular proteins and TCOD / COD.

[0062] Starch group: Insoluble starch was used instead of carbon source. The optimization of organic matter solubility / hydrolysis in three stages (no micro-aeration, micro-aeration, and no micro-aeration (2)) was investigated by measuring the changing trends of macromolecular protein and TCOD / COD content.

[0063] The results of proteomic experiments are as follows Figure 2 、 Figure 3 The figures show the changes in total protein and TCOD / SCOD content in the sludge mixture when protein is used as the carbon source. It can be clearly seen that after the addition of dissolved protein, the protein and TCOD / SCOD in the three groups increased similarly. Figure 2 The solubility / hydrolysis efficiency of macromolecular organic matter was improved under micro-aeration conditions. The protein degradation rate of the micro-aeration group was increased by 120.78%-586.51% compared with the blank group without membrane micro-aeration. In addition, the TCOD removal rate of the protein group under micro-aeration conditions was 68.45%-73.74% higher than that of the group without micro-aeration. Figure 3 ).

[0064] The experimental results of starch group are as follows Figure 4 、 Figure 5 Displayed separately: Figure 4 The dissolved polysaccharides in the three groups increased to a certain extent after the first day of administration, indicating that the injected starch was partially dissolved. However, compared with the micro-aeration group, the polysaccharide dissolution / hydrolysis efficiency of the non-micro-aeration group was significantly lower. The polysaccharide content in the micro-aeration group increased significantly from day 1 to day 6, and then decreased rapidly. This may be due to the rapid hydrolysis of insoluble starch and the rapid consumption after dissolution. Figure 5In the group without micro-aeration, TCOD fluctuated significantly, but generally showed a slow downward trend, while SCOD showed a continuous upward trend, indicating that the utilization rate of dissolved organic matter by microorganisms was low (the COD degradation rate was only 10.20%). On the first day of starch addition, TCOD showed a jump-like growth in the micro-aeration group and the group without micro-aeration (2), and then showed a downward trend. SCOD mainly showed a state of first increasing and then decreasing. This shows that microorganisms have a continuous effect on the utilization of organic matter after micro-aeration (the COD degradation rate of the micro-aeration group was 37.53%, and that of the group without micro-aeration (2) was 20.78).

[0065] The above results show that membrane micro-aeration has an excellent effect in promoting the dissolution / hydrolysis of organic matter.

[0066] Example 3

[0067] The filtration performance of the membrane assembly was measured using negative pressure suction from a peristaltic pump 5. The critical flux of the membrane assembly 10 was measured under both no and micro-aeration conditions. The effect of micro-aeration on membrane fouling potential control was evaluated by observing the temporal changes in transmembrane pressure (TMP) under different membrane flux conditions.

[0068] The test system consists of a filtration membrane assembly 10, a water inlet pipe 2, a third valve 4, a fourth valve 6, a fifth valve 8, a pressure gauge 3, a peristaltic pump 5, and a measuring cylinder 7. When the third valve 4 and the fourth valve 6 are opened and the fifth valve 8 is closed, the membrane flux of the filtration membrane assembly 10 can be measured. When the third valve 4 and the fifth valve 8 are opened and the fourth valve 6 is closed, its critical flux can be measured. The results are shown in FIG. Figure 6 、 Figure 7 As shown in the figure, the critical flux of protein under no micro-aeration and micro-aeration conditions is shown. It can be clearly seen from the figure that under micro-aeration conditions, the transmembrane pressure (TMP) rises slowly in low-flux operation. By simple linear fitting, the critical flux of protein under no micro-aeration and micro-aeration conditions is 1.76 and 2.71 L / m 2 / h micro-aeration conditions, the slopes of TMP increase with time were 0.0041 and 0.0718 ( Figure 7 ), while the slopes without micro-aeration were 0.0065 and 0.167 ( Figure 6 ).

[0069] The results showed that micro-aeration was very effective in controlling membrane fouling under low flux operating conditions, which may be due to the optimization of the settling properties of the sludge mixture.

