Anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater

Abstract

The present invention discloses an anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater, which belongs to the technical field of traditional Chinese medicine wastewater biological treatment, including a raw water tank, an anaerobic EGSB reactor, a microaerobic EGSB reactor and an MBSBR reactor. The raw water tank is connected to the water inlet of the anaerobic EGSB reactor through a first water inlet pump, the anaerobic EGSB reactor is connected to the first water reservoir through a first water outlet pipe, the first water reservoir is connected to the water inlet of the microaerobic EGSB reactor through a second water inlet pump, the microaerobic EGSB reactor is connected to the second water reservoir through a second water outlet pipe, and the second water reservoir is connected to the MBSBR reactor through a third water inlet pump. The present invention adopts an anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater of the above structure, uses an anaerobic-microaerobic-aerobic combined process, improves the organic load upper limit of the combined system, realizes the effective removal of pollutants in high-ammonia nitrogen and high-concentration traditional Chinese medicine wastewater, and the effluent meets the emission limit, which can save energy consumption while achieving a high removal rate.

Description

Technical Field

[0001] The present invention relates to the technical field of biological treatment of traditional Chinese medicine wastewater, and in particular to an anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater. Background Art

[0002] Traditional Chinese medicine resources are important national strategic materials and the material foundation for safeguarding national health and developing the national medicine industry. Despite the thousands of years of development of the TCM industry, its production and processing cannot be considered a green and clean process. The production of TCM produces many residues, including wastewater, waste gas, and waste residue, which inevitably puts pressure on the ecological environment. TCM wastewater has a complex composition and may contain non-water-soluble components such as medicinal residues and debris, as well as water-soluble components such as polysaccharides, cellulose, and organic acids. It also has high concentrations of SS and organic matter, which may be biotoxic and difficult to treat. Single physical, chemical, or biological treatment processes are unable to effectively degrade the high concentrations of organic pollutants in TCM wastewater. Currently, scholars at home and abroad are widely using combined processes to treat TCM wastewater.

[0003] Combined treatment processes often use physicochemical methods as pretreatment, followed by anaerobic-aerobic and other biochemical processes as the main process, and finally, physicochemical methods as the final terminal treatment for advanced wastewater treatment. While combined processes can remove most COD and suspended solids (SS) in the anaerobic stage, traditional two-stage biological treatment systems have a low upper limit for organic loading. To prevent acidification of the anaerobic system due to load shock, high-concentration TCM wastewater must be diluted several times before entering the system for treatment. Furthermore, microorganisms such as nitrifying bacteria and phosphate-accumulating bacteria are not adaptable to anaerobic environments. Anaerobic treatment cannot simultaneously remove organic matter and nitrogen and phosphorus pollutants, resulting in poor nitrogen and phosphorus removal efficiency in anaerobic-aerobic two-stage treatment. For high-concentration TCM wastewater with high ammonia and nitrogen content, traditional anaerobic-aerobic two-stage biological treatment processes struggle to meet discharge standards. Physicochemical advanced treatment is also costly. Furthermore, in the context of my country's pursuit of carbon neutrality and the development of an ecological civilization system, developing an economical, efficient, and environmentally friendly treatment process to enhance industrial technological innovation and achieve green, low-carbon, and circular development has become a major trend.

[0004] Based on this, an anaerobic-microaerobic-aerobic three-stage combined process was proposed. Summary of the Invention

[0005] The purpose of the present invention is to provide an anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater. The anaerobic-microaerobic-aerobic three-stage combined process is used to increase the organic load upper limit of the combined system, effectively solve the disadvantage that the nitrogen and phosphorus pollutants in the effluent of the traditional treatment process do not meet the standards, and achieve effective removal of pollutants in high-concentration traditional Chinese medicine wastewater with high ammonia nitrogen, and the effluent meets the emission limit. Under low dissolved oxygen conditions, it can achieve a high removal rate while saving energy consumption.

