CN111646648A - Remote treatment method for excrement wastewater of modular railway train excrement collector - Google Patents
Remote treatment method for excrement wastewater of modular railway train excrement collector Download PDFInfo
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Abstract
The invention provides a modular long-term treatment method of excrement wastewater of a railway train excrement collector, which comprises the steps of using a treatment device, wherein the treatment device comprises a pretreatment system and a nitrogen and phosphorus removal system, the pretreatment system comprises a first stack screw dehydrator and an air floatation machine, the nitrogen and phosphorus removal system comprises a short-cut nitrification and denitrification module, an anaerobic ammonia oxidation tank and a synchronous nitrification and denitrification module, the short-cut nitrification and denitrification module comprises a denitrification tank, a nitrosation tank and a first sedimentation tank, and the synchronous nitrification and denitrification module comprises a membrane biological filter and a second sedimentation tank; the device also comprises a sludge treatment system and an advanced treatment system; the treatment method correspondingly comprises a pretreatment step, a nitrogen and phosphorus removal step, an advanced treatment step and a sludge treatment step. The invention realizes high-efficiency denitrification by combining the multiple modules and the multistage reaction tank, and the operation cost is reduced by 50 percent compared with the prior art.
Description
Technical Field
The invention relates to a modularized railway train excrement wastewater treatment device and method for a toilet bowl, and belongs to the field of railway train sewage treatment.
Background
With the rapid development of the social economy and the accelerated advancement of urbanization in China, domestic high-speed railway trains (high-speed railway trains, hereinafter referred to as high-speed rails) are rapidly developed. It is reported that in 2008, the total mileage of high-speed rail in China is 672 kilometers and less than 1% of the total operating mileage of the railway, and in 2015, the total operating mileage of high-speed rail in China reaches 1.9 kilometers and accounts for 15.7% of the total operating mileage of the railway. It follows that high-speed rail construction is developing very rapidly.
The rapid development of high-speed rails brings rapid and convenient traffic to people, shortens the travel time of people, makes people more comfortable and convenient to travel, and brings some problems at the same time. In the past, the railway train toilets in China are all in a direct discharge mode, but with the increasing strength of comprehensive national power in China, the environment protection industry is more and more emphasized by the nation, people have higher and higher requirements on the environment, and the excrement collectors are all used for collecting passenger excrement sewage since the high-speed opening. With the rapid development of high-speed railways, the amount of high-speed railway excrement sewage is also rapidly increased, and according to the regulations of health departments, the sewage of the excrement collector of the high-speed railway train (hereinafter referred to as the sewage of the excrement collector of the high-speed railway) cannot be directly discharged along the line and must be collected and then treated in a centralized manner. Therefore, how to treat the high-speed rail fecal sewage economically and effectively is urgent.
The train toilet wastewater has the characteristics of high organic matter, high suspended matter, high ammonia nitrogen, high phosphorus, low carbon-nitrogen ratio and the like, namely four high and one low, and simultaneously has the advantages of high chroma, high biotoxicity and high treatment difficulty due to the fact that the wastewater contains various inhibiting substances, so that the wastewater becomes the key point for treating the wastewater in the railway industry.
At present, the sewage of the train toilet wastewater collector is collected and then enters a multi-grid septic tank, and after anaerobic treatment for several months, the sewage is discharged into a municipal pipe network or is treated with other sewage generated by a high-speed railway station in a unified way.
Patent CN201611101840 provides a system and a method for centralized treatment of sewage of a toilet bowl of a high-speed railway carriage. Firstly, a rotary roller grid is used for removing toilet paper and large excrement in the sewage of the excrement collector; setting a pretreatment regulating tank and adding bleaching powder for removing part of ammonia nitrogen and suspended matters in the sewage and regulating the water quality and the water quantity; an internal circulation micro-aerobic reactor is arranged to receive 2/3 excrement collector sewage, 100-150 meshes of micro-electrolysis catalytic carrier particles are added, and short-cut nitrification can be realized through granular sludge; an internal circulation anaerobic reactor is utilized to realize the removal of partial ammonia nitrogen and nitrate nitrogen; a dual-circulation aerobic reactor is arranged to realize synchronous nitrification and denitrification of aerobic granular sludge; a special-effect denitrification aeration filter is arranged, and the deep treatment of sewage is realized by utilizing the action of a micro-electrolysis catalytic biological carrier; treating the water with chlorine dioxide (ClO)2) And (4) performing disinfection treatment to realize standard emission.
