CN213950873U - Recovery system of ammonia nitrogen wastewater and treatment system of nitrogen oxide incineration flue gas - Google Patents
Recovery system of ammonia nitrogen wastewater and treatment system of nitrogen oxide incineration flue gas Download PDFInfo
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- CN213950873U CN213950873U CN202023025257.2U CN202023025257U CN213950873U CN 213950873 U CN213950873 U CN 213950873U CN 202023025257 U CN202023025257 U CN 202023025257U CN 213950873 U CN213950873 U CN 213950873U
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Abstract
Recovery system and nitrogen oxide of ammonia nitrogen waste water burn processing system of flue gas, recovery system includes: the system comprises a pretreatment system, a reinforced stripping system and an ammonia gas collection system; an ultrasonic module and/or a magnetization module are/is arranged in the liquid ammonia strengthening module; the stripping tower is provided with a gas inlet, a stripping outlet and liquid ammonia reinforcementAn ammonia water input end communicated with the module; the stripping output port is connected with the input end of the ammonia gas collecting system and is used for outputting ammonia gas separated from the ammonia nitrogen wastewater to the ammonia gas collecting system; a processing system, comprising: a recovery system and a denitrification reactor; the ammonia gas collecting system is used for introducing ammonia gas into the denitration reactor, so that the ammonia gas and the nitrogen oxide in the incineration system react in the denitration reactor to realize flue gas denitration. The system can realize resource utilization of the ammonia nitrogen wastewater and can recycle NH obtained from the ammonia nitrogen wastewater3Used as a raw material for realizing flue gas denitration of an incineration system.
Description
Technical Field
The utility model relates to a waste recovery technical field especially relates to recovery system and nitrogen oxide of ammonia nitrogen waste water burn processing system of flue gas.
Background
With the rapid development of industrial economy and the accelerated urbanization, the pressure caused by the increased emission of pollutants is enormous. The discharge of a large amount of ammonia nitrogen wastewater into the water body not only causes eutrophication of the water body and black and odorous water body, but also increases the difficulty and cost of water supply treatment and even has toxic action on people and organisms. The influence of ammonia nitrogen wastewater on the environment has led to high attention in the environmental protection field and even in the global scope. According to the report, red tide occurs up to 77 times in 2001 in China's sea area, ammonia nitrogen is one of important causes of pollution, and particularly the pollution caused by high-concentration ammonia nitrogen wastewater is serious. At present, the discharge of a large amount of ammonia nitrogen wastewater becomes an important problem for protecting the ecological environment of water in China, and ammonia nitrogen exceeds COD and becomes a main pollution source of surface water. Therefore, the economic and effective control of the high-concentration ammonia nitrogen wastewater pollution also becomes an important subject and direction of the current water pollution treatment work and research, and is highly valued by the people in the industry.
At present, aiming at the treatment of ammonia nitrogen wastewater, the main research methods in the industry comprise: biological nitrification and denitrification, zeolite adsorption, stripping and stripping, and the like. However, each method has certain limitations in the application stage. If the biological denitrification relates to the culture of tolerant bacteria, the waste water treatment usually takes longer time, and the production efficiency of enterprises is influenced; although zeolite has better adsorption efficiency on ammonia nitrogen, the regeneration and reuse of saturated zeolite is a main problem which limits the use of the saturated zeolite at present; the nitrogen removal by the stripping method is widely applied in industry, but is greatly influenced by reaction conditions such as pH, temperature, gas-liquid ratio or stripping time and the like; the ideal effect of treating the high-concentration ammonia nitrogen wastewater by using a single method is difficult to achieve, and the combined application of a plurality of methods is often needed.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a recovery system of ammonia nitrogen waste water, it blows the ammonia that takes off in the waste water and takes off through pretreatment systems, intensive pressure-sensitive adhesive tape system and ammonia collecting system cooperation to collect in ammonia collecting system.
