CN116903140A - Device and method for treating high-salt wastewater - Google Patents
Device and method for treating high-salt wastewater Download PDFInfo
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- CN116903140A CN116903140A CN202311074661.4A CN202311074661A CN116903140A CN 116903140 A CN116903140 A CN 116903140A CN 202311074661 A CN202311074661 A CN 202311074661A CN 116903140 A CN116903140 A CN 116903140A
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/163—Nitrates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The application provides a device and a method for treating high-salt wastewater, wherein the device comprises the following components in turn communicated with each other: a primary biochemical facultative tank 17, a primary aerobic reaction tank 18, an optional nitrifying tank 19, an optional degassing tank 20, a secondary facultative tank 21 and a secondary aerobic reaction tank 14. The device for treating the high-salt wastewater adopts a two-stage facultative aerobiotic treatment structure, so that after the wastewater with high salt concentration is subjected to twice AO treatment, the COD and ammonia nitrogen content in the wastewater are greatly reduced, the high-salt wastewater is treated more efficiently, and meanwhile, the ozone pollution is reduced.
Description
Technical Field
The application relates to the technical field of wastewater treatment, in particular to a device and a method for treating high-salt wastewater.
Background
At present, with the continuous acceleration of the industrialization process and the continuous deepening of the environment-friendly trend of near zero emission, the yield of high-salt wastewater is increased increasingly. The salt-containing wastewater has wide sources, mainly comprises concentrated wastewater generated in the fresh water recycling process in industries such as chemical industry, pharmacy, petroleum, food processing and the like, and wastewater generated by using a large amount of inorganic salt in the pesticide production process, and meanwhile, the finally discharged strong brine has high salt content, lower COD content and high ammonia nitrogen content due to the adoption of biochemical treatment measures and the like at the upstream, but cannot meet the environmental protection requirements of discharging or reducing the impurity salt content by subsequent salt separation crystallization.
The high-salt low-COD high-ammonia nitrogen wastewater generated in the coal chemical industry refers to wastewater with high organic matter content, salt content generally higher than 10000mg/L (TDS), COD lower than 800mg/L and ammonia nitrogen lower than 150mg/L. The salt substance mainly comprises Ca 2+ 、Cl - 、Mg 2+ 、Na + 、SO 4 2- 、K + The salt ions of the isostere and the salt changes greatly; meanwhile, after COD and ammonia nitrogen are further treated by adopting technical measures such as biochemistry and the like along with the pretreatment process, organic matters which are easy to be biochemically treated in the wastewater are degraded, but the organic matters impurities in the wastewater are further controlled based on the requirements of a follow-up environment-friendly or salt separation system on the COD and the ammonia nitrogen. Therefore, although the concentration of organic matters in the wastewater is low, the wastewater has the characteristics of complex components, high salinity, high chromaticity, poor biodegradability and the like, is difficult to treat, belongs to typical wastewater which is difficult to treat in coal chemical industry, and is difficult to reach the standard in actual treatment. Therefore, the treatment of high-salt, low-COD and high-ammonia nitrogen wastewater in the coal chemical industry is always a key bottleneck problem in the zero-emission process.
At present, the treatment process for COD in the high-salt wastewater in the coal chemical industry is mainly divided into conventional treatment methods (including ozone catalytic oxidation, micro-electrolysis-Fenton oxidation, multidimensional electro-catalysis, organic concentration and biochemical methods), and the technology cannot effectively treat ammonia nitrogen pollutants in water at the same time. The specific merits and applicability are shown in Table 1.
Table 1 comparison of COD treatment process for high salt wastewater
The biochemical method is one of the most widely used water treatment technologies at present due to the economical and efficient characteristics, but the biochemical method can only treat the salt-containing wastewater with the salt concentration lower than 1 percent, and meanwhile, the COD is required to be more than 1200 mg/l. The application of the biological method in the treatment of high-salt organic chemical wastewater can be seriously influenced under the condition of high salt. The mechanism of the microbial influence is mainly as follows: (1) The high salinity and high osmotic pressure can dehydrate cells, which in turn can separate the cytoplasmic walls of microorganisms, leading to cell disruption and death; (2) The high concentration of chloride ions has toxic effect on microbial cells; (3) High salinity can reduce microbial enzyme activity, and destroy normal metabolism of cells; (4) The high salinity can increase the density of the wastewater, so that the activated sludge floats upwards and is very easy to run off from a biological treatment system. At present, the biological treatment of high-salt water is mainly based on salt-tolerant complex bacteria and improves biochemical technology to improve the biochemical treatment effect, wherein the biochemical technology mainly comprises A/O, A2/O, SBR, MBR, contact oxidation and other technologies.
Therefore, the economic and efficient treatment mode of low COD and high ammonia nitrogen pollutants in the high-salt wastewater in the coal chemical industry is one of the industrial bottlenecks all the time, and the application efficiency of the biochemical treatment of the high-salt wastewater in the coal chemical industry in the industry cannot achieve industrial use and normal treatment effect. The problem of how to improve the utilization rate of a biochemical system, stabilize the treatment and reduce the discharge of a hydrogen oxidant such as ozone and the like in the treatment of high-salt wastewater and the reduction of the running cost of enterprises gradually becomes a hot spot.
Disclosure of Invention
The application mainly aims to provide a device and a method for treating high-salt wastewater, which are used for solving the problem that the prior art cannot carry out biochemical treatment on high ammonia nitrogen and low COD in the high-salt wastewater.
In order to achieve the above object, according to a first aspect of the present application, there is provided an apparatus for treating high-salt wastewater, the apparatus comprising, in communication: a primary biochemical facultative tank 17, a primary aerobic reaction tank 18, an optional nitrifying tank 19, an optional degassing tank 20, a secondary facultative tank 21 and a secondary aerobic reaction tank 14.
