Whole-process treatment device and treatment method for high-organic-matter high-ammonia wastewater

Abstract

The invention relates to the technical field of wastewater treatment, in particular to a whole-process treatment device and method for high-organic-matter and high-ammonia wastewater. The invention provides a whole-process treatment device for high-organic-matter high-ammonia wastewater. The whole-process treatment device comprises an anaerobic tower, a short-cut denitrification-anaerobic ammonia oxidation tank, a nitrosation-anaerobic ammonia oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification carbon removal tank and a final sedimentation tank which are connected in sequence. According to the treatment device, the short-cut denitrification-anaerobic ammonia oxidation tank is arranged in front, so that the influence of organic matters on subsequent autotrophic microorganism denitrification is effectively avoided. And the treatment device has the characteristics of low cost and high efficiency when being used for treating the high-organic-matter high-ammonia wastewater.

Description

Technical Field

[0001] The present invention relates to the technical field of wastewater treatment, and in particular to a full-process treatment device and method for high-organic-matter and high-ammonia wastewater. Background Art

[0002] With the development of science and technology, the discharge of high-organic matter and high-ammonia wastewater has increased year by year, such as kitchen and fermentation. For this type of wastewater, the traditional process uses anaerobic methanation to recover energy, and then uses nitrification / denitrification process for biological denitrification. In this coupled process, denitrification requires a large amount of organic matter, resulting in the inability to fully recover organic matter in the previous anaerobic methanation process; secondly, the nitrification process converts ammonia nitrogen into nitrates, which requires a large amount of aeration. In order to fully utilize the organic carbon source in the raw water for denitrification, the nitrified liquid of the subsequent nitrification process needs to be returned to the front denitrification tank for denitrification. The high aeration volume and high reflux ratio lead to high power consumption, and the final denitrification cost is extremely high.

[0003] As a new type of autotrophic biological denitrification technology, partial nitrification / anaerobic ammonium oxidation has the advantages of low carbon source dependence, high efficiency and low aeration power consumption, and has received widespread attention in the treatment of high-ammonia wastewater. However, the growth conditions of anaerobic ammonium oxidizing bacteria are extremely harsh, and the doubling time of functional microorganisms is as long as 7 to 13 days. The entry of organic matter promotes the rapid growth of heterotrophic microorganisms, and the proportion of autotrophic microorganisms will gradually decrease, making it difficult to achieve the denitrification advantages of partial nitrification / anaerobic ammonium oxidation through sludge age control. Although studies have shown that the entry of low amounts of organic matter will promote the improvement of partial nitrification / anaerobic ammonium oxidation denitrification efficiency, in the face of industrial wastewater with actual fluctuations in organic matter, how to avoid the impact of high organic matter on subsequent autotrophic microbial denitrification is still an urgent problem to be solved. Secondly, the ammonia nitrogen concentration of industrial wastewater is very likely to fluctuate widely due to changes in the production end, especially in fermentation, kitchen waste (seasonal catering changes), food and other industries. As we all know, fluctuations in ammonia nitrogen in the influent can easily lead to ammonia nitrogen accumulation in the system, which not only forms free ammonia that is toxic to microorganisms, but also causes the effluent water quality to exceed the standard. Therefore, how to enhance the system's tolerance to ammonia nitrogen shock through process construction is also an important issue in the engineering process. Summary of the invention

[0004] In view of this, the purpose of the present invention is to provide a full-process treatment device and method for high-organic and high-ammonia wastewater. The treatment device places a short-range denitrification-anaerobic ammonia oxidation tank in front, effectively avoiding the impact of organic matter on subsequent autotrophic microbial denitrification.

[0005] In order to achieve the above-mentioned object of the invention, the present invention provides the following technical solutions:

[0006] The present invention provides a full-process treatment device for high-organic matter and high-ammonia wastewater, comprising an anaerobic tower, a short-range denitrification-anaerobic ammonium oxidation tank, a nitrite-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank and a final sedimentation tank which are connected in sequence.

[0007] Preferably, the nitrite-anaerobic ammonium oxidation tank is also connected to the short-cut denitrification-anaerobic ammonium oxidation tank through a first reflux system;

[0008] The denitrification swing pool is also connected to the short-cut denitrification-anaerobic ammonia oxidation pool through a second reflow system;

[0009] The nitrification and carbon removal tank is also connected to the denitrification tank through a third reflux system;

[0010] The intermediate sedimentation tank is also connected to the short-range denitrification-anaerobic ammonia oxidation tank through a fourth reflux system;

[0011] The final sedimentation tank is also connected to the denitrification tank through a fifth reflux system.

