CN113087298B

CN113087298B - Device and method for treating organic wastewater based on advanced oxidation and EGSB

Info

Publication number: CN113087298B
Application number: CN202110375721.0A
Authority: CN
Inventors: 江进; 沈桐; 胡颖斌; 李宁; 郭钦; 许燕滨
Original assignee: Guangdong University of Technology
Current assignee: Guangdong University of Technology
Priority date: 2021-04-08
Filing date: 2021-04-08
Publication date: 2022-08-12
Anticipated expiration: 2041-04-08
Also published as: CN113087298A

Abstract

The invention discloses a device and a method for treating organic wastewater based on advanced oxidation and EGSB. The device comprises an SBR reaction system and an EGSB reaction system; the SBR reaction system comprises a water inlet tank, an SBR reactor, an SBR constant temperature system, an aeration system and a stirrer; the EGSB reaction system comprises an EGSB reactor, a carbon source water inlet tank and an EGSB constant temperature system. The method for treating the nitrobenzene-containing wastewater by using the device comprises the following steps: s1, reacting wastewater in an SBR reactor filled with desulfurized ash by utilizing advanced oxidation, and discharging supernatant liquid to a temporary storage tank; and S2, reacting the supernatant liquid and a carbon source in an EGSB reactor containing denitrification coupling anaerobic ammonia oxidation granular sludge, discharging the treated wastewater through a second water outlet through a three-phase separator, and discharging waste gas through a gas outlet. The high-efficiency treatment of wastewater containing nitrobenzene is obtained by combining an SBR reaction system and an EGSB reaction system and combining an advanced oxidation method and a biological anaerobic treatment method.

Description

Device and method for treating organic wastewater based on advanced oxidation and EGSB

Technical Field

The invention relates to the technical field of organic wastewater treatment, in particular to a device and a method for treating organic wastewater based on advanced oxidation and EGSB.

Background

At present, most of power plants in China generate power through thermal power, discharged flue gas often contains pollutant sulfur dioxide, and the power plants usually adopt a limestone dry desulphurization process, so that a large amount of desulfurized ash, namely a mixture which takes calcium sulfite and calcium sulfate as main components and carries a small amount of heavy metals, is generated. The conventional treatment method of the desulfurization ash is to prepare additives of building materials, roadbed materials and concrete or directly fill the additive, but the physical and chemical properties of the desulfurization ash components are not effectively utilized in the treatment mode, and the resource utilization advantage is not exerted.

In organic wastewater, wastewater containing nitrobenzene compounds is a technical problem since the wastewater is high in toxicity and difficult to biodegrade, and nitrobenzene compounds cannot be efficiently degraded by traditional organic matter removal methods such as a physical adsorption method, a filtration method, a biological method and the like. The advanced oxidation technology is characterized in that hydroxyl free radicals (OH) with strong oxidation capacity are generated, and under the reaction conditions of high temperature, high pressure, electricity, sound, light irradiation, catalysts and the like, macromolecular refractory organic matters are oxidized into low-toxicity or non-toxic micromolecular substances. Today, advanced oxidation technology is more widely used in the field of wastewater treatment.

For example, the chinese patent application CN104724852A reports a method for the blow-off oxidative degradation of high-concentration nitrobenzene-containing wastewater, wherein the high-concentration nitrobenzene-containing wastewater and fresh air complete the blow-off mass transfer process in a supergravity device; then the wastewater is sent into a liquid storage tank to be mixed with hydrogen peroxide, and then the wastewater is in contact reaction with ozone gas in a hypergravity device, and the residual organic matters in the wastewater are treated by ozone and H ₂ O ₂ Degrading under the synergistic action. The method degrades nitrobenzene compounds in wastewater by hydroxyl radicals.

However, for nitrobenzene compounds, hydroxyl radicals are more prone to hydrogen extraction and addition, and do not have oxidation and degradation advantages on aromatic pollutants containing benzene rings, so that the treatment efficiency of organic wastewater is poor.

Therefore, it is required to develop a device and a method for treating nitrobenzene organic wastewater with high treatment efficiency and good effect.