Further, biological implantation filling materials 5 are arranged in the first-stage biochemical facultative reaction tank 17, the first-stage aerobic reaction tank 18, the second-stage facultative reaction tank 21 and the second-stage aerobic reaction tank 14, and the biological implantation filling materials 5 consist of 1 at the center and 6 surrounding attachment beds; and the biological implantation filler 5 is suspended in water; preferably, the biological implantation packingAnd 5, the filler is biomembrane sludge. Preferably, the density of the biological implantation packing 5 is 0.94-0.99g/cm 3 The method comprises the steps of carrying out a first treatment on the surface of the Preferably, the number of the biological implantation filling materials 5 in the primary biochemical facultative reaction tank 17 and the primary aerobic reaction tank 18 is 1-2; preferably, the number of the biological implantation packing 5 in the secondary facultative tank 21 and the secondary aerobic reaction tank 14 is 1 to 2.
Further, the first-stage biochemical facultative reaction tank 17 comprises a plug flow stirring fan 8, and the plug flow stirring fan 8 is arranged at the bottom of the first-stage biochemical facultative reaction tank 17; preferably, the number of the plug flow stirring fans 8 is 1-2.
Further, an annular groove is arranged in the first-stage biochemical facultative reaction tank 17, and a circulating diving stirring system is arranged in the annular groove.
Further, the primary aerobic reaction tank 18, the nitrification tank 19 and the secondary aerobic reaction tank 14 comprise small-hole aeration systems 7, each small-hole aeration system 7 comprises an aeration main pipe and a plurality of aeration branch pipes communicated with the aeration main pipe, the plurality of aeration branch pipes extend from the tops of the primary aerobic reaction tank 18, the nitrification tank 19 and the secondary aerobic reaction tank 14 to the bottoms of the primary aerobic reaction tank 18, the nitrification tank 19 and the secondary aerobic reaction tank 14 respectively, the tail end of each aeration branch pipe is connected with an aeration pore plate, and a plurality of aeration holes are formed in the aeration pore plate; preferably, the plurality of aeration holes are arranged in an array on the aeration orifice plate; preferably, the material used for the small pore aeration system 7 is HDPE; preferably, the diameter of the aeration holes is 1-3mm; preferably, the distribution density of the aeration holes on the aeration pore plate is 1600/m 2 The method comprises the steps of carrying out a first treatment on the surface of the Preferably, the number of the aeration branch pipes is 2-4 in the primary aerobic reaction tank 18 and 1-2 in the nitrification tank 19; the number of the secondary aerobic reaction tanks 14 is 1-2.
Further, the nitrification tank 19 includes a nitrifying liquid reflux pump 15, and the nitrifying liquid reflux pump 15 is disposed at the bottom of the nitrifying tank 19; the nitrifying pond 19 and the first-stage biochemical facultative reaction pond 17 are communicated through a nitrifying liquid reflux pipeline 3 communicated with the nitrifying liquid reflux pump 15.
Further, the degassing tank 20 includes an intermediate degassing stirrer 16, the intermediate degassing stirrer 16 including a stirring rod and a paddle at an end of the stirring rod, the stirring rod passing through a top of the degassing tank 20 and extending to a bottom of the degassing tank 20; preferably, the number of intermediate degassing agitators 16 is 1-2.
Further, the secondary facultative tank 21 includes an anaerobic stirrer 22, the anaerobic stirrer 22 includes a stirring rod and a paddle at the end of the stirring rod, the stirring rod passes through the top of the secondary facultative tank 21 and extends to the bottom of the secondary facultative tank 21; preferably, the number of anaerobic agitators 22 is 1-2.
Further, the secondary aerobic reaction tank 14 comprises a water outlet filter screen 11, a water producing overflow weir 12 and a water producing pipeline 13, and the water filter screen 11, the water producing overflow weir 12 and the water producing pipeline 13 are sequentially arranged on the right side of the top of the secondary aerobic reaction tank 14 according to the water outflow direction.
Further, the walls of the primary biochemical facultative reaction tank 17 and the secondary facultative tank 21 are respectively provided with a composite salt-tolerant strain nutrient solution feeding pipeline 6; preferably, the wall of the primary biochemical facultative reaction tank 17 is also provided with a sludge return pipe 2 and/or a nitrified liquid return pipeline 3; preferably, the primary biochemical and facultative reaction tank 17 comprises a return channel 4, the return channel 4 is positioned below the outlet of the sludge return pipe 2 and the outlet of the nitrified liquid return pipeline 3 in the primary biochemical and facultative reaction tank 17 and near the tank top, and the materials returned by the sludge return pipe 2 and the nitrified liquid return pipeline 3 are returned into the primary biochemical and facultative reaction tank 17 through the return channel 4.
Further, overflow weirs are arranged between the first-stage biochemical facultative tank 17 and the first-stage aerobic reaction tank 18, between the first-stage aerobic reaction tank 18 and the nitrifying tank 19, between the nitrifying tank 19 and the degassing tank 20, between the degassing tank 20 and the second-stage facultative tank 21, and between the second-stage facultative tank 21 and the second-stage aerobic reaction tank 14, and are communicated through overflow weirs; preferably, a filter screen is provided in the overflow weir.
Further, the bottom of the first-stage biochemical facultative tank 17, the first-stage aerobic reaction tank 18, the degassing tank 20, the second-stage facultative tank 21 and the second-stage aerobic reaction tank 14 are all provided with an emptying pipe 9.
Further, a composite salt-tolerant strain is attached to the biological implantation filler 5, and preferably, the composite salt-tolerant strain includes nitrifying bacteria, denitrifying bacteria and halophilic bacteria.
Further, the building materials of the first-stage biochemical facultative tank 17, the first-stage aerobic reaction tank 18, the nitrifying tank 19, the degassing tank 20, the second-stage facultative tank 21 and the second-stage aerobic reaction tank 14 are concrete, and the materials in the tanks are all corrosion-resistant materials, preferably, the corrosion-resistant materials comprise glass fiber reinforced plastics.
In order to achieve the above object, according to a second aspect of the present application, there is provided a method for treating high-salt wastewater by the above-mentioned apparatus for treating high-salt wastewater, characterized by comprising: the high-salt wastewater sequentially enters a first-stage biochemical facultative reaction tank 17, a first-stage aerobic reaction tank 18 and a nitrifying tank 19 to obtain nitrifying liquid; reflux part of the nitrified liquid to a first-stage biochemical facultative reaction tank 17 by using a nitrified liquid reflux pump 15 for circulation; the rest part of nitrifying liquid sequentially enters a degassing tank 20, a secondary facultative tank 21 and a secondary aerobic reaction tank 14 to finish the treatment of the high-salt wastewater.