The utility model discloses still provide a nitrogen oxide burns processing system of flue gas, it includes: and the recovery system and the denitration reactor are used for blowing off ammonia in the wastewater, collecting the ammonia in the ammonia collecting system, and reacting the ammonia with nitrogen oxides.
To achieve the purpose, the utility model adopts the following technical proposal:
a recovery system of ammonia nitrogen waste water includes: the system comprises a pretreatment system, a reinforced stripping system and an ammonia gas collection system;
the pretreatment system, the intensified stripping system and the ammonia gas collecting system are sequentially connected through pipelines;
the pretreatment system is provided with a pH adjusting module; the pH adjusting module has a pH adjusting function and is used for adjusting the pH of the ammonia nitrogen wastewater;
the reinforced stripping system comprises: a liquid ammonia strengthening module and a stripping tower; the liquid ammonia strengthening module, the stripping tower and the ammonia gas collecting system are sequentially connected;
an ultrasonic module and/or a magnetization module are/is arranged in the liquid ammonia strengthening module; the ultrasonic module is used for carrying out ultrasonic treatment on the ammonia nitrogen wastewater; the magnetization module is used for carrying out magnetization treatment on the ammonia nitrogen wastewater;
the stripping tower is provided with a gas inlet, a stripping output port and an ammonia water input end communicated with the liquid ammonia strengthening module, and the gas inlet is used for introducing gas into the stripping tower; the air stripping output port is connected with the input end of the ammonia gas collecting system and is used for outputting ammonia gas separated from the ammonia nitrogen wastewater to the ammonia gas collecting system;
the ammonia gas collecting system is used for collecting ammonia gas.
Preferably, the stripping tower is provided with a packing layer;
the packing layer is arranged below the ammonia water input end; the stripping output port is arranged above the ammonia water input end; the gas inlet is arranged below the packing layer.
Preferably, the pretreatment system is provided with a stirring module and/or a filtering module;
the stirring module is used for stirring and mixing the ammonia nitrogen wastewater;
and the filtering module is used for filtering the ammonia nitrogen wastewater.
Preferably, the method further comprises the following steps: an air output device;
and the output end of the air output device is communicated with the gas inlet and is used for introducing air into the stripping tower.
Preferably, the method further comprises the following steps: a blow-off pump; and the input end of the stripping pump is communicated with the output end of the liquid ammonia strengthening module, and the output end of the stripping pump is communicated with the ammonia water input end.
Preferably, the method further comprises the following steps: a blow-off reflux pipe; and the input end of the stripping return pipe is communicated with the bottom of the stripping tower, and the output end of the stripping return pipe is communicated with a connecting pipeline between the stripping pump and the liquid ammonia strengthening module.
Preferably, the method further comprises the following steps: a pre-treatment output pump; and the input end of the pretreatment output pump is communicated with the output end of the pretreatment system, and the output end of the pretreatment output pump is communicated with the input end of the liquid ammonia strengthening module.
A treatment system for nitrogen oxide incineration flue gas comprises: a recovery system and a denitrification reactor;
the recovery system is the recovery system; the denitration reactor has a heating function;
the output end of the ammonia gas collecting system is communicated with the input end of the denitration reactor and is used for introducing ammonia gas or a mixture of the ammonia gas and air into the denitration reactor, so that the ammonia gas and nitrogen oxides generated in the incineration process react in the denitration reactor.
Preferably, a fan is arranged in the denitration reactor.
Preferably, the denitration reactor comprises: a rotary kiln and a second combustion chamber;
the rotary kiln and the secondary combustion chamber are respectively connected with the ammonia gas collecting system; the rotary kiln and/or the secondary combustion chamber are/is provided with the fan.
The utility model has the advantages that:
1. the recovery system is used for recovering ammonia in the ammonia water waste liquid, effectively reduces the direct discharge of a large amount of ammonia nitrogen waste water into a water body, effectively solves the problems of water eutrophication and water body black and odor caused by waste water, and reduces the difficulty and cost of water supply treatment.