[0012] Preferably, the anaerobic tower is an anaerobic internal circulation reactor, an anaerobic upflow sludge blanket reactor or an anaerobic membrane reactor;

[0013] The COD load of the anaerobic tower is 5 to 15 kg / (m 3 ·d).

[0014] Preferably, the short-cut denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank are all provided with biological fillers;

[0015] The biological filler is a mobile filler or a fixed filler. When the biological filler is a mobile filler, the filling ratio of the biological filler is 20-40%. When the biological filler is a fixed filler, the filling spacing of the biological filler is 150-300 mm.

[0016] Preferably, the short-cut denitrification-anaerobic ammonium oxidation tank and the denitrification tank are both provided with a stirring device;

[0017] The bottoms of the nitrite-anaerobic ammonium oxidation tank, the denitrification swing tank and the nitrification and carbon removal tank are all provided with an aeration system; the tops of the nitrite-anaerobic ammonium oxidation tank, the denitrification swing tank and the nitrification and carbon removal tank are all provided with a gas collection system.

[0018] The present invention also provides a method for treating high-organic matter and high-ammonia wastewater using the treatment device described in the above technical solution, comprising the following steps:

[0019] The high-organic and high-ammonia wastewater is sequentially passed through an anaerobic tower, a short-cut denitrification-anaerobic ammonium oxidation tank, a nitrification-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank, and a final sedimentation tank for anaerobic treatment, short-cut denitrification-anaerobic ammonium oxidation denitrification, nitrification-anaerobic ammonium oxidation denitrification, denitrification, sedimentation, denitrification, nitrification and carbon removal, and final sedimentation to obtain recycled water;

[0020] The COD concentration in the high-organic and high-ammonia wastewater is 5000-20000 mg / L, the ammonia nitrogen is 300-2000 mg / L, and the total nitrogen is 400-2000 mg / L.

[0021] Preferably, the dissolved oxygen concentration in the nitrite-anaerobic ammonium oxidation tank is 0.5-1.5 mg / L, the dissolved oxygen concentration in the denitrification swing tank is 0-1.5 mg / L, and the dissolved oxygen concentration in the nitrification and carbon removal tank is 2-3 mg / L;

[0022] The dissolved oxygen concentrations in the anaerobic tower, the short-cut denitrification-anaerobic ammonia oxidation tank, the intermediate sedimentation tank, the denitrification tank and the final sedimentation tank are all ≤0.1 mg / L.

[0023] Preferably, the suspended sludge concentration of the short-cut denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank after stable operation is ≤1000 mg / L;

[0024] When the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is 1 to 1.2, the dissolved oxygen in the denitrification swing tank is 0.1 to 0.2 mg / L;

[0025] When the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is less than 1, the dissolved oxygen in the denitrification swing tank is 0.2-1.5 mg / L.

[0026] Preferably, when the BOD / TN of the high-organic and high-ammonia wastewater is greater than 5, the high-organic and high-ammonia wastewater not only enters the anaerobic tower for anaerobic treatment, but also enters the denitrification-anaerobic ammonia oxidation tank and the denitrification tank as a supplementary source of organic carbon source;

[0027] When the BOD / TN in the high-organic and high-ammonia wastewater is less than 5, additional carbon source is added.

[0028] The present invention provides a full-process treatment device for high-organic matter and high-ammonia wastewater, including an anaerobic tower, a short-cut denitrification-anaerobic ammonium oxidation tank, a nitrite-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank, and a final sedimentation tank connected in sequence. The present invention uses a pre-placed short-cut denitrification-anaerobic ammonium oxidation tank to fully utilize the residual organic matter in the anaerobic methanogenic effluent to convert the nitrate produced in the nitrite / anaerobic ammonium oxidation tank and the denitrification swing tank into nitrite in the tank, and at the same time, utilizes the ammonia nitrogen in the effluent of the anaerobic tower to directly carry out the anaerobic ammonium oxidation reaction, which is beneficial to flexibly adjust the reflux ratio according to the concentration change of BOD in the anaerobic methanogenic effluent (the effluent of the anaerobic tower) and thereby reduce its influence on autotrophic microorganisms. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 It is a full-process treatment device for high-organic matter and high-ammonia wastewater according to the present invention, wherein 1 is an anaerobic tower, 2 is a short-range denitrification-anaerobic ammonium oxidation tank, 3 is a nitrite-anaerobic ammonium oxidation tank, 4 is a denitrification swing tank, 5 is an intermediate sedimentation tank, 6 is a denitrification tank, 7 is a nitrification and carbon removal tank, 8 is a final sedimentation tank, 9 is a first reflux system, 10 is a second reflux system, 11 is a third reflux system, 12 is a fourth reflux system, 13 is a fifth reflux system, 14 is a high-efficiency denitrification system and 15 is a deep denitrification system. DETAILED DESCRIPTION

