CN216005557U - Integrated treatment system for high-ammonia-nitrogen wastewater difficult to biodegrade - Google Patents
Integrated treatment system for high-ammonia-nitrogen wastewater difficult to biodegrade Download PDFInfo
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- CN216005557U CN216005557U CN202122211746.5U CN202122211746U CN216005557U CN 216005557 U CN216005557 U CN 216005557U CN 202122211746 U CN202122211746 U CN 202122211746U CN 216005557 U CN216005557 U CN 216005557U
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Abstract
The application relates to the technical field of sewage treatment, in particular to a comprehensive treatment system for high ammonia nitrogen wastewater difficult to biodegrade. The comprehensive treatment system for the high-ammonia-nitrogen wastewater difficult to biodegrade comprises a facultative reactor, a Fenton oxidation reactor and an AO type biochemical reactor which are sequentially connected; the facultative reactor comprises a first facultative reaction area, a second facultative reaction area and a facultative sludge-water separation area which are sequentially connected, wherein the first facultative reaction area is provided with a stirring device and an aeration device, and the second facultative reaction area is provided with an aeration device; the Fenton oxidation reactor comprises an oxidation reaction zone and a Fenton oxidation sludge water separation zone; the AO-type biochemical reactor comprises an anoxic reaction zone, an aerobic reaction zone and an AO sludge-water separation zone which are sequentially connected, wherein the anoxic reaction zone is provided with a stirring device, and the aerobic reaction zone is provided with an aeration device. The comprehensive treatment system for the high ammonia nitrogen wastewater difficult to biodegrade can fully reduce the ammonia nitrogen content of the effluent under the condition of less carbon source and alkalinity supplement.
Description
Technical Field
The application relates to the technical field of sewage treatment, in particular to a comprehensive treatment system for high ammonia nitrogen wastewater difficult to biodegrade.
Background
In the process of economic development, pollutants harmful to the environment are generated in industrial production and social life, and waste water is a common pollutant. The industrial wastewater generated by the factory has the characteristics of high pollution, difficult degradation, complex components, variable properties and the like, and is difficult to treat.
The treatment method for the refractory wastewater comprises a physical-chemical method, a biological method and the like. The common physical and chemical method is to decompose or separate refractory organic matters by physical and chemical means, such as coagulating sedimentation, adsorption, extraction and membrane separation. The chemical method is mainly a chemical oxidation method, and commonly includes electrocatalytic oxidation, ozone oxidation, fenton-like oxidation and the like. The biological method mainly uses a microbial method to lead the microbes to obtain nutrients from the wastewater and simultaneously degrade and utilize harmful substances.
The physicochemical method has poor adaptability to wastewater with complex components and higher concentration and relatively complex operation. The chemical method has certain selectivity of the oxidant and the production cost is expensive. The biological method is not very effective for highly polluted and difficult-to-degrade waste water. Therefore, in practical applications, a combination of multiple methods is often used.
When a plurality of methods are combined, the used device usually comprises a biochemical treatment device and a Fenton oxidation treatment device which are connected in sequence, wherein the biochemical treatment device is generally subjected to anoxic treatment and aerobic treatment, then mud-water separation is carried out, then organic matters are fully degraded under the action of ferrous sulfate and hydrogen peroxide, and then mud-water separation is carried out to obtain the treated wastewater with low ammonia nitrogen content.
In view of the above-mentioned related art, the inventors considered that the ammonia nitrogen content of the finally treated wastewater is still high only by using the biochemical treatment apparatus and the fenton oxidation treatment apparatus.
SUMMERY OF THE UTILITY MODEL
In order to fully reduce the ammonia nitrogen content in the waste water, the application provides a comprehensive treatment system of high ammonia nitrogen waste water difficult to biodegrade.
The application provides a high ammonia-nitrogen concentration wastewater's that difficult biodegradable integrated processing system adopts following technical scheme:
a comprehensive treatment system for high ammonia nitrogen wastewater difficult to biodegrade comprises a facultative reactor, a Fenton oxidation reactor and an AO type biochemical reactor which are sequentially connected; the facultative reactor comprises a first facultative reaction area, a second facultative reaction area and a facultative sludge-water separation area which are sequentially connected, and the first facultative reaction area is provided with a wastewater inlet; the first facultative reaction area is provided with a stirring device and an aeration device, and the second facultative reaction area is provided with an aeration device;
the Fenton oxidation reactor comprises an oxidation reaction zone and a Fenton oxidation sludge water separation zone;
the AO-type biochemical reactor comprises an anoxic reaction zone, an aerobic reaction zone and an AO sludge-water separation zone which are sequentially connected, wherein a water inlet of the anoxic reaction zone is connected with a water outlet of the Fenton oxidation sludge-water separation zone of the Fenton oxidation reactor, the anoxic reaction zone is provided with a stirring device, and the aerobic reaction zone is provided with an aeration device.