Further, the high-salt wastewater has a TDS salt content of 1-2%, a COD concentration of 100-800mg/L and an ammonia nitrogen content of 30-150mg/L.
Further, the volume ratio of the filler in the first-stage biochemical facultative reaction tank 17 is 40-45%; preferably, the volume ratio of the filler in the primary aerobic reaction tank 18 is 45-50%; preferably, the volume ratio of the filler in the secondary facultative tank 21 is 40-45%; preferably, the volume ratio of the filler in the secondary aerobic reaction tank 14 is 45-50%.
Further, the reflux volume ratio of the nitrifying liquid is 200-400%.
Further, the circulating flow is 5-6 times of the water inlet flow.
By applying the technical scheme of the application, the device for treating the high-salt wastewater adopts a two-stage facultative and aerobic treatment structure, so that the COD and ammonia nitrogen content in the high-salt wastewater with low COD and high ammonia nitrogen is greatly reduced after the high-salt wastewater with low ammonia nitrogen is subjected to twice AO treatment, the high-salt wastewater is treated more efficiently, and ozone pollution is reduced.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the application. In the drawings:
FIG. 1 shows a front view of an apparatus for treating high salt wastewater according to the present application;
FIG. 2 shows a plan view of the apparatus for treating high salt wastewater of the present application;
FIG. 3 shows a schematic elevation of the apparatus for treating high-salinity wastewater of the present application;
wherein, the above figure 1 comprises the following reference numerals:
1. a water inlet pipe; 2. a sludge return pipe; 3. a nitrifying liquid reflux pipeline; 4. a return channel; 5. a biological implantation filler; 6. adding a composite salt-tolerant strain nutrient solution into a pipeline; 7. a small-hole aeration system; 8. a plug flow mixer; 9. an evacuation tube; 10. overflow weir and filter screen; 11. a water outlet filter screen; 12. a water-producing overflow weir; 13. a water production line; 14. a secondary aerobic reaction tank; 15. a nitrifying liquid reflux pump; 16. an intermediate degassing stirrer; 17. a first-stage biochemical facultative reaction tank; 18. a primary aerobic reaction tank; 19. a nitrifying pond; 20. a degassing tank; 21. a secondary facultative tank; 22. an anaerobic stirrer.
Detailed Description
It should be noted that, without conflict, the embodiments of the present application and features of the embodiments may be combined with each other. The present application will be described in detail with reference to examples.
As mentioned in the background, biochemical processes are economical and efficient for wastewater treatment. However, biochemical processes are generally only capable of treating wastewater containing salts at salt concentrations below 1%. The wastewater with high salt concentration (more than 1 percent) can have certain influence on the biological treatment, and mainly microorganisms can cause cell dehydration, rupture and death under the environment with high salinity and high osmotic pressure; high salts can reduce microbial enzyme activity, disrupt normal cellular metabolism, etc. Meanwhile, the biochemical effect and the nitrification and denitrification effect are poor when the COD is lower than 300mg/l and the ammonia nitrogen content is high by 50mg/l, and the COD removal effect is less than 30% in similar experimental data. Therefore, the method is extremely low in efficiency in the aspect of treating low COD and high ammonia nitrogen pollutants in high-salt wastewater, and is not suitable for practical application. In the application, the inventor combines a device applying two-stage facultative plus aerobic treatment with a composite salt-tolerant strain to treat COD and ammonia nitrogen pollutants in high-salt wastewater in a targeted and efficient manner, thereby achieving the aim of treating the high-salt wastewater by using a biochemical treatment method to reduce the cost of enterprises.
In a first exemplary embodiment of the present application, there is provided an apparatus for treating high-salinity wastewater, the apparatus comprising, in sequential communication: a primary biochemical facultative tank 17, a primary aerobic reaction tank 18, an optional nitrifying tank 19, an optional degassing tank 20, a secondary facultative tank 21 and a secondary aerobic reaction tank 14.
The application introduces a two-stage AO process into a device for treating high-salt wastewater (shown in figure 1), and the device is a two-stage facultative and aerobic treatment system which is composed of a biochemical facultative reaction tank (A1), a primary aerobic reaction tank (O1), a secondary facultative reaction tank (A2) and a secondary aerobic reaction tank (O2), and the denitrification is carried out by the one-stage biochemical facultative reaction tank to treat nitrate Nitrogen (NO) 3 - ) Conversion to N 2 Nitrifying in a primary aerobic reaction tank to obtain ammonia Nitrogen (NH) 3 Conversion of-N) to nitrate Nitrogen (NO) 3 - ) The method comprises the steps of carrying out a first treatment on the surface of the The total nitrogen content in the wastewater treated by the first-stage AO still needs to be treated by the second-stage AO, and after the wastewater enters a second-stage facultative tank for secondary denitrification, the nitrification is carried out again in a second-stage aerobic reaction tank, so that COD in the wastewater can be removed, and the total nitrogen content in the wastewater can be reduced to the greatest extent. The two-stage facultative and aerobic treatment system can be used for efficiently removing low COD and high ammonia nitrogen in the high-salt wastewater under the biochemical treatment method so as to achieve the aim that the treated wastewater reaches the standard.
Wherein, partial nitrifying liquid after primary AO treatment in the optional nitrifying pond can return to the primary biochemical facultative reaction pond for circulation, and the related reaction in the primary biochemical facultative reaction pond and the primary aerobic reaction pond is carried out again together with the high-salt wastewater to be treated; part of the wastewater flows to an optional degassing tank through a nitrifying tank, and oxygen in the wastewater is removed in the degassing tank.
The first-stage biochemical facultative reaction tank 17, the first-stage aerobic reaction tank 18, the second-stage facultative reaction tank 21 and the second-stage aerobic reaction tank 14 are respectively internally provided with a biological implantation filler 5, wherein the biological implantation filler 5 is formed by 1 at the center and 6 attached beds surrounding the periphery, and the biological implantation filler is suspended in water. In a preferred embodiment, the attachment bed is made of a spiral wire having a hollow diameter of 1-2cm, and the filler is placed inside the hollow of the attachment bed.