Disclosure of Invention

In order to overcome the defect of poor organic wastewater treatment efficiency in the prior art, the invention provides the device for treating the organic wastewater based on advanced oxidation and EGSB, and the high-efficiency treatment effect on the wastewater containing nitrobenzene is obtained by combining the SBR reaction system and the EGSB reaction system and combining the advanced oxidation method and the biological anaerobic treatment method.

Another object of the present invention is to provide a method for treating organic wastewater using the above apparatus.

In order to solve the technical problems, the invention adopts the technical scheme that:

an apparatus for treating organic wastewater based on advanced oxidation and EGSB, comprising: an SBR reaction system, an EGSB reaction system and a temporary storage tank;

the SBR reaction system comprises a water inlet tank, an SBR reactor, an SBR constant temperature system, an aeration system and a stirrer;

the SBR reactor is provided with a first water inlet, a first water outlet and a feed inlet, a water inlet tank is communicated with the first water inlet, and the first water outlet is communicated with a temporary storage tank;

the SBR constant temperature system is arranged around the periphery of the shell of the SBR reactor;

the aeration system comprises an aeration blower and an aeration disc, the aeration blower is arranged outside the SBR reactor, the aeration disc is arranged at the bottom in the SBR reactor, and the aeration disc is connected with the aeration blower through an aeration pipe;

the stirrer is fixed inside the SBR reactor;

the EGSB reaction system comprises a carbon source water inlet tank, an EGSB reactor and an EGSB constant temperature system;

a muddy water reaction chamber positioned at the bottom and a three-phase separator positioned at the top are arranged in the EGSB reactor;

the EGSB reactor is provided with a second water inlet, an EGSB sampling port, a second water outlet, a gas outlet and a reflux pump outlet; the second water inlet is arranged at the bottom of the EGSB reactor and is communicated with the temporary storage tank and the carbon source water inlet tank; the second water outlet is arranged at the top of the EGSB reactor; the outlet of the backflow pump is communicated with the second water inlet through the backflow pump;

the EGSB constant temperature system is arranged around the periphery of the shell of the EGSB reactor.

The invention combines the SBR reaction system and the EGSB reaction system, and combines the advanced oxidation method and the biological anaerobic treatment method to obtain the high-efficiency treatment effect on the wastewater containing nitrobenzene.

In the SBR reaction system, the wastewater containing nitrobenzene is treated by using desulfurized ash, and biologically resistant aromatic organic compounds are efficiently oxidized by sulfate radicals generated by the desulfurized ash, so that the biodegradability of the wastewater is improved. The byproducts generated in the process of treating nitrobenzene wastewater by desulfurized fly ash are introduced into an EGSB reaction system, and the denitrification is coupled with the anaerobic ammonia oxidation reaction process, so that the organic wastewater which is difficult to be biochemically degraded reaches the standard and is discharged, and the final discharge of the treated wastewater meets the allowable discharge concentration of the pollutant discharge standard of urban sewage treatment plants.

Meanwhile, in the advanced oxidation process, easily degradable organic matters, carbon dioxide and nitrate nitrogen are generated in the reaction process of sulfate radicals and nitrobenzene, so that the input amount of an additional carbon source is reduced compared with that of the traditional denitrification reactor, the operation cost is greatly reduced, and the desulfurized ash is effectively recycled.

Preferably, the SBR constant temperature system and the EGSB constant temperature system are both constant temperature jacket circulating water systems.

Preferably, the constant-temperature jacket circulating water system comprises a constant-temperature water bath tank, a circulating infusion part and a constant-temperature jacket, wherein the constant-temperature jacket is provided with a constant-temperature water inlet and a constant-temperature water outlet; the circulating transfusion component is connected with the constant-temperature water bath box, and the circulating transfusion component is communicated with the constant-temperature water inlet and the constant-temperature water outlet to form a circulating loop.

By carrying out constant temperature control on the SBR reactor and the EGSB reactor, the generation efficiency of sulfite radicals and the subsequent biological denitrification effluent effect are better.

Preferably, the constant temperature water inlet is arranged at the lower part of the constant temperature jacket, and the constant temperature water outlet is arranged at the upper part of the constant temperature jacket.

Preferably, the circulating transfusion part is a circulating pump.

Preferably, the aeration disc is provided with at least three aeration outlets.

Preferably, the side wall of the SBR reactor is also provided with an SBR sampling port.