The three steps of synchronous shortcut nitrification and denitrification, anaerobic ammonia oxidation and synchronous nitrification and denitrification in the patent are realized by a single reactor, specifically, the three steps are respectively carried out in an internal circulation micro-aerobic reactor 3, an internal circulation anaerobic reactor 4 and a dual circulation aerobic reactor 5, so that the sewage treatment system is difficult to realize high-efficiency denitrification. Meanwhile, 100-150 meshes of micro-electrolysis catalytic carrier particles are required to be added into the internal circulation micro-aerobic reactor 3, the internal circulation anaerobic reactor 4 and the dual-circulation aerobic reactor 5 of the sewage treatment system, and the operation cost of the system is high.
Chinese patent CN200910092443 relates to a method for centralized treatment of excrement, which comprises the following steps: the method comprises the following steps of solid-liquid separation, flocculation dehydration, aerobic composting, anaerobic treatment of sewage, facultative aerobic treatment of sewage, membrane bioreaction treatment of sewage and odor treatment, and by the steps, 100% harmlessness, 99.7% reduction and 100% recycling of excrement and mud of the city are realized. In this patent, the anaerobic sludge in the anaerobic treatment step, the facultative sludge in the facultative treatment step, and the aerobic sludge in the aerobic treatment step of the sewage are all returned to the dehydration step. The excrement centralized treatment method in the patent requires sludge return, and the sewage in the patent also needs anaerobic treatment before the denitrification step. The efficiency and cost of this treatment scheme is high.
Therefore, a new method and a new device for treating the waste water of the excrement of the railway train excrement collector are needed in the field.
Disclosure of Invention
The invention provides a modularized railway train excrement collector wastewater treatment device and method aiming at the problems that the domestic high-speed railway train is rapidly developed and the sewage of a high-speed railway excrement collector needs to be solved urgently, and the modularized railway train excrement collector wastewater treatment device and method can effectively treat the sewage of the excrement collector and reduce the impact of the sewage discharged into the operation stability of a medium and small sewage treatment plant.
In order to solve the technical problems, the technical scheme of the invention is as follows:
the invention provides a long-term treatment method of excrement wastewater of a modular railway train excrement collector, which comprises the steps of using a treatment device, the treatment device comprises a pretreatment system (1) and a nitrogen and phosphorus removal system (2) which are arranged in sequence in the flow direction of wastewater, the pretreatment system comprises a first spiral shell-stacking dehydrator (1.1) and an air flotation machine (1.2) which are arranged in sequence in the wastewater flowing direction, the nitrogen and phosphorus removal system comprises a short-cut nitrification and denitrification module (2.1), an anaerobic ammonia oxidation tank (2.2) and a synchronous nitrification and denitrification module (2.3) which are arranged in sequence in the flow direction of wastewater, the short-cut nitrification and denitrification module comprises a denitrification tank (2.11), a nitrosation tank (2.12) and a first sedimentation tank (2.13) which are arranged in sequence in the flow direction of the wastewater, the synchronous nitrification and denitrification module comprises a membrane biological filter (2.31) and a second sedimentation tank (2.32) which are arranged in sequence in the flow direction of wastewater; the device also comprises a sludge treatment system (4), and the sludge treatment system comprises a sludge deposition pool (4.1) and a second spiral shell-overlapping dehydrator (4.2) which are arranged in sequence in the wastewater flow direction; the device also comprises an advanced treatment system (3), wherein the advanced treatment system (3) comprises an MABR (3.1) for further denitrifying the wastewater and an advanced oxidation reactor (3.2) for decoloring and disinfecting the wastewater which are arranged in sequence in the flow direction of the wastewater;
the processing method comprises the following steps:
step A, pretreatment step: removing a large amount of solid particles in the wastewater through a pretreatment system comprising a first spiral shell-stacking dehydrator and an air floatation machine, and removing partial organic matters, nitrogen and phosphorus by combining with adding of a medicament to reduce the chroma; liquid in the first screw-stacking dehydrator enters an air flotation machine, and solid obtained by separation in the first screw-stacking dehydrator is transported and discharged; the solid obtained by separation in the air flotation machine enters a sludge sedimentation tank (4.1), and the liquid obtained by separation in the air flotation machine enters a denitrification tank (2.11);
b, nitrogen and phosphorus removal: the pretreated wastewater enters a denitrification and dephosphorization system, the wastewater sequentially passes through a denitrification tank (2.11), a nitrosation tank (2.12), a first sedimentation tank (2.13), an anaerobic ammonia oxidation tank (2.2), a membrane biological filter (2.31) and a second sedimentation tank (2.32), and water discharged from the second sedimentation tank (2.32) enters a step C for advanced treatment; the sludge generated in the nitrogen and phosphorus removal system enters the sludge sedimentation tank (4.1);
step C, deep treatment step: wastewater flowing in from the second sedimentation tank is subjected to deep denitrification by an MABR (membrane aeration biofilm reactor), wastewater flowing out of the MABR enters a high-grade oxidation reactor for decolorization and disinfection, sludge generated in the MABR is also fed into the sludge sedimentation tank, and the wastewater discharged after being treated by the deep treatment system (3) can be directly used;
step D, sludge treatment: supernatant in the sludge deposition pool (4.1) returns to the nitrogen and phosphorus removal system (2) for retreatment, slurry in the sludge deposition pool (4.1) is pumped to the second spiral dehydrator (4.2) for solid-liquid separation, the solid obtained by separation is transported and discharged, and the liquid obtained by separation also returns to the nitrogen and phosphorus removal system (2) for retreatment.