The biological implantation filler passes through the suspended filler with larger specific surface area to enhance the treatment effect of the wastewater. Any biological implantation filler that can achieve the cultivation of the composite salt tolerant bacterial species is suitable for use in the present application, and in a preferred embodiment, the filler in the biological implantation filler is biofilm sludge. The formation time of the biomembrane sludge is 20-40 days, the biological phases are numerous and stable, and meanwhile, microorganisms are subjected to self-oxidative decomposition, so that the sludge with the concentration of more than 20% can be degraded, and the sludge treatment cost is reduced.
Wherein, the compound salt-tolerant strain refers to a strain which grows and grows in a high-salt environment, has the characteristic of adapting to high salt concentration, and can maintain the normal functions of cells by regulating the osmotic substances and ion balance in cells.
The filler at any density is suitable for the purpose of culturing composite salt-tolerant strains, and in a preferred embodiment, the density of the biological implantation filler is 0.94-0.99g/cm 3 . The packing density on the biological implantation determines the growth of the composite salt-tolerant bacterial strain attached to the biological implantation, and the culture needs to be carried out by selecting the proper packing density. The loading capacity of the filler on the biological implantation is 2-4 times that of the prior art, the carrier surface area is large enough to be suitable for the adsorption growth of filler microorganisms, and the effective biological concentration cultured on the carrier surface area is more than 10g/L (the traditional activated sludge is only 2-4 g/L).
Any amount of biological implantation filler capable of achieving the treatment effect is suitable for the present application, and in a preferred embodiment, the amount of biological implantation filler in the primary biochemical facultative reaction tank 17 and the primary aerobic reaction tank 18 is 1 to 2; in a preferred embodiment, the number of biological implantation packing in the secondary facultative tank 21 and the secondary aerobic reaction tank 14 is 1 to 2. In order to economically and efficiently complete the treatment of high ammonia nitrogen in wastewater, a proper amount of biological implantation filler is required to be selected for the composite salt-tolerant strain.
The first-stage biochemical facultative reaction tank 17 comprises a plug flow stirring fan 8, and the plug flow stirring fan 8 is arranged at the bottom of the first-stage biochemical facultative reaction tank 17. The plug flow stirring fan enables the wastewater in the reaction tank to be fully circulated, and chemical reaction in the wastewater can be more thoroughly carried out.
Any number of impeller agitators that can achieve the treatment effect is suitable for use in the present application, and in a preferred embodiment, the number of impeller agitators is 1-2.
An annular groove (shown in fig. 2) is arranged in the first-stage biochemical facultative reaction tank 17, and a circulating submerged stirring system is arranged in the annular groove. The circulating system can circulate the liquid for treatment reaction in the tank in a large flow rate, and in the stirring circulating system, the reaction of the wastewater to be treated is more complete.
The primary aerobic reaction tank 18, the nitrification tank 19 and the secondary aerobic reaction tank 14 comprise small-hole aeration systems 7, each small-hole aeration system 7 comprises an aeration main pipe and a plurality of aeration branch pipes communicated with the aeration main pipe, the plurality of aeration branch pipes extend from the tops of the primary aerobic reaction tank 18, the nitrification tank 19 and the secondary aerobic reaction tank 14 to the bottoms of the primary aerobic reaction tank 18, the nitrification tank 19 and the secondary aerobic reaction tank 14 respectively, the tail end of each aeration branch pipe is connected with an aeration pore plate, and a plurality of aeration holes are formed in the aeration pore plate.
The aeration device used in the device is a small-hole aeration system, compared with the traditional conventional aerator, the small-hole aeration device is simpler to install, and can achieve larger aeration quantity (1-1.5 m under the condition of relatively less investment 3 Per min, the ventilation of the conventional aerator is 0.5-1.4 m 3 /min). And the small-hole aeration device is different in material, so that the problem that the traditional rubber microporous aerator is easy to damage is thoroughly solved, the maintenance-free small-hole aeration device can be used for a long time, the daily maintenance and overhaul cost is greatly reduced, and the long-time continuous operation of the system is ensured. The higher ventilation rate combined with the rotation of the stirrer can increase the impact and cutting on bubbles in water, break large bubbles, prolong the residence time of the bubbles in water, improve the oxygen utilization rate by 3 to 5 percent, and has the advantages ofEffectively reduces the oxygen supply energy consumption.
The aeration holes on the aeration orifice plate described above are arranged in any form suitable for use in the present application, and in a preferred embodiment, the aeration holes on the aeration orifice plate are arranged in an array.
The pore aeration system is made of HDPE, the pore diameter of the porous plane of the pore aeration system is 1-3cm, and the pore density is 1600 pores/m 2 . The material used in the small-hole aeration system is high-density polyethylene, which is different from the rubber micropore material used in the conventional aerator and is easy to damage the aerator. The cost can be reduced, and the long-term continuous operation of the system can be ensured.
Any number of aeration branches that can achieve the aeration effect is suitable for the present application, and in a preferred embodiment, there are 2 to 4 aeration branches in the primary aerobic reaction tank 18 and 1 to 2 aeration branches in the nitrification tank 19; the secondary aerobic reaction tank 14 is provided with 1-2 aeration branch pipes. The aeration branch pipes with proper quantity are arranged to adjust the aeration quantity in the reaction tanks, so as to adjust the biochemical reaction degree in each reaction tank.
The nitrification tank 19 comprises a nitrifying liquid reflux pump 15, and the nitrifying liquid reflux pump 15 is arranged at the bottom of the nitrifying tank 19; the nitrifying pond 19 and the first-stage biochemical facultative reaction pond 17 are communicated through a nitrifying liquid reflux pipeline 3 communicated with the nitrifying liquid reflux pump 15. And (3) re-entering part of the nitrified liquid treated by the primary aerobic reaction tank into a primary biochemical facultative reaction tank through a nitrified liquid reflux pump in the nitrifying tank, and carrying out circulation and primary AO treatment on the waste water to be treated again to carry out denitrification and nitration reaction.