[0006] To achieve the above objectives, the present invention provides an anaerobic-microaerobic EGSB and MBSBR combined treatment device for traditional Chinese medicine wastewater, comprising a raw water tank, an anaerobic EGSB reactor, a microaerobic EGSB reactor and an MBSBR reactor; the raw water tank is connected to the water inlet end of the anaerobic EGSB reactor through a first water inlet pump, the anaerobic EGSB reactor is connected to the first water storage tank through a first water outlet pipe, the first water storage tank is connected to the water inlet end of the microaerobic EGSB reactor through a second water inlet pump, the microaerobic EGSB reactor is connected to the second water storage tank through a second water outlet pipe, and the second water storage tank is connected to the MBSBR reactor through a third water inlet pump.

[0007] Preferably, the anaerobic EGSB reactor includes a reaction zone and a three-phase separation zone, the reaction zone is made of a plexiglass column with an outer diameter of 50 mm, an inner diameter of 40 mm, a height of 400 mm, and an effective volume of 500 mL, the outer layer of the reaction zone is provided with a constant temperature interlayer, and the outer wall of the reaction zone is evenly provided with multiple first sampling ports, the three-phase separation zone includes a gas separation zone and an overflow weir arranged at the upper end of the gas separation zone, the overflow weir is arranged in a sawtooth shape, the gas separation zone is arranged in an inverted cone shape, and the upper part of the gas separation zone is connected to the gas bag.

[0008] Preferably, the structural setting of the microaerobic EGSB reactor is the same as that of the anaerobic EGSB reactor, the return sewage outlet end of the microaerobic EGSB reactor is connected to an aeration tank through a reflux pump, an aeration head is provided at the bottom of the aeration tank, and the aeration tank is connected to the water inlet end of the microaerobic EGSB reactor through a second internal circulation pump.

[0009] Preferably, the MBSBR reactor is configured as a cylindrical structure made of plexiglass with an inner diameter of 8 cm, an outer diameter of 9 cm, a height of 30 cm, an effective volume of 1.5 L, and is wrapped with tin foil on the outside to avoid light. A plurality of second sampling ports are evenly arranged on the outer wall, an agitator is provided at the top, and an aeration disk is provided at the bottom. The aeration disk and the aeration head are both connected to the air compressor through a glass rotor air flow meter.

[0010] Preferably, a suspended filler is provided in the MBSBR reactor, and the suspended filler is a modified polyurethane filler.

[0011] Preferably, the return sewage outlet of the anaerobic EGSB reactor is connected to the water inlet of the anaerobic EGSB reactor through a first internal circulation pump.

[0012] Preferably, the hydraulic retention time of the reaction zones in the anaerobic EGSB reactor and the microaerobic EGSB reactor is 12 to 36 hours, and the rising flow rate is 1.5 to 3 m / h.

[0013] An anaerobic-microaerobic EGSB and MBSBR combined treatment process for traditional Chinese medicine wastewater comprises the following steps:

[0014] S1. Two groups of anaerobic EGSB reactors were started by artificial water distribution and low organic load operation mode. The artificial water distribution was controlled to control COD:N:P=250~400:5:1, and OLR=1~3kg COD / (m 3 d); add trace elements, and for the first time add an appropriate amount of NaHCO3 to adjust the pH value of the influent to 6.5-7.5 to enrich the hydrolytic acidifying bacteria;

[0015] S2. After successful startup, the influent is traditional Chinese medicine wastewater. A second dose of NaHCO3 is added to adjust the influent pH to 6.5-7.5. A set of EGSB reactors is adjusted to a microaerobic state through external aeration and oxygenation of the return sewage in the aeration tank. The dissolved oxygen concentration at the outlet above the microaerobic EGSB reactor is measured in real time to control the reactor to a microaerobic environment with DO = 0.30-1 mg / L. The raw water dilution ratio is gradually reduced and the organic load of the influent is increased. After the influent organic load reaches the upper limit of the system treatment, the anaerobic-microaerobic EGSB combination system is connected in series.

[0016] S3 and MBSBR reactors use diluted raw water to start acclimating sludge, gradually increasing the organic load of the influent and thus gradually increasing the metabolic activity of microorganisms in the MBSBR reactor. The MBSBR reactor operation phase is controlled to perform water inlet, stirring, aeration, sedimentation, drainage, and idle steps; after successful startup, the anaerobic-microaerobic EGSB and MBSBR combination systems are connected in series.