Through adopting above-mentioned technical scheme, the processing system of this application links to each other facultative reactor, fenton oxidation reactor, AO type biochemical reactor in proper order, makes the ammonia nitrogen in the waste water turn into nitrate nitrogen reconversion nitrogen gas in facultative reactor. In the first facultative reaction area, the nitration reaction rate and the denitrification reaction rate can be controlled to be basically consistent, the process from ammonia nitrogen to nitrate nitrogen and then to nitrogen is synchronously completed, and the second facultative reaction area mainly carries out nitration reaction. The wastewater enters the Fenton oxidation reactor to carry out the Fenton oxidation reaction, so that macromolecular organic nitrogen in the wastewater can be converted into micromolecular organic nitrogen or ammonia nitrogen, and can be converted into nitrate nitrogen under the condition of high oxidation-reduction potential, the biodegradability of the wastewater is improved, and a foundation is provided for the biochemical reaction in the AO-type biochemical reactor. The wastewater is subjected to denitrification reaction and nitration reaction in the AO-type biochemical reactor, so that nitrogen in the wastewater is removed to the maximum extent, and the final ammonia nitrogen and COD in the effluent are ensured to reach the discharge standard.
The facultative reactor adopts two facultative reaction zones which are connected, in the first facultative reaction zone, the original carbon source and/or the carbon source or sludge added into the first facultative reaction zone are utilized to carry out nitration reaction and denitrification reaction, and after the reaction (aerobic nitration reaction) is continuously carried out in the second facultative reaction zone, sludge-water separation is carried out, so that the nitration reaction and the denitrification reaction are fully carried out.
Preferably, the Fenton oxidation reactor comprises a mixing zone, the oxidation reaction zone, a neutralization zone, a gas-water separation zone, a flocculation zone and the Fenton oxidation sludge-water separation zone which are connected in sequence; the mixing area is provided with a water inlet connected with the water outlet of the facultative sludge water separation area, and the mixing area is provided with an acid liquid adding port; the mixing zone or the oxidation reaction zone is provided with an iron catalyst feeding port; an oxidant inlet is arranged on the oxidation reaction zone; the neutralization area is provided with an alkali adding port; a flocculating agent adding port is arranged on the flocculation area.
Through adopting above-mentioned technical scheme, among the fenton oxidation reactor, waste water mixes at first with the acidizing fluid in the mixed zone, adjusts the pH of waste water to be suitable for carrying out the fenton oxidation reaction, then make waste water react with iron catalyst and oxidant in the oxidation reaction zone, produce the hydroxyl radical, the hydroxyl radical reacts with the organic matter in the waste water, makes the organic matter of difficult decomposition decomposed by the decomposition, reduces COD, improves the biodegradability of waste water simultaneously. After the Fenton oxidation reaction, the pH value is adjusted by adding alkali in a neutralization area, so that ferric iron generated by the Fenton oxidation reaction is converted into ferric hydroxide, then the ferric hydroxide enters an air-water separation area to remove air bubbles in the wastewater (acid gas in the wastewater is removed by aeration), and then flocculation reaction and precipitation separation are carried out. In the Fenton oxidation reactor, each step is separately carried out, so that the wastewater flows in and is mixed with each medicament more uniformly and fully, the full degree of each reaction is improved, and the ammonia nitrogen content in the wastewater is further reduced.
Preferably, the mixing zone (21), the oxidation reaction zone (22), the neutralization zone (23) and the flocculation zone (25) are all provided with stirring devices.
Through adopting above-mentioned technical scheme, all set up agitating unit in a plurality of regions of fenton oxidation reactor, can make more thorough that oxidation reaction takes place, make the organic matter fully convert nitrate nitrogen into wherein, improve the biodegradability of waste water.
Preferably, the second facultative reaction zone is provided with an alkalinity supplement addition port.
By adopting the technical scheme, the pH value of the wastewater is easy to drop in the nitration reaction process, so that the nitration reaction rate is reduced, the alkalinity supplement adding port is arranged on the second facultative reaction zone, a small amount of sodium carbonate and the like can be added into the second facultative reaction zone as an alkalinity supplement when needed, the pH value of the wastewater is adjusted, and the nitration reaction is ensured.
Preferably, the first facultative reaction zone is provided with an oxidation-reduction potential monitor for monitoring the oxidation-reduction potential of the wastewater in the first facultative reaction zone; the second facultative reaction area is provided with a dissolved oxygen detector for monitoring the content of the dissolved oxygen in the wastewater in the second facultative reaction area.
Through adopting above-mentioned technical scheme, set up the redox potential monitor in first facultative reaction district, the redox potential in real time monitoring first facultative reaction district, when the redox potential is higher, can promote the growth of aerobic bacteria, be unfavorable for the growth of facultative microorganisms. Therefore, when the fluctuation of the oxidation-reduction potential is large, the aeration amount is adjusted by the aeration device through the stirring device and the aeration device which are arranged in the first facultative reaction zone, and the stirring is carried out by matching with the stirring device, so that the oxidation-reduction potential is ensured to be in a proper range, and the growth of facultative microorganisms is promoted.
Preferably, the facultative reactor also comprises a first mixed liquid reflux device for refluxing the mixed liquid in the second facultative reaction area to the first facultative reaction area and a first sludge reflux device for refluxing the sludge in the facultative sludge water separation area to the first facultative reaction area, wherein the first sludge reflux device comprises a reflux pipe, one end of the reflux pipe is arranged at the bottom of the facultative sludge water separation area, and the other end of the reflux pipe is connected with the first facultative reaction area.
