Nitrogen-containing waste gas treatment equipment considering resource utilization rate and cost

Abstract

The invention relates to the technical field of nitrogen-containing waste gas resourceful treatment, and particularly discloses nitrogen-containing waste gas treatment equipment considering both resource utilization rate and cost, the nitrogen-containing waste gas treatment equipment comprises a first storage tank, and a water outlet of the first storage tank is connected with a first reaction kettle; a liquid outlet of the first reaction kettle is connected with a first absorption tower; a liquid outlet of the first absorption tower is connected with a second reaction kettle, a water outlet of the second reaction kettle is connected with the first storage tank, and a solid product outlet of the second reaction kettle is connected with a second storage tank; an exhaust port of the first absorption tower is connected with a fixed bed reactor; comprising a second absorption tower, and a second atomizer is arranged at the top in the second absorption tower and connected with a third storage tank through a pipeline; a liquid outlet of the second absorption tower is connected with a third reaction kettle, a water outlet of the third reaction kettle is connected with the first storage tank, and a liquid outlet of the third reaction kettle is connected with a fourth storage tank. The method has the characteristics of high resource utilization rate, high waste gas absorption rate and low treatment cost.

Description

Technical Field

[0001] This invention relates to the field of nitrogen-containing waste gas resource utilization treatment technology, and in particular to a nitrogen-containing waste gas treatment device that balances resource utilization rate and cost. Background Technology

[0002] With the rapid industrial development in recent years, the use and consumption of organic nitrogen compounds and inorganic ammonium salts have increased significantly, leading to a larger scale of nitrogen-containing waste gas generation. Chemical production processes produce large quantities of odorous and irritating waste gases, such as ammonia, trimethylamine, formamide, and nitrogen dioxide—typical inorganic ammonia, organic amines, and nitrogen oxides. These large emissions not only pollute the environment but also harm the health of on-site operators, severely hindering the healthy development of the chemical industry. Therefore, nitrogen-containing waste gas has become one of the main targets of pollution control. Currently, physicochemical methods are commonly used to treat this type of waste gas, mainly including adsorption, absorption, thermal destruction, and plasma methods. Adsorption methods often use activated carbon as the adsorption medium. However, while activated carbon has a good adsorption effect on non-polar compounds, its adsorption performance on polar substances (such as methylamine) is poor, resulting in problems such as low adsorption capacity, short breakthrough time, frequent replacement cycles, and high operating costs. Absorption methods are not suitable for intermittent pollutant emissions or large fluctuations in pollution load. Furthermore, the waste liquid after absorption can easily cause secondary pollution. Thermal destruction methods are expensive to operate, making them unaffordable for most companies, and also raise concerns about equipment safety. Plasma technology is a relatively new treatment technology, but it requires significant investment, has low safety, and high operating and maintenance costs. With the decrease in arable land and agricultural population, increasing crop yields through fertilizer application has become a trend in agricultural development. Fertilizers are diverse, and based on their effectiveness, they can be divided into nitrogen fertilizers, potassium fertilizers, phosphate fertilizers, and compound fertilizers. Industrial fertilizer preparation using chemical or biosynthetic techniques suffers from high energy consumption, significant pollution, and large amounts of waste emissions. Therefore, seeking a safe, environmentally friendly, green, and economical fertilizer preparation process is of great significance. The patent application CN106348267A discloses a method for producing diammonium phosphate from nitrogen- and phosphorus-containing wastewater. Specifically, the nitrogen- and phosphorus-containing wastewater generated during the production of monoammonium phosphate (MAP) is fed to a MAP tail gas scrubber as makeup water to wash and absorb the tail gas from the MAP unit. The MAP tail gas scrubbing circulating liquid is then fed to the scrubber and mixed with concentrated phosphoric acid in a specific ratio to absorb dust- and ammonia-containing waste gas from the MAP unit's main line. The concentrated phosphoric acid and scrubber washing liquid are then fed to a tubular reactor storage tank for mixing and acid preparation to achieve the required specific gravity and neutralization degree for the MAP tubular reactor reaction. The appropriately proportioned mixed acid is then fed into the tubular reactor to react with liquid ammonia to generate a slurry, which is then rapidly sprayed into the granulator bed for granulation. While this method utilizes the nitrogen- and phosphorus-containing wastewater generated during the MAP unit's production to produce diammonium phosphate, the issue of disclosing the utilization rate of nitrogen and phosphorus elements in the wastewater remains. Summary of the Invention

[0003] In order to solve the above-mentioned technical problems existing in the treatment of nitrogen-containing waste gas, the present invention provides a nitrogen-containing waste gas treatment device that takes into account both resource utilization and cost. It has the characteristics of high resource utilization, high absorption rate of waste gas and low treatment cost.