[0017] Preferably, the sewage flow route in the process is as follows: the raw water tank pumps the sewage into the anaerobic EGSB reactor through the first water inlet pump, the effluent of the anaerobic EGSB reactor flows into the first water storage tank, and is pumped into the microaerobic EGSB reactor by the second water inlet pump, and the effluent flows into the second water storage tank. The sewage in the second water storage tank is pumped into the MBSBR reactor by the third water inlet pump.

[0018] Preferably, in S3, after the reactor has been running stably for a period of time during the startup process, filler is added to the MBSBR reactor with a filling ratio of 20 to 50% (v / v), the sludge retention time is controlled to be 12 to 20 days, the hydraulic retention time is controlled to be 9 to 15 hours, and the time controller is used to control the anoxic stirring for 120 to 240 minutes. The DO concentration in the system is measured in real time by a portable dissolved oxygen meter, and the dissolved oxygen concentration in the MBSBR reactor is controlled to be 2 to 6 mg / L in the aeration stage, aerobic aeration for 360 to 600 minutes, static sedimentation for 30 to 50 minutes, and drainage for 10 minutes. The idle time is set according to the cycle time requirements.

[0019] Therefore, the present invention adopts an anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater using the above structure, which has the following beneficial effects:

[0020] (1) Under microaerobic conditions, molecular oxygen can act as an electron acceptor, relieve the accumulation and feedback inhibition of NADH, increase the activity of dehydrogenase and electron transfer, and effectively degrade pollutants through various metabolic pathways under the joint action of aerobic, facultative and anaerobic microorganisms.

[0021] (2) The anaerobic-microaerobic two-stage EGSB treatment increased the upper limit of the organic load of the combined system. When OLR = 12.5 kgCOD / (m 3 d) Two-stage EGSB combined system for COD and NH4 + The average removal rates of -N, TN and TP were 90.32%, 86.15%, 72.58% and 68.34%, respectively, providing a good matrix for aerobic treatment.

[0022] (3) The mass transfer resistance within the MBSBR causes a spatial concentration gradient of DO at different depths within the packing. The sequencing batch operation mode causes the DO concentration to change periodically over time. Therefore, the MBSBR has superior nitrogen and phosphorus removal performance compared to conventional aerobic reactors. Furthermore, under low dissolved oxygen conditions (DO = 2.5 mg / L), the microbial dehydrogenase and specific oxygen consumption rates within the MBSBR reactor are higher, leading to more vigorous metabolism and better pollutant removal performance than under high dissolved oxygen conditions.

[0023] (4) When the influent COD, TN, NH4 + When the average concentrations of -N and TP reach 12500, 400, 300 and 25 mg / L, the concentrations in the effluent are lower than 100, 8, 20 and 0.5 mg / L respectively. The effluent from the combined process can meet the emission limits of the "Discharge Standard of Water Pollutants for Traditional Chinese Medicine Pharmaceutical Industry (GB21906-2008)". The aerobic section can achieve high removal rates while saving energy consumption under low dissolved oxygen conditions. It is an effective method for treating high-concentration traditional Chinese medicine wastewater with high ammonia nitrogen.

[0024] The technical solution of the present invention is further described in detail below through the accompanying drawings and embodiments. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 This is a schematic structural diagram of an anaerobic-microaerobic EGSB and MBSBR combined treatment device for traditional Chinese medicine wastewater according to the present invention;

[0026] Figure 2 The diagrams of the inlet and outlet water changes of the anaerobic-microaerobic two-stage EGSB of the present invention are shown, where (a) and (b) are COD change diagrams, and (c) and (d) are NH4 + -N change diagram, (e) and (f) are TN change diagrams, (g) and (h) are TP change diagrams;

[0027] Figure 3 The diagrams of the inlet and outlet water changes of two groups of MBSBR in the present invention are shown in Figure 1, where (a) is the COD change diagram and (b) is the NH4 + -N variation diagram, (c) is TP variation diagram;

[0028] Figure 4 This is a UV-Vis scanning spectrum of the combined process of the present invention after the inlet and outlet water are diluted 50 times during the stable operation stage;

[0029] Figure 5 The UV is diluted 50 times by the inlet and outlet water during the stable operation stage of the combined process of the present invention. 254 Degradation diagram along the process;