[0030] like Figure 1 As shown, the present invention provides a full-process treatment device for high-organic matter and high-ammonia wastewater, including an anaerobic tower, a short-range denitrification-anaerobic ammonium oxidation tank, a nitrite-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank and a final sedimentation tank connected in sequence.

[0031] In the present invention, the short-range denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank constitute a high-efficiency denitrification system; the denitrification tank and the nitrification and carbon removal tank constitute a deep denitrification system.

[0032] As an embodiment of the present invention, the anaerobic tower is preferably an anaerobic internal circulation reactor (IC), an anaerobic upflow sludge blanket reactor (UASB) or an anaerobic membrane reactor; the COD load of the anaerobic tower is preferably 5 to 15 kg / (m 3 ·d). The materials of the anaerobic internal circulation reactor (IC), the anaerobic upflow sludge blanket reactor (UASB) and the anaerobic membrane reactor are preferably steel or concrete.

[0033] As an embodiment of the present invention, the nitrification-anaerobic ammonium oxidation tank is also connected to the short-range denitrification-anaerobic ammonium oxidation tank through a first reflux system; the denitrification swing tank is also connected to the short-range denitrification-anaerobic ammonium oxidation tank through a second reflux system; the nitrification and carbon removal tank is also connected to the denitrification tank through a third reflux system; the intermediate sedimentation tank is also connected to the short-range denitrification-anaerobic ammonium oxidation tank through a fourth reflux system; the final sedimentation tank is also connected to the denitrification tank through a fifth reflux system. In the present invention, the reflux modes of the first reflux system, the second reflux system, the third reflux system, the fourth reflux system and the fifth reflux system are independently preferably mechanical pump reflux or airlift reflux. When the reflux mode of the first reflux system, the second reflux system, the third reflux system, the fourth reflux system or the fifth reflux system is airlift reflux, the airlift reflux preferably relies on the gas collected in the aeration tank or the remaining gas after aeration in the aeration system by a blower as power to return the sewage in the low liquid level tank body to the high liquid level tank body.

[0034] As an embodiment of the present invention, the short-range denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank are all provided with biological fillers; the biological fillers are mobile fillers or fixed fillers. When the biological fillers are mobile fillers, the filling ratio of the biological fillers is 20-40%; when the biological fillers are fixed fillers, the filling spacing of the biological fillers is 150-300 mm.

[0035] As an embodiment of the present invention, the biological fillers filled in the short-cut denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank are biological fillers well known in the water treatment industry.

[0036] As an embodiment of the present invention, a stirring device is provided in both the short-cut denitrification-anaerobic ammonium oxidation tank and the denitrification tank; in the present invention, the stirring mode of the stirring device is preferably mechanical stirring or hydraulic and air mixing stirring.

[0037] As an embodiment of the present invention, the bottom of the nitrite-anaerobic ammonium oxidation tank, the denitrification swing tank and the nitrification and carbon removal tank are all provided with an aeration system; the top of the nitrite-anaerobic ammonium oxidation tank, the denitrification swing tank and the nitrification and carbon removal tank are all provided with a gas collection system.

[0038] The present invention also provides a method for treating high-organic matter and high-ammonia wastewater using the treatment device described in the above technical solution, comprising the following steps:

[0039] The high-organic and high-ammonia wastewater is sequentially passed through an anaerobic tower, a short-cut denitrification-anaerobic ammonium oxidation tank, a nitrification-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank, and a final sedimentation tank to perform anaerobic methanation treatment of organic matter, short-cut denitrification-anaerobic ammonium oxidation denitrification, nitrification-anaerobic ammonium oxidation denitrification, denitrification, sedimentation, denitrification, nitrification and carbon removal, and final sedimentation to obtain recycled water;

[0040] The high-organic and high-ammonia wastewater has a COD concentration of 5000-20000 mg / L, a BOD concentration of 4000-8000 mg / L, ammonia nitrogen of 300-2000 mg / L, and a total nitrogen of 400-20000 mg / L.