2. This processing system of nitrogen oxide incineration flue gas, the ammonia that can retrieve through recovery system, be arranged in with denitration reactor in the solid waste burns the flue gas nitrogen oxide do the denitration reaction, the ammonia that retrieves can regard as the reduction medicament of denitration reaction, the coprocessing of two kinds of pollutants of NOx in high concentration ammonia nitrogen waste water and the solid waste burns the flue gas has been realized, accord with the theory of "treating waste with the waste", especially in the solid waste treatment garden (sewage, mud, msw incineration power generation) of synthesizing, can be through coprocessing high concentration ammonia nitrogen waste water and msw incineration flue gas NOx pollutant, the scheme rationality has, technical feasibility, can realize resource comprehensive utilization, improve the benefit of retrieving.
Drawings
FIG. 1 is a schematic structural diagram of a treatment system for nitrogen oxide incineration flue gas.
Wherein:
a recovery system 01;
the system comprises a pretreatment system 1, an enhanced stripping system 2 and an ammonia gas collection system 3; an air follower 4; a blow-off pump 5; a reflux removal pipe 6; a denitration reactor 7; a fan 8;
a pH adjusting module 11; a stirring module 12 and a filtering module 13;
a liquid ammonia strengthening module 21 and a stripping tower 22; a filler layer 23;
an ultrasonic module 211 and a magnetization module 212;
a gas inlet 221, a stripping outlet 222 and an ammonia water inlet 223;
rotary kiln 71, second combustion chamber 72.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
Ammonia nitrogen waste water's recovery system 01 includes: the system comprises a pretreatment system 1, an enhanced stripping system 2 and an ammonia gas collection system 3;
the pretreatment system 1, the intensified air stripping system 2 and the ammonia gas collecting system 3 are sequentially connected through pipelines;
the pretreatment system 1 is provided with a pH adjusting module 11; the pH adjusting module 11 has a pH adjusting function and is used for adjusting the pH of the ammonia nitrogen wastewater 02;
the reinforced stripping system 2 comprises: a liquid ammonia strengthening module 21 and a stripping tower 22; the liquid ammonia strengthening module 21, the stripping tower 22 and the ammonia gas collecting system 3 are connected in sequence;
an ultrasonic module 211 and/or a magnetization module 212 are/is arranged in the liquid ammonia strengthening module 21; the ultrasonic module 211 is used for carrying out ultrasonic treatment on the ammonia nitrogen wastewater; the magnetization module 212 is used for carrying out magnetization treatment on the ammonia nitrogen wastewater;
the stripping tower 22 is provided with a gas inlet 221, a stripping outlet 222 and an ammonia water input end 223 communicated with the liquid ammonia strengthening module 21, wherein the gas inlet 221 is used for introducing gas into the stripping tower 22; the stripping output port 222 is connected to the input end of the ammonia gas collecting system 3, and is used for outputting ammonia gas separated from the ammonia nitrogen wastewater to the ammonia gas collecting system 3;
the ammonia gas collecting system 3 is used for collecting ammonia gas.
The recovery system 01 is used for recovering ammonia in the ammonia water waste liquid, effectively reduces the direct discharge of a large amount of ammonia nitrogen waste water into a water body, effectively solves the problems of water eutrophication and water body black and odor caused by waste water, and reduces the difficulty and cost of water supply treatment.
Specifically, a pretreatment system 1, an enhanced stripping system 2 and an ammonia gas collection system 3 are connected in sequence; the pH adjusting module 11 of the pretreatment system 1 can adjust the pH of the ammonia nitrogen wastewater; the ammonia in the wastewater is mainly ammonium ion (NH)+ 4) And free ammonia (NH)3) There are two main forms of transformation relations:
NH3+H2O＝NH+ 4+OH-
the most important factor influencing the existence form of ammonia nitrogen in water can be seen from the reaction relation formula. Volatile NH in wastewater at 25 DEG C3The mass fraction of the total ammonia nitrogen at different pH values is as follows: wNH3＝10pH/(Kb/Kw+10pH) × 100%, wherein: kbIs the ionization constant, K, of the ammonium ionwIs the ionization constant of water. As can be seen from the above formula, the proportion of free ammonia is gradually increased along with the increase of the pH value, when the pH value is increased to more than 11, the ammonia nitrogen in the water almost completely exists in the form of free ammonia, and at the moment, the ammonia gas in the water can be promoted to transfer from the water to the atmosphere by utilizing the physical actions of air stripping and the like, so that the collection of the ammonia gas can be realized.