[0030] Figure 6 The three-dimensional fluorescence spectra of the inlet and outlet water along the process after being diluted 50 times during the stable operation stage of the combined process of the present invention, wherein (a) is anaerobic inlet water, (b) is anaerobic effluent, (c) is microaerobic effluent, (d) is MBSBR1 effluent, and (e) is MBSBR2 effluent;

[0031] Reference numerals:

[0032] 1. Raw water tank; 2. First water inlet pump; 3. Anaerobic EGSB reactor; 4. Reaction zone; 5. First sampling port; 6. Constant temperature interlayer; 7. Three-phase separation zone; 8. Overflow weir; 9. First outlet pipe; 10. Gas separation zone; 11. Air bag; 12. First internal circulation pump; 13. First water storage tank; 14. Second water inlet pump; 15. Microaerobic EGSB reactor; 16. Reflux pump; 17. Second internal circulation pump; 18. Aeration tank; 19. Aeration head; 20. Glass rotor air flow meter; 21. Air compressor; 22. Second water storage tank; 23. Third water inlet pump; 24. MBSBR reactor; 25. Second sampling port; 26. Agitator; 27. Suspended filler; 28. Aeration disk; 29. Second outlet pipe. DETAILED DESCRIPTION

[0033] The technical solution of the present invention is further described below with reference to the accompanying drawings and embodiments.

[0034] In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments.

[0035] like Figure 1 As shown, the present invention provides a combined anaerobic-microaerobic EGSB and MBSBR treatment device for traditional Chinese medicine wastewater, comprising a raw water tank 1, an anaerobic EGSB reactor 3, a microaerobic EGSB reactor 15, and an MBSBR reactor 24. The MBSBR reactor 24 is a Moving Bed Sequencing Batch Reactor (MBSBR). This device effectively removes pollutants from high-concentration traditional Chinese medicine wastewater containing high ammonia and nitrogen concentrations. Anaerobic treatment improves the biodegradability of the wastewater and reduces some of the organic load.

[0036] The raw water tank 1 is connected to the water inlet of the anaerobic EGSB reactor 3 via a first water inlet pump 2. The anaerobic EGSB reactor 3 comprises a reaction zone 4 and a three-phase separation zone 7. The reaction zone 4 is made of a plexiglass column with an outer diameter of 50 mm, an inner diameter of 40 mm, a height of 400 mm, and an effective volume of 500 mL. The hydraulic retention time of the reaction zone within the anaerobic EGSB reactor and the microaerobic EGSB reactor is 12 to 36 hours, and the upward flow rate is 1.5 to 3 m / h. The outer layer of the reaction zone 4 is provided with a constant temperature interlayer 6, which is connected to the constant temperature hot water in the water bath via a submersible pump. The hot water is pumped into the constant temperature interlayer 6 and continuously circulated to maintain the temperature within the reactor at a constant temperature of 37±1°C. Multiple first sampling ports 5 are evenly distributed on the outer wall of the reaction zone 4. The three-phase separation zone 7 includes a gas separation zone 10 and an overflow weir 8 disposed at the upper end of the gas separation zone 10. The overflow weir 8 is configured in a sawtooth shape, and the gas separation zone 10 is configured in an inverted cone shape. The upper portion of the gas separation zone 10 is connected to an air bag 11. The return wastewater outlet of the anaerobic EGSB reactor 3 is connected to the water inlet of the anaerobic EGSB reactor 3 via a first internal circulation pump 12.

[0037] The anaerobic EGSB reactor 3 is connected to the first water storage tank 13 through the first outlet pipe 9. The first water storage tank 13 is connected to the water inlet end of the microaerobic EGSB reactor 15 through the second water inlet pump 14. The structural setting of the microaerobic EGSB reactor 15 is the same as that of the anaerobic EGSB reactor 3. The return sewage outlet end of the microaerobic EGSB reactor 15 is connected to the aeration tank 18 through the return pump 16. The bottom of the aeration tank 18 is provided with an aeration head 19. The aeration tank 18 is connected to the water inlet end of the microaerobic EGSB reactor 15 through the second internal circulation pump 17, so that the return sewage in the aeration tank 18 is pumped into the microaerobic EGSB reactor 15 again.