The SBR sampling port can sample the reaction liquid in the SBR reactor more quickly and conveniently so as to detect the nitrate nitrogen concentration and the pH value of the reaction liquid.

Preferably, the EGSB reaction system is further provided with a gas flow meter connected with the gas outlet.

Preferably, the EGSB sampling ports are at least two.

More preferably, the EGSB sampling port is provided in the side wall and/or the top of the EGSB reactor.

The invention also discloses a method for treating organic wastewater by using the device, which comprises the following steps:

s1, introducing the wastewater into an SBR reactor filled with desulfurized ash and manganese sand from a first water inlet, adjusting the pH value to 2-4, starting aeration, and reacting for 5-7 hours at a constant temperature of 50-60 ℃ under stirring conditions to obtain a reaction solution; adding zero-valent iron powder into the reaction liquid under an anoxic condition, adjusting the pH to 7-8, standing, and discharging the upper layer liquid to a temporary storage tank;

s2, introducing the supernatant and a carbon source in the S1 into an EGSB reactor containing denitrification coupling anaerobic ammonia oxidation granular sludge from a second water inlet to obtain a mixed liquid, adjusting the pH value of the mixed liquid in the EGSB reactor to be 7-8, reacting at a constant temperature of 30-40 ℃ at a reflux ratio of 2-8 in the EGSB reactor, allowing hydraulic retention time to be 10-12 h, discharging the treated wastewater through a second water outlet through a three-phase separator, and discharging waste gas through a gas outlet.

In the SBR reactor, desulfurized ash mainly containing calcium sulfite reacts with manganese sand (manganese dioxide) to generate sulfite radicals, and then the sulfite radicals are oxidized into sulfate radicals by oxygen under the aeration condition, so that nitrobenzene compounds in the wastewater are efficiently oxidized. In the process, the nitrobenzene compounds are degraded to produce a large amount of nitrate nitrogen and a very small amount of nitrophenol by-products, and simultaneously, a small amount of heavy metals of chromium, nickel and iron can be dissolved out from the desulfurized fly ash.

Therefore, after the reaction of S1, zero-valent iron powder is added for treatment, and heavy metals are generated by ferrous ions or ferric ions through the zero-valent iron, and the ferrous ions and the ferric ions have good adsorption and flocculation properties and can synergistically precipitate the heavy metals dissolved out from the desulfurized fly ash; under the anoxic condition, part of nitrate nitrogen is reduced into ammonia nitrogen and a small amount of nitrite nitrogen, and supernatant containing the nitrate nitrogen, the ammonia nitrogen, the small amount of nitrite nitrogen and easily degradable organic matters is obtained. And due to the generation of ammonia nitrogen, a small amount of carbon source required by the short-cut denitrification coupling anaerobic ammonia oxidation is provided, and the adding cost of the subsequent carbon source is reduced.

And (3) after the supernatant is introduced into the EGSB reactor, denitrifying bacteria perform short-range denitrification under the action of a carbon source and denitrification coupling anaerobic ammonium oxidation granular sludge, nitrate nitrogen is converted into nitrite nitrogen, the anaerobic ammonium oxidation flora utilizes ammonia nitrogen as an electron donor and nitrite nitrogen as an electron acceptor to perform biological denitrification, and finally the wastewater is subjected to high-efficiency treatment and then is discharged after reaching the standard.

Meanwhile, more oxygen is consumed in the process of generating sulfate radicals by the reaction of calcium sulfite in the SBR reactor, and the concentration of dissolved oxygen in water is in a lower range, so that the continuous operation of the EGSB reactor is facilitated.

Controlling the temperature of the EGSB reactor to be 30-40 ℃ to provide a growth condition for a bacterial community; the reaction speed and degree of the calcium sulfite and the manganese sand in the desulfurized fly ash can be increased by controlling the temperature of the SBR reactor to be 50-60 ℃, and the maintained energy consumption is low.

The inventor detects that the effluent of the second water outlet meets the indexes of pollutant emission standard of urban sewage treatment plant (GB18918-2002), wherein the total nitro compounds and the total nickel meet the highest allowable emission concentration of a selection control project, the total chromium meets the highest allowable emission concentration of a class of pollutants, and the ammonia nitrogen and the total nitrogen meet the highest allowable emission concentration of a first-level A standard.