The liquid ammonia strengthening module 21 is provided with the ultrasonic module 211 and/or the magnetization module 212, so that the stripping effect can be greatly improved, the requirement of stripping on the physicochemical property of ammonia wastewater is reduced, namely the pH of the ammonia nitrogen wastewater does not need to be adjusted to be more than 11, the stripping time can be greatly shortened, and the stripping power input is reduced; for the ultrasonic module 211, ultrasonic waves can not only cause cavitation in water to generate cavitation bubbles and NH3The volatilization and mass transfer effects in water are greatly accelerated, and when the cavitation bubbles collapse and disappear in the water, local high temperature and local high pressure are generated in a tiny space range around the cavitation bubbles, and strong shock waves and microjet flow are generated along with the collapse and disappearance of the cavitation bubbles, so that water molecules are rapidly cracked into strong oxidation free radicals to oxidize organic matters in the water. For the magnetization module 212, after the water is pre-magnetized, some physical parameters of the water may be changed, such as dissolved oxygen, osmotic pressure, volatility, conductivity, pH value, refractive index, etc. are increased, and density, surface tension, evaporation rate, viscosity, etc. are decreased, so that NH is generated3More easily escaping from the water.
After the liquid ammonia strengthening module 21 is output to the stripping tower 22, gas is introduced into the stripping tower 22 through the gas inlet 221, so that the introduced gas is fully distributed in the stripping tower 22 and has the function of lifting up ammonia gas, and the introduced gas can be preferably air; the air fully contacts the ammonia nitrogen wastewater, ammonia in the ammonia nitrogen wastewater is separated from the ammonia nitrogen wastewater, the ammonia is output to the ammonia collecting system 3 from the stripping output port 222, and the waste liquid falls to the lower part of the stripping tower 22, so that the separation of the ammonia and the waste liquid is realized.
The deamination waste water can be returned to the air stripping tower 22 for circular air stripping treatment, and can also be discharged into a sewage subsequent treatment unit for continuous treatment and is discharged after reaching the standard. NH (NH)3Delivering the ammonia gas to an ammonia gas collecting system 3 through a delivery pump, and enabling NH to be acted by a compressor3The pressurized liquefied liquid ammonia is conveyed to an ammonia gas collecting system 3 for storage, and the flue gas denitration reducing agent NH is ensured3Stable storage and continuous supply.
Preferably, the stripping tower 22 is provided with a packing layer 23;
the packing layer 23 is arranged below the ammonia water input end 223; the stripping output port 222 is arranged above the ammonia water input port 223; the gas inlet 221 is disposed below the filler layer 23.
The packing layer 23 is provided to separate the gas inlet 221 and the ammonia water inlet 223, and the gas introduced from the gas inlet 221 contacts the waste liquid through the packing layer 23, and can blow out free ammonia on the surface of the packing layer 23. The filler layer 23 is arranged to limit the contact amount of the gas and the waste liquid so as to further improve the purity of the ammonia gas collected by the ammonia gas collecting system 3; meanwhile, the filler layer 23 can be provided with an alkaline filler, so that ammonia gas is easier to be removed by improving the alkalinity of the wastewater.
It should be noted that the number of the filler layers 23 may be plural; as shown in fig. 1, the number of the packing layers 23 is 2, an ammonia water input port 223 is provided above any one of the packing layers 23, the gas inlet port 221 is provided below the plurality of packing layers 23, and the stripping outlet port 222 is provided above the plurality of packing layers 23.