[0038] The microaerobic EGSB reactor 15 is connected to the second water storage tank 22 via a second outlet pipe 29. Both the first outlet pipe 9 and the second outlet pipe 29 are S-shaped water-sealed outlet pipes. The second water storage tank 22 is connected to the MBSBR reactor 24 via a third water inlet pump 23. The MBSBR reactor 24 is configured as a cylindrical structure made of organic glass with an inner diameter of 8 cm, an outer diameter of 9 cm, a height of 30 cm, and an effective volume of 1.5 L. The outer side is wrapped with tin foil to prevent light from growing photosynthetic bacteria. Its outer wall is evenly provided with multiple second sampling ports 25, a stirrer 26 is provided at the top, and an aeration disk 28 is provided at the bottom. The aeration disk 28 and the aeration head 19 are both connected to the air compressor 21 via a glass rotor air flow meter 20. A suspended filler 27 is provided in the MBSBR reactor 24. The suspended filler is a modified polyurethane filler, which is a cubic modified polyurethane sponge with a side length of 1 cm.

[0039] An anaerobic-microaerobic EGSB and MBSBR combined treatment process for traditional Chinese medicine wastewater comprises the following steps:

[0040] S1. Two groups of anaerobic EGSB reactors were started by artificial water distribution and low organic load operation mode. The artificial water distribution was controlled to control COD:N:P=250~400:5:1, and OLR=1~3kg COD / (m 3 d); add trace elements, and for the first time add an appropriate amount of NaHCO3 to adjust the pH value of the influent to 6.5-7.5 to enrich the hydrolytic acidifying bacteria;

[0041] S2. After successful startup, the influent is traditional Chinese medicine wastewater, and NaHCO3 is added for the second time to adjust the influent pH value to 6.5-7.5. A set of EGSB reactors is adjusted to a microaerobic state through external aeration and oxygenation of the return sewage in the aeration tank. The dissolved oxygen concentration at the outlet above the microaerobic EGSB reactor is measured in real time to control the reactor to a microaerobic environment (DO = 0.30-1 mg / L). The raw water dilution ratio is gradually reduced, and the organic load of the influent is increased. After the organic load of the influent reaches the upper limit of the system treatment, the anaerobic-microaerobic EGSB combination system is connected in series;

[0042] The S3 MBSBR reactor is started with diluted raw water to acclimate the sludge. The organic load of the influent is gradually increased, thereby gradually increasing the metabolic activity of the microorganisms within the MBSBR reactor. The MBSBR operation phase is controlled through the following steps: water inlet, stirring, aeration, sedimentation, drainage, and idle time. After a period of stable operation during the startup process, modified polyurethane filler is added to the MBSBR reactor at a filling ratio of 20-50% (v / v). The sludge retention time is controlled to 12-20 days, and the hydraulic retention time is controlled to 9-15 hours. Anoxic stirring is controlled using a time controller for 120-240 minutes. A portable dissolved oxygen meter is used to measure the DO concentration in the system in real time. The MBSBR reactor's dissolved oxygen concentration during the aeration phase is controlled to 2-6 mg / L, followed by aerobic aeration for 360-600 minutes, static sedimentation for 30-50 minutes, and drainage for 10 minutes. The idle time is set according to the cycle time required. After successful startup, the anaerobic-microaerobic EGSB and MBSBR combined system is connected in series.

[0043] The sewage flow route in the process is as follows: the raw water tank pumps the sewage into the anaerobic EGSB reactor through the first water inlet pump, the effluent of the anaerobic EGSB reactor flows into the first water storage tank, and is pumped into the microaerobic EGSB reactor by the second water inlet pump, and the effluent flows into the second water storage tank. The sewage in the second water storage tank is pumped into the MBSBR reactor by the third water inlet pump.

[0044] In this process, aerobic, facultative, and anaerobic microorganisms in a microaerobic environment spontaneously form an orderly distribution state, and efficiently remove nitrogen through multiple pathways such as simultaneous nitrification and denitrification, short-range denitrification, etc. The introduction of oxygen is also conducive to the enrichment of polyphosphate bacteria. During the operation of the MBSBR reactor, the joint changes in dissolved oxygen concentration in time and space make it have superior denitrification and phosphorus removal performance compared to ordinary aerobic reactors. The introduction of a microaerobic environment and the selection of an aerobic MBSBR reactor jointly improve the denitrification and phosphorus removal treatment capacity of the combined system, effectively solving the problem of substandard nitrogen and phosphorus pollutants in the effluent of traditional treatment processes. On this basis, the front-end anaerobic-microaerobic two-stage EGSB treatment increases the organic load upper limit of the combined system, making up for the defect of the low organic load upper limit of the traditional process, and realizing the effective removal of high ammonia nitrogen and high-concentration pollutants.