[0004] The first technical solution of the present invention: a nitrogen-containing waste gas treatment device that balances resource utilization and cost, comprising: a first storage tank; the drain outlet of the first storage tank is connected to a first reaction vessel via a pipeline; a first temperature control jacket is fitted on the outer circumference of the first reaction vessel; the inlet of the first temperature control jacket is connected to a cooling water source; the drain outlet of the first reaction vessel is connected to a first absorption tower via a pipeline; a first atomizer is provided at the top of the first absorption tower; the first atomizer is connected to the drain outlet of the first reaction vessel via a pipeline; a first gas distributor is provided at the bottom of the first absorption tower; the first gas distributor is connected to a nitrogen-containing waste gas source via a pipeline; a second temperature control jacket is fitted on the outer circumference of the first absorption tower; the inlet of the second temperature control jacket is connected to a cooling water source; the drain outlet of the first absorption tower is connected to a second reaction vessel via a pipeline; the drain outlet of the second reaction vessel is connected to the first storage tank via a pipeline; the solid product outlet of the second reaction vessel is connected to the second storage tank via a pipeline; the exhaust outlet of the first absorption tower is connected to a fixed-bed reactor via a pipeline. The fixed-bed reactor is equipped with an oxygen inlet connected to an oxygen source via a pipeline. The reactor is filled with a solid-phase catalyst. A third temperature-controlled jacket is fitted over the outer periphery of the fixed-bed reactor, and its inlet is connected to a cooling water source via a pipeline. The reactor also includes a second absorption tower. A second gas distributor is located at the bottom of the second absorption tower and is connected to the exhaust port of the fixed-bed reactor via a pipeline. The second gas distributor is also connected to an oxygen source via a pipeline. A second atomizer is located at the top of the second absorption tower and is connected to a third storage tank via a pipeline. The third storage tank is located outside the second absorption tower and contains a potassium hydroxide solution. The exhaust port of the second absorption tower is connected to external air via a pipeline. A fourth temperature-controlled jacket is fitted over the outer periphery of the second absorption tower, and its inlet is connected to a cooling water source. The drain port of the second absorption tower is connected to a third reaction vessel via a pipeline. The drain port of the third reaction vessel is connected to a first storage tank via a pipeline, and the drain port of the third reaction vessel is connected to a fourth storage tank via a pipeline. This invention utilizes a first storage tank to store deionized water for precise dilution of concentrated phosphoric acid solution, a first reaction vessel to prepare the solution from concentrated phosphoric acid to dilute phosphoric acid solution, and a first temperature-controlled jacket fitted onto the outer circumference of the first reaction vessel. Cooling water is used to precisely control the temperature during the preparation of the dilute phosphoric acid solution, quickly dissipating the heat generated during dilution and preventing decomposition of the phosphoric acid solution. Furthermore, this invention employs a first absorption tower to achieve complete absorption of inorganic ammonia from nitrogen-containing waste gas by the dilute phosphoric acid solution. A first atomizer is installed at the top of the first absorption tower to atomize and spray the dilute phosphoric acid solution into the tower, allowing for more thorough contact and reaction between the dilute phosphoric acid solution and the inorganic ammonia in the nitrogen-containing waste gas.By installing a first gas distributor at the bottom of the first absorption tower, the nitrogen-containing waste gas is well distributed within the tower, allowing it to fully react counter-currently with the falling dilute phosphate solution. This enables the dilute phosphate solution to absorb the inorganic ammonia in the nitrogen-containing waste gas, generating an ammonium phosphate solution. A second temperature-controlled jacket is installed on the outer surface of the first absorption tower, using cooling water to precisely control the temperature throughout the counter-current reaction process, ensuring complete absorption of the inorganic ammonia. A second reaction vessel is used to receive the generated ammonium phosphate solution, further separating it into ammonium phosphate solid and water. A second storage tank is used to store the separated ammonium phosphate. Solids are stored in the container; water is recycled to the first storage tank for reuse. Ammonium phosphate solids, used as compound fertilizer, provide a certain economic source for agricultural production, further protecting the environment and improving resource utilization, thus saving resources. The entire process has a relatively fast reaction rate. The dilute phosphate solution has high absorption efficiency for inorganic ammonia in nitrogen-containing waste gas, laying a good foundation for subsequent treatment processes and ensuring that inorganic ammonia in nitrogen-containing waste gas is fully absorbed. This invention uses a fixed-bed reactor to catalytically oxidize reduced nitric oxide in waste gas into nitrogen dioxide gas. By filling the inside of the fixed-bed reactor with a solid-phase catalyst, the oxidation process of reduced nitric oxide is accelerated. By installing a third temperature-controlled jacket on the outer surface of the fixed-bed reactor and using cooling water to precisely control the temperature throughout the catalytic oxidation reaction process, the reduced nitric oxide is more fully converted into nitrogen dioxide gas. The addition of oxygen also pressurizes the entire reaction system, providing online pressure compensation for the gas consumed in the reaction, greatly improving the reaction efficiency of nitric oxide. This invention incorporates a second absorption tower, which, on the one hand, allows the potassium hydroxide solution to absorb the reacted nitrogen dioxide and react it into potassium nitrate solution; on the other hand, it also allows the residual reduced nitric oxide to react again. A second gas distributor is installed at the bottom of the second absorption tower to ensure proper distribution of the mixed gas. Inside the second absorption tower, the falling potassium hydroxide solution can fully react countercurrently, allowing it to absorb nitrogen dioxide from the mixed gas and generate potassium nitrate solution. A second atomizer at the top of the second absorption tower atomizes and sprays the potassium hydroxide solution into the tower, further enhancing its contact and reaction with nitrogen dioxide. A third storage tank stores the potassium hydroxide solution. A fourth temperature-controlled jacket is fitted onto the outer surface of the second absorption tower, using cooling water to precisely control the temperature throughout the reaction process, ensuring more complete absorption of nitrogen dioxide into potassium nitrate solution.Throughout the entire process of introducing nitrogen dioxide gas, oxygen is introduced simultaneously. The oxygen continuously oxidizes the residual nitric oxide in the waste gas, resulting in more thorough treatment. At the same time, the oxygen replaces the waste gas to pressurize the reaction system, providing online pressure compensation for the waste gas consumed in the reaction, greatly improving the absorption efficiency and achieving complete absorption and zero emissions. This invention uses a third reaction vessel to receive the potassium nitrate solution generated after the reaction, further separating the potassium nitrate solution into solid potassium nitrate and water. A fourth storage tank is used to store the separated solid potassium nitrate. The solid potassium nitrate, used as compound fertilizer, effectively saves on subsequent treatment investment costs while further realizing the resource utilization of waste gas.