Preferably, the carbon source is a sodium acetate solution and/or a sodium bicarbonate solution.

Preferably, step S1 is repeated at least 3 times.

The repeated process of step S1 can degrade nitrobenzene in the wastewater as much as possible, which is beneficial to more efficient and thorough treatment of the wastewater.

More preferably, step S1 is repeated until the nitrobenzene concentration in the supernatant is less than or equal to 2 mg/L.

Preferably, the mass ratio of the desulfurized ash to the manganese sand in S1 is (9-11): 1.

Preferably, the molar ratio of carbon to nitrogen in the mixed liquid in the step S2 is (1-3): 1.

Compared with the prior art, the invention has the beneficial effects that:

the invention develops a device for treating organic wastewater based on advanced oxidation and EGSB and a method for treating organic wastewater by using the device. By combining the SBR reaction system and the EGSB reaction system and combining the advanced oxidation method and the biological anaerobic treatment method, the high-efficiency treatment effect on the wastewater containing nitrobenzene is obtained. In an SBR reaction system, sulfate radicals generated by desulfurized ash are utilized to efficiently oxidize aromatic organic compounds with biological resistance, so that the biodegradability of wastewater is improved; the byproduct generated in the process of treating nitrobenzene wastewater by using desulfurized fly ash is introduced into an EGSB reaction system, and the denitrification is coupled with the anaerobic ammoxidation reaction process, so that nitrobenzene compounds which are difficult to biochemically degrade in the wastewater are efficiently degraded, and the wastewater is treated and then discharged after reaching the standard.

Drawings

FIG. 1 is a schematic view showing the construction of an apparatus for treating organic wastewater based on advanced oxidation and EGSB of example 1.

Detailed Description

The present invention will be further described with reference to the following embodiments.

The same or similar reference numerals in the drawings of the embodiments of the present invention correspond to the same or similar components; in the description of the present invention, it is to be understood that the terms "upper", "lower", "left", "right", "top", "bottom", "inner", "outer", and the like, if any, are used in the orientations and positional relationships indicated in the drawings only for the convenience of describing the present invention and simplifying the description, but not for indicating or implying that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and therefore the terms describing the positional relationships in the drawings are used for illustrative purposes only and are not to be construed as limiting the present patent.

Furthermore, if the terms "first," "second," and the like are used for descriptive purposes only, they are used for mainly distinguishing different devices, elements or components (the specific types and configurations may be the same or different), and they are not used for indicating or implying relative importance or quantity among the devices, elements or components, but are not to be construed as indicating or implying relative importance.

The starting materials in the examples and comparative examples are all commercially available, wherein:

desulfurized ash, which is taken from a certain thermal power plant in Guangdong;

manganese sand, alatin bio-technology corporation;

wastewater, prepared in the laboratory, nitrobenzene compounds were purchased from Guangzhou foxtail technologies, Inc.;

denitrifying coupled anaerobic ammonium oxidation granular sludge is obtained by culturing anaerobic sludge in a certain duck farm in Yunfo City.

Reagents, methods and apparatus used in the present invention are conventional in the art unless otherwise indicated.

Example 1

Example 1 provides an apparatus for treating organic wastewater based on advanced oxidation and EGSB, the structural schematic diagram is shown in fig. 1, comprising an SBR reaction system and an EGSB reaction system;

the SBR reaction system comprises a water inlet tank 1, an SBR reactor 2, an SBR constant temperature system 3, an aeration system 4 and a stirrer 5;

the SBR reactor 2 is provided with a first water inlet 21, a first water outlet 22 and a feed inlet 23, the water inlet tank 1 is communicated with the first water inlet 21, the stirrer 5 is fixed in the SBR reactor 2, and the first water outlet 22 is communicated with the temporary storage tank 6; the side wall of the SBR reactor 2 is provided with an SBR sampling port 24;

the SBR constant temperature system 3 is arranged around the periphery of the shell of the SBR reactor 2;

the aeration system 4 comprises an aeration blower 41 and an aeration disc 42, wherein the aeration disc 42 is arranged at the bottom in the SBR reactor 2, and the aeration disc 42 is provided with six aeration outlets;

the EGSB reaction system 2 comprises a carbon source water inlet tank 8, an EGSB reactor 7 and an EGSB constant temperature system 9;