[0045] Example

[0046] An anaerobic-microaerobic EGSB and MBSBR combined treatment process for traditional Chinese medicine wastewater comprises the following steps:

[0047] S1. Two groups of anaerobic EGSB reactors were started using artificial water distribution and low organic load operation mode. Glucose, ammonium chloride and potassium dihydrogen phosphate were used to provide carbon source, nitrogen source and phosphorus source respectively. COD:N:P=250:5:1 and OLR=2kgCOD / (m 3d); Add trace elements and add NaHCO3 in an appropriate amount for the first time to adjust the pH value of the influent to 6.5-7.5 to enrich the hydrolytic acidifying bacteria.

[0048] S2, after successful startup, the influent is Chinese medicine wastewater, and NaHCO3 is added in an appropriate amount for the second time to adjust the influent pH to 6.5-7.5. In this embodiment, a licorice enzymatic hydrolysis sugar wastewater produced in the process of resource utilization of Chinese medicine residues is used, with COD 50000-55000 mg / L, ammonia nitrogen 1200-1400 mg / L, total nitrogen 2200-1500 mg / L, total phosphorus 100-120 mg / L, UV 254 The value is 34 to 38 cm -1 , pH is about 4.24, acidic, containing aromatic compounds such as humic acid and tyrosine. A group of EGSB reactors are adjusted to a microaerobic state by external aeration and oxygenation of the return sewage. The dissolved oxygen concentration at the outlet above the EGSB reactor is measured in real time, and the DO in the reactor is controlled to be 0.30 mg / L. The rising flow rate in the anaerobic EGSB reactor and the microaerobic EGSB reactor is 1.93 m / h, and the hydraulic retention time (HRT) is controlled to be 24 h. The raw water dilution ratio is gradually reduced to increase the organic load of the influent and gradually acclimate the sludge. After the influent organic load reaches the upper limit of the system treatment, the anaerobic-microaerobic EGSB combination system is connected in series.

[0049] The S3 and MBSBR reactors were started with diluted raw water to acclimate the sludge. The influent organic load was gradually increased to enhance microbial metabolic activity. The daily sludge discharge was approximately 100 mL, resulting in a controlled SRT of approximately 15 days, to enrich the nitrogen and phosphorus removal microorganisms. After a period of stable operation during startup, modified polyurethane filler was added to the MBSBR reactors at a filling ratio of 30% (v / v). The hydraulic retention time (HRT) was controlled at 12 hours. Water was manually added, and anoxic stirring was controlled for 180 minutes using a time controller. A portable dissolved oxygen (DO) meter was used to measure the system's DO concentration in real time. The two MBSBR reactors were controlled to have dissolved oxygen concentrations of 2.5 mg / L and 5 mg / L, respectively, during the aeration phase. Aerobic aeration lasted 480 minutes, followed by 50 minutes of settling and 10 minutes of drainage. The idle time was set based on the desired cycle time. After successful startup, the anaerobic-microaerobic EGSB and MBSBR systems were connected in series.

[0050] like Figure 2 As shown in the figure, anaerobic biological treatment improves the biodegradability of wastewater and reduces some organic loads. Under microaerobic conditions, molecular oxygen can act as an electron acceptor, relieve the accumulation and feedback inhibition of NADH, increase the activity of dehydrogenase and electron transfer, and effectively degrade pollutants through multiple metabolic pathways under the joint action of aerobic, facultative and anaerobic microorganisms. Anaerobic-microaerobic two-stage EGSB treatment has a significant impact on COD and NH4 +The average removal rates of -N, TN and TP were 90.32%, 86.15%, 72.58% and 68.34%, respectively, providing a good matrix for aerobic treatment.