By adopting the technical scheme, the mixed liquid in the second facultative reaction area flows back to the first facultative reaction area, and the sludge in the facultative sludge-water separation area also flows back to the first facultative reaction area, so that the sludge and the microorganisms can be fully recycled, and the efficiency of the nitrification reaction and the denitrification reaction in the first facultative reaction area is improved.
Preferably, the anoxic reaction zone is provided with an oxidation-reduction potential monitor for monitoring the oxidation-reduction potential of the wastewater in the anoxic reaction zone; the aerobic reaction zone is provided with a dissolved oxygen monitor for monitoring the dissolved oxygen content of the wastewater in the aerobic reaction zone.
By adopting the technical scheme, the oxidation-reduction potential monitor is arranged in the anoxic reaction zone of the AO-type biochemical reaction zone, the dissolved oxygen detector is arranged in the aerobic reaction zone, the oxidation-reduction potential of the anoxic reaction zone and the dissolved oxygen content of the aerobic reaction zone can be monitored in real time, the stirring speed and the aeration amount of the anoxic reaction zone and the aerobic reaction zone are adjusted, and the oxidation-reduction potential of the anoxic reaction zone and the dissolved oxygen content of the aerobic reaction zone are ensured to be in a proper range.
Preferably, the AO-type biochemical reactor comprises a second mixed liquid reflux device for refluxing the mixed liquid in the aerobic reaction zone to the anoxic reaction zone; the AO type biochemical reactor comprises a second sludge reflux device which is used for refluxing the sludge in the AO sludge-water separation area to the anoxic reaction area.
By adopting the technical scheme, the second mixed liquid reflux device and the second sludge reflux device are arranged in the AO-type biochemical reactor, so that the mixed liquid in the aerobic reaction zone and the sludge at the bottom of the AO sludge-water separation zone can be refluxed to the anoxic reaction zone in the wastewater treatment process, the higher-level sludge concentration in the anoxic reaction zone is maintained, and the denitrification reaction and the nitrification reaction are ensured.
In summary, the present application includes at least one of the following beneficial technical effects:
1. the comprehensive treatment system for the nonbiodegradable high ammonia nitrogen wastewater sequentially connects the facultative reactor, the Fenton oxidation reactor and the AO-type biochemical reactor, can reduce the ammonia nitrogen content of the effluent to below 25mg/L under the condition of low-level carbon source and alkalinity supplement, and reduce COD to below 100mg/L, thereby achieving the secondary standard of pollutant discharge Standard of urban wastewater treatment plants (GB 18918-2002).
2. The comprehensive treatment system for the high-ammonia-nitrogen wastewater difficult to biodegrade further adopts an oxidation-reduction potential monitor and a dissolved oxygen detector which are arranged in the facultative reactor and the AO-type biochemical reactor, monitors the oxidation-reduction potential and the dissolved oxygen content of the wastewater in the facultative reactor and the AO-type biochemical reactor in real time, controls the oxidation-reduction potential and the dissolved oxygen of corresponding reaction areas of the facultative reactor and the AO-type biochemical reactor to be in reasonable intervals by adjusting the stirring speed of a stirring device in the facultative reactor and the AO-type biochemical reactor and the aeration airflow flow of an aeration device, and promotes the efficiency of organic matter degradation reaction.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment 1 of the integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater.
FIG. 2 is a schematic structural diagram of an embodiment 2 of the integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater.
Description of reference numerals:
1. a facultative reactor; 11. a first facultative reaction zone; 111. a water inlet line; 112. a first organic carbon source addition line; 113. a first stirring device; 114. a first aeration device; 12. a second facultative reaction zone; 121. An alkalinity supplement addition line; 122. a second aeration device; 13. a facultative water separation zone; 14. a first mixed liquid reflux unit; 15. a first sludge recirculation apparatus; 2. a Fenton oxidation reactor; 21. a mixing zone; 211. a Fenton oxidation water inlet line; 212. adding acid liquor into a pipeline; 213. a catalyst addition line; 22. an oxidation reaction zone; 221. an oxidant addition line; 23. a neutralization zone; 231. a base addition line; 24. a gas-water separation zone; 25. a flocculation zone; 251. a flocculant addition line; 26. a Fenton oxidation sludge water separation zone; 3. an AO-type biochemical reactor; 31. an anoxic reaction zone; 311. an AO biochemical water inlet line; 312. a second organic carbon source addition line; 32. an aerobic reaction zone; 33. an AO sludge-water separation zone; 34. a second mixed liquid reflux device; 35. and a second sludge reflux device.
Detailed Description
The present application will be described in further detail with reference to the following drawings and examples.
In the comprehensive treatment system of the high ammonia-nitrogen wastewater difficult to biodegrade, a first facultative reaction area 11 is provided with a carbon source adding port for adding a carbon source to the first facultative reaction area 11 when needed.
In the case of the Fenton oxidation reactor, an alkali addition port is provided in the neutralization zone 23 to add an alkali to the neutralization zone 23 to adjust the pH of the wastewater.