In a specific embodiment, an intensified oxidative coagulation decolorizing agent is added into the air floatation machine, and the intensified oxidative coagulation decolorizing agent comprises polyaluminium chloride and/or polyacrylamide.
In a specific embodiment, a phosphorus removal agent is added into the second sedimentation tank (2.32) to remove phosphorus from the wastewater, and the phosphorus removal agent is one or more of lime, iron salt and aluminum salt.
In a particular embodiment, the apparatus further comprises a return line for the waste water from the nitritation tank (2.12) back to the denitrification tank (2.11), through which return line the waste water at the outlet of the nitritation tank (2.12) can flow back into the denitrification tank (2.11) in addition to the first sedimentation tank (2.13).
In a particular embodiment, the apparatus further comprises a first cross-over conduit for return of wastewater from the outlet of the first sedimentation tank (2.13) to the denitrification tank (2.11).
In a particular embodiment, the apparatus further comprises a second cross-over conduit for wastewater flowing directly from the outlet of the first sedimentation tank (2.13) to the membrane biofilter (2.31).
Compared with the prior art, the invention has the following beneficial effects:
1) after the wastewater is pretreated, biologically denitrified and dephosphorized and deeply treated, the effluent meets the requirements of urban greening and vehicle washing water quality in the standard of urban wastewater recycling urban miscellaneous water quality (GB/T18920-2002). The removal rate of COD in the wastewater is more than 98.6 percent, and the removal rates of SS, ammonia nitrogen and TN can reach more than 99 percent.
2) The nitrogen and phosphorus removal system adopts various technical combinations beneficial to increasing the number and the types of microorganisms, so that the number of the microorganisms is increased under the scheme of the invention, and the wastewater treatment is efficient and rapid. And the floor area is only half of that of the traditional method by matching with the high integration of integrated equipment and the optimized design of buildings, so that the problem of insufficient space is solved.
3) Each process unit is in modular design, and a through pipeline is arranged between the process units, so that the process units can be flexibly combined according to the actual operation condition, the effluent is guaranteed to reach the standard, and the operation cost is saved. When the nitrogen content of the inlet water in the anaerobic ammonia oxidation tank 2.2 does not reach the standard, the first through pipeline is used for carrying out denitrification treatment on the wastewater by the shortcut nitrification and denitrification module 2.1 again. When the inflow water of the anaerobic ammonia oxidation tank 2.2 reaches the inflow water standard of the membrane biological filter 2.31, the anaerobic ammonia oxidation step is not needed, and the wastewater in the first sedimentation tank 2.13 is directly sent into the membrane biological filter 2.31 by using a second crossing pipeline. The treatment device is highly integrated, the first and second penetrating pipelines are arranged, and the wastewater path can be flexibly combined and adjusted according to the water quality and the effluent standard.
In summary, compared with the prior art, the shortcut nitrification and denitrification of the invention are realized by the combination of the denitrification tank 2.11, the nitrosation tank 2.12 and the first sedimentation tank 2.13 in sequence, while the synchronous nitrification and denitrification of the invention are realized by the combination of the membrane biological filter 2.31 and the second sedimentation tank 2.32 in sequence. Therefore, in the device, after the sludge is added for the first time, namely the strains are added, the sludge can be used once and for all, and no medicament or strains are added in the subsequent operation process, so that the operation cost of the device is low. When the device is constructed and the strain is added for the first time, the corresponding common sludge from a sewage treatment plant is added into the denitrification tank 2.11, the nitrosation tank 2.12, the membrane biological filter 2.31 and the MABR, and the anaerobic ammonium oxidation tank 2.2 is required to be added with anaerobic ammonium oxidation bacteria. The invention realizes high-efficiency denitrification by combining the multiple modules and the multistage reaction tank, and the operation cost is reduced by 50 percent compared with the prior art.