[0051] like Figure 3 As shown in the figure, under low dissolved oxygen conditions (DO = 2.5 mg / L) in the stable stage of the MBSBR reactor, the microbial dehydrogenase and specific oxygen consumption rates are higher, the metabolism is more vigorous, and the pollutant removal performance is better than that under high dissolved oxygen conditions. + The average removal rates of -N and TP were 90.56%, 66.14% and 69.05% respectively, and the COD and NH4 + -N, TN and TP concentrations are lower than 100, 8, 20 and 0.5 mg / L respectively. The effluent from the combined system meets the emission limits of water pollutant discharge standards for traditional Chinese medicine pharmaceutical industry. Low dissolved oxygen conditions can achieve high removal rates while saving energy consumption.

[0052] like Figure 4-5 As shown, the raw water exhibits obvious absorption at 192 and 260 nm, indicating that the wastewater may contain a large amount of aromatic compounds and aldehydes, ketones, and carboxylic acid compounds. The overall absorption intensity of the inlet and outlet water gradually decreases along the combined process. 254 The UV value can reflect the concentration of humic organic matter and aromatic compounds containing unsaturated bonds in the water body. It is usually used as an indicator of the concentration of aromatic substances and can also be used to predict the acute toxicity of traditional Chinese medicine wastewater. 254 The values were 9.174±0.536, 6.609±1.127, 3.433±0.510, 0.605±0.127, and 0.585±0.139 cm -1 The removal effect of organic matter is better under low oxygen conditions. The anaerobic-microaerobic two-stage EGSB and MBSBR combined treatment system can effectively treat high-ammonia nitrogen and high-concentration traditional Chinese medicine wastewater.

[0053] like Figure 6As shown, the raw water primarily contains large amounts of aromatic proteins such as tyrosine and tryptophan, as well as various humic acids and small amounts of small-molecule compounds such as fulvic acid. The fluorescence intensity of the regions containing these organic compounds in the effluent of the anaerobic EGSB reactor decreased significantly. Some of the large-molecule organic matter in the anaerobic effluent was further broken down into a large number of easily degradable small-molecule intermediates under the metabolism of microaerobic microorganisms, resulting in increased concentrations of humic and fulvic acids in the microaerobic effluent. The characteristic peaks in the regions of tyrosine-based aromatic proteins and fulvic acids in the effluents of both MBSBR systems almost disappeared, and these two types of organic matter were nearly removed after aerobic treatment. The organic composition of the effluents from the two MBSBR systems was relatively similar, with no significant difference between high- and low-oxygen treatments. Both achieved good treatment results. Low dissolved oxygen conditions achieved high removal rates while saving energy.

[0054] Therefore, the present invention adopts an anaerobic-microaerobic EGSB and MBSBR combined treatment device and process for traditional Chinese medicine wastewater of the above structure, and uses an anaerobic-microaerobic-aerobic three-stage combined process to improve the organic load upper limit of the combined system, effectively solving the disadvantage of the traditional treatment process that the nitrogen and phosphorus pollutants in the effluent do not meet the standards, and realizes the effective removal of pollutants in high-concentration traditional Chinese medicine wastewater with high ammonia nitrogen, and the effluent meets the emission limit. Under low dissolved oxygen conditions, it can achieve a high removal rate while saving energy consumption.

[0055] 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 the same. Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that they can still modify or replace the technical solutions of the present invention with equivalents, and these modifications or equivalent replacements cannot cause the modified technical solutions to deviate from the spirit and scope of the technical solutions of the present invention.

Claims

1. An anaerobic-microaerobic EGSB and MBSBR combined treatment device for traditional Chinese medicine wastewater, characterized by: It includes a raw water tank, an anaerobic EGSB reactor, a microaerobic EGSB reactor and an MBSBR reactor; the raw water tank is connected to the water inlet of the anaerobic EGSB reactor through a first water inlet pump, the anaerobic EGSB reactor is connected to a first water storage tank through a first water outlet pipe, the first water storage tank is connected to the water inlet of the microaerobic EGSB reactor through a second water inlet pump, the microaerobic EGSB reactor is connected to a second water storage tank through a second water outlet pipe, and the second water storage tank is connected to the MBSBR reactor through a third water inlet pump; The anaerobic EGSB reactor includes a reaction zone and a three-phase separation zone. The outer layer of the reaction zone is provided with a constant temperature interlayer. The outer wall of the reaction zone is evenly provided with multiple first sampling ports. The three-phase separation zone includes a gas separation zone and an overflow weir provided at the upper end of the gas separation zone. The upper part of the gas separation zone is connected to the gas bag. The structural setting of the microaerobic EGSB reactor is the same as that of the anaerobic EGSB reactor. The return sewage outlet end of the microaerobic EGSB reactor is connected to an aeration tank via a return pump. An aeration head is provided at the bottom of the aeration tank, and the aeration tank is connected to the water inlet end of the microaerobic EGSB reactor via a second internal circulation pump. A suspended filler is provided in the MBSBR reactor, and the suspended filler is a modified polyurethane filler; The hydraulic retention time in the anaerobic EGSB reactor and the microaerobic EGSB reactor is 12-36 hours, and the rising flow rate is 1.5-3 m / h.