Preferably, the pretreatment system 1 is provided with a stirring module 12 and/or a filtration module 13;
the stirring module 12 is used for stirring and mixing the ammonia nitrogen wastewater;
and the filtering module 13 is used for filtering the ammonia nitrogen wastewater.
The stirring module 12 can be used for stirring the ammonia nitrogen wastewater, so that ammonia can be fully dissolved in the wastewater, and the ammonia is prevented from being separated from the wastewater at the pretreatment system 1.
The filtering module 13 is used for filtering solid particles in the wastewater to prevent the particles from influencing the subsequent process.
Preferably, the method further comprises the following steps: an air follower 4;
the output end of the air output device 4 is communicated with the gas inlet 221 and is used for introducing air into the stripping tower 22.
According to the scheme, air is preferably introduced into the stripping tower 22, so that the air is easy to obtain; on the other hand, the density of the ammonia gas is lower than that of the air, so that the ammonia gas in the ammonia nitrogen wastewater can be blown out more easily when the air is blown upwards, and the separation of the ammonia gas and the wastewater is realized. In addition, when selecting for use the air, when air and ammonia mix and collect to ammonia collecting system 3, when follow-up denitration reactor 7 that uses, the air can be for the oxygen that provides in the denitration reaction, has realized the multiple utilization of air.
Preferably, the method further comprises the following steps: a blow-off pump 5;
the input end of the stripping pump 5 is communicated with the output end of the liquid ammonia strengthening module 21, and the output end of the stripping pump is communicated with the ammonia water input end 223.
The stripping pump 5 can pump the ammonia nitrogen wastewater in the liquid ammonia strengthening module 21 to the ammonia water input end 223, and directional output of the ammonia nitrogen wastewater is realized.
Preferably, the method further comprises the following steps: a blow-off reflux pipe 6;
the input end of the stripping return pipe 6 is communicated with the bottom of the stripping tower 22, and the output end of the stripping return pipe is communicated with a connecting pipeline between the stripping pump 5 and the liquid ammonia strengthening module 21.
The ammonia nitrogen wastewater in the stripping tower 22 falls to the bottom of the stripping tower 22 after ammonia gas is stripped; at this moment, accessible blowdown pump 5 flows back this part of deamination waste water to blowdown back flow 6, finally exports to the blowdown tower 22 in through aqueous ammonia input 223 again under the effect of blowdown pump 5 in, makes waste water carry out many times deamination and handles, further makes the ammonia in the waste water get rid of completely, makes the ammonia recycle once more in the waste water, reduces a large amount of ammonia nitrogen waste water and directly discharges into the water.
Preferably, the method further comprises the following steps: a pretreatment output pump 9; the input end of the pretreatment output pump is communicated with the output end of the pretreatment system 1, and the output end of the pretreatment output pump is communicated with the input end of the liquid ammonia strengthening module 21.
A treatment system for nitrogen oxide incineration flue gas comprises: a recovery system 01 and a denitration reactor 7;
the recovery system 01 is the recovery system 01 of any of the above embodiments;
the denitration reactor 7 has a heating function, and nitrogen oxide is reserved when the denitration reactor is combusted;
the output end of the ammonia gas collecting system 3 is communicated with the input end of the denitration reactor 7, and is used for introducing ammonia gas or a mixture of ammonia gas and air into the denitration reactor 7, so that the ammonia gas and nitrogen oxide react in the denitration reactor 7.
This processing system of nitrogen oxide incineration flue gas, the ammonia that can retrieve through recovery system 01, be arranged in with denitration reactor 7 in the solid waste burns the flue gas nitrogen oxide do the denitration reaction, the ammonia of retrieving can regard as the reduction medicament of denitration reaction, the coprocessing of two kinds of pollutants of NOx in high concentration ammonia nitrogen waste water and the solid waste burns the flue gas has been realized, accord with the theory of "treating waste with waste", especially in the solid waste treatment garden (sewage, mud, msw incineration power generation) of synthesizing, can be through coprocessing high concentration ammonia nitrogen waste water and msw incineration flue gas pollutant, the scheme rationality has, technical feasibility, can realize resource comprehensive utilization, improve the benefit of retrieving.