[0070] Critical flux test of starch group under no micro-aeration and micro-aeration conditions Figure 8 and Figure 9 The results were similar to those of the protein group. The TMP of the micro-aeration group increased more slowly over time (1.47 L / m 2 / h is 0.0315, 2.47L / m 2 / h is 0.0871, and when operated under similar low flux conditions, the TMP without micro-aeration increases faster with time (1.41 L / m 2 / h is 0.0815, 2.65L / m 2 / h is 0.1201), indicating that micro-aeration is helpful to membrane fouling control.

[0071] exist Figure 10 and Figure 11 The results show that sludge particle size has a significant tendency to increase under membrane micro-aeration conditions. Membrane fouling is controlled by improving sludge particle size. Sludge particles deposited on the membrane surface can form a filter cake layer, causing contamination. However, biogas aeration scouring exerts shear force on sludge particles in one direction (away from the membrane surface), and this shear force is proportional to particle size. Therefore, larger particle size results in greater shear force away from the membrane surface, making it less likely for sludge particles to deposit on the membrane surface, and thus reducing the membrane fouling rate.

[0072] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the above embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the above embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. An anaerobic membrane bioreactor, comprising: The reactor body (9) is characterized in that it further comprises: a selective oxygen permeable micro-aeration membrane assembly (12); the selective oxygen permeable micro-aeration membrane assembly (12) is arranged inside the reactor body (9); the selective oxygen permeable micro-aeration membrane assembly (12) is respectively connected to an air inlet pipeline and an air outlet pipeline (19); the air inlet pipeline is connected to a micro-aeration pump (17); The redox potential is monitored simultaneously.

2. The anaerobic membrane bioreactor according to claim 1, characterized in that The selective oxygen permeable micro-aeration membrane component (12) is a selective oxygen permeable dense hollow fiber aeration membrane.

3. The anaerobic membrane bioreactor according to claim 1, characterized in that Also includes: An oxidation-reduction potential measuring instrument (18); the oxidation-reduction potential measuring instrument (18) is arranged on the side wall of the reactor body (9).

4. The anaerobic membrane bioreactor according to claim 3, characterized in that A flow meter (16) is provided on the air intake pipeline.

5. The anaerobic membrane bioreactor according to claim 4, characterized in that A first valve is provided on the air intake pipeline; and a second valve is provided on the exhaust pipeline (19).

6. The anaerobic membrane bioreactor according to claim 5, characterized in that: A filter membrane assembly (10) is provided inside the reactor body (9); the selective oxygen permeable micro-aeration membrane assembly (12) and the filter membrane assembly (10) are arranged side by side relative to each other.

7. The anaerobic membrane bioreactor according to claim 6, characterized in that: The filter membrane assembly (10) is respectively connected to a water outlet pipeline (2) and a water inlet pipeline; the water outlet pipeline (2) is sequentially connected to a pressure gauge (3), a third valve (4), a peristaltic pump (5), a fourth valve (6) and a measuring cylinder (7).

8. The anaerobic membrane bioreactor according to claim 7, characterized in that: A return water pipeline is connected between the peristaltic pump (5) and the fourth valve (6); the end of the return water pipeline is located above the interior of the reactor body (9), and a fifth valve (8) is provided on the return water pipeline.

9. The anaerobic membrane bioreactor according to claim 8, characterized in that The reactor body (9) further comprises: a vacuum biogas circulation pump (15); the vacuum biogas circulation pump (15) is connected to a biogas circulation inlet pipe (14) and a biogas circulation outlet pipe (13); the end of the biogas circulation inlet pipe (14) is connected to a filter port (20) located above the interior of the reactor body (9); and the end of the biogas circulation outlet pipe (13) is provided with a perforated aeration pipe (11) located below the interior of the reactor body (9).

10. The anaerobic membrane bioreactor according to claim 9, characterized in that: The top of the reactor body (9) is provided with a sample inlet (1).

Images