[0041] In the present invention, when the BOD / TN in the high-organic and high-ammonia wastewater is greater than 5, the high-organic and high-ammonia wastewater not only enters the anaerobic tower for anaerobic treatment, but also enters the denitrification-anaerobic ammonia oxidation tank and the denitrification tank as a supplementary source of organic carbon source. In the present invention, when the high-organic and high-ammonia wastewater is used as an organic carbon source to supplement short-range denitrification-anaerobic ammonia oxidation, the amount of organic carbon source that can be provided by the high-organic and high-ammonia wastewater is the amount of all BOD in the raw water, and the total amount of BOD entering should ensure that all nitrates in the reflux system are converted into nitrites; when the high-organic and high-ammonia wastewater is used as an organic carbon source to supplement the denitrification tank, the amount of organic carbon source that can be provided by the high-organic and high-ammonia wastewater is preferably the difference between the mass of the BOD in the high-organic and high-ammonia wastewater and 5*the mass difference of the total nitrogen in the high-organic and high-ammonia wastewater. The water inflow of the high-organic and high-ammonia wastewater in the denitrification tank preferably ensures that the mass concentration ratio of the organic carbon source that can be provided by the high-organic and high-ammonia wastewater to the nitrate in the denitrification tank is 2 to 3:1.

[0042] In the present invention, when the BOD / TN in the high-organic and high-ammonia wastewater is less than 5, the denitrification tank needs to be supplemented with additional carbon source.

[0043] In the present invention, the COD load of the anaerobic tower is preferably 5 to 15 kg / (m 3 ·d), more preferably 10kg / (m 3 ·d). In the present invention, the concentration of dissolved oxygen in the anaerobic tower is preferably ≤0.1 mg / L. In the present invention, the temperature in the anaerobic tower is preferably 30-35°C, and the pH is preferably 7-8. In the present invention, the anaerobic tower is preferably inoculated with anaerobic methanogenic granular sludge, and the initial inoculation amount of the anaerobic methanogenic granular sludge is preferably 20-30% of the effective volume of the anaerobic tower.

[0044] When the BOD / TN in the effluent of the anaerobic tower is greater than 1, the second reflux system is turned on to return the nitrate in the denitrification swing tank to the short-cut denitrification-anaerobic ammonium oxidation tank, and the nitrate is used to consume the organic matter in the effluent of the anaerobic tower, and the BOD / TN ratio in the short-cut denitrification-anaerobic ammonium oxidation tank is controlled to be lower than 0.1, so as to further avoid the inhibitory effect of organic matter on the autotrophic microorganisms in part of the nitrite-anaerobic ammonium oxidation tank.

[0045] In the present invention, the dissolved oxygen concentration in the short-cut denitrification-anaerobic ammonium oxidation tank is preferably ≤0.1 mg / L. The short-cut denitrification-anaerobic ammonium oxidation tank is preferably inoculated with municipal sludge and anaerobic ammonium oxidation sludge, and the initial inoculation amount of the municipal sludge is preferably 4000 mgMLSS / L, and the initial inoculation amount of the anaerobic ammonium oxidation sludge is preferably 4000 mgMLSS / L. The initial inoculation amount of the short-cut denitrification-anaerobic ammonium oxidation tank is preferably 4000 mgMLSS / L, and the suspended sludge concentration after stable operation is preferably ≤1000 mg / L, so as to increase the utilization rate of dissolved oxygen and the pollution load of microorganisms on the filler. In the present invention, the temperature in the short-cut denitrification-anaerobic ammonium oxidation tank is preferably 30-35°C, and the pH is preferably 7-8.

[0046] In the present invention, short-cut denitrification-anaerobic ammonium oxidation denitrification is carried out in the short-cut denitrification-anaerobic ammonium oxidation pool by using the remaining organic carbon source in the anaerobic tower effluent as an electron donor for denitrification, controlling nitrate denitrification at the nitrite stage, and reducing the carbon source demand in the latter stage of nitrate removal through the coupling of short-cut denitrification-anaerobic ammonium oxidation, enhancing the supply of nitrite in the anaerobic ammonium oxidation process, and avoiding the influence of organic matter on subsequent autotrophic biological denitrification.

