CN112158955B - High-salinity high-nitrogen wastewater integrated biological treatment device and method based on sulfur circulation - Google Patents

High-salinity high-nitrogen wastewater integrated biological treatment device and method based on sulfur circulation Download PDF

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CN112158955B
CN112158955B CN202011080546.4A CN202011080546A CN112158955B CN 112158955 B CN112158955 B CN 112158955B CN 202011080546 A CN202011080546 A CN 202011080546A CN 112158955 B CN112158955 B CN 112158955B
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CN112158955A (en
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李巍
梁霄
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Dalian Maritime University
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    • 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
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • 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
    • C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
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    • C02F3/00—Biological treatment of water, waste water, or sewage
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C02F3/345—Biological treatment of water, waste water, or sewage characterised by the microorganisms used for biological oxidation or reduction of sulfur compounds
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    • C02F2101/00—Nature of the contaminant
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    • C02F2101/16—Nitrogen compounds, e.g. ammonia
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    • C02F2101/166—Nitrites
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    • C02F2101/30—Organic compounds
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    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry

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Abstract

The invention relates to a sulfur-cycle-based high-salinity high-nitrogen wastewater integrated biological treatment device and method. The device comprises a device shell, wherein an oxygenation zone, a buffer transition zone, an anaerobic reaction zone I, an anaerobic reaction zone II, an anaerobic reaction zone III, a water outlet zone and a reflux zone are sequentially arranged in the shell at intervals by vertical baffles; along the water flow direction, the front end and the rear end of the oxygen charging area are respectively communicated with the reflux area and the buffer transition area, and other areas are sequentially connected in an initial position; the tail end of the water outlet area is communicated with the reflux area without baffle isolation; the bottoms of the 3 reaction zones are a fine sand zone, a coarse sand zone and a seawater zone from low to high in sequence; one side of the anaerobic reaction zone is provided with an inspection sampling port from low to high in sequence. The method integrates the ammonia oxidation reaction, the sulfate reduction reaction, the carbon degradation reaction, the autotrophic desulfurization denitrification reaction, the heterotrophic denitrification reaction and the like, and realizes the synchronous, efficient and stable treatment of the high-salinity and high-nitrogen wastewater.

Description

High-salinity high-nitrogen wastewater integrated biological treatment device and method based on sulfur circulation
Technical Field
The invention relates to a sulfur-cycle-based high-salinity high-nitrogen wastewater integrated biological treatment device and method, in particular to a method and device for treating marine product culture and processing wastewater.
Background
In the process of marine product culture, the release of a large amount of culture bait and the natural excretion of cultured organisms cause the generated wastewater to contain high-concentration nitrogen and organic pollutants. The large amount of discharged wastewater causes serious pollution to the water body environment of the surrounding sea area, damages to the ecological balance and frequent eutrophication and red tide phenomena. At present, various marine environmental protection laws and regulations are provided at the national level and the local level of China, and the wastewater discharge of the breeding industry is regulated. However, since the treatment of the high-salinity high-nitrogen wastewater with seawater is extremely difficult, the phenomenon of excessive nitrogen discharge sometimes occurs. Meanwhile, a large amount of high-salt organic wastewater is generated in the marine product processing industry close to the mariculture region, the treatment difficulty is in removal of high-concentration nitrogen-containing organic matters, and compared with the treatment of mariculture wastewater, the treatment cost of the marine product processing wastewater of unit volume is higher.
At present, two methods are mainly adopted for treating high-salt high-nitrogen wastewater: physicochemical and biological methods. The physical and chemical method is mainly to add chemical agents into the wastewater and treat refractory organics through catalysis-oxidation or chemical precipitation and other methods. However, the discharge amount of the aquaculture wastewater is large, the concentration of organic matters in the marine product processing wastewater is high, so that the use amount of chemical agents required in the treatment process is large, the cost is high, and secondary pollution can be caused due to improper control. The biological method is used for treating nitrogen-containing substances and organic pollutants by utilizing the absorption, metabolism and degradation of microorganisms, and has the advantages of low cost, high efficiency, no secondary pollution and the like. However, the biological treatment method adopted at the present stage is mostly a segmented and serial process, namely processes such as aeration oxidation, regulation acidification, anaerobic degradation and the like are respectively applied to separate reaction systems, and then the systems are connected in series. Meanwhile, the wastewater of mariculture and marine product processing is also treated separately. Such a treatment method brings practical problems of a large number of treatment facilities, a large floor space, high management cost, and the like.
The main pollutants of the marine product culture wastewater are nitrite nitrogen, ammonia nitrogen and organic matters, and a large amount of wastewater containing nitrite nitrogen, organic matters and ammonia nitrogen is discharged in some marine product processing industries. The above two types of waste water can be treated jointly, usually in the geographical proximity of the mariculture and seafood processing industries. The invention provides a device and a method for cooperatively treating two kinds of waste water, which comprises the following steps: a large amount of organic matters contained in the marine product processing wastewater are used as a carbon source for aerobic oxidation of nitrogenous substances in the mariculture wastewater and an electron donor required by anaerobic denitrification, and a large amount of sulfate specially contained in seawater is used as an intermediate substance to promote removal of nitrogen and carbon, so that the number of treatment facilities and the floor area are reduced, and a large amount of manpower, material resources and financial resources can be saved by treating wastes with the wastes. During the process, a large amount of sulfate in the seawater is reduced under an anaerobic condition to generate sulfide which is an intermediate product, and the sulfide can be oxidized into sulfate to return to the seawater again in the desulfurization denitrification reaction for removing nitrite nitrogen, so that new pollutants are not introduced.
Disclosure of Invention
The invention provides a device and a method for biologically treating high-salinity high-nitrogen wastewater based on sulfur circulation, which can achieve the purpose of synchronously removing ammonia nitrogen, nitrite and organic matters by utilizing microbial sulfate reduction, autotrophic desulfurization denitrification, heterotrophic denitrification and aerobic ammoxidation.