The nitrogen oxides and the ammonia gas can be subjected to denitration reaction in the denitration reactor 7, and the flue gas denitration includes SCR denitration and SNCR denitration. SNCR denitration (selective non-catalytic reduction) is to spray a reducing agent such as ammonia water, urea and other solutions into a denitration reactor 7 at 850-1150 ℃ and to thermally decompose NH rapidly from the reducing agent without the action of a catalyst3And reacts with nitrogen oxides in the flue gas to generate N2And H2And O. The method takes a hearth as a denitration reactor 7 and can be realized by modifying a boiler.
In a proper temperature region, the main reaction formula using ammonia water as a reducing agent is as follows:
4NH3+4NO+O2→4N2+6H2O
the denitration efficiency of SNCR flue gas is generally 30-80%, and the denitration efficiency is greatly influenced by the structural size of a boiler. The flue gas denitration process of the SNCR system is completed by the following four basic processes: a receiving and storing reducing agent, b injecting reducing agent at proper position of boiler, c metering out reducing agent, d mixing and diluting with water.
Preferably, a fan 8 is arranged in the denitration reactor 7.
Preferably, the SCR and SNCR are of two different types, each of which, in the presence of ammonia as reducing agent, dissociate to form NH in the incineration system3In the process, NH is easy to appear3The phenomenon of incomplete reduction denitration reaction caused by uneven distribution. The fan 8 is arranged through the rotary kiln 71 and/or the second combustion chamber 72, and NH can be directly distributed through the fan 83The method improves the circulation of the ammonia gas, ensures that the ammonia gas is fully contacted with more nitrogen oxides, and solves the problem of incomplete denitration reaction.
Meanwhile, the burning materials have complex components and often contain partial heavy metals and the like, and NH is distributed from the rotary kiln 713Or the SCR denitration reaction is realized under the catalytic influence of certain special heavy metals in the relatively low-temperature environment of the kiln head, the SNCR denitration of the flue gas can be realized in the relatively high-temperature environment of the middle-rear section of the rotary kiln 71 and the secondary combustion chamber 72, and the thorough denitration of the flue gas is ensured.
Preferably, the denitration reactor 7 includes: a rotary kiln 71 and a secondary combustion chamber 72;
the rotary kiln 71 and the secondary combustion chamber 72 are respectively connected with the ammonia gas collecting system 3; the rotary kiln 71 and/or the secondary combustion chamber 72 are/is provided with the fan 8.
A treatment method of nitrogen oxide incineration flue gas comprises the following steps:
(1) the pretreatment system 1 collects ammonia nitrogen wastewater, adjusts the pH value of the ammonia nitrogen wastewater and outputs the ammonia nitrogen wastewater to the reinforced stripping system 2;
(2) in the liquid ammonia strengthening module 21, ammonia nitrogen wastewater is treated by the ultrasonic module 211 and/or the magnetization module 212 and is output to the stripping tower 22;
(3) when the ammonia nitrogen wastewater is introduced into the stripping tower 22, introducing air into the stripping tower 22 so that ammonia gas in the ammonia nitrogen wastewater is separated from the ammonia nitrogen wastewater after contacting the packing layer 23 of the stripping tower 22, and the ammonia gas is output to the ammonia gas collecting system 3 from the stripping output port 222;
(4) and outputting the ammonia gas collected by the ammonia gas collecting system 3 to a denitration reactor 7, so that the ammonia gas and the nitrogen oxide are subjected to denitration reaction.
The technical principle of the present invention is described above with reference to specific embodiments. The description is made for the purpose of illustrating the principles of the invention and should not be construed in any way as limiting the scope of the invention. Based on the explanations herein, those skilled in the art will be able to conceive of other embodiments of the present invention without any inventive effort, which would fall within the scope of the present invention.