Drawings
FIG. 1 is a schematic structural view of a remote treatment device for excrement wastewater of a modular toilet stool of a railway train.
FIG. 2 is a conventional biological denitrification pathway.
FIG. 3 shows a shortcut nitrification-denitrification biological denitrification process.
FIG. 4 is an anammox denitrification pathway.
Reference numerals: the device comprises a pretreatment system 1, a first spiral shell-overlapping dehydrator 1.1, an air flotation machine 1.2, a nitrogen and phosphorus removal system 2, a short-cut nitrification and denitrification module 2.1, a denitrification tank 2.11, a nitrosation tank 2.12, a first sedimentation tank 2.13, an anaerobic ammonia oxidation tank 2.2, a synchronous nitrification and denitrification module 2.3, a membrane biological filter 2.31, a second sedimentation tank 2.32, an advanced treatment system 3, an MABR3.1, a high-level oxidation reactor 3.2, a sludge treatment system 4, a sludge sedimentation tank 4.1 and a second spiral shell-overlapping dehydrator 4.2.
Detailed Description
The present invention will be described in detail with reference to examples. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
In the invention, the thick liquid in the first screw-stacking dehydrator 1.1 enters an air flotation machine, and the solid separated from the first screw-stacking dehydrator 1.1 is transported outside.
In the invention, PAC (coagulant) and/or PAM (flocculant) are generally required to be added into the air flotation machine 1.2, the air flotation machine comprises a coagulation tank and a flocculation tank, and the ideal effect can be achieved by adding one PAC or PAM.
In the invention, a waste water return channel returning to the denitrification tank 2.11 is generally arranged in the nitrosation tank 2.12, and the return ratio from the nitrosation tank 2.12 to the denitrification tank 2.11 can be adjusted according to the actual treatment condition of waste water.
In the invention, when the wastewater treatment device is initially constructed, sludge of a common municipal sewage treatment plant is used as strains in the denitrification tank 2.11, the nitrosation tank 2.12, the membrane biological filter 2.31 and the MABR3.1, namely, the same sludge is used in different tanks when a bacterial colony is constructed, and the tanks are divided into the denitrification tank, the nitrosation tank or other conditions under a normal operation state only under different culture environments of the tanks. In the present invention, the anammox bacteria used in the initial construction of the wastewater treatment apparatus can be purchased from, for example, a college or a scientific research institute.
In the invention, the anaerobic ammonia oxidation tank 2.2 has high requirement on the content of total Suspended Solids (SS), and the SS content is not suitable for the growth of anaerobic ammonia oxidation bacteria (rhodobacter). According to the invention, the first sedimentation tank 2.13 is arranged behind the nitrosation tank 2.12, so that the waste liquid entering the anaerobic ammonia oxidation tank 2.2 can smoothly carry out anaerobic ammonia oxidation and denitrification reaction.
In the invention, the biofilm culturing in the membrane biological filter 2.31 can move up and down, when the biofilm culturing is upwards separated from the water surface and placed in the air, aerobic bacteria mainly take effect and nitration reaction is mainly generated, and when the biofilm culturing is downwards immersed in the water, heterotrophic bacteria mainly take effect and denitrification reaction is mainly generated. The membrane biological filter 2.31 generally has no complete anaerobic state, but has alternating facultative zone and aerobic zone states.
In the present invention, the dephosphorising agent is generally added in the second sedimentation basin 2.32. If the phosphorus content in the effluent of the membrane biological filter 2.31 reaches the standard, the second sedimentation tank 2.32 does not need to be added with a dephosphorizing agent. The phosphorus removing agent is one or more of lime, iron salt and aluminum salt. The consumption of the phosphorus removal agent required by chemical phosphorus removal is related to the phosphorus content of the required effluent, and when the phosphorus content of the effluent is required to be less than or equal to 1.0mg/L, 1.7kg of iron or 0.8kg of aluminum is required to be added for removing 1kg of phosphorus. The amount of metal salt added is generally determined experimentally for a particular wastewater. The concentration of the TP of the inlet water is different from the expected phosphorus removal rate, and the corresponding phosphorus removal agent dosage is also different.