the inside of the EGSB reactor 7 is provided with a muddy water reaction chamber 71 at the bottom and a three-phase separator 72 at the top;

the EGSB reactor 7 is provided with a second water inlet 73, an EGSB sampling port 74, a second water outlet 75, a gas outlet 76 and a reflux pump outlet 77; the second water inlet 73 is arranged at the bottom of the EGSB reactor 7 and is communicated with the temporary storage tank 6 and the carbon source water inlet tank 8; the second water outlet 75 is arranged at the top of the EGSB reactor 7; the return pump outlet 77 is communicated with the second water inlet 75 through the return pump 78;

the EGSB constant temperature system 9 is arranged around the periphery of the shell of the EGSB reactor 7;

seven EGSB sampling ports 74 are arranged on the side wall of the EGSB reactor 7 from bottom to top, and one EGSB sampling port is arranged on the top of the EGSB reactor 7;

the SBR constant temperature system 3 and the EGSB constant temperature system 9 are both constant temperature jacket circulating water systems, and comprise a constant temperature water bath tank 31, a circulating transfusion component 32 and a constant temperature jacket 33, wherein the constant temperature jacket 33 is provided with a constant temperature water inlet and a constant temperature water outlet; the circulating transfusion part 32) is connected with the constant temperature water bath box 31, and the circulating transfusion part 32 is communicated with the constant temperature water inlet and the constant temperature water outlet to form a circulating loop;

the constant-temperature water inlet is arranged at the lower part of the constant-temperature jacket 33, and the constant-temperature water outlet is arranged at the upper part of the constant-temperature jacket 33; the circulating transfusion part 32 is a circulating pump;

the gas flow meter 79 is connected to the gas outlet 76.

The method for treating the organic wastewater by using the device comprises the following steps:

s1, introducing 6L of wastewater containing 40mg/L nitrobenzene into an SBR reactor filled with 1000g of desulfurized ash and 100g of manganese sand from a first water inlet, adjusting the pH value to 3 by using 0.1M dilute hydrochloric acid, starting aeration, and reacting for 5 hours at the constant temperature of 55 ℃ under the stirring condition to obtain a reaction solution;

taking a small amount of reaction liquid from an SBR sampling port, detecting that the nitrogen concentration of nitrate is 30mg/L, adding about 0.3g of zero-valent iron powder into the reaction liquid under the anoxic condition to ensure that the iron concentration is 50mg/L, adjusting the pH value to be 8 by using acid-base adjusting liquid, standing, and discharging the upper layer liquid to a temporary storage tank;

repeating the steps until the nitrobenzene concentration of the upper layer liquid is less than or equal to 2 mg/L.

S2, introducing the supernatant in the temporary storage tank into an EGSB reactor containing the denitrification coupling anaerobic ammonia oxidation granular sludge from a second water inlet at the speed of 1-2L/H, simultaneously taking a small amount of supernatant to detect the nitrogen concentration and the COD concentration, and introducing a carbon source sodium bicarbonate solution stored in a carbon source water inlet tank into the EGSB reactor according to the concentration in the proportion of C/N to 2:1 to obtain a mixed solution; and (3) adjusting the pH value of the mixed liquid in the EGSB reactor to be 7.5 by using an acid-base adjusting liquid, setting the reflux ratio of the EGSB reactor to be 3, reacting at the constant temperature of 30-40 ℃, wherein the hydraulic retention time is 12h, discharging the treated wastewater through a second water outlet by using a three-phase separator, and discharging the waste gas through a gas outlet.

The treated wastewater had a nitrobenzene content of 1.7mg/L, a COD of 43mg/L and a total nitrogen of 14.3 mg/L.