In order to realize the purpose, the invention adopts the following technical scheme:
the invention provides an integrated biological treatment device for high-salinity and high-nitrogen wastewater, which comprises a device shell; the shell is internally provided with an oxygenation zone, a buffer transition zone, an anaerobic reaction zone I, an anaerobic reaction zone II, an anaerobic reaction zone III, a water outlet zone and a reflux zone at intervals by vertical baffles in sequence; the aeration zone, the buffer transition zone, the anaerobic reaction zone I, the anaerobic reaction zone II, the anaerobic reaction zone III and the water outlet zone are parallel to each other, and the reflux zone is vertical to each zone;
the front end and the rear end of the oxygenation zone are respectively communicated with the reflux zone and the buffer transition zone along the water flow direction, and the buffer transition zone, the anaerobic reaction zone I, the anaerobic reaction zone II, the anaerobic reaction zone III and the water outlet zone are sequentially connected end to end; the tail end of the water outlet area is communicated with the reflux area without baffle isolation; all the areas are connected end to form a communicated cycle;
the bottom of the anaerobic reaction zone I, the bottom of the anaerobic reaction zone II and the bottom of the anaerobic reaction zone III are a fine sand zone, a coarse sand zone and a seawater zone from low to high in sequence;
the upper part of the shell is provided with a water outlet, the lower part of the shell is provided with a water inlet, and the water outlet and the water inlet are both communicated with the reflux area;
an inspection sampling port I, an inspection sampling port II and an inspection sampling port III are sequentially arranged on one side, corresponding to the anaerobic reaction area I, of the shell from low to high;
the shell is provided with an inspection sampling port four, an inspection sampling port five and an inspection sampling port six in sequence from low to high, which correspond to one side of the anaerobic reaction zone II;
an inspection sampling port seven, an inspection sampling port eight and an inspection sampling port nine are sequentially arranged on one side of the shell corresponding to the anaerobic reaction zone III from low to high;
and a first water outlet inspection port and a second water outlet inspection port are respectively arranged on one side of the shell corresponding to the water outlet area.
In the technical scheme, furthermore, the vertical heights of the fine sand area, the coarse sand area and the seawater area account for 10-20%, 10-20% and 60-80% of the total height of the reaction system in sequence; the equivalent diameter of the fine sand in the fine sand area is 0.1-1mm, and the equivalent diameter of the coarse sand in the coarse sand area is 1-3 mm; the regions are of the same width.
In the technical scheme, furthermore, the vertical heights of the centers of the first water outlet inspection port and the second water outlet inspection port from the bottom are both 2-5 cm; the vertical height from the center of the third inspection sampling port, the sixth inspection sampling port and the ninth inspection sampling port to the top of the seawater area is 2-5 cm; the vertical height between the centers of the second inspection sampling port, the fifth inspection sampling port and the eighth inspection sampling port and the top of the coarse sand area is 2-5 cm; the vertical height from the center of the first inspection sampling port, the fourth inspection sampling port and the seventh inspection sampling port to the top of the fine sand area is 2-5 cm.
In the technical scheme, the diameters of the inspection sampling port and the effluent inspection port are both 1-3 cm.
In the technical scheme, the water outlet area is provided with a stirring paddle I, the reflux area is provided with a stirring paddle II, and the communication part of the oxygenation area and the buffer transition area is provided with a stirring paddle III; the height of the stirring paddle II accounts for 40-60% of the total reaction system height; the stirring paddles I and III are positioned at the same height and are positioned 20-30cm above the top limit of the coarse sand area.
In the above technical scheme, further, the bottom of the oxygen charging area is provided with an air charging pipe and an air charging head.
Among the above-mentioned technical scheme, further, still include mud storage tank and intake case, mud storage tank is through advancing dredge pump and water inlet intercommunication, and the intake case is through intake pump and water inlet intercommunication.
The invention also provides a method for biological treatment of high-salinity high-nitrogen wastewater based on sulfur cycle, which uses the device of claim 1 and comprises three steps:
step one, an activated sludge acclimation stage:
inoculating aerobic activated sludge into an oxygenation zone, and inoculating anaerobic activated sludge into an anaerobic reaction zone I, an anaerobic reaction zone II and an anaerobic reaction zone III;
will contain NH 4 + High-salinity wastewater with macromolecular organic matters enters from the water inlet, the wastewater enters the aeration zone to be fully contacted with aerobic activated sludge under the action of aeration and stirring of the aeration head, and NH is generated 4 + Is oxidized to NO 2 - The macromolecular organic matter is oxidized into micromolecular organic matter and CO 2 ，NO 2 - And part of organic matters enter the buffer transition area along with the water flow and flow through other subsequent areas;
introducing organic wastewater of seawater and SO in water into the anaerobic reaction zone I through inspection of a sampling port 4 2- Fully contacts with organic matters and anaerobic activated sludge, and is respectively converted into S under the action of sulfate reduction reaction 2- And CO 2 Enters a subsequent reaction area along with the water flow;
the S is introduced into the four-way anaerobic reaction zone II through the inspection sampling port 2- And NO 2 - With SO in the front zone effluent 4 2- 、S 2- 、NO 2 - Is mixed with a small amount of organic matters and fully contacts with anaerobic activated sludge, and S is subjected to sulfate reduction reaction and mixotrophic desulfurization denitrification reaction 2- 、NO 2 - 、SO 4 2- And a small amount of organic matter is converted into S 0 (SO 4 2- )、N 2 、S 2- And CO 2 Enters a subsequent reaction area along with the water flow;
introducing S-containing gas into the anaerobic reaction zone III (12) through an inspection sampling port 2- And NO 2 - Seawater wastewater and NO in the front zone influent 2 - And S 2- Are converged and fully contacted with anaerobic activated sludge and are respectively converted into S under the action of autotrophic desulfurization denitrification reaction 0 (SO 4 2- ) And N 2 The effluent is finally discharged from the first effluent inspection port and the second effluent inspection port;
adopting an intermittent water feeding mode, feeding water for 1 time every 24-48h, wherein the liquid level of each reaction zone is 20-30cm higher than the upper limit of the coarse sand zone after water feeding each time; controlling the pH value of the inlet water to be more than 7.5; three paddles do not operate at this stage;