In the invention, the oxygen supply mechanisms of the membrane biological filter 2.31 and the MABR3.1 are different. The biofilm culturing in the membrane biofilter mainly utilizes oxygen in the air, and different reactions, namely nitrification and denitrification, occur in the same membrane biofilter at two different time points or time periods when the biofilm culturing is soaked in wastewater or exposed in the air. The oxygen on the MABR can penetrate through the membrane material, and different reactions, namely nitrification and denitrification, occur at different positions on the same MABR. In addition, the efficiency of the MABR is higher than that of the membrane biofilter. In the present invention, the sludge produced in the MABR3.1 is also sent to the sludge settling tank 4.1, but the MABR has a small sludge production amount, so that it is not shown in the figure.
The advanced oxidation reactor 3.2 used in the invention can be a micro-nano bubble generating device which is directly purchased and is also called a micro-nano aeration device; the reactor provides nano-scale or micro-scale ozone or oxygen for wastewater. Furthermore, no sludge is produced in the advanced oxidation reactor 3.2.
In the invention, PAC or PAM can be added into the sludge sedimentation tank 4.1 or a pipeline at the downstream of the sludge sedimentation tank to increase coagulation and flocculation. The sludge sedimentation tank 4.1 mainly plays a role in sludge concentration and collection, wherein a rough solid-liquid separation effect between sludge and wastewater can be generated, and the supernatant in the sludge sedimentation tank 4.1 is generally returned to the nitrogen and phosphorus removal system 2 for treatment. The primary purpose of the second stack screw dewaterer 4.2 is to reduce the moisture content of the sludge so that the sludge from the sludge settling tank 4.1 becomes or approaches solid sludge, which typically contains around 80 wt% moisture in the transported out dry solid sludge. In the invention, the liquid separated from the second spiral dehydrator 4.2 also returns to the nitrogen and phosphorus removal system 2.
The conventional biological denitrification, shortcut nitrification and denitrification biological denitrification and anaerobic ammonia oxidation denitrification in the invention shown in fig. 2-4 are the prior art well known to those skilled in the art. Further, denitrification occurring in the denitrification tank 2.11, nitrosation occurring in the nitrosation tank 2.12, anammox occurring in the anammox tank, simultaneous nitrification and denitrification occurring in the membrane biofilter, and deep denitrification occurring in the MABR are also known to those skilled in the art. The invention is characterized in that all the unit modules are combined in a certain sequence and process to form the device and the method for efficiently and inexpensively treating the wastewater of the train toilet wastewater. In addition, the stack screw dehydrator, the air flotation machine, the membrane biofilter, the MABR and the advanced oxidation reactor which are involved in the invention can be obtained commercially, and the innovation of the equipment and the details thereof is not involved in the invention.
Example 1
Taking a certain high-speed rail station collection and distribution center in Yunnan Kunming as an example, as the high-speed rail station collection and distribution center is a key traffic hub, a plurality of station trains exist, and the high-speed rail excrement collector wastewater has higher concentration and large water quantity. The waste water of the excrement collector is pumped by a vacuum pumping system and then is placed in a septic tank, the COD of the waste water of the septic tank is 5800mg/L, the SS is 2650mg/L, the ammonia nitrogen is 1500mg/L, the total nitrogen is 1800mg/L, and the total phosphorus is 200 mg/L. The treated wastewater meets the requirements of urban greening and vehicle washing water quality in the standards of urban wastewater recycling urban miscellaneous water quality (GB/T18920-2002).
As shown in figure 1, the sewage passes through a pretreatment system → a nitrogen and phosphorus removal system → an advanced treatment system, and the sludge generated in the sewage treatment process enters a sludge treatment system, which comprises the following treatment steps:
a medicament configuration; respectively preparing 25% polyaluminium chloride and 0.2% polyacrylamide solution for later use;
step A: and (5) preprocessing by a system. The effluent of the septic tank is firstly subjected to solid-liquid separation by overlapping, the liquid enters a dissolved air flotation machine, 300mg/L of polyaluminium chloride and 5mg/L of polyacrylamide are added, and part of SS, organic matters and TP are further removed under the actions of coagulation, oxidation and air flotation. The solid after solid-liquid separation and sludge generated in the sewage treatment process are dewatered and then transported to outside for disposal.