For the AO-type biochemical reactor, an organic carbon source inlet is provided on the anoxic reaction zone 31.
Further, the comprehensive treatment of the nonbiodegradable high ammonia nitrogen wastewater of the application also comprises a controller and a storage, wherein the controller is connected with a speed regulating switch of a stirring device of the first facultative reaction zone 11, a flow regulating switch of an aeration device of the second facultative reaction zone 12, a speed regulating switch of a stirring device of a mixing zone 21, an oxidation reaction zone 22, a neutralization zone 23 and a flocculation zone 25 of the Fenton oxidation reactor, and simultaneously is connected with a speed regulating switch of a stirring device of an anoxic reaction zone 31 of the AO-type biochemical reactor and a flow regulating switch of an aeration device of an aerobic reaction zone 32 of the AO-type biochemical reactor so as to control the devices to be opened, closed or changed in speed.
The controller is also connected with an oxidation-reduction potential monitor of the first facultative reaction zone 11, a dissolved oxygen monitor of the second facultative reaction zone 12, an oxidation-reduction potential monitor of the anoxic reaction zone 31 and a dissolved oxygen monitor of the aerobic reaction zone 32, so that data monitored by the monitors can be transmitted to the controller and compared with preset related threshold values in the memory, and when the data exceed the set threshold value range, the controller controls corresponding switches.
In the integrated processing system of difficult biodegradable high ammonia-nitrogen concentration waste water of this application, in the fenton oxidation reactor, the redox potential is higher, is favorable to turning into little molecular organic nitrogen or ammonia nitrogen with macromolecule organic nitrogen to turn into nitrate nitrogen.
For the second facultative reaction zone 12, the dissolved oxygen content of the waste water therein is controlled within the range of 0-2 mg/L. When the dissolved oxygen content of the second facultative reaction zone 12 exceeds 0-2mg/L, the aeration gas flow rate of the second facultative reaction zone 12 is regulated so as to be maintained in the range of 0-2 mg/L.
The oxidation-reduction potential of the wastewater in the anoxic reaction zone 31 is controlled within the range of-200 mV to-100 mV, and when the oxidation-reduction potential of the wastewater in the anoxic reaction zone 31 exceeds-200 mV to-100 mV, the stirring speed of the anoxic reaction zone 31 is adjusted so as to be maintained within the range of-200 mV to-100 mV. When the oxidation-reduction potential is lower than-200 mV, the stirring speed is increased, and when the oxidation-reduction potential is higher than-100 mV, the stirring speed is reduced or the stirring is stopped.
For the aerobic reaction zone 32, the dissolved oxygen content therein is controlled to be in the range of 2-4mg/L, and when the dissolved oxygen content of the aerobic reaction zone 32 exceeds 2-4mg/L, the aeration gas flow rate of the aerobic reaction zone 32 is adjusted to maintain the dissolved oxygen content thereof in the range of 2-4 mg/L. When the dissolved oxygen content is higher than 4mg/L, the aeration gas flow rate is decreased or the aeration is stopped, and when the dissolved oxygen content is lower than 2mg/L, the aeration rate is increased.
The application provides a processing system of high ammonia-nitrogen wastewater of difficult biodegradable.
Example 1
Referring to fig. 1, the integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater of the present embodiment comprises a facultative reactor 1, a fenton oxidation reactor 2, and an AO-type biochemical reactor 3, which are connected in sequence, wherein the facultative reactor 1, the fenton oxidation reactor 2, and the AO-type biochemical reactor 3 are connected through a pipeline or a channel.
The facultative reactor 1 includes a first facultative reaction zone 11, a second facultative reaction zone 12, and a facultative sludge water separation zone 13, which are connected in sequence. The first facultative reaction zone 11, the second facultative reaction zone 12 and the facultative water separation zone 13 are all of a tank structure, and in other embodiments, these reaction zones may be reaction vessels with a small volume.
The first and second facultative reaction zones 11, 12 and the facultative separation zone 13 are arranged in the same direction in sequence, a partition is arranged between the first and second facultative reaction zones 11 and 12, and the bottom of the partition is provided with a communicating hole, so that the waste water at the lower part of the first facultative reaction zone 11 can enter the second facultative reaction zone 12. A partition plate is also arranged between the second facultative reaction area 12 and the facultative mud water separation area 13, a communicating hole is arranged on the partition plate, a pipeline passes through a through hole of the partition plate and enters the facultative mud water separation area, a central water inlet cylinder is arranged in the facultative mud water separation area, and the pipeline passes through the through hole of the partition plate and enters the upper part of the central water inlet cylinder, so that the waste water in the second facultative reaction area 12 can enter the facultative mud water separation area 13.
In this embodiment, the facultative mud-water separation zone 13 is a vertical sedimentation tank, a vertically extending central water inlet tube is disposed at the center of the upper portion of the vertical sedimentation tank, an overflow weir is disposed on the inner wall of the upper end of the vertical sedimentation tank to form a clear water collection tank, and a water outlet is disposed on the clear water collection tank.