NH in the water entering the oxygen charging zone 4 + The concentration is 100-200mgN/L in terms of N, and the concentration of the organic matter is 250-300mgC/L in terms of C; SO in inlet water of anaerobic reaction zone I 4 2- The concentration is 850-950mgS/L in terms of S, and the concentration of the organic matter is 600-1000mgC/L in terms of C; in the water inlet S of the anaerobic reaction zone II 2- The concentration is 200-300mgS/L in terms of S, NO 2 - The concentration is 100-200mgN/L in terms of N; anaerobic reaction zone III in water S 2- The concentration is 50-100mgS/L calculated by S, NO 2 - The concentration is 50-100mgN/L calculated by N;
when it is in the oxygen charging zone NH 4 + Removal rate, S in anaerobic reaction zone II and anaerobic reaction zone III (12) 2- And NO 2 - The removal rate is kept above 90 percent, and SO is in the anaerobic reaction zone I 4 2- When the removal rate reaches more than 50%, successfully domesticating the activated sludge;
step two, a reactor starting stage:
adopting an operation mode of intermittent water inlet and no water outlet, feeding water for 1 time every 12-24h, wherein the water inlet volume accounts for 5% -20% of the total effective volume of the reaction system each time, gradually increasing the water inlet amount to slowly improve the water inlet load, and discharging water through the first water outlet inspection port, the second water outlet inspection port and the water outlet to maintain the water surface height of the reaction system unchanged after the reaction system is filled;
high-salt organic wastewater enters an oxygenation area through a water inlet, and NH in the inlet water 4 + Fully contacts with the aerobic activated sludge under the action of aeration and stirring of the aeration head to form NH 4 + Is oxidized to NO 2 - The macromolecular organic matter is oxidized into micromolecular organic matter and CO 2 ，NO 2 - And residual organic matters enter a buffer transition area along with water flow, and SO in seawater 4 2- No reaction occurs in this region; part of suspended sludge in the oxygenation zone enters a buffer transition zone along with water flow, and DO in the water is consumed in the zone; NO 2 - 、SO 4 2- And the residual organic matters enter an anaerobic reaction zone I along with water flow, and SO in the water 4 2- Fully contacts with organic matters and anaerobic activated sludge, and is respectively converted into S under the action of sulfate reduction reaction 2- And CO 2 Entering a subsequent anaerobic reaction zone II along with the water flow; in the anaerobic reaction zone II, SO contained in water 4 2- 、S 2- 、NO 2 - Fully contacts with a small amount of organic matters and anaerobic activated sludge, and is respectively converted into S under the action of sulfate reduction reaction and mixotrophic desulfurization denitrification reaction 2- 、S 0 (SO 4 2- )、N 2 And CO 2 Entering an anaerobic reaction zone III along with the water flow; in the anaerobic reaction zone III, residual S in water 2- And NO 2 - Fully contacts with anaerobic activated sludge and is respectively converted into S under the action of autotrophic desulfurization denitrification reaction 0 (SO 4 2- ) And N 2 ；
Controlling the pH value of the inlet water to be more than 7.5; the rotating speed of the stirring paddle II is 60-500 rpm/min; the rotating speeds of the stirring paddle I and the stirring paddle III are 30-100 rpm/min;
NH in the feed water 4 + Concentration is 100-400mgN/L in terms of N, TOC is 300-1000mgC/L in terms of C, SO 4 2- The concentration is 500-950mgS/L in terms of S;
when NO is present 2 - When the TOC removal rate and the TOC removal rate are both kept above 90%, the system is started successfully;
step three, the reactor operation stage:
the operation is carried out by adopting a continuous flow water inlet mode, and the hydraulic retention time HRT is 12-48 h;
controlling the pH value of the inlet water to be more than 7.5; the rotating speed of the stirring paddle II is 60-500 rpm/min; the rotating speeds of the stirring paddle I and the stirring paddle III are 30-100 rpm/min;
NH in the feed water 4 + Concentration is 100-400mgN/L in terms of N, TOC is 300-1000mgC/L in terms of C, SO 4 2- The concentration is 500-950mgS/L in terms of S.
In the above technical solution, further, the DO value in the oxygenation zone is controlled at 3-5 mg/L; the dissolved oxygen in water is consumed by utilizing a buffer transition zone, and the DO value at the tail end of the buffer transition zone is less than or equal to (1-2) mg/L.
In the above technical scheme, further, the pH of the feed water is NaHCO 3 Adjusting; the temperature of each area is more than or equal to 15 ℃; supplementing aerobic activated sludge to the oxygenation zone for 1 time every 1-6h, wherein the volume of supplemented sludge accounts for 10-50% of the total volume of bottom sludge in the oxygenation zone;
in the technical scheme, furthermore, the aerobic activated sludge and the anaerobic activated sludge are both taken from a residual activated sludge return pipe of a municipal sewage treatment plant, and the residual activated sludge is subjected to aeration treatment to obtain the aerobic activated sludge.
The invention adopts an integrated process, integrates sulfate reduction reaction, heterotrophic denitrification reaction, organic carbon degradation reaction, mixotrophic desulfurization denitrification reaction, autotrophic desulfurization denitrification reaction and aerobic ammoxidation reaction, and realizes NH through the synergistic effect of the reactions 4 + 、NO 2 - And high-efficiency removal of high-concentration organic matters. Through the end-to-end connection of reaction zones in the system and the directional domestication of activated sludge, a reaction system is established, wherein an oxygenation zone is beneficial to ammonia oxidizing bacteria, a front anaerobic zone is beneficial to sulfate reducing bacteria and organic carbon degrading bacteria, and a rear anaerobic zone is beneficial to the growth of desulfurization denitrifying bacteria. In the oxygen charging zone, NH is controlled at 3-5mg/L due to the dissolved oxygen DO 4 + Is incompletely oxidized to NO 2 - See formula (1); meanwhile, part of the organic matter is oxidized, and the reaction is shown in formula (2). In the anaerobic reaction zone I (10), the organic matter concentration in the incoming water is high, and the seawater contains a large amount of SO 4 2- ，SO 4 2- Is reduced to S 2- See formula (3); at the same time, a large amount of NO is generated in the oxygen charging zone (8) 2 - After entering a subsequent anaerobic area, the wastewater is reduced into N under the action of heterotrophic denitrifying bacteria 2 The reaction is shown in formula (4). In the anaerobic reaction zone II (11), the front incoming water contains a large amount of S 2- 、NO 2 - And a small amount of organic carbon, which is beneficial to the generation of the mixotrophic desulfurization denitrification reaction, see formula (5), formula (6) and formula (7); meanwhile, a large amount of SO still exists in the incoming water 4 2- And the remaining organic carbon, in which the reactions of the formulae (3) and (4) also occur. In the anaerobic reaction zone III (12), due to organic mattersThe reaction of the substances in the front zone is basically finished, and the reaction in the zone is mainly an autotrophic desulfurization denitrification reaction, which is shown in formula (5), formula (6) and formula (7). Wherein the SO in the seawater 4 2- Firstly, electrons obtained from organic substances are converted into S 2- ，S 2- Then transfer electrons to NO 2 - Regeneration of SO 4 2- Only present as an intermediate auxiliary substance, i.e. promoting NO 2 - And degradation of organic carbon, without causing secondary pollution.