After pretreatment, SS in the sewage is reduced to 234mg/L, the removal rate reaches 91.2%, and the removal rate of COD is more than 80%.
And B: a nitrogen and phosphorus removal system. After two-stage solid-liquid separation in a pretreatment system, the content of suspended matters is greatly reduced, most of COD, partial ammonia nitrogen and TP in wastewater are removed, dissolved air flotation effluent automatically flows into a preposed denitrification unit, the BOD and partial total nitrogen of the influent water are removed by utilizing granular sludge in a denitrification tank, and certain alkalinity is generated; then the sewage enters a high-efficiency nitrosification unit, and partial nitrosification of ammonia nitrogen is realized by using the sludge in the nitrosification pool; part of sewage with the proportion of ammonia nitrogen and nitrite nitrogen controlled within the proportion range required by anaerobic ammonia oxidation after nitrosation enters an anaerobic ammonia oxidation tank after SS is removed by precipitation in a first precipitation tank, and ammonia nitrogen and TN are removed; and after the anaerobic ammonia oxidation treatment, the sewage enters a membrane biological filter for synchronous nitrification and denitrification for further denitrification, and meanwhile, chemical phosphorus removal is carried out by adding a phosphorus removal agent into a second rear sedimentation tank. The phosphorus removing agent is aluminum salt polyaluminium chloride, and the dosage of the experimental medicament is 90 mg/L.
After passing through the nitrogen and phosphorus removal system, COD in the sewage is 213mg/L, ammonia nitrogen is 22mg/L, total nitrogen is 56mg/L, and total phosphorus is 8 mg/L. The COD removal rate of the nitrogen and phosphorus removal system is 85%, the COD removal rate after passing through the pretreatment system and the nitrogen and phosphorus removal system reaches 96.3%, the ammonia nitrogen and total nitrogen removal rate reaches more than 95%, specifically 98.5% and 96.9%, respectively, and the TP removal rate reaches 96%.
And C, deeply processing the system. In particular to the deep denitrification of MABR and the decoloration and disinfection of an advanced oxidation reactor.
And the effluent treated by the nitrogen and phosphorus removal system enters an MABR integrated device for deep nitrogen removal. By utilizing the special aeration mode and oxygen transfer mechanism of the MABR, the microbial film can generate an obvious layered structure and can be roughly divided into 3 basic functional layers, namely an aerobic layer and a facultative layer which are close to the film and an anaerobic layer which is contacted with a bulk solution, so that the MABR has the capability of synchronous nitrification and denitrification. The aeration power efficiency of the MABR technology can reach 14kgO2the/kWh is 3-4 times of that of the traditional aeration mode, and accordingly, the aeration power consumption can be saved by about 75%.
After the advanced denitrification of the MABR integrated equipment, the contents of ammonia nitrogen and TN in the sewage are 6mg/L and 21mg/L, the removal rates of pollutants reach more than 60%, and the removal rates of ammonia nitrogen and TN in the step are 72.7% and 62.5% respectively.
The tail end of the system is provided with an advanced oxidation reactor for decoloring and sterilizing, and particularly adopts a micro-nano generating device of ozone or oxygen, so that ozone or oxygen bubbles entering the sewage reach a nano level, the dissolving concentration in the sewage is improved, the contact probability with the sewage is increased, and the gas mass transfer coefficient and the sewage treatment efficiency are improved. After the wastewater is subjected to advanced oxidation, the pollutants such as the chromaticity, COD and the like of the wastewater are further reduced, and the urban greening and vehicle washing standards of urban wastewater recycling urban miscellaneous water quality (GB/T18920-2002) are met.
In the step A, after sewage is collected by a train excrement collector, a vacuumizing system is adopted to suck the sewage of the excrement collector into a septic tank for collection, then the sewage enters a first spiral-wound dehydrator of the pretreatment system, solid garbage and large particles such as paper towels and the like are removed by the spiral-wound dehydrator, liquid obtained by solid-liquid separation of the spiral-wound dehydrator enters a dissolved air flotation machine, and a reinforced oxidation coagulation decoloration agent is added to further remove part of SS (total suspended solids), organic matters and TP under the actions of coagulation, oxidation and air flotation. The load of a subsequent biochemical system is reduced through two-stage reinforced coagulation filtration of 'stack screw and air flotation', and the stable operation of the biochemical system is ensured.