[0047] In the present invention, the dissolved oxygen concentration in the nitrite-anaerobic ammonium oxidation tank is preferably 0.5-1.5 mg. In the present invention, the suspended sludge concentration in the nitrite-anaerobic ammonium oxidation tank is preferably ≤1000 mg / L. In the present invention, the nitrite-anaerobic ammonium oxidation tank is preferably inoculated with ordinary activated sludge and then domesticated. The ordinary activated sludge is preferably industrial residual sludge close to the source of sewage, and the initial inoculation amount is preferably 4000 mgMLSS / L; the domestication method is preferably to gradually increase the pollutant load. In the present invention, the temperature in the nitrite-anaerobic ammonium oxidation tank is preferably 30-35°C, and the pH is preferably 7-8. In the present invention, the temperature for nitrite-anaerobic ammonium oxidation denitrification is preferably 35°C, and the pH value is preferably 8.

[0048] In the present invention, the nitrite-anaerobic ammonium oxidation denitrification is carried out in the nitrite-anaerobic ammonium oxidation tank mainly by controlling the stability of nitrite by low dissolved oxygen and free ammonia (FA), and controlling the ammonia nitrogen concentration in the effluent to be within the range of 20 to 150 mg / L, which is beneficial to the stability of the system.

[0049] In the present invention, the dissolved oxygen concentration in the denitrification swing tank is preferably 0-1.5 mg / L; more preferably, when the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is 1-1.2 (anaerobic ammonium oxidation denitrification is mainly used at this time), the dissolved oxygen in the denitrification swing tank is 0.1-0.2 mg / L; when the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is less than 1, the dissolved oxygen in the denitrification swing tank is 0.2-1.5 mg / L (this can increase the dissolved oxygen concentration in the tank, at which time the nitrite capacity gradually increases and the anaerobic ammonium oxidation capacity gradually decreases, which promotes the conversion of ammonia nitrogen as much as possible, strengthens the system's resistance to ammonia nitrogen shock, provides pretreatment for deep denitrification in the subsequent denitrification process, and reduces the power consumption of reflux nitrification liquid in the traditional pre-denitrification process). In the present invention, the suspended sludge concentration in the denitrification swing tank is preferably ≤1000 mg / L. In the present invention, the sludge inoculated in the denitrification swing tank is preferably ordinary activated sludge, and the ordinary activated sludge is specifically municipal sludge or industrial residual sludge close to the source of sewage, and is more preferably the same as the sludge in the nitrite-anaerobic ammonium oxidation tank. In the present invention, the initial inoculation amount of the sludge in the denitrification swing tank is preferably 3000-5000 mgMLSS / L, more preferably 4000 mgMLSS / L. In the present invention, the temperature in the denitrification swing tank is preferably 30-35°C, and the pH is preferably 7-8.

[0050] In the present invention, the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is controlled to control the degree of nitrite, which will be beneficial to the further stable removal of nitrogen and at the same time convert the ammonia nitrogen in the effluent into nitrite nitrogen or nitrate nitrogen as much as possible.

[0051] In the present invention, the dissolved oxygen concentration of the denitrification pool is preferably ≤0.1 mg / L. In the present invention, the temperature for denitrification in the denitrification pool is preferably 35°C, and the pH value is preferably 8.

[0052] In the present invention, denitrification in the denitrification pool is to directly utilize the carbon source for deep nitrogen removal, which will greatly reduce the burden of the nitrification and carbon removal pool on ammonia nitrogen conversion and return to the denitrification pool, and has the effect of energy saving and consumption reduction.

[0053] In the present invention, the dissolved oxygen concentration in the nitrification and carbon removal tank is preferably 2-3 mg / L, more preferably 3 mg / L.

[0054] In the present invention, the nitrification and carbon removal in the nitrification and carbon removal tank is to convert the remaining ammonia nitrogen into nitrite or nitrate.

[0055] In the present invention, the slow-growing autotrophic microorganisms are fixed and grown by setting the above-mentioned microbial filler, and the suspended growth of heterotrophic bacteria is promoted by adjusting parameters such as suspended sludge optimization, and then flowing out of the system with water, which can further effectively avoid the influence of organic matter on the denitrification of the autotrophic microbial system.