2NH 4 + +3O 2 →2H 2 O+2NO 2 - +4H + (1)
Macromolecule org-C + O 2 → small molecule org-C + CO 2 (2)
SO 4 2- +org-C→S 2- +CO 2 (3)
2NO 2 - +org-C+H 2 O→N 2 +CO 2 +2OH - (4)
3S 2- +8NO 2 - +8H + →3SO 4 2- +4N 2 +4H 2 O (5)
3S 2- +2NO 2 - +8H + →3S 0 +N 2 +4H 2 O (6)
S 0 +2NO 2 - →SO 4 2- +N 2 (7)
Compared with the prior art, the invention has the beneficial effects that:
1. the device and the treatment method can treat two kinds of wastewater of mariculture and marine product processing simultaneously, treat the wastewater by using the waste, reduce the operation cost and the occupied space, and have higher economic benefit and environmental benefit.
2. The invention can simultaneously remove NH in the wastewater 4 + 、NO 2 - And organic matter, NH 4 + And NO 2 - The removal rate of the TOC can reach 100 percent, the removal rate of the TOC can reach 98 percent, the treatment efficiency is high, and no secondary pollution is caused.
3. The inoculated activated sludge is gradually domesticated in a real seawater environment, is favorable for the rapid formation of salt-tolerant heterotrophic flora and autotrophic desulfurization denitrification flora, and can cope with salinity impact of high-salinity wastewater;
4. along the direction of wastewater flow, the length of the anaerobic reaction zone is far greater than that of the oxygen charging zone, so that suspended activated sludge in the aerobic zone can be subjected to free precipitation after entering a subsequent zone, and the whole reaction system does not need to be provided with a sludge precipitation device independently.
Drawings
FIG. 1 is a schematic view of a reaction apparatus of the present invention; a. a front view; b. cross-sectional view along AA;
in the figure, 1, a stirring paddle II, 2, a stirring paddle I, 3, a stirring paddle III, 4, a seawater area, 5, a water inlet pump, 6, a water inlet tank, 7, a water outlet, 8, an oxygen charging area, 9, a buffer transition area, 10, an anaerobic reaction area I, 11, an anaerobic reaction area II, 12, an anaerobic reaction area III, 13, a water outlet area, 14, a reflux area, 15, a water inlet, 16, a stirring machine II, 17, a stirring machine I, 18, a stirring machine III, 19, an air charging pump, 20, an air charging head, 21, an air charging pipe, 22, a coarse sand area, 23, a fine sand area, 24, a checking sampling port III, 25, a checking sampling port VI, 26, a checking sampling port nine, 27, a checking sampling port II, 28, a checking sampling port V, 29, a checking sampling port eight, 30, a checking sampling port I, 31, a checking sampling port IV, 32, a checking sampling port VII, 33, a water outlet checking port I, 34, a water outlet checking port II, 35. a sludge inlet pump, 36 sludge storage tank, 37 shell.
Different stages of the reactor operation NO in the embodiment of FIG. 2 2 - And TOC removal rate;
FIG. 3 depicts the heat map of the genus of the top 30 relative abundances in the three anaerobic reaction zones of the reactor in the example.
Detailed Description
The invention is further illustrated but is not in any way limited by the following specific examples. In the present embodiment, the terms of orientation such as "front", "rear", "high", and "low" used in the case where no description is made on the contrary are defined with reference to the drawings of the corresponding drawings.
The following non-limiting examples are presented to enable those of ordinary skill in the art to more fully understand the present invention and are not intended to limit the invention in any way.
An integrated biological treatment device for high-salinity high-nitrogen wastewater comprises a device shell 37; the shell 37 is internally provided with an oxygen charging zone 8, a buffer transition zone 9, an anaerobic reaction zone I10, an anaerobic reaction zone II 11, an anaerobic reaction zone III 12, a water outlet zone 13 and a reflux zone 14 at intervals in turn by vertical baffles, so that the functional action of the system is partitioned and the reaction contact time is maintained; the oxygenation zone 8, the buffer transition zone 9, the anaerobic reaction zone I10, the anaerobic reaction zone II 11, the anaerobic reaction zone III 12 and the water outlet zone 13 are parallel to each other, and the reflux zone 14 is vertical to each zone;
along the water flow direction, the front end and the rear end of the oxygenation zone 8 are respectively communicated with the reflux zone 14 and the buffer transition zone 9, the anaerobic reaction zone I10, the anaerobic reaction zone II 11, the anaerobic reaction zone III 12 and the water outlet zone 13 are sequentially connected in an initial position; the tail end of the water outlet area 13 is communicated with the reflux area 14 without baffle isolation, one end of the reflux area 14 is communicated with the oxygen charging area 8, and the other end is communicated with the water outlet area 13, so that all areas are connected end to form communicated circulation; the width of each area is the same; the bottoms of the anaerobic reaction zone I10, the anaerobic reaction zone II 11 and the anaerobic reaction zone III 12 are a fine sand zone 23, a coarse sand zone 22 and a seawater zone 4 in sequence from low to high; the vertical heights of the fine sand area 23, the coarse sand area 22 and the seawater area 4 account for 20 percent, 20 percent and 60 percent of the total height of the reaction system in sequence; the equivalent diameter of the fine sand in the fine sand area 23 is 0.5mm, and the equivalent diameter of the coarse sand in the coarse sand area 22 is 3 mm;
the water outlet area is provided with a stirring paddle I2, the reflux area is provided with a stirring paddle II 1, the communication part of the oxygenation area and the buffer transition area is provided with a stirring paddle III 3, and the stirring paddle I2, the stirring paddle II 1 and the stirring paddle III 3 are respectively connected with a stirrer I17, a stirrer II 16 and a stirrer III 18; the height of the stirring paddle II 1 accounts for 50% of the total height of the reaction system; the heights of the stirring paddles I2 and III 3 are consistent, and the stirring paddles are 20cm above the top limit of the coarse sand area 22;
the bottom of the oxygen charging area 8 is provided with an air charging pipe 21 and an air charging head 20;
the upper part of the shell 37 is provided with a water outlet 7, the lower part of the shell 37 is provided with a water inlet 15, and the water outlet 7 and the water inlet 15 are both communicated with the return area 14; the device also comprises a sludge storage tank 36 and a water inlet tank 6, wherein the sludge storage tank 36 is communicated with the water inlet 15 through a sludge inlet pump 35, and the water inlet tank 6 is communicated with the water inlet 15 through a water inlet pump 5.