In the step B of nitrogen and phosphorus removal, the partial accumulation of nitrite nitrogen is realized through reasonable process combination, the ratio of nitrite nitrogen to ammonia nitrogen is controlled at the optimal reaction ratio, the alkalinity and free ammonia are controlled at the optimal level, and the efficient nitrogen removal under the conditions of high nitrogen and low carbon-nitrogen ratio is realized. In the step B, particularly, after two-stage solid-liquid separation of the pretreatment step, the content of suspended matters is greatly reduced, most of COD, partial ammonia nitrogen and TP in the wastewater are removed, the effluent of the dissolved air floatation machine automatically flows into a preposed denitrification tank, the BOD and partial total nitrogen of the influent are removed by utilizing granular sludge, and a certain alkalinity is generated; then the ammonia nitrogen enters a high-efficiency nitrosification pool to realize nitrosification of the ammonia nitrogen part; part of sewage with the proportion of ammonia nitrogen and nitrite nitrogen controlled within the proportion range required by anaerobic ammonia oxidation after nitrosation enters an anaerobic ammonia oxidation tank after SS is removed in a first sedimentation tank, and ammonia nitrogen and TN are removed; and after the anaerobic ammonia oxidation treatment, the sewage enters a membrane biological filter for synchronous nitrification and denitrification for further denitrification, and meanwhile, chemical phosphorus removal is carried out by adding a phosphorus removal agent into a second rear sedimentation tank.
In the invention, the nitrogen and phosphorus removal system in the step B is formed by combining the short-cut nitrification and denitrification module, the anaerobic ammonia oxidation tank and the synchronous nitrification and denitrification module, and the short-cut nitrification and denitrification module and the synchronous nitrification and denitrification module are combined by a plurality of tanks, so that the high-efficiency nitrogen removal under the conditions of high nitrogen and low carbon nitrogen ratios is realized.
In the invention, after the advanced treatment by the advanced treatment system 3 in the step C, TN, COD and chroma of the effluent are further reduced, so that the effluent meets higher treatment requirements.
And the advanced treatment system in the step C is MABR (membrane aeration biofilm reactor) advanced denitrification and advanced oxidation reactor decoloration and disinfection. The tail end of the system is provided with an advanced oxidation reactor, so that the pollution indexes such as chroma, COD and the like in the sewage are further reduced. In the step C, microorganisms are utilized by using a special aeration mode and an oxygen transfer mechanism of the MABRThe membrane will produce a distinct layered structure, the microbial membrane of which can be roughly divided into 3 basic functional layers, namely an aerobic layer and a facultative layer close to the membrane and an anaerobic layer in contact with the bulk solution, so that the MABR has the capability of simultaneous nitrification and denitrification. The aeration power efficiency of the MABR technology can reach 14kgO2the/kWh is 3-4 times of that of the traditional aeration mode, and accordingly, the aeration power consumption can be saved by about 75%. The invention is provided with an advanced treatment system MABR advanced denitrification and advanced oxidation reactor decoloration and disinfection, can further denitrify and dephosphorize and reduce organic matters and chroma in wastewater.
The invention researches out the most suitable pretreatment system for the high-iron wastewater: and (3) the spiral shell overlapping dehydrator and the air floatation machine are used for removing most of solid suspended matters and carrying out coagulating sedimentation pretreatment before denitrification treatment.