The degassing tank 20 includes an intermediate degassing stirrer 16, and the intermediate degassing stirrer 16 includes a stirring rod passing through the top of the degassing tank 20 and extending to the bottom of the degassing tank 20, and paddles at the ends of the stirring rod. And (3) allowing part of the nitrified liquid to enter a degassing tank, and stirring by an intermediate degassing stirrer to achieve the purpose of removing oxygen in the wastewater.
Any number of intermediate degassing agitators that can achieve a degassing effect is suitable for use in the present application, and in a preferred embodiment, the number of intermediate degassing agitators is 1-2. In order to achieve more cost-effective removal of oxygen from wastewater, the degassing tank of the present application requires an appropriate number of agitators.
The secondary facultative tank 21 includes an anaerobic stirrer 22, and the anaerobic stirrer 22 includes a stirring rod and a blade at the end of the stirring rod, and the stirring rod extends from the top of the secondary facultative tank 21 to the bottom of the secondary facultative tank 21. Note that the intermediate deaeration mixer 16 is identical in structure to the anaerobic mixer 22, but has a different action area. Any number of anaerobic agitators that can achieve the treatment effect is suitable for use in the present application, and in a preferred embodiment, the number of impeller agitators is 1-2. Since most denitrifying bacteria are heterotrophic, the proper number of anaerobic agitators can be installed to better perform denitrification.
The secondary aerobic reaction tank 14 comprises a water outlet filter screen 11, a water producing overflow weir 12 and a water producing pipeline 13, wherein the water filter screen 11, the water producing overflow weir 12 and the water producing pipeline 13 are sequentially arranged on the right side of the top of the secondary aerobic reaction tank 14 according to the water outflow direction. The ammonia nitrogen and COD in the wastewater are further removed by the nitrification of the wastewater in the secondary aerobic reaction tank, and the wastewater flows out of the device through the water outlet filter screen, the water production overflow weir and the water production pipeline to finish the treatment of the high-salinity wastewater.
The walls of the first-stage biochemical facultative reaction tank 17 and the second-stage facultative tank 21 are respectively provided with a composite salt-tolerant strain nutrient solution feeding pipeline 6. The primary biochemical facultative reaction tank and the secondary facultative reaction tank contain compound salt-tolerant bacteria to perform biochemical reaction for treating the wastewater, so that the nutritional ingredients of the compound salt-tolerant bacteria are timely supplemented, the activity of the bacteria is ensured, and a certain guarantee is provided for the wastewater treatment efficiency.
Because the sludge on the biological implantation filler can fall off along with the wastewater in the wastewater circulation process, a certain amount of filler is lost, in a preferred embodiment, a sludge return pipe 2 and/or a nitrifying liquid return pipeline 3 are further arranged on the wall of the first-stage biochemical facultative reaction tank 17, so that the purpose of recycling the fallen sludge is achieved, and the reaction efficiency in the reaction tank is ensured.
In order to make the wastewater in the first-stage biochemical and anaerobic reaction tank circulate as completely as possible, in a preferred embodiment, the first-stage biochemical and anaerobic reaction tank 17 includes a return channel 4, the return channel 4 is located below the outlet of the sludge return pipe 2 and the outlet of the nitrifying liquid return pipe 3 in the first-stage biochemical and anaerobic reaction tank 17 and near the top of the tank, and the materials returned by the sludge return pipe 2 and the nitrifying liquid return pipe 3 are returned to the first-stage biochemical and anaerobic reaction tank 17 through the return channel 4. The recycled sludge and nitrifying liquid re-enter the reaction tanks through the backflow channels, so that each component participating in the reaction in each reaction tank is circulated in a large flow way, and the thorough progress of the reaction is ensured.
Overflow weirs are arranged between the first-stage biochemical facultative tank 17 and the first-stage aerobic reaction tank 18, between the first-stage aerobic reaction tank 18 and the nitrifying tank 19, between the nitrifying tank 19 and the degassing tank 20, between the degassing tank 20 and the second-stage facultative tank 21, and between the second-stage facultative tank 21 and the second-stage aerobic reaction tank 14, and are communicated through overflow weirs. When the wastewater in each reaction tank reaches the height of the overflow weir (as shown in fig. 3), the wastewater enters the other reaction tank from one reaction tank through the overflow weir. Any weir that achieves the purpose of circulating wastewater is suitable for use in the present application, and in a preferred embodiment, a screen is disposed within the weir.
The bottom of the first-stage biochemical facultative tank 17, the first-stage aerobic reaction tank 18, the degassing tank 20, the second-stage facultative tank 21 and the second-stage aerobic reaction tank 14 are all provided with an emptying pipe 9. The reactants in each reaction cell can be emptied through an emptying pipe when the device is in a suspended state or needs to be maintained.
The biological implantation filler 5 is attached with a composite salt-tolerant strain, and any strain capable of performing denitrification and nitrification reaction is suitable for the present application, and in a preferred embodiment, the composite salt-tolerant strain includes nitrifying bacteria, denitrifying bacteria, halophiles, and the like. The compound salt-resistant strain used in the application has key effects on the treatment of high-salt wastewater so as to generate high-concentration biomass to ensure that the high-concentration biomass is kept in the reaction tank all the time, organic matters in the wastewater quality can be rapidly decomposed, the stability of the effluent quality is ensured, and the biochemical treatment efficiency of the device can be greatly improved by selecting the strain which is resistant to high salt and can perform high-efficiency chemical reaction. Furthermore, in a preferred embodiment, a carbon source is provided for denitrification to ensure proper operation of denitrification, and methanol may also be added to the facultative tank.