Claims (10)
1. The utility model provides a recovery system of ammonia nitrogen waste water which characterized in that includes: the system comprises a pretreatment system, a reinforced stripping system and an ammonia gas collection system;
the pretreatment system, the intensified stripping system and the ammonia gas collecting system are sequentially connected through pipelines;
the pretreatment system is provided with a pH adjusting module; the pH adjusting module has a pH adjusting function and is used for adjusting the pH of the ammonia nitrogen wastewater;
the reinforced stripping system comprises: a liquid ammonia strengthening module and a stripping tower; the liquid ammonia strengthening module, the stripping tower and the ammonia gas collecting system are sequentially connected;
an ultrasonic module and/or a magnetization module are/is arranged in the liquid ammonia strengthening module; the ultrasonic module is used for carrying out ultrasonic treatment on the ammonia nitrogen wastewater; the magnetization module is used for carrying out magnetization treatment on the ammonia nitrogen wastewater;
the stripping tower is provided with a gas inlet, a stripping output port and an ammonia water input end communicated with the liquid ammonia strengthening module, and the gas inlet is used for introducing gas into the stripping tower; the air stripping output port is connected with the input end of the ammonia gas collecting system and is used for outputting ammonia gas separated from the ammonia nitrogen wastewater to the ammonia gas collecting system;
the ammonia gas collecting system is used for collecting ammonia gas.
2. The recovery system of claim 1, wherein the stripping column is provided with a packing layer;
the packing layer is arranged below the ammonia water input end; the stripping output port is arranged above the ammonia water input end; the gas inlet is arranged below the packing layer.
3. A recovery system according to claim 1, characterized in that the pre-treatment system is provided with a stirring module and/or a filtering module;
the stirring module is used for stirring and mixing the ammonia nitrogen wastewater;
and the filtering module is used for filtering the ammonia nitrogen wastewater.
4. The recycling system according to claim 1, further comprising: an air output device;
and the output end of the air output device is communicated with the gas inlet and is used for introducing air into the stripping tower.
5. The recycling system according to claim 1 or 2, further comprising: a blow-off pump;
and the input end of the stripping pump is communicated with the output end of the liquid ammonia strengthening module, and the output end of the stripping pump is communicated with the ammonia water input end.
6. The recycling system of claim 5, further comprising: a blow-off reflux pipe;
and the input end of the stripping return pipe is communicated with the bottom of the stripping tower, and the output end of the stripping return pipe is communicated with a connecting pipeline between the stripping pump and the liquid ammonia strengthening module.
7. The recycling system according to claim 1, further comprising: a pre-treatment output pump; and the input end of the pretreatment output pump is communicated with the output end of the pretreatment system, and the output end of the pretreatment output pump is communicated with the input end of the liquid ammonia strengthening module.
8. A processing system of nitrogen oxide incineration flue gas, characterized by comprising: a recovery system and a denitrification reactor;
the recovery system is the recovery system of any one of claims 1-7;
the denitration reactor has a heating function;
the output end of the ammonia gas collecting system is communicated with the input end of the denitration reactor and is used for introducing ammonia gas or a mixture of the ammonia gas and air into the denitration reactor, so that the ammonia gas and nitrogen oxides generated in the incineration process react in the denitration reactor.
9. The treatment system of claim 8, wherein a fan is disposed within the denitrification reactor.
10. The treatment system of claim 9, wherein the denitrification reactor comprises: a rotary kiln and a second combustion chamber;
the rotary kiln and the secondary combustion chamber are respectively connected with the ammonia gas collecting system; the rotary kiln and/or the secondary combustion chamber are/is provided with the fan.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116282688A (en) * | 2023-02-28 | 2023-06-23 | 大唐环境产业集团股份有限公司 | System and method for recycling urea hydrolysis wastewater |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116282688A (en) * | 2023-02-28 | 2023-06-23 | 大唐环境产业集团股份有限公司 | System and method for recycling urea hydrolysis wastewater |
| CN116282688B (en) * | 2023-02-28 | 2023-10-27 | 大唐环境产业集团股份有限公司 | System and method for recycling urea hydrolysis wastewater |
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