[0005] Preferably, a first delivery pump and a first back pressure valve are installed on the pipeline between the first storage tank and the first reaction vessel, with the first back pressure valve positioned closer to the first reaction vessel than the first delivery pump. The first delivery pump efficiently delivers deionized water from the first storage tank into the first reaction vessel. The first back pressure valve is interlocked online with a densitometer, allowing for intelligent switching based on the specific concentration of the dilute phosphate solution, thereby accurately preparing the required concentration of the dilute phosphate solution. Preferably, a densitometer is connected to the first reaction vessel, and the densitometer is interlocked online with the first back pressure valve. The densitometer monitors the concentration of the phosphate solution in the first reaction vessel in real time, ensuring the accuracy of the final prepared dilute phosphate solution concentration. Preferably, a second back pressure valve is installed on the pipeline between the inlet of the first temperature control jacket and the cooling water source. A first thermometer is connected to the first reaction vessel, and the first thermometer is interlocked online with the second back pressure valve. The first thermometer monitors the reaction temperature inside the first reaction vessel in real time and adjusts the opening of the second back pressure valve according to the specific temperature conditions, controlling the flow rate of the cooling water to maintain the temperature inside the first reaction vessel within a suitable range.

[0006] Preferably, a second delivery pump and a third back pressure valve are installed on the pipeline between the first reactor and the first absorption tower. The third back pressure valve is closer to the first absorption tower than the second delivery pump. The second delivery pump can efficiently deliver the prepared dilute phosphate solution into the first absorption tower. The third back pressure valve is related to the amount of nitrogen-containing waste gas entering the first absorption tower. The opening of the third back pressure valve is adjusted in real time according to the amount of nitrogen-containing waste gas entering, so that the amount of dilute phosphate solution entering can fully react and absorb the inorganic ammonia in the nitrogen-containing waste gas. Preferably, a third delivery pump and a fourth back pressure valve are installed on the pipeline between the nitrogen-containing waste gas source and the first gas distributor. The fourth back pressure valve is closer to the first absorption tower than the third delivery pump. The third delivery pump can stably deliver the nitrogen-containing waste gas into the first gas distributor. The fourth back pressure valve is interlocked with the third back pressure valve online, so that the amount of nitrogen-containing waste gas entering is adapted to the amount of dilute phosphate solution, allowing the amount of dilute phosphate solution to fully react and absorb the inorganic ammonia in the nitrogen-containing waste gas.