[0056] The technical solutions in the present invention will be described clearly and completely below in conjunction with the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, not all of them. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0057] Example 1

[0058] Treatment object: high organic and high ammonia wastewater (COD concentration is 10000mg / L, BOD concentration is 9000mg / L, ammonia nitrogen concentration is 1000mg / L, total nitrogen concentration is 1200mg / L, BOD / TN7.5);

[0059] Treatment process: First, 85% of the wastewater enters the anaerobic IC reactor for methanogenic treatment. The effluent COD concentration is 800mg / L, the BOD concentration is 700mg / L, the ammonia nitrogen concentration is 1200mg / L due to amination, and the total nitrogen concentration is 1200mg / L; at this time, the IC effluent and the water of the first reflux system (reflux ratio 200%) of the intermediate sedimentation tank enter the short-cut denitrification-anaerobic ammonia oxidation tank together. The COD of the IC effluent converts the nitrate in the reflux liquid into nitrite, but there is still COD remaining, then the effluent of the denitrification swing tank is also refluxed into the short-cut nitrification-anaerobic ammonia oxidation tank through the second reflux system (reflux ratio 200%) for the same reaction. The effluent COD of the short-cut denitrification-anaerobic ammonia oxidation tank is 1200mg / L. The concentration is 150mg / L, the BOD concentration is 50mg / L, the ammonia nitrogen concentration is 150mg / L, and the total nitrogen concentration is 260mg / L; the nitrite nitrogen is 90mg / L, and the nitrate nitrogen is 10mg / L; the effluent enters the short-range nitrification-anaerobic ammonia oxidation tank, the dissolved oxygen is 0.5mg / L, the temperature is 35℃, and the aerobic ammonia oxidizing bacteria use the dissolved oxygen to convert part of the ammonia nitrogen into nitrite. At the same time, the anaerobic ammonia oxidizing bacteria use ammonia nitrogen and nitrite to produce nitrogen gas and a small amount of nitrate. The effluent COD concentration is 138mg / L, the BOD concentration is 20mg / L, the ammonia nitrogen concentration is 60mg / L, the nitrite is 80mg / L, the nitrate concentration is 34mg / L, and the total nitrogen concentration is 180mg / L. Then it enters the denitrification swing tank. Because the nitrite / ammonia nitrogen concentration ratio is 1.38, the dissolved oxygen in the tank is 0.2 mg / L and the temperature is 35°C. At this time, the intake air mainly plays a mixing role, and anaerobic ammonia-oxidizing bacteria are continuously used to convert nitrite and ammonia into nitrogen. The effluent COD concentration is 120 mg / L, BOD concentration is 15 mg / L, ammonia nitrogen concentration is 10 mg / L, nitrite is 40 mg / L, nitrate concentration is 87 mg / L, and total nitrogen concentration is 139 mg / L. In the next stage, the sludge enters the intermediate sedimentation tank for mud-water separation, and the sludge is returned to the short-range denitrification-anaerobic ammonia oxidation tank through the return system 3 (return ratio 40%); 15% raw water is added to the DN tank, and the BOD in the raw water is used to convert all the nitrate / nitrite in the effluent of the denitrification swing tank into nitrogen gas, and the ammonia nitrogen carried in the raw water and the ammonia nitrogen in the denitrification swing tank all enter the nitrification and carbon removal tank; at this time, the nitrification and carbon removal tank uses the nitrification process to convert all the ammonia nitrogen into nitrate, and all enter the denitrification tank through the return system 3 (return ratio 200%) for denitrification removal, and the effluent enters the final sedimentation tank for sedimentation, and the sludge is returned to the denitrification tank through the return system 3 (return ratio 80%) to ensure that the effluent COD concentration is 100mg / L, the BOD concentration is 15mg / L, the ammonia nitrogen concentration is 8mg / L, the nitrite is 0mg / L, the nitrate concentration is 23mg / L, and the total nitrogen concentration is 35mg / L.