In addition, as the biological implantation filler 5 is loaded with the biological film sludge, the biological implantation filler is suitable for the growth of nitrifying bacteria and can obtain high-concentration nitrifying bacteria, the nitrifying and denitrifying capability is remarkable, and the nitrifying efficiency at 25 ℃ reaches 720-1000 g NH 4 -N/m 3 D, the nitrification efficiency is lower than 100-200 g NH under the condition that the sludge concentration is 3g/L by the traditional activated sludge method 4 -N/m 3 ·d。
The building materials of the first-stage biochemical facultative tank 17, the first-stage aerobic reaction tank 18, the nitrifying tank 19, the degassing tank 20, the second-stage facultative tank 21 and the second-stage aerobic reaction tank 14 are concrete, and the materials in the tanks are corrosion-resistant materials. The corrosion-resistant material can effectively prevent the traditional rubber microporous aerator from being damaged easily, thereby greatly reducing the daily maintenance and overhaul cost and ensuring the long-term continuous operation of the system. Any material that achieves corrosion resistance is suitable for use in the present application, and in a preferred embodiment, the corrosion resistant material comprises glass fiber reinforced plastic. In the process of high-salt wastewater treatment, a series of corrosive chemical substances such as ozone generated by biochemical reaction can cause a certain degree of damage to the device, so that the device can be ensured to be used in quality and the service life of the device can be prolonged by selecting corrosion-resistant materials to protect the device to a certain degree.
In a second exemplary embodiment of the present application, there is provided a method for high-salinity wastewater treatment using the above-described apparatus for treating high-salinity wastewater, the method comprising: the high-salt wastewater sequentially enters a first-stage biochemical facultative reaction tank 17, a first-stage aerobic reaction tank 18 and a nitrifying tank 19 to obtain nitrifying liquid; reflux part of the nitrified liquid to a first-stage biochemical facultative reaction tank 17 by using a nitrified liquid reflux pump 15 for circulation; the remaining part of nitrifying liquid sequentially enters the degassing tank 20, the secondary facultative tank 21 and the secondary aerobic reaction tank 14 to finish the treatment of the high-salt wastewater.
Through the treatment method, firstly, the high-salt wastewater to be treated is treated by first-stage AO, and the large amount of wastewater is treated by denitrificationAmount of NO 3 - Reduction to N 2 Nitrifying under aerobic condition to convert ammonia nitrogen into NO 3 - And simultaneously degrading COD. Wherein, the nitrified liquid part after the first-stage AO treatment returns the one section biochemical facultative reaction pond through nitrifying liquid reflux pump and circulates, carries out first-stage AO treatment again, and the nitrified liquid of another part is from flowing into second-stage AO treatment, is further total nitrogen in the waste water that gets rid of. The wastewater entering the secondary AO treatment is required to undergo denitrification and nitrification processes as well as the primary AO treatment. In addition, the nitrifying liquid needs to be passed through a degassing tank for removing oxygen in the wastewater before the secondary AO treatment. Finally, the wastewater subjected to the twice AO treatment flows out of the secondary aerobic reaction tank, and the treatment of the high-salt wastewater is completed.
The sludge concentration of the high-salt wastewater is 800-1500mg/L, the TDS salt content of the high-salt wastewater is 1-2%, the COD concentration is 100-800mg/L, and the ammonia nitrogen content is 30-150mg/L. The device can efficiently treat the wastewater with high ammonia nitrogen and high salt concentration with low COD, thereby improving the technical level of biochemical treatment of the wastewater with high salt concentration, and obtaining the wastewater after treatment with good indexes while utilizing lower cost of biochemical treatment of the wastewater with high salt concentration.
The biological implantation filler in the first-stage biochemical facultative reaction tank, the first-stage aerobic reaction tank, the second-stage facultative reaction tank and the second-stage aerobic reaction tank are filled with filler suitable for the growth of composite salt-tolerant strains, and different strain fillers can be filled for achieving different treatment purposes. Wherein the filling volume ratio of the filling material is any numerical value capable of achieving the aim of culturing the composite salt-tolerant strain, and in a preferred embodiment, the filling material volume ratio of the first section of biochemical facultative reaction tank 17 is 40-45%; the volume ratio of the filler in the primary aerobic reaction tank 18 is 45-50%; the volume ratio of the filling materials in the secondary facultative tank 21 is 40-45%; the volume ratio of the filler in the secondary aerobic reaction tank 14 is 45-50%. The filler volume ratio in the biological implantation filler plays a key role in the growth of the composite salt-tolerant strain attached to the filler, so that the filling of the filler with the proper volume ratio is particularly important in the efficient action of the composite salt-tolerant strain attached to the filler.
The nitrifying liquid reflux ratio of the nitrifying liquid reflux pump for refluxing part of nitrifying liquid to the first-stage biochemical facultative reaction tank is 200-400%. The nitrified liquid subjected to the first-stage AO treatment is recycled through one-time reflux, so that the total nitrogen content in the wastewater can be reduced as much as possible, and the efficiency of the reflux recycling treatment can be ensured by ensuring a reflux ratio in a certain proportion.
The flow rate of the nitrifying liquid circulating in the first-stage biochemical facultative reaction tank is 5-6 times of the water inlet flow rate. The nitrifying liquid is pumped back into the first-stage biochemical and anaerobic reaction tank for circulation, and the nitrifying liquid and the high-salt wastewater to be treated can be fully and circularly reacted in the first-stage biochemical and anaerobic reaction tank with high circulation flow.
The application is described in further detail below in connection with specific examples which are not to be construed as limiting the scope of the application as claimed.
Examples
The salt content of the high-salt wastewater to be treated is 19000mg/L, the salt concentration is 1.9%, the COD concentration is 300mg/L, and the ammonia nitrogen content is 50mg/L.
The high-salt wastewater to be treated enters a first-stage biochemical facultative reaction tank 17 through a water inlet pipe 1, the first-stage biochemical facultative reaction tank 17 is in an annular groove type, 1 set of high-flow circulating submersible stirring system is arranged in each annular groove, the circulating flow is 5 times of the water inlet flow, and the wastewater in the first-stage biochemical facultative reaction tank 17 is subjected to denitrification to obtain a large amount of NO 3 - Reduction to N 2 Enters a primary aerobic reaction tank 18 through an overflow weir and a filter screen 10. Wherein denitrifying bacteria are attached to the biomembrane sludge filler of the biological implantation filler 5 in the first-stage biochemical facultative reaction tank 17, and the filling rate of the biomembrane sludge is 40%. A plug flow stirrer 8 is also arranged in the first-stage biochemical and facultative reaction tank 17 to promote the circulation efficiency of the wastewater in the first-stage biochemical and facultative reaction tank 17. The top of the first-stage biochemical facultative reaction tank 17 is provided with a sludge return pipe 2 so as to achieve the purpose of recycling the shed sludge and ensure the reaction efficiency in the reaction tank.