A first inspection sampling port 30, a second inspection sampling port 27 and a third inspection sampling port 24 are sequentially arranged on one side, corresponding to the anaerobic reaction zone I10, of the shell 37 from low to high; a fourth inspection sampling port 31, a fifth inspection sampling port 28 and a sixth inspection sampling port 25 are sequentially arranged on one side, corresponding to the anaerobic reaction zone II 11, of the shell 37 from low to high; a seventh inspection sampling port 32, an eighth inspection sampling port 29 and a ninth inspection sampling port 26 are sequentially arranged on one side of the shell 37, which corresponds to the anaerobic reaction zone III 12, from low to high; the vertical heights from the centers of the inspection sampling port III 24, the inspection sampling port VI 25 and the inspection sampling port ninth 26 to the top of the seawater area 4 are all 5 cm; the vertical heights between the centers of the second inspection sampling port 27, the fifth inspection sampling port 28 and the eighth inspection sampling port 29 and the top of the coarse sand area 22 are all 5 cm; the vertical heights from the centers of the first inspection sampling port 30, the fourth inspection sampling port 31 and the seventh inspection sampling port 32 to the top of the fine sand area 23 are all 5 cm.
A first water outlet inspection port 33 and a second water outlet inspection port 34 are respectively arranged on one side of the shell 37 corresponding to the water outlet area 13, and the vertical heights of the centers of the first water outlet inspection port 33 and the second water outlet inspection port 34 from the bottom are both 3 cm;
the diameters of the 9 inspection sampling ports and the 2 water outlet inspection ports are all 1.5 cm.
The invention relates to a method for biologically treating high-salinity high-nitrogen wastewater based on sulfur circulation, which comprises the following three steps:
step one, an activated sludge acclimation stage; step two, a reactor starting stage; step three, the reactor operation stage;
step one, filling fine sand and coarse sand at the bottom of an anaerobic reaction zone in sequence, inoculating aerobic activated sludge to an oxygenation zone 8, and inoculating anaerobic activated sludge to an anaerobic reaction zone I10, an anaerobic reaction zone II 11 and an anaerobic reaction zone III 12;
active sludge in each reaction area in the system adopts a separate domestication mode, the quality of inlet water is different, and a water inlet pump 5 is utilized to lead the active sludge to contain NH 4 + And macromoleculesThe seawater wastewater of organic matters is pumped from the water inlet at the bottom of the reactor, the wastewater enters the aeration zone 8 and is fully contacted with the aerobic activated sludge under the action of aeration and stirring of the aeration head 20, and NH is generated 4 + Is oxidized to NO 2 - The macromolecular organic matter is oxidized into micromolecular organic matter and CO 2 ，NO 2 - And part of organic matters enter the buffer transition zone 9 along with the water flow and flow through other subsequent zones; the seawater organic wastewater and the SO in the water are introduced into the anaerobic reaction zone I10 through a first inspection sampling port 30 4 2- Fully contacts with organic matters and anaerobic activated sludge, and is respectively converted into S under the action of sulfate reduction reaction 2- And CO 2 Enters a subsequent reaction area along with the water flow; the anaerobic reaction zone II 11 is introduced with the S-containing liquid through an inspection sampling port four 31 2- And NO 2 - With SO in the front zone effluent 4 2- 、S 2- 、NO 2 - Is mixed with a small amount of organic matters and fully contacts with anaerobic activated sludge, and S is subjected to sulfate reduction reaction and mixotrophic desulfurization denitrification reaction 2- 、NO 2 - 、SO 4 2- And a small amount of organic matter is converted into S 0 (SO 4 2- )、N 2 、S 2- And CO 2 Enters a subsequent reaction area along with the water flow; the anaerobic reaction zone III 12 is introduced with the liquid containing S through an inspection sampling port seven 32 2- And NO 2 - Of seawater and S in the front zone incoming water 2- And NO 2 - Are converged and fully contacted with anaerobic activated sludge and are respectively converted into S under the action of autotrophic desulfurization denitrification reaction 0 (SO 4 2- ) And N 2 The effluent is finally discharged from the first effluent inspection port 33 and the second effluent inspection port 34;
adopting an intermittent water inlet mode, feeding water for 1 time every 24-48h, gradually reducing the water inlet interval, and after water is fed for each time, the liquid level of each reaction zone should exceed the upper limit of the coarse sand zone 22 by 30 cm; adopting NaHCO as feed water 3 Controlling the pH value to be more than 7.5; the paddles do not operate at this stage;
NH in the water inlet of the oxygenation zone 8 4 + In the concentration ofN is 200mgN/L, and the concentration of organic matters is 300mgC/L in terms of C; SO in the influent of anaerobic reaction zone I10 4 2- The concentration is 900mgS/L in terms of S, and the concentration of organic matters is 1000mgC/L in terms of C; anaerobic reaction zone II 11 influent S 2- The concentration is 300mgS/L in terms of S, NO 2 - The concentration is 200mgN/L in terms of N; anaerobic reaction zone III 12 influent S 2- The concentration is 100mgS/L in terms of S, NO 2 - The concentration is 100mgN/L calculated by N;
when NH in the oxygen charging zone 8 4 + Removal Rate, S in anaerobic reaction zone II 11 and anaerobic reaction zone III 12 2- And NO 2 - The removal rate is kept above 90 percent, and SO in the anaerobic reaction zone I10 4 2- When the removal rate reaches more than 50%, successfully domesticating the activated sludge;
step two, adopting an operation mode of intermittent water inlet and no water outlet at the initial stage of system starting, gradually reducing the water inlet interval by feeding water for 1 time every 12-24h, wherein the water inlet volume accounts for 10% of the total effective volume of the reaction system each time, gradually increasing the water inlet amount to slowly improve the water inlet load until the reaction system is filled, and then discharging water through a first water outlet inspection port 33, a second water outlet inspection port 34 and a water outlet 7 to maintain the water surface height of the reaction system unchanged;