The upper end of the first facultative reaction area 11 is provided with a water inlet and a first organic carbon source adding port, the water inlet is connected with a water inlet pipeline 111, the first organic carbon source adding port is connected with a first organic carbon source adding pipeline 112, the water inlet pipeline 111 is used for introducing wastewater to be treated into the first facultative reaction area 11, and the first organic carbon source adding port is used for adding macromolecular organic carbon sources such as starch into the first facultative reaction area 11 when necessary. The first facultative reaction area 11 is provided with an oxidation-reduction potential monitor (also called an oxidation-reduction potential detector), and an electrode of the oxidation-reduction potential monitor is installed in the wastewater of the first facultative reaction area 11 in a submerged manner.
The first facultative reaction area 11 is further provided with a first stirring device 113 and a first aeration device 114, the first stirring device 113 is a vertical stirrer, a stirring motor of the vertical stirrer is fixedly arranged above the first reaction area, and the lower end of the stirring shaft is provided with a stirring blade and extends into the bottom of the wastewater. The aeration means comprises an aeration hose provided at the bottom of the first facultative reaction zone 11 and a blowing means for supplying air into the aeration hose.
The second facultative reaction area 12 is provided with an alkalinity supplement inlet, which is connected with an alkalinity supplement inlet line 121 for adding alkalinity supplements such as sodium carbonate into the second facultative reaction area 12 to maintain the pH of the second facultative reaction area 12. The second facultative reaction area 12 is provided with a dissolved oxygen monitor (also called dissolved oxygen measuring instrument or dissolved oxygen measuring instrument), and a probe (also called sensor) of the dissolved oxygen monitor is installed in the wastewater of the second facultative reaction area 12 in a sinking manner.
The second aerobic reaction zone 12 is provided with a second aeration device 122, and the second aeration device 122 comprises an aeration hose arranged at the bottom of the second aerobic reaction zone 12 and a blower device for supplying air into the aeration hose.
The comprehensive treatment system for the nonbiodegradable high ammonia nitrogen wastewater further comprises a controller, wherein a storage is connected to the controller, and switches are arranged on the first aeration device 114 of the first facultative reaction area 11 and the second aeration device 122 of the second facultative reaction area 12 and are connected with the controller. Furthermore, the oxidation-reduction potential monitor of the first facultative reaction zone 11 is connected to the controller, and transmits the monitored oxidation-reduction potential information to the controller.
An oxidation-reduction potential threshold value is preset in a memory connected to the controller, and when the oxidation-reduction potential information of the first facultative reaction zone 11 received by the controller is compared with the threshold value in the memory and exceeds the oxidation-reduction potential threshold value, the controller controls to turn on (or turn off) the aeration device of the first facultative reaction zone 11, or increase (or decrease) the flow rate of the aeration device of the first facultative reaction zone 11, and simultaneously increase (or decrease) the stirring speed of the stirrer of the first facultative reaction zone 11, so that the oxidation-reduction potential of the first facultative reaction zone 11 is maintained in a set range.
A dissolved oxygen threshold value is preset in a memory connected with the controller, and when the dissolved oxygen concentration of the second facultative reaction area 12 received by the controller exceeds the dissolved oxygen threshold value, the controller closes the aeration device of the second facultative reaction area 12 or adjusts the flow rate of the aeration device of the second facultative reaction area 12.
Be provided with first mixed liquid reflux unit 14 between second facultative reaction district 12 and the first facultative reaction district 11, first facultative reaction district 11 upper end is provided with mixed liquid backward flow mouth, first mixed liquid reflux unit 14 includes the back flow, back flow one end sets up the waste water bottom in second facultative reaction district 12, the upper end water inlet at first facultative reaction district 11 is connected to the other end, be connected with air on the back flow and carry and push away the device and regard as air source power equipment, in order to pump back the mixed liquid of second facultative reaction district 12 to first facultative reaction district 11.
A first sludge reflux device 15 is arranged between the facultative sludge separation area 13 and the first facultative reaction area 11, a sludge reflux port is arranged at the upper end of the first facultative reaction area 11, the first sludge reflux device 15 comprises a sludge reflux pipe, one end of the sludge reflux pipe is arranged at the bottom of the facultative sludge separation area 13, the other end of the sludge reflux pipe is connected to the sludge reflux port of the first facultative reaction area 11, and a sludge reflux pump is connected to the sludge reflux pipe to pump the sludge at the bottom of the first facultative reaction area 11. The sludge reflux pump can be replaced by an air source power device such as an air lifting and pushing device.
The adjusting switches of the first mixed liquor refluxing device 14 and the first sludge refluxing device 15 are also connected to the controller to adjust the refluxing ratio according to the oxidation-reduction potential of the first facultative reaction zone 11 and the dissolved oxygen content of the second facultative reaction zone 12.
The Fenton oxidation reactor 2 comprises a mixing zone 21, an oxidation reaction zone 22, a neutralization zone 23, a gas-water separation zone 24, a flocculation zone 25 and a Fenton oxidation sludge water separation zone 26 which are connected in sequence.