2. The anaerobic-microaerobic EGSB and MBSBR combined treatment device for traditional Chinese medicine wastewater according to claim 1, characterized in that: The MBSBR reactor is configured as a cylindrical structure made of organic glass, with multiple second sampling ports evenly arranged on its outer wall, an agitator arranged at the top, and an aeration disk arranged at the bottom. The aeration disk and the aeration head are both connected to the air compressor through a glass rotor air flow meter.

3. The anaerobic-microaerobic EGSB and MBSBR combined treatment device for traditional Chinese medicine wastewater according to claim 2, characterized in that: The return sewage outlet of the anaerobic EGSB reactor is connected to the water inlet of the anaerobic EGSB reactor through a first internal circulation pump.

4. A treatment process for Chinese medicine wastewater based on the anaerobic-microaerobic EGSB and MBSBR combined treatment device according to any one of claims 1 to 3, characterized in that: The following steps are involved: S1. Two groups of anaerobic EGSB reactors were started using artificial water distribution and low organic load operation mode. Artificial water distribution was used to control COD:N:P=250~400:5:1 and OLR=1~3 kg COD / (m 3 d); add trace elements, and for the first time add an appropriate amount of NaHCO3 to adjust the pH value of the influent to 6.5~7.5 to enrich the hydrolytic acidifying bacteria; S2. After successful startup, the influent is traditional Chinese medicine wastewater. A second dose of NaHCO3 is added to adjust the influent pH to 6.5-7.

5. A set of EGSB reactors is adjusted to a microaerobic state through external aeration and oxygenation of the return sewage in the aeration tank. The dissolved oxygen concentration at the outlet above the microaerobic EGSB reactor is measured in real time to control the reactor to a microaerobic environment with DO = 0.30-1 mg / L. The raw water dilution ratio is gradually reduced and the organic load of the influent is increased. After the influent organic load reaches the upper limit of the system treatment, the anaerobic-microaerobic EGSB combination system is connected in series. S3. The MBSBR reactor uses diluted raw water to start acclimating the sludge, gradually increasing the organic load of the influent and thus gradually increasing the metabolic activity of the microorganisms in the MBSBR reactor. The MBSBR reactor is controlled during the operation phase to carry out water inflow, stirring, aeration, sedimentation, drainage, and idle steps. After successful startup, the anaerobic-microaerobic EGSB and MBSBR combined systems are connected in series. During the startup process, after the reactor has been running stably for a period of time, fillers are added to the MBSBR reactor with a filling ratio of 20~50% (v / v), the sludge retention time is controlled to 12~20d, the hydraulic retention time is controlled to 9~15h, and a time controller is used to control the anoxic stirring for 120~240min. The DO concentration in the system is measured in real time by a portable dissolved oxygen meter. The dissolved oxygen concentration in the aeration stage of the MBSBR reactor is controlled to be 2~6mg / L, aerobic aeration for 360~600min, static sedimentation for 30~50min, and drainage for 10min.

5. The treatment process according to claim 4, characterized in that: The sewage flow route in the process is as follows: the raw water tank pumps the sewage into the anaerobic EGSB reactor through the first water inlet pump, the effluent of the anaerobic EGSB reactor flows into the first water storage tank, and is pumped into the microaerobic EGSB reactor by the second water inlet pump, and the effluent flows into the second water storage tank. The sewage in the second water storage tank is pumped into the MBSBR reactor by the third water inlet pump.

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