[0060] Example 2

[0061] Treatment object: high organic and high ammonia wastewater (COD concentration is 5000mg / L, BOD concentration is 4800mg / L, ammonia nitrogen concentration is 900mg / L, total nitrogen concentration is 1000mg / L, BOD / TN=4.8);

[0062] Treatment process: First, 95% of the wastewater enters the anaerobic IC reactor for methanogenic treatment. The effluent COD concentration is 250mg / L, the BOD concentration is 200mg / L, the ammonia nitrogen concentration is 1000mg / L due to amination, and the total nitrogen concentration is 1000mg / L; at this time, the IC effluent and the water of the first reflux system (reflux ratio 200%) of the intermediate sedimentation tank enter the short-range denitrification-anaerobic ammonia oxidation tank together. The COD of the IC effluent converts the nitrate in the reflux liquid into nitrite. Because the IC effluent COD is insufficient, 5% of the raw water enters the PD to supplement the short-range denitrification carbon source. The effluent of the denitrification swing pool is also refluxed into the short-range nitrification-anaerobic ammonia oxidation tank through the second reflux system (reflux ratio 200%) for the same reaction. Short-range denitrification - The effluent COD concentration of the anaerobic ammonium oxidation pool is 100mg / L, the BOD concentration is 60mg / L, the ammonia nitrogen concentration is 100mg / L, and the total nitrogen concentration is 150mg / L; the nitrite nitrogen is 40mg / L, and the nitrate nitrogen is 8mg / L; the effluent enters the short-range nitrification-anaerobic ammonium oxidation pool, the dissolved oxygen is 0.5mg / L, the temperature is 35℃, and the aerobic ammonia oxidizing bacteria use the dissolved oxygen to convert part of the ammonia nitrogen into nitrite. At the same time, the anaerobic ammonia oxidizing bacteria use ammonia nitrogen and nitrite to produce nitrogen gas and a small amount of nitrate. The effluent COD concentration is 98mg / L, the BOD concentration is 21mg / L, the ammonia nitrogen concentration is 45mg / L, the nitrite is 30mg / L, the nitrate concentration is 30mg / L, and the total nitrogen concentration is 120mg / L. Then it enters the denitrification swing tank. Because the nitrite / ammonia nitrogen concentration ratio is 0.67, the dissolved oxygen in the tank is 0.8 mg / L and the temperature is 35°C. On the one hand, nitrite bacteria and anaerobic ammonia oxidizing bacteria are continuously used to reduce ammonia nitrogen and nitrite in the influent. On the other hand, the nitrification process is fully utilized to reduce ammonia nitrogen. The effluent COD concentration is 90 mg / L, BOD concentration is 18 mg / L, ammonia nitrogen concentration is 20 mg / L, nitrite is 15 mg / L, nitrate concentration is 39 mg / L, and total nitrogen concentration is 78 mg / L.The next stage is to enter the intermediate sedimentation tank for mud and water separation, and the sludge is returned to the short-range denitrification-anaerobic ammonia oxidation tank through the return system 3 (return ratio 40%); because the BOD / TN in the raw water is 3.8, additional organic carbon sources are added in the DN tank to convert all nitrates / nitrites in the effluent of the denitrification swing tank into nitrogen gas, and the effluent COD concentration is 110mg / L, BOD concentration is 20mg / L, ammonia nitrogen concentration is 20mg / L, nitrite concentration is 2mg / L, nitrate concentration is 3mg / L, and total nitrogen concentration is 30mg / L; denitrification swing All the remaining ammonia nitrogen in the pool enters the nitrification and carbon removal pool; at this time, the nitrification and carbon removal pool uses the nitrification process to convert all the ammonia nitrogen into nitrates, and enters the denitrification pool through the return system 3 (return ratio 200%) for denitrification removal, and the effluent enters the final sedimentation tank for sedimentation. The sludge is returned to the denitrification pool through the return system 3 (return ratio 80%) to ensure that the effluent COD concentration is 80mg / L, the BOD concentration is 10mg / L, the ammonia nitrogen concentration is 5mg / L, the nitrite is 0mg / L, the nitrate concentration is 13mg / L, and the total nitrogen concentration is 23mg / L.

[0063] The above description is only a preferred embodiment of the present invention and does not limit the present invention in any form. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be regarded as the protection scope of the present invention.

Claims

1. A full-process treatment device for high-organic matter and high-ammonia wastewater, characterized in that: It includes an anaerobic tower, a short-range denitrification-anaerobic ammonium oxidation tank, a nitrite-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank and a final sedimentation tank which are connected in sequence.