A clapboard is arranged between the mixing area 21 and the oxidation reaction area 22, a communication hole is arranged at the lower part of the clapboard, a clapboard is arranged between the oxidation reaction area 22 and the neutralization area 23, a communication hole is arranged at the upper part of the clapboard, a clapboard is arranged between the neutralization area 23 and the air-water separation area 24, a communication hole is arranged at the lower part of the clapboard, a clapboard is arranged between the air-water separation area 24 and the flocculation area 25, a communication hole is arranged at the upper part of the clapboard, a clapboard is arranged between the flocculation area 25 and the Fenton oxidation sludge water separation area 26, a pipeline is arranged at the middle part of the clapboard, and the flocculation area 25 is communicated with a central water inlet cylinder arranged in the Fenton oxidation sludge water separation area 26.
The upper end of the mixing area 21 is provided with a water inlet, the water inlet is connected with a Fenton oxidation water inlet pipeline 211, the water inlet of the mixing area 21 is connected with a water outlet of a clear water collecting tank of the facultative mud and water separation area 13 of the facultative reaction area through the Fenton oxidation water inlet pipeline 211, and upper clear water obtained by the facultative mud and water separation area 13 enters the mixing area 21 of the Fenton oxidation reactor 2.
An acid liquid adding port is further formed at the upper end of the mixing zone 21, and an acid liquid adding pipeline 212 is connected to the acid liquid adding port and used for adding acid liquid into the mixing zone 21, wherein the acid liquid is any one of dilute sulfuric acid and hydrochloric acid. The upper end of the mixing zone 21 is also provided with a catalyst feeding port, and the catalyst feeding port is connected with a catalyst feeding pipeline 213 for feeding ferrous sulfate into the mixing zone 21.
The upper end of the oxidation reaction zone 22 is provided with an oxidant inlet, and the oxidant inlet is connected with an oxidant adding pipeline 221 for adding hydrogen peroxide into the oxidation reaction zone 22. An alkali adding port is arranged at the upper end of the neutralization zone 23, and an alkali adding pipeline 231 is connected to the alkali adding port and is used for adding alkali liquor into the neutralization zone 23.
The upper end of the flocculation area 25 is provided with a flocculant adding port, and the flocculant adding port is connected with a flocculant adding pipeline 251 for adding a flocculant to the flocculation area 25.
Mechanical stirring devices are arranged in the mixing zone 21, the oxidation reaction zone 22 and the neutralization zone 23, the mechanical stirring devices are vertical stirrers, such as paddle stirrers or hyperboloid stirrers, and the surfaces of the liquid receiving parts of the equipment adopt non-metal anticorrosive coatings. In other embodiments, the mechanical agitation means may be replaced with an air agitation means (perforated pipe air agitation means). The flocculation area 25 is provided with a frame mixer. The Fenton oxidation mud water separation zone 26 adopts a vertical flow type sedimentation tank, a vertically extending water inlet pipe is arranged at the center of the upper part of the vertical flow type sedimentation tank, an overflow weir is arranged on the inner wall of the upper end of the vertical flow type sedimentation tank to form a clear water collecting tank, and a water outlet is arranged on the clear water collecting tank. The treated wastewater in the flocculation zone 25 is fed into the water inlet pipe at the center of the Fenton oxidation sludge water separation zone 26 through the communicating pipe.
The AO-type biochemical reactor 3 comprises an anoxic reaction zone 31, an aerobic reaction zone 32 and an AO sludge-water separation zone 33 which are connected in sequence. The upper end of the anoxic reaction zone 31 is provided with a water inlet, and the water inlet is connected with an AO biochemical water inlet pipeline 311 which is connected with a clear water outlet of the Fenton oxidation sludge water separation zone 26. The partition plates are arranged between the anoxic reaction zone 31 and the aerobic reaction zone 32, and between the aerobic reaction zone 32 and the AO sludge-water separation zone 33, the communication holes are arranged on the partition plates, one orifice of each communication hole is covered with a filtering screen for intercepting the filler, and the aperture of each filtering screen is 5 +/-1 mm.
The anoxic reaction zone 31 is added with a filler which can be an organic polymer filler K, the filling ratio is 50 percent, and the specific surface area of the filler is 800 m2/m3. The filling ratio of the organic polymer filler P added into the aerobic reaction zone 32 is 40 percent, and the specific surface area of the filler is 80000 m2/m3. The organic polymer filler K is elastic plastic.
The anoxic reaction zone 31 is provided with a stirring device which is a vertical stirrer. The aerobic reaction zone 32 is provided with an aeration device which is a tubular aerator, and the tubular aerator comprises a hard aeration pipe and an aeration membrane.
The upper end of the anoxic reaction zone 31 is provided with a second organic carbon source adding port, and the second organic carbon source adding port is connected with a second organic carbon source adding pipeline 312 for adding small molecular organic carbon sources such as sodium acetate and the like into the anoxic reaction zone 31.
The anoxic reaction zone 31 is further provided with an oxidation-reduction potential monitor (also called an oxidation-reduction potential detector), and an electrode of the oxidation-reduction potential monitor is installed in the wastewater in the anoxic reaction zone 31 in a submerged manner. The aerobic reaction zone 32 is provided with a dissolved oxygen monitor (also called a dissolved oxygen meter or a dissolved oxygen meter), and a probe (also called a sensor) of the dissolved oxygen monitor is installed in the wastewater in the aerobic reaction zone 32 in a sinking manner.