Example 2

Example 2 provides an apparatus for treating organic wastewater based on advanced oxidation and EGSB, the structure of which is schematically shown in FIG. 1, and a method for treating organic wastewater using the apparatus, comprising the following steps:

s1, introducing 6L of wastewater containing 60mg/L nitrobenzene into an SBR reactor filled with 2200g of desulfurized fly ash and 200g of manganese sand from a first water inlet, adjusting the pH value to 3 by using 0.1M dilute hydrochloric acid, starting aeration, and reacting for 7 hours at the constant temperature of 55 ℃ under the stirring condition to obtain a reaction solution;

taking a small amount of reaction liquid from an SBR sampling port, detecting that the nitrogen concentration of nitrate is 50mg/L, adding about 0.5g of zero-valent iron powder into the reaction liquid under the anoxic condition to ensure that the iron concentration is 80mg/L, adjusting the pH value to be 8 by using acid-base adjusting liquid, standing, and discharging the upper layer liquid to a temporary storage tank;

S2, introducing the supernatant in the temporary storage tank into an EGSB reactor containing the denitrification coupling anaerobic ammonia oxidation granular sludge from a second water inlet at the speed of 1-2L/H, simultaneously taking a small amount of supernatant to detect the nitrogen concentration and the COD concentration, and introducing a carbon source sodium bicarbonate solution stored in a carbon source water inlet tank into the EGSB reactor according to the concentration in the proportion of C/N to 3:1 to obtain a mixed solution; and (3) adjusting the pH value of the mixed liquid in the EGSB reactor to be 7.5 by using an acid-base adjusting liquid, setting the reflux ratio of the EGSB reactor to be 6, reacting at the constant temperature of 30-40 ℃, wherein the hydraulic retention time is 10h, the treated wastewater is discharged through a second water outlet by a three-phase separator, and the waste gas is discharged through a gas outlet.

The treated wastewater had a nitrobenzene content of 1.8mg/L, a COD of 57mg/L and a total nitrogen of 14.1 mg/L.

Comparative example 1

Comparative example 1 provides a method for treating organic wastewater based on advanced oxidation using an SBR reaction system in an apparatus as shown in fig. 1, the method comprising the steps of:

introducing 6L of wastewater containing 40mg/L of nitrobenzene into an SBR reactor filled with 1000g of desulfurized ash and 100g of manganese sand from a first water inlet, adjusting the pH value to 3 by using 0.1M dilute hydrochloric acid, starting aeration, and reacting for 5 hours at the constant temperature of 55 ℃ under the stirring condition to obtain a reaction solution;

taking a small amount of reaction liquid from an SBR sampling port, detecting that the nitrogen concentration of nitrate is 30mg/L, adding about 0.3g of zero-valent iron powder into the reaction liquid under the anoxic condition to ensure that the iron concentration is 50mg/L, adjusting the pH value to be 8 by using an acid-base adjusting liquid, standing, and discharging supernatant liquid to obtain the treated wastewater.

Through detection, the nitrobenzene content in the treated wastewater is 1.7mg/L, and the total nitrogen is 28 mg/L.

Comparative example 2

Comparative example 2 provides a method for treating organic wastewater based on EGSB using an EGSB reaction system in an apparatus as shown in fig. 1, the method comprising the steps of:

introducing 6L of wastewater containing 40mg/L nitrobenzene into an EGSB reactor containing the denitrification coupling anaerobic ammonia oxidation granular sludge from a second water inlet at a speed of 1-2L/h, simultaneously taking a small amount of supernatant to detect the nitrogen concentration and the COD concentration, and introducing a carbon source sodium bicarbonate solution stored in a carbon source water inlet tank into the EGSB reactor according to the concentration in a C/N (2: 1) ratio to obtain a mixed solution; and (3) adjusting the pH value of the mixed liquid in the EGSB reactor to be 7.5 by using an acid-base adjusting liquid, setting the reflux ratio of the EGSB reactor to be 3, reacting at the constant temperature of 30-40 ℃, wherein the hydraulic retention time is 12h, discharging the treated wastewater through a second water outlet by using a three-phase separator, and discharging the waste gas through a gas outlet.

Through detection, the nitrobenzene content in the treated wastewater is 38mg/L, and the COD is 178 mg/L.

From the test results of the above examples and comparative examples, it can be seen that the treatment of wastewater containing nitrobenzene using the apparatus of the present invention achieves an efficient treatment effect of wastewater containing nitrobenzene by combining the SBR reaction system and the EGSB reaction system in combination with the advanced oxidation process and the biological anaerobic treatment process.

The total nitrogen content of the wastewater treated by the advanced oxidation method is too high, and the content of nitrobenzene in the wastewater cannot be effectively reduced by only using the EGSB treatment method, so that the wastewater treatment efficiency is low and the effect is poor.