the seawater organic wastewater in the water inlet tank 6 enters an oxygenation area 8 from a water inlet at the bottom of the reaction system through a water inlet pump 5, and NH in the inlet water 4 + Fully contacts with the aerobic activated sludge under the action of aeration and stirring of the aeration head 20 to form NH 4 + Is oxidized to NO 2 - The macromolecular organic matter is oxidized into micromolecular organic matter and CO 2 ，NO 2 - And the residual organic matters enter the buffer transition area 9 along with the water flow, and SO in the seawater 4 2- No significant reaction occurs in this region; a portion of the suspended sludge in the oxygenation zone 8 will follow the water flow into the buffer transition zone 9 where there is no oxygenation equipment and the DO in the water is depleted; NO 2 - 、SO 4 2- And the residual organic matters enter an anaerobic reaction zone I10 along with water flow, and SO in the water 4 2- Fully contacts with organic matters and anaerobic activated sludgeAre converted into S under the action of sulfate reduction reaction 2- And CO 2 Enters a subsequent anaerobic reaction zone II 11 along with the water flow; in the anaerobic reaction zone II 11, SO contained in water 4 2- 、S 2- 、NO 2 - Sufficiently contacting with a small amount of organic matters and anaerobic activated sludge to obtain SO 4 2- Is converted into S under the action of sulfate reducing bacteria 2- And CO 2 ，S 2- And NO 2 - Are respectively converted into S under the action of mixotrophic desulfurization denitrification reaction 0 (SO 4 2- ) And N 2 Enters an anaerobic reaction zone III 12 along with the water flow; in the anaerobic reaction zone III 12, the residual S in the water 2- And NO 2 - Fully contacts with anaerobic activated sludge and is respectively converted into S under the action of autotrophic desulfurization denitrification reaction 0 (SO 4 2- ) And N 2 ；
Adopting NaHCO as feed water 3 Controlling the pH value to be more than 7.5; the rotating speed of the stirring paddle II 1 is 60-500rpm/min, and the regulation and control are carried out according to the removal rate of the effluent pollutants; the rotating speeds of the stirring paddle I2 and the stirring paddle III 3 are 30 rpm/min;
NH in the feed water 4 + The concentration was 400mgN/L in terms of N, TOC was 1000mgC/L in terms of C, and SO 4 2- The concentration was 900mgS/L in terms of S.
When NO is present 2 - When the TOC removal rate and the TOC removal rate are both kept above 90%, the system is started successfully.
Step three, adopting a continuous flow water inlet mode to operate, and continuously improving the load of pollutants; the HRT was gradually decreased and finally maintained at 18 h.
Adopting NaHCO as feed water 3 Controlling the pH value to be more than 7.5; the rotating speed of the stirring paddle II 1 is 60-500 rpm/min; the rotating speeds of the stirring paddle I2 and the stirring paddle III 3 are 30 rpm/min;
NH in the feed water 4 + The concentration was 400mgN/L in terms of N, TOC was 1000mgC/L in terms of C, and SO 4 2- The concentration was 900mgS/L in terms of S.
In the three steps, the DO value in the oxygenation zone 8 is controlled at 5 mg/L; the buffer transition zone 9 is used for consuming dissolved oxygen in water, and the DO value at the tail end of the zone is less than or equal to 2 mg/L; the temperature of all the areas is more than or equal to 15 ℃; because the activated sludge in the oxygenation zone 8 is suspended sludge, a small amount of sludge enters a subsequent zone along with water flow, aerobic activated sludge in the sludge storage tank 36 is supplemented to the oxygenation zone 8 for 1 time by the sludge inlet pump 35 every 4 hours, and the volume of supplemented sludge accounts for 15 percent of the total volume of the bottom layer sludge of the oxygenation zone 8 every time;
aerobic activated sludge and anaerobic activated sludge used in the embodiment are both taken from a residual activated sludge return pipe of a municipal sewage treatment plant, and the residual activated sludge is aerated to be aerobic activated sludge;
NH in the present embodiment for the operating phase of the reactor 4 + The TOC removal effect and the TOC removal effect were monitored separately and the results are shown in fig. 2. NH (NH) 4 + The highest removal rate of the TOC can reach 100 percent, the highest removal rate of the TOC can reach 98 percent, and the removal effect is stable.
The activated sludge microorganism diversity of the lower, middle and upper parts of the bottom of the anaerobic reaction zone I10, the anaerobic reaction zone II 11 and the anaerobic reaction zone III 12 is detected by adopting Miseq detection technology, and the result is shown in figure 3. The dominant functional bacteria in the anaerobic reaction zone I10 are mainly Desulfobacter, Desulfuromusa, Fastidiosipila and Pseudomonas, which shows that the dominant functional bacteria mainly undergo sulfate reduction reaction, heterotrophic denitrification reaction and organic matter anaerobic degradation. The dominant functional bacteria in the anaerobic reaction zone II 11 are mainly Fusibacter, Thauera, Sulfurimonas and Desulfobacter, and the portion mainly generates mixotrophic desulfurization denitrification reaction, sulfate reduction reaction and heterotrophic denitrification reaction. The dominant functional bacteria in the anaerobic reaction zone III 12 are Paracoccus, Sulfurimonas, Defluvimonas, Hypophorbium, Rhodobacter, Thauera, Ottopia and Acidovorax, and the detected biological diversity is large, which indicates that the organic matter is fully degraded at the moment, so that the abundance of heterotrophic microorganisms is reduced, the abundance of autotrophic organisms is increased, and the autotrophic desulfurization denitrification reaction is the main reaction. Meanwhile, the types of the functional bacteria in the upper layer and the middle layer of each area are different from the types of the main functional bacteria in the lower layer, which shows that the effective separation of the functional bacteria in the system is realized in the flow direction, and the space separation effect of the functional bacteria at different heights of the same area is better, so that the foundation for ensuring the synergistic and efficient proceeding of sulfate reduction, desulfurization denitrification and heterotrophic denitrification is provided.