The anoxic reaction zone 31 is further provided with a mixed liquid return port, a second mixed liquid return device 34 is arranged between the anoxic reaction zone 31 and the aerobic reaction zone 32, the second mixed liquid return device 34 comprises a mixed liquid return pipe, one end of the mixed liquid return pipe is arranged at the bottom of the liquid in the aerobic reaction zone 32, and the other end of the mixed liquid return pipe is connected with the mixed liquid return port of the anoxic reaction zone 31. An air ejector is also arranged on the mixed liquid return pipe and is used as an air source power device.
Be provided with second sludge reflux unit 35 between oxygen deficiency reaction zone 31 and the AO sludge water separation zone 33, oxygen deficiency reaction zone 31 upper end is provided with the sludge return mouth, and second sludge reflux unit 35 includes the sludge return pipe, and sludge return pipe one end sets up in the bottom of AO sludge water separation zone 33, and the other end is connected to the sludge return mouth of oxygen deficiency reaction zone 31, still is connected with the sludge reflux pump on the sludge return pipe, takes out the mud of AO sludge water separation zone 33 bottom to oxygen deficiency reaction zone 31.
The implementation principle of the treatment system for the nonbiodegradable high ammonia nitrogen wastewater of the embodiment is as follows: wastewater is introduced into the first facultative reaction zone 11, and simultaneously a certain amount of starch is added as a macromolecular organic carbon source (one-time addition), and simultaneously the first stirring device 113 and the first aeration device 114 of the first facultative reaction zone 11 and the second aeration device 122 of the second facultative reaction zone 12 are started. When the wastewater enters the second facultative reaction zone 12, the first mixed liquid reflux device 14 is started, and when the wastewater enters the facultative sludge separation zone 13, the first sludge reflux device 15 is started to reflux the sludge at the bottom to the first facultative reaction zone 11. The alkalinity supplement is added through alkalinity supplement addition line 121 on the second facultative reaction zone 12 when the pH of the second facultative reaction zone 12 is below the set point. The effluent of the facultative reactor 1 enters a Fenton oxidation reactor 2, acid liquor and ferrous sulfate are added into a mixing zone 21, all stirring devices of the Fenton oxidation reactor 2 are started, the wastewater is mixed with the acid liquor and the ferrous sulfate and then enters an oxidation reaction zone 22, hydrogen peroxide is added into the oxidation reaction zone 22 to carry out the Fenton oxidation reaction, the effluent enters a neutralization zone 23 to add alkali to adjust the pH value, and then enters a gas-liquid separation zone to remove carbon dioxide in the waterThe mixed liquid is recovered to be neutral, then enters the flocculation area 25, is uniformly mixed with the flocculating agent, then enters the flocculation sludge-water separation area for sludge-water separation, clear water enters the anoxic reaction area 31 of the AO-type biochemical reactor 3, enters the aerobic reaction area 32 after reacting under the stirring condition of the anoxic reaction area 31, and enters the AO sludge-water separation area 33 after reacting under the aeration condition. The embodiment is suitable for treating water with the amount of less than 1200m3And d, treating the wastewater.
Example 2
Referring to FIG. 2, the treatment system for nonbiodegradable high ammonia-nitrogen wastewater of this embodiment is different from that of embodiment 1 in that the stirring device in the first facultative reaction zone 11 is configured as a submersible stirrer, and the stirring device in the anoxic reaction zone 31 is also configured as a submersible packed fluidized plug flow stirrer.
The facultative mud-water separation zone 13 and the AO mud-water separation zone 33 adopt rectangular sedimentation tanks which enter and exit simultaneously, and comprise a water distribution channel, a water outlet channel, a sludge return channel and a truss car type mud suction scraper, and the Fenton oxidation mud-water separation zone 26 adopts the same rectangular sedimentation tank.
The embodiment is suitable for treating water with the amount of not less than 1200m3And d, treating the wastewater.
The rest are the same as in example 1.
Example 3
The processing system of difficult biodegradable high ammonia-nitrogen wastewater of this embodiment differs from embodiment 1 in that, the oxidation reaction zone 22 of the fenton oxidation reactor 2 is provided with a catalyst inlet and an oxidant inlet, which are respectively used for adding ferrous sulfate and hydrogen peroxide to the oxidation reaction zone 22, and the ferrous sulfate and the hydrogen peroxide are added into the oxidation reaction zone 22.
In other embodiments, the fenton oxidation reactor 2 only comprises an oxidation reaction zone 22 and a fenton oxidation separation zone which are sequentially arranged, and the effluent of the facultative reactor 1 directly enters the oxidation reaction zone 22 for oxidation reaction, and then enters the fenton oxidation sludge water separation zone 26 for separation.
In other embodiments, no packing is disposed in the anoxic reaction zone 31 and the aerobic reaction zone 32 of the AO-type biochemical reactor.
In other embodiments, the facultative reactor 1 and the AO-type biochemical reactor 3 are not provided with the first mixed liquid reflux device 14 and the first sludge reflux device 15, and carbon sources or sludge are added into the corresponding reaction zones according to actual needs.