The nitrification is carried out under the aerobic condition to convert ammonia nitrogen into nitrate nitrogen and degrade COD. The nitrifying liquid generated in the primary aerobic reaction tank 18 enters the nitrifying tank 19 through the overflow weir and the filter screen 10, and part of the nitrifying liquid generated in the nitrifying tank 19 flows through the nitrifying liquid reflux pump 15, flows through the nitrifying liquid reflux pipeline 3 and enters the primary biochemical facultative reaction tank 17 through the reflux channel 4 for denitrification, wherein the nitrifying liquid reflux ratio is 200%. Biofilm sludge is filled in the biological implantation filler 5 in the primary aerobic reaction tank 18, and the filling proportion is 45%. Residual nitrate nitrogen in the nitrifying pond 19 is degassed by the degassing pond 20 through the intermediate degassing stirrer 16, then enters the secondary facultative tank 21 through the overflow weir and the filter screen 10 for further denitrification, residual total nitrogen is removed, the total nitrogen content of produced water reaches the standard, and an anaerobic stirrer 22 is arranged in the secondary facultative tank 21. The water produced by the secondary facultative tank 21 enters the secondary aerobic reaction tank 14 through the overflow weir and the filter screen 10 to further remove COD in the wastewater. The finally treated wastewater passes through a water outlet filter screen 11, passes through a water production overflow weir 12 and finally flows out of the device through a water production pipeline 13, and is subjected to subsequent industrial production.
The biofilm sludge filler filling proportion of the biological implantation filler 5 in the secondary facultative tank 21 and the secondary aerobic reaction tank 14 is 40 percent and 45 percent respectively. The primary aerobic reaction tank 18, the nitrifying tank 19 and the secondary aerobic reaction tank 14 are provided with small-hole aeration systems 7. The bottom of the first-stage biochemical facultative reaction tank 17, the first-stage aerobic reaction tank 18, the degassing tank 20, the second-stage facultative reaction tank 21 and the second-stage aerobic reaction tank 14 are provided with the emptying pipe 9, and the tops of the first-stage biochemical facultative reaction tank 17 and the second-stage facultative reaction tank 21 are provided with the composite salt-tolerant strain nutrient solution adding pipeline 6, so that nutrition required by growth of the composite salt-tolerant strain can be timely supplemented.
The sludge concentration in the treated solution is 10000mg/L, the salt content is 19000mg/L, the COD concentration is 50mg/L, the ammonia nitrogen content is 3mg/L, and the total nitrogen is less than 10mg/L. Wherein the COD removal rate reaches more than 80%, and the ammonia nitrogen removal rate is about 94%.
From the above description, it can be seen that the above embodiments of the present application achieve the following technical effects: the device for treating the high-salt wastewater adopts a structure of combining two-stage facultative and aerobic treatment with biological implantation filler, so that after the wastewater with high salt concentration (1.9%) is treated by AO twice, the COD and ammonia nitrogen content in the wastewater is greatly reduced, the high-salt wastewater is treated more efficiently, and meanwhile, the ozone pollution is reduced. In addition, the device of the application can reduce the structure volume and the occupied area by 1-3 times compared with the device in the prior art. Different filling rates of biological implantation fillers can be selected according to different incoming water quality so as to obtain corresponding treatment capacity and meet the requirement of further sewage expansion in the future.
The above description is only of the preferred embodiments of the present application and is not intended to limit the present application, but various modifications and variations can be made to the present application by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (19)
1. An apparatus for treating high-salinity wastewater, the apparatus comprising: a primary biochemical facultative reaction tank (17), a primary aerobic reaction tank (18), an optional nitrifying tank (19), an optional degassing tank (20), a secondary facultative tank (21) and a secondary aerobic reaction tank (14).
2. The device according to claim 1, characterized in that biological implantation filler (5) is arranged in each of the first-stage biochemical facultative reaction tank (17), the first-stage aerobic reaction tank (18), the second-stage facultative reaction tank (21) and the second-stage aerobic reaction tank (14), the biological implantation filler (5) consists of 1 centrally located, 6 peripherally enclosed attachment beds, and the biological implantation filler (5) is suspended in water;
preferably, the filler in the biological implantation filler (5) is biomembrane sludge;
preferably, the density of the biological implantation filler (5) is 0.94-0.99g/cm 3 ；
Preferably, the number of the biological implantation fillers (5) in the primary aerobic reaction tank (18) and the primary biochemical facultative reaction tank (17) is 1-2;
preferably, the number of the biological implantation filler (5) in the secondary facultative tank (21) and the secondary aerobic reaction tank (14) is 1-2.
3. The device according to claim 1, characterized in that the one-stage biochemical facultative reaction tank (17) comprises a plug flow stirring fan (8), the plug flow stirring fan (8) being arranged at the bottom of the one-stage biochemical facultative reaction tank (17);
preferably, the number of the plug flow stirring fans (8) is 1-2.
4. The device according to claim 1, wherein an annular groove is arranged in the first section of biochemical facultative reaction tank (17), and a circulating submerged stirring system is arranged in the annular groove.
5. The device according to claim 1, wherein the primary aerobic reaction tank (18), the nitrification tank (19) and the secondary aerobic reaction tank (14) all comprise a small-hole aeration system (7), the small-hole aeration system (7) comprises an aeration main pipe and a plurality of aeration branch pipes communicated with the aeration main pipe, the aeration branch pipes respectively extend from the tops of the primary aerobic reaction tank (18), the nitrification tank (19) and the secondary aerobic reaction tank (14) to the bottoms of the primary aerobic reaction tank (18), the nitrification tank (19) and the secondary aerobic reaction tank (14), and an aeration pore plate is connected to the tail end of each aeration branch pipe, and a plurality of aeration holes are arranged on the aeration pore plate;
preferably, a plurality of the aeration holes are arranged in an array on the aeration hole plate;
preferably, the material used for the small-hole aeration system (7) is HDPE;
preferably, the diameter of the aeration holes is 1-3mm;
preferably, the distribution density of the aeration holes on the aeration hole plate is 1600/m 2 ；
Preferably, the number of the aeration branch pipes is 2-4 in the primary aerobic reaction tanks (18), and 1-2 in the nitrifying tanks (19); 1-2 secondary aerobic reaction tanks (14) are arranged.