It will be apparent to those skilled in the art from this disclosure that many changes and modifications can be made, or equivalents modified, in the embodiments of the invention without departing from the scope of the invention. Therefore, any simple modification, equivalent change and modification made to the above embodiments according to the technical essence of the present invention shall still fall within the protection scope of the technical solution of the present invention, unless the contents of the technical solution of the present invention are departed.

Claims (9)

1. An integrated biological treatment device for high-salinity high-nitrogen wastewater is characterized by comprising a device shell (37);
an oxygenation zone (8), a buffer transition zone (9), an anaerobic reaction zone I (10), an anaerobic reaction zone II (11), an anaerobic reaction zone III (12), a water outlet zone (13) and a reflux zone (14) are sequentially arranged in the shell (37) at intervals;
along the water flow direction, the front end and the rear end of the oxygenation zone (8) are respectively communicated with the reflux zone (14) and the buffer transition zone (9), the anaerobic reaction zone I (10), the anaerobic reaction zone II (11), the anaerobic reaction zone III (12) and the water outlet zone (13) are sequentially connected end to end; the tail end of the water outlet area (13) is communicated with the reflux area (14);
the bottom of the anaerobic reaction zone I (10), the bottom of the anaerobic reaction zone II (11) and the bottom of the anaerobic reaction zone III (12) are a fine sand zone (23), a coarse sand zone (22) and a seawater zone (4) in sequence from low to high;
a water outlet (7) is arranged at the upper part of the shell (37), a water inlet (15) is arranged at the lower part of the shell (37), and the water outlet (7) and the water inlet (15) are both communicated with the reflux area (14);
a first inspection sampling port (30), a second inspection sampling port (27) and a third inspection sampling port (24) are sequentially arranged on one side, corresponding to the anaerobic reaction zone I (10), of the shell (37) from low to high;
a fourth inspection sampling port (31), a fifth inspection sampling port (28) and a sixth inspection sampling port (25) are sequentially arranged on one side, corresponding to the anaerobic reaction zone II (11), of the shell (37) from low to high;
a seventh inspection sampling port (32), an eighth inspection sampling port (29) and a ninth inspection sampling port (26) are sequentially arranged on one side, corresponding to the anaerobic reaction zone III (12), of the shell (37) from low to high;
a first water outlet inspection port (33) and a second water outlet inspection port (34) are respectively arranged on one side of the shell (37) corresponding to the water outlet area (13);
the vertical heights of the fine sand area (23), the coarse sand area (22) and the seawater area (4) account for 10-20%, 10-20% and 60-80% of the total reaction system height in sequence;
the water outlet area is provided with a stirring paddle I (2), the reflux area is provided with a stirring paddle II (1), and the communication part of the oxygenation area and the buffer transition area is provided with a stirring paddle III (3); the height of the stirring paddle II (1) accounts for 40-60% of the total reaction system height; the stirring paddles I (2) and III (3) are consistent in height and are located 20-30cm above the top limit of the coarse sand area (22).
2. The integrated biological treatment device for high-salinity high-nitrogen wastewater as recited in claim 1, characterized in that the equivalent diameter of fine sand of the fine sand area (23) is 0.1-1mm, and the equivalent diameter of coarse sand of the coarse sand area (22) is 1-3 mm; the regions are of the same width.
3. The integrated biological treatment device for the high-salinity high-nitrogen wastewater as recited in claim 1, wherein the vertical heights of the centers of the first outlet inspection port (33) and the second outlet inspection port (34) from the bottom are both 2-5 cm; the vertical heights from the centers of the third inspection sampling port (24), the sixth inspection sampling port (25) and the ninth inspection sampling port (26) to the top of the seawater area (4) are all 2-5 cm; the vertical heights of the centers of the second inspection sampling port (27), the fifth inspection sampling port (28) and the eighth inspection sampling port (29) from the top of the coarse sand area (22) are all 2-5 cm; the vertical height from the center of the first inspection sampling port (30), the fourth inspection sampling port (31) and the seventh inspection sampling port (32) to the top of the fine sand area (23) is 2-5 cm; the diameters of the inspection sampling port and the water outlet inspection port are both 1-3 cm.
4. The integrated biological treatment device for high-salinity high-nitrogen wastewater according to claim 1, characterized in that an aeration pipe (21) and an aeration head (20) are arranged at the bottom of the aeration zone (8).
5. The integrated biological treatment device for the high-salinity high-nitrogen wastewater as claimed in claim 1, further comprising a sludge storage tank (36) and a water inlet tank (6), wherein the sludge storage tank (36) is communicated with the water inlet (15) through a sludge inlet pump (35), and the water inlet tank (6) is communicated with the water inlet (15) through a water inlet pump (5).