Biological denitrification is a key difficulty in wastewater treatment, the invention adopts a biological denitrification process mainly based on anaerobic ammonia oxidation, cooperates with partial nitrification and denitrification and synchronous nitrification and denitrification, and specifically reduces BOD and ammonia nitrogen load through a preposed denitrification tank, then realizes stable nitrosation in a nitrosation tank, and controls ammonia nitrogen/nitrosation nitrogen to be 1: 1; then the anaerobic ammonia oxidation realizes high-efficiency denitrification. Then, two groups of filter curtains which are symmetrically staggered and densely distributed are adopted in the membrane biological filter (also called a biological membrane pool), and an alternating and facultative aerobic zone and an aerobic zone are formed on the surfaces of the filter curtains to realize synchronous nitrification and denitrification, so that the sewage is purified. The whole nitrogen and phosphorus removal system 2 does not need to carry out sludge backflow, does not need to add any strain or catalyst after the device is constructed, and has low operation energy consumption.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions and substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (6)
1. A method for the long-term treatment of excrement wastewater of a modular railway train excrement collector comprises the steps of using a treatment device, the treatment device comprises a pretreatment system (1) and a nitrogen and phosphorus removal system (2) which are arranged in sequence in the flow direction of wastewater, the pretreatment system comprises a first spiral shell-stacking dehydrator (1.1) and an air flotation machine (1.2) which are arranged in sequence in the wastewater flowing direction, the nitrogen and phosphorus removal system comprises a short-cut nitrification and denitrification module (2.1), an anaerobic ammonia oxidation tank (2.2) and a synchronous nitrification and denitrification module (2.3) which are arranged in sequence in the flow direction of wastewater, the short-cut nitrification and denitrification module comprises a denitrification tank (2.11), a nitrosation tank (2.12) and a first sedimentation tank (2.13) which are arranged in sequence in the flow direction of the wastewater, the synchronous nitrification and denitrification module comprises a membrane biological filter (2.31) and a second sedimentation tank (2.32) which are arranged in sequence in the flow direction of wastewater; the device also comprises a sludge treatment system (4), and the sludge treatment system comprises a sludge deposition pool (4.1) and a second spiral shell-overlapping dehydrator (4.2) which are arranged in sequence in the wastewater flow direction; the device also comprises an advanced treatment system (3), wherein the advanced treatment system (3) comprises an MABR (3.1) for further denitrifying the wastewater and an advanced oxidation reactor (3.2) for decoloring and disinfecting the wastewater which are arranged in sequence in the flow direction of the wastewater;
the processing method comprises the following steps:
step A, pretreatment step: removing a large amount of solid particles in the wastewater through a pretreatment system comprising a first spiral shell-stacking dehydrator and an air floatation machine, and removing partial organic matters, nitrogen and phosphorus by combining with adding of a medicament to reduce the chroma; liquid in the first screw-stacking dehydrator enters an air flotation machine, and solid obtained by separation in the first screw-stacking dehydrator is transported and discharged; the solid obtained by separation in the air flotation machine enters a sludge sedimentation tank (4.1), and the liquid obtained by separation in the air flotation machine enters a denitrification tank (2.11);
b, nitrogen and phosphorus removal: the pretreated wastewater enters a denitrification and dephosphorization system, the wastewater sequentially passes through a denitrification tank (2.11), a nitrosation tank (2.12), a first sedimentation tank (2.13), an anaerobic ammonia oxidation tank (2.2), a membrane biological filter (2.31) and a second sedimentation tank (2.32), and water discharged from the second sedimentation tank (2.32) enters a step C for advanced treatment; the sludge generated in the nitrogen and phosphorus removal system enters the sludge sedimentation tank (4.1);
step C, deep treatment step: wastewater flowing in from the second sedimentation tank is subjected to deep denitrification by an MABR (membrane aeration biofilm reactor), wastewater flowing out of the MABR enters a high-grade oxidation reactor for decolorization and disinfection, sludge generated in the MABR is also fed into the sludge sedimentation tank, and the wastewater discharged after being treated by the deep treatment system (3) can be directly used;
step D, sludge treatment: supernatant in the sludge deposition pool (4.1) returns to the nitrogen and phosphorus removal system (2) for retreatment, slurry in the sludge deposition pool (4.1) is pumped to the second spiral dehydrator (4.2) for solid-liquid separation, the solid obtained by separation is transported and discharged, and the liquid obtained by separation also returns to the nitrogen and phosphorus removal system (2) for retreatment.
2. The treatment method as claimed in claim 1, wherein an intensified oxidative coagulation decolorizing agent is added into the air flotation machine, and the intensified oxidative coagulation decolorizing agent comprises polyaluminium chloride and/or polyacrylamide.
3. The treatment method according to claim 1, characterized in that a phosphorus removal agent is added into the second sedimentation tank (2.32) to remove phosphorus from the wastewater, and the phosphorus removal agent is one or more of lime, iron salt and aluminum salt.
4. A method according to claim 1, characterized in that the apparatus further comprises a return conduit for waste water from the nitritation tank (2.12) back to the denitrification tank (2.11), through which return conduit the waste water at the outlet of the nitritation tank (2.12) can flow back to the denitrification tank (2.11) in addition to the first sedimentation tank (2.13).
5. A treatment method according to any of claims 1-3, characterized in that the apparatus further comprises a first crossing conduit for returning the waste water from the outlet of the first sedimentation tank (2.13) to the denitrification tank (2.11).
6. A treatment method according to any one of claims 1 to 5, characterized in that the apparatus further comprises a second cross-over conduit for wastewater flowing from the outlet of the first sedimentation tank (2.13) directly to the membrane biological filter (2.31).
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