6. The device according to claim 1, characterized in that the nitrification tank (19) comprises a nitrification liquid reflux pump (15), the nitrification liquid reflux pump (15) being arranged at the bottom of the nitrification tank (19); the nitrifying pond (19) is communicated with the one-stage biochemical facultative reaction pond (17) through a nitrifying liquid reflux pipeline (3) communicated with a nitrifying liquid reflux pump (15).
7. The apparatus of claim 1, wherein the degassing tank (20) comprises an intermediate degassing stirrer (16), the intermediate degassing stirrer (16) comprising a stirring rod and a paddle at the end of the stirring rod, the stirring rod passing through the top of the degassing tank (20) and extending to the bottom of the degassing tank (20);
preferably, the number of intermediate degassing agitators (16) is 1-2.
8. The apparatus of claim 1, wherein the secondary facultative tank (21) comprises an anaerobic agitator (22), the anaerobic agitator (22) comprising an agitator bar and a paddle at the end of the agitator bar, the agitator bar passing through the top of the secondary facultative tank (21) and extending to the bottom of the secondary facultative tank (21);
preferably, the number of the anaerobic agitators (22) is 1-2.
9. The device according to claim 1, wherein the secondary aerobic reaction tank (14) comprises a water outlet filter screen (11), a water producing overflow weir (12) and a water producing pipeline (13), and the water filter screen (11), the water producing overflow weir (12) and the water producing pipeline (13) are sequentially arranged on the right side of the top of the secondary aerobic reaction tank (14) according to the water outflow direction.
10. The device according to claim 1, characterized in that the walls of the first-stage biochemical facultative reaction tank (17) and the second-stage facultative tank (21) are provided with a composite salt-tolerant strain nutrient solution feeding pipeline (6);
preferably, a sludge return pipe (2) and/or a nitrified liquid return pipeline (3) are also arranged on the tank wall of the first-stage biochemical facultative reaction tank (17);
preferably, the one-stage biochemical and facultative reaction tank (17) comprises a backflow channel (4), the backflow channel (4) is positioned below the outlet of the sludge backflow pipe (2) and the outlet of the nitrifying liquid backflow pipeline (3) in the one-stage biochemical and facultative reaction tank (17) and near the tank top, and materials which flow back through the sludge backflow pipe (2) and the nitrifying liquid backflow pipeline (3) flow back into the one-stage biochemical and facultative reaction tank (17) through the backflow channel (4).
11. The apparatus according to any one of claims 1 to 9, wherein overflow weirs are provided between the primary biochemical facultative tank (17) and the primary aerobic reaction tank (18), between the primary aerobic reaction tank (18) and the nitrification tank (19), between the nitrification tank (19) and the degassing tank (20), between the degassing tank (20) and the secondary facultative tank (21), and between the secondary facultative tank (21) and the secondary aerobic reaction tank (14), and are communicated by the overflow weirs;
preferably, a filter screen is arranged in the overflow weir.
12. The device according to any one of claims 1 to 9, wherein the primary biochemical facultative tank (17), the primary aerobic reaction tank (18), the degassing tank (20), the secondary facultative tank (21) and the secondary aerobic reaction tank (14) are each provided with an evacuation pipe (9) at the bottom.
13. The device according to claim 2, characterized in that the biological implantation filler (5) has attached thereto a complex salt tolerant bacterial species, preferably comprising nitrifying bacteria, denitrifying bacteria and halophiles.
14. The device according to claim 1, characterized in that the building materials of the primary biochemical facultative tank (17), the primary aerobic reaction tank (18), the nitrification tank (19), the degassing tank (20), the secondary facultative tank (21) and the secondary aerobic reaction tank (14) are concrete, and the materials in the tanks are all corrosion-resistant materials, preferably, the corrosion-resistant materials comprise glass fiber reinforced plastics.
15. A method of high salt wastewater treatment using the apparatus for treating high salt wastewater of any one of claims 1 to 14, the method comprising:
the high-salt wastewater sequentially enters the primary biochemical facultative reaction tank (17), the primary aerobic reaction tank (18) and the nitrifying tank (19) to obtain nitrifying liquid;
reflux part of the nitrifying liquid to the first-stage biochemical facultative reaction tank (17) by using the nitrifying liquid reflux pump (15) for circulation;
and the rest part of the nitrifying liquid sequentially enters the degassing tank (20), the secondary facultative tank (21) and the secondary aerobic reaction tank (14) to finish the treatment of the high-salt wastewater.
16. The method according to claim 15, wherein the high-salt wastewater has a TDS salt content of 1% -2%, a COD concentration of 100-800mg/L and an ammonia nitrogen content of 30-150mg/L.
17. The method according to claim 15, characterized in that the filler volume ratio in the one-stage biochemical facultative reaction tank (17) is 40-45%;
preferably, the volume ratio of the filler in the primary aerobic reaction tank (18) is 45-50%;
preferably, the volume ratio of the filling materials in the secondary facultative tank (21) is 40-45%;
preferably, the volume ratio of the filler in the secondary aerobic reaction tank (14) is 45-50%.
18. The method according to claim 15, wherein the nitrifying liquid reflux volume ratio is 200-400%.
19. The method of claim 15, wherein the flow rate of the circulation is 5-6 times the flow rate of the inlet water.
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| CN202311074661.4A CN116903140A (en) | 2023-08-24 | 2023-08-24 | Device and method for treating high-salt wastewater |
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| CN202311074661.4A CN116903140A (en) | 2023-08-24 | 2023-08-24 | Device and method for treating high-salt wastewater |
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