6. A method for biological treatment of high salinity high nitrogen wastewater based on sulfur cycle, characterized in that the method uses the device of claim 1, comprising three steps:
step one, an activated sludge acclimation stage:
inoculating aerobic activated sludge into an oxygenation zone (8), and inoculating anaerobic activated sludge into an anaerobic reaction zone I (10), an anaerobic reaction zone II (11) and an anaerobic reaction zone III (12);
will contain NH 4 + High-salinity wastewater with macromolecular organic matters enters from a water inlet (15), the wastewater enters an aeration zone (8) and is fully contacted with aerobic activated sludge under the action of aeration and stirring of an aeration head (20), and NH is generated 4 + Is oxidized to NO 2 - The macromolecular organic matter is oxidized into micromolecular organic matter and CO 2 ，NO 2 - And part of organic matters enter a buffer transition area (9) along with the water flow and flow through other subsequent areas;
introducing seawater organic wastewater and SO in the water into an anaerobic reaction zone I (10) through a first inspection sampling port (30) 4 2- Fully contact with organic matter and anaerobic activated sludge, in sulfate reduction reactionAre respectively converted into S under the action of 2- And CO 2 Enters a subsequent reaction area along with the water flow;
the anaerobic reaction zone II (11) is introduced with the S-containing gas through the inspection sampling port four (31) 2- And NO 2 - With SO in the front zone effluent 4 2- 、S 2- 、NO 2 - Is mixed with a small amount of organic matters and fully contacts with anaerobic activated sludge, and S is subjected to sulfate reduction reaction and mixotrophic desulfurization denitrification reaction 2- Is converted into S 0 And SO 4 2- ，NO 2 - 、SO 4 2- And a small amount of organic matter is converted into N 2 、S 2- And CO 2 Enters a subsequent reaction area along with the water flow;
introducing S-containing gas into the anaerobic reaction zone III (12) through a check sampling port seven (32) 2- And NO 2 - Of seawater and S in the front zone incoming water 2- And NO 2 - Converging, fully contacting with anaerobic activated sludge, and performing autotrophic desulfurization and denitrification reaction on the sludge 2- Is converted into S 0 And SO 4 2- ，NO 2 - Is converted into N 2 The effluent is finally discharged from the first effluent inspection port (33) and the second effluent inspection port (34);
adopting an intermittent water feeding mode, feeding water for 1 time every 24-48h, wherein the liquid level of each reaction zone is 20-30cm higher than the upper limit of the coarse sand zone (22) after water feeding each time; controlling the pH value of the inlet water to be more than 7.5; three paddles do not operate at this stage;
NH in the water entering the oxygen charging zone (8) 4 + The concentration is 100-200mgN/L in terms of N, and the concentration of the organic matter is 250-300mgC/L in terms of C; SO in the influent of anaerobic reaction zone I (10) 4 2- The concentration is 850-950mgS/L in terms of S, and the concentration of the organic matter is 600-1000mgC/L in terms of C; anaerobic reaction zone II (11) is fed with water S 2- The concentration is 200-300mgS/L in terms of S, NO 2 - The concentration is 100-200mgN/L in terms of N; anaerobic reaction zone III (12) inlet water S 2- The concentration is 50-100mgS/L calculated by S, NO 2 - The concentration is calculated by NIs 50-100 mgN/L;
when the oxygen charging zone (8) is NH 4 + Removal rate, S in anaerobic reaction zone II (11) and anaerobic reaction zone III (12) 2- And NO 2 - The removal rate is kept above 90 percent, and SO is in an anaerobic reaction zone I (10) 4 2- When the removal rate reaches more than 50%, successfully domesticating the activated sludge;
step two, a reactor starting stage:
adopting an operation mode of intermittent water inlet and no water outlet, feeding water for 1 time every 12-24h, wherein the water inlet volume accounts for 5% -20% of the total effective volume of the reaction system each time, gradually increasing the water inlet amount to slowly improve the water inlet load, and discharging water through a first water outlet inspection port (33), a second water outlet inspection port (34) and a water outlet (7) to keep the water surface height of the reaction system unchanged after the reaction system is filled;
high-salt organic wastewater enters an oxygenation area (8) through a water inlet (15), and NH in the inlet water 4 + Fully contacts with the aerobic activated sludge under the action of aeration and agitation of the aeration head (20) to form NH 4 + Is oxidized to NO 2 - The macromolecular organic matter is oxidized into micromolecular organic matter and CO 2 ，NO 2 - And the residual organic matters enter a buffer transition area (9) along with the water flow, and SO in the seawater 4 2- No reaction occurs in this region; a part of suspended sludge in the oxygenation zone (8) enters a buffer transition zone (9) along with water flow, and DO in the water is consumed in the zone; NO 2 - 、SO 4 2- And the residual organic matter enters an anaerobic reaction zone I (10) along with water flow, and SO in the water 4 2- Fully contacts with organic matters and anaerobic activated sludge, and is respectively converted into S under the action of sulfate reduction reaction 2- And CO 2 Enters a subsequent anaerobic reaction zone II (11) along with the water flow; in the anaerobic reaction zone II (11), SO contained in the water 4 2- 、S 2- 、NO 2 - Fully contacts with a small amount of organic matters and anaerobic activated sludge, and S is generated under the action of sulfate reduction reaction and mixotrophic desulfurization denitrification reaction 2- Is turned toIs formed as S 0 And SO 4 2- ，SO 4 2- 、NO 2 - And a small amount of organic matter is converted into S 2- 、N 2 And CO 2 Enters an anaerobic reaction zone III (12) along with the water flow; in the anaerobic reaction zone III (12), the residual S in the water 2- And NO 2 - Fully contacts with anaerobic activated sludge, and S is generated under the action of autotrophic desulfurization denitrification reaction 2- Is converted into S 0 And SO 4 2- ，NO 2 - Is converted into N 2 ；
Controlling the pH value of the inlet water to be more than 7.5; the rotating speed of the stirring paddle II (1) is 60-500 rpm/min; the rotating speeds of the stirring paddle I (2) and the stirring paddle III (3) are 30-100 rpm/min;
NH in the feed water 4 + Concentration is 100-400mgN/L in terms of N, TOC is 300-1000mgC/L in terms of C, SO 4 2- The concentration is 500-950mgS/L in terms of S;
when NO is present 2 - When the TOC removal rate and the TOC removal rate are both kept above 90%, the system is started successfully;
step three, the reactor operation stage:
the operation is carried out by adopting a continuous flow water inlet mode, and the hydraulic retention time HRT is 12-48 h;
controlling the pH value of the inlet water to be more than 7.5; the rotating speed of the stirring paddle II (1) is 60-500 rpm/min; the rotating speeds of the stirring paddle I (2) and the stirring paddle III (3) are 30-100 rpm/min;
NH in the feed water 4 + Concentration is 100-400mgN/L in terms of N, TOC is 300-1000mgC/L in terms of C, SO 4 2- The concentration is 500-950mgS/L in terms of S.
7. The method for biological treatment of high-salinity high-nitrogen wastewater based on sulfur cycle as claimed in claim 6, characterized in that DO value in the oxygenation zone is controlled at 3-5 mg/L; the dissolved oxygen in the water is consumed by the buffer transition zone (9), and the DO value at the tail end of the buffer transition zone (9) is less than or equal to 1-2 mg/L.
8. The high-salinity high-nitrogen wastewater organism based on the sulfur cycle as claimed in claim 6The treatment method is characterized in that the pH value of the feed water is NaHCO 3 Adjusting; the temperature of each area is more than or equal to 15 ℃; aerobic activated sludge is supplemented to the oxygenation zone (8) for 1 time every 1-6 hours, and the volume of the supplemented sludge accounts for 10-50% of the total volume of the bottom layer sludge of the oxygenation zone (8).
9. The method for biologically treating high-salt high-nitrogen wastewater based on sulfur cycle as claimed in claim 6, wherein the aerobic activated sludge and the anaerobic activated sludge are both taken from a residual activated sludge return pipe of a municipal sewage treatment plant, and the residual activated sludge is aerated to be aerobic activated sludge.
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