2. The full-process treatment device for high-organic-matter-high-ammonia wastewater according to claim 1, characterized in that: The nitrite-anaerobic ammonium oxidation tank is also connected to the short-cut denitrification-anaerobic ammonium oxidation tank through a first reflux system; The denitrification swing pool is also connected to the short-cut denitrification-anaerobic ammonia oxidation pool through a second reflow system; The nitrification and carbon removal tank is also connected to the denitrification tank through a third reflux system; The intermediate sedimentation tank is also connected to the short-cut denitrification-anaerobic ammonia oxidation tank through a fourth reflux system; The final sedimentation tank is also connected to the denitrification tank through a fifth reflux system.

3. The full-process treatment device for high-organic-matter-high-ammonia wastewater according to claim 1, characterized in that: The anaerobic tower is an anaerobic internal circulation reactor, an anaerobic upflow sludge blanket reactor or an anaerobic membrane reactor; The COD load of the anaerobic tower is 5 to 15 kg / (m 3 ·d).

4. The full-process treatment device for high-organic-matter-high-ammonia wastewater according to claim 1, characterized in that: The short-range denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank are all provided with biological fillers; The biological filler is a mobile filler or a fixed filler. When the biological filler is a mobile filler, the filling ratio of the biological filler is 20-40%. When the biological filler is a fixed filler, the filling spacing of the biological filler is 150-300 mm.

5. The full-process treatment device for high-organic-matter-high-ammonia wastewater according to claim 1, characterized in that: The short-cut denitrification-anaerobic ammonium oxidation tank and the denitrification tank are both provided with a stirring device; The bottoms of the nitrite-anaerobic ammonium oxidation tank, the denitrification swing tank and the nitrification and carbon removal tank are all provided with an aeration system; the tops of the nitrite-anaerobic ammonium oxidation tank, the denitrification swing tank and the nitrification and carbon removal tank are all provided with a gas collection system.

6. A method for treating high-organic-matter and high-ammonia wastewater using the treatment device according to any one of claims 1 to 5, characterized in that: The following steps are involved: The high-organic and high-ammonia wastewater is sequentially passed through an anaerobic tower, a short-cut denitrification-anaerobic ammonium oxidation tank, a nitrification-anaerobic ammonium oxidation tank, a denitrification swing tank, an intermediate sedimentation tank, a denitrification tank, a nitrification and carbon removal tank, and a final sedimentation tank to perform anaerobic methanation treatment of organic matter, short-cut denitrification-anaerobic ammonium oxidation denitrification, nitrification-anaerobic ammonium oxidation denitrification, denitrification, sedimentation, denitrification, nitrification and carbon removal, and final sedimentation to obtain recycled water; The high-organic and high-ammonia wastewater has a COD concentration of 5000-20000 mg / L, a BOD concentration of 4000-8000 mg / L, ammonia nitrogen of 300-2000 mg / L, and a total nitrogen of 400-2000 mg / L.

7. The method according to claim 6, characterized in that The dissolved oxygen concentration in the nitrite-anaerobic ammonium oxidation tank is 0.5-1.5 mg / L, the dissolved oxygen concentration in the denitrification swing tank is 0-1.5 mg / L, and the dissolved oxygen concentration in the nitrification and carbon removal tank is 2-3 mg / L; The dissolved oxygen concentrations in the anaerobic tower, the short-cut denitrification-anaerobic ammonia oxidation tank, the intermediate sedimentation tank, the denitrification tank and the final sedimentation tank are all ≤0.1 mg / L.

8. The method according to claim 7, characterized in that The suspended sludge concentration of the short-cut denitrification-anaerobic ammonium oxidation tank, the nitrite-anaerobic ammonium oxidation tank and the denitrification swing tank after stable operation is ≤1000 mg / L; When the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is 1 to 1.2, the dissolved oxygen in the denitrification swing tank is 0.1 to 0.2 mg / L; When the ratio of nitrite to ammonia nitrogen in the effluent of the nitrite-anaerobic ammonium oxidation tank is less than 1, the dissolved oxygen in the denitrification swing tank is 0.2-1.5 mg / L.

9. The method according to claim 6, characterized in that When the BOD / TN of the high-organic and high-ammonia wastewater is greater than 5, the high-organic and high-ammonia wastewater not only enters the anaerobic tower for anaerobic treatment, but also enters the denitrification-anaerobic ammonia oxidation tank and the denitrification tank as a supplementary source of organic carbon source; When BOB / TN in the high-organic and high-ammonia wastewater is less than 5, additional carbon source is added.

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