In other embodiments, the oxidation-reduction potential monitor and the dissolved oxygen detector of the facultative reactor 1 and the AO-type biochemical reactor 3 may be omitted, and the stirring speed and the aeration flow rate may be adjusted according to the actual sampling result, or may be adjusted according to experience.
In other embodiments, the organic carbon source inlet, the mixed liquid return port, and the sludge return port of the first facultative reaction zone 11 are all one large opening.
The treatment system of difficult biodegradable high ammonia-nitrogen concentration waste water of this application can fully reduce the ammonia-nitrogen content in the waste water, adopts the system among embodiment 1 to handle waste water, and before handling, ammonia-nitrogen concentration is about 300 mg/L in the waste water, and COD is about 3000mg/L, B/C > 0.28, and after handling, ammonia-nitrogen concentration is not more than 20 mg/L, COD and is not more than 80mg/L, reaches emission standard.
Claims (8)
1. A comprehensive treatment system for high-ammonia nitrogen wastewater difficult to biodegrade is characterized by comprising a facultative reactor (1), a Fenton oxidation reactor (2) and an AO-type biochemical reactor (3) which are sequentially connected; the facultative reactor (1) comprises a first facultative reaction zone (11), a second facultative reaction zone (12) and a facultative sludge-water separation zone (13) which are connected in sequence, and the first facultative reaction zone (11) is provided with a wastewater inlet; the first facultative reaction zone (11) is provided with a stirring device and an aeration device, and the second facultative reaction zone (12) is provided with an aeration device;
the Fenton oxidation reactor (2) comprises an oxidation reaction zone (22) and a Fenton oxidation sludge water separation zone (26);
the AO-type biochemical reactor (3) comprises an anoxic reaction zone (31), an aerobic reaction zone (32) and an AO sludge-water separation zone (33) which are sequentially connected, a water inlet of the anoxic reaction zone (31) is connected with a water outlet of a Fenton oxidation sludge-water separation zone (26) of the Fenton oxidation reactor (2), the anoxic reaction zone (31) is provided with a stirring device, and the aerobic reaction zone (32) is provided with an aeration device.
2. The integrated treatment system for high ammonia nitrogen wastewater difficult to biodegrade according to claim 1, characterized in that the Fenton oxidation reactor (2) comprises a mixing zone (21), the oxidation reaction zone (22), a neutralization zone (23), a gas-water separation zone (24), a flocculation zone (25) and the Fenton oxidation sludge water separation zone (26) which are connected in sequence; the mixing area (21) is provided with a water inlet connected with the water outlet of the facultative sludge water separation area (13), and the mixing area (21) is provided with an acid liquid inlet; the mixing zone (21) or the oxidation reaction zone (22) is provided with an iron catalyst feeding port; an oxidant inlet is arranged on the oxidation reaction zone (22); the neutralization area (23) is provided with an alkali adding port; a flocculating agent adding port is arranged on the flocculation area (25).
3. The comprehensive treatment system for the nonbiodegradable high ammonia nitrogen wastewater according to claim 2, characterized in that the mixing zone (21), the oxidation reaction zone (22), the neutralization zone (23) and the flocculation zone (25) are all provided with stirring devices.
4. The integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater according to claim 1, characterized in that the second facultative reaction zone (12) is provided with an alkalinity supplement addition port.
5. The integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater according to claim 1, characterized in that the first facultative reaction zone (11) is provided with an oxidation-reduction potential monitor for monitoring the oxidation-reduction potential of wastewater in the first facultative reaction zone (11); the second facultative reaction area (12) is provided with a dissolved oxygen detector for monitoring the content of the dissolved oxygen in the wastewater in the second facultative reaction area (12).
6. The integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater according to claim 5, characterized in that the facultative reactor (1) further comprises a first mixed liquor reflux device (14) for refluxing the mixed liquor of the second facultative reaction zone (12) to the first facultative reaction zone (11) and a first sludge reflux device (15) for refluxing the sludge of the facultative sludge-water separation zone (13) to the first facultative reaction zone (11), wherein the first sludge reflux device (15) comprises a reflux pipe, one end of which is arranged at the bottom of the facultative sludge-water separation zone (13), and the other end of which is connected with the first facultative reaction zone (11).
7. The integrated treatment system for nonbiodegradable high ammonia nitrogen wastewater according to claim 1, characterized in that the anoxic reaction zone (31) is provided with an oxidation-reduction potential monitor for monitoring the oxidation-reduction potential of the wastewater in the anoxic reaction zone (31); the aerobic reaction zone (32) is provided with a dissolved oxygen monitor for monitoring the dissolved oxygen content of the wastewater in the aerobic reaction zone (32).
8. The integrated treatment system for wastewater with high ammonia nitrogen content and difficult to biodegrade according to claim 7, characterized in that the AO-type biochemical reactor comprises a second mixed liquor reflux device (34) for refluxing the mixed liquor of the aerobic reaction zone (32) to the anoxic reaction zone (31); the AO-type biochemical reactor includes a second sludge returning device (35) for returning the sludge of the AO sludge-water separation zone (33) to the anoxic reaction zone (31).
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