It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. Any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the claims of the present invention.

Claims

1. A method for treating organic wastewater by using a device, which is characterized by comprising an SBR reaction system, an EGSB reaction system and a temporary storage tank (6);

the SBR reaction system comprises a water inlet tank (1), an SBR reactor (2), an SBR constant temperature system (3), an aeration system (4) and a stirrer (5);

the SBR reactor (2) is provided with a first water inlet (21), a first water outlet (22) and a feed inlet (23), the water inlet tank (1) is communicated with the first water inlet (21), and the first water outlet (22) is communicated with the temporary storage tank (6);

the SBR constant temperature system (3) is arranged around the periphery of the shell of the SBR reactor (2);

the aeration system (4) comprises an aeration blower (41) and an aeration disc (42), wherein the aeration blower (41) is arranged outside the SBR reactor (2), the aeration disc (42) is arranged at the bottom in the SBR reactor (2), and the aeration disc (42) is connected with the aeration blower (41) through an aeration pipe;

the stirrer (5) is fixed inside the SBR reactor (2);

the EGSB reaction system comprises an EGSB reactor (7), a carbon source water inlet tank (8) and an EGSB constant temperature system (9);

a muddy water reaction chamber (71) positioned at the bottom and a three-phase separator (72) positioned at the top are arranged in the EGSB reactor (7);

the EGSB reactor (7) is provided with a second water inlet (73), an EGSB sampling port (74), a second water outlet (75), a gas outlet (76) and a reflux pump outlet (77); the second water inlet (73) is formed in the bottom of the EGSB reactor (7), and the temporary storage tank (6) and the carbon source water inlet tank (8) are respectively communicated with the second water inlet (73); the second water outlet (75) is arranged at the top of the EGSB reactor (7); the return pump outlet (77) is communicated with the second water inlet (73) through a return pump (78);

the EGSB constant temperature system (9) is arranged around the periphery of the shell of the EGSB reactor (7);

the method comprises the following steps:

s1, introducing the wastewater into an SBR reactor filled with desulfurized ash and manganese sand, adjusting the pH value to 2-4, starting aeration, and reacting for 5-7 hours at a constant temperature of 50-60 ℃ under the stirring condition to obtain a reaction solution; adding zero-valent iron powder into the reaction liquid under an anoxic condition, adjusting the pH to 7-8, standing, and discharging the upper layer liquid to a temporary storage tank;

s2, introducing the supernatant and a carbon source in the step S1 into an EGSB reactor containing denitrification coupling anaerobic ammonium oxidation granular sludge to obtain a mixed liquid, adjusting the pH value of the mixed liquid in the EGSB reactor to be 7-8, reacting at a constant temperature of 30-40 ℃ in a reflux ratio of 2-8 in the EGSB reactor, and allowing the treated wastewater to pass through a three-phase separator and be discharged through a second water outlet, wherein the waste gas is discharged through a gas outlet.

2. The method according to claim 1, characterized in that the SBR constant temperature system (3) and the EGSB constant temperature system (9) are both constant temperature jacket circulating water systems.

3. The method according to claim 2, wherein the constant-temperature jacket circulating water system comprises a constant-temperature water bath tank (31), a circulating transfusion component (32) and a constant-temperature jacket (33), and the constant-temperature jacket (33) is provided with a constant-temperature water inlet and a constant-temperature water outlet; the circulating transfusion component (32) is connected with the constant-temperature water bath box (31), and the circulating transfusion component (32) is communicated with the constant-temperature water inlet and the constant-temperature water outlet to form a circulating loop.

4. The method of claim 1, wherein the aeration tray (42) is provided with at least three aeration outlets.

5. The method according to claim 1, characterized in that the side wall of the SBR reactor (2) is provided with a SBR sampling opening (24).

6. A method according to claim 1, wherein the EGSB reaction system is further provided with a gas flow meter (79), and the gas flow meter (79) is in communication with a gas outlet (76).

7. The method of claim 1, wherein the EGSB sampling ports (74) are at least two.

8. The method as claimed in claim 1, wherein the nitrobenzene concentration of the supernatant is less than or equal to 2 mg/L.

9. The method according to claim 1, wherein the mass ratio of the desulfurized fly ash to the manganese sand in S1 is (9-11): 1.