[0007] Preferably, an ammonia detector is connected to the first absorption tower. The ammonia detector can monitor the inorganic ammonia content in the first absorption tower in real time. The ammonia detector is interlocked with the third back pressure valve online. When the ammonia detector shows that the inorganic ammonia content is too high, the opening of the fourth back pressure valve is reduced and the opening of the third back pressure valve is increased, so that more dilute phosphate solution can be used to absorb the inorganic ammonia and control the inorganic ammonia content to be as close to zero as possible.

[0008] Preferably, a fifth back pressure valve is installed on the pipeline between the inlet of the second temperature control jacket and the cooling water source. A second thermometer is connected to the first absorption tower, and the second thermometer is interlocked online with the fourth back pressure valve. The second thermometer can monitor the reaction temperature in the first absorption tower in real time and adjust the opening of the fifth back pressure valve in real time according to the specific temperature conditions. By controlling the flow rate of the cooling water entering the first absorption tower, the temperature in the first absorption tower is controlled within a suitable range. Preferably, a fourth delivery pump and a sixth back pressure valve are installed on the pipeline between the second reactor and the first absorption tower. The fourth delivery pump is closer to the first absorption tower than the sixth back pressure valve. The sixth back pressure valve, the fourth back pressure valve, the ammonia detector, and the third back pressure valve are interlocked online. The fourth delivery pump can effectively deliver the ammonium phosphate solution in the first absorption tower into the second reactor. The sixth back pressure valve is interlocked online with the fourth back pressure valve, the ammonia detector, and the third back pressure valve. When the ammonium phosphate solution in the first absorption tower reaches a certain amount, it can be promptly delivered into the second reactor.

[0009] Preferably, a fifth delivery pump and a seventh back pressure valve are installed on the pipeline between the first storage tank and the drain outlet of the second reactor. The fifth delivery pump is closer to the second reactor than the seventh back pressure valve. The fifth delivery pump can stably deliver the water after vacuum distillation in the second reactor to the first storage tank, allowing the water to be recycled and reused. The seventh back pressure valve can flexibly open and close according to the water volume in the second reactor, thereby ensuring the stable operation of the entire vacuum distillation process in the second reactor. Preferably, an eighth back pressure valve and a sixth delivery pump are installed on the pipeline between the second storage tank and the solid product outlet of the second reactor. The eighth back pressure valve is closer to the second reactor than the sixth delivery pump. The sixth delivery pump can efficiently deliver the ammonium phosphate solid product after vacuum distillation in the second reactor into the second storage tank. The eighth back pressure valve can flexibly open and close according to the amount of ammonium phosphate solid product in the second reactor, thereby ensuring the stable operation of the entire vacuum distillation process in the second reactor. Preferably, a seventh delivery pump and a ninth back pressure valve are installed on the pipeline between the fixed bed reactor and the exhaust outlet of the first absorption tower. The ninth back pressure valve is closer to the fixed bed reactor than the seventh delivery pump. The seventh delivery pump can effectively send the waste gas treated by the first absorption tower into the fixed bed reactor for further reaction. The ninth back pressure valve is interlocked online with the reduced nitrogen detector. The opening degree is adjusted according to the real-time data detected by the reduced nitrogen detector to ensure that the reduced nitrogen in the waste gas entering the fixed bed reactor can be completely oxidized.

[0010] Preferably, an eighth delivery pump and a tenth back pressure valve are installed on the pipeline between the oxygen source and the fixed-bed reactor inlet. The tenth back pressure valve is closer to the fixed-bed reactor than the eighth delivery pump. The eighth delivery pump can stably deliver oxygen into the fixed-bed reactor, thereby completely oxidizing the reduced nitrogen in the fixed-bed reactor. The tenth back pressure valve is interlocked online with the ninth back pressure valve and the reduced nitrogen detector, and can be flexibly adjusted according to the reaction situation and gas pressure in the fixed-bed reactor to ensure that the reduced nitrogen in the waste gas of the fixed-bed reactor can be completely oxidized under stable gas pressure. Preferably, an eleventh back pressure valve is installed on the pipeline between the cooling water source and the third temperature control jacket. A third thermometer is connected to the fixed-bed reactor, and the third thermometer is interlocked online with the eleventh back pressure valve. The third thermometer can monitor the reaction temperature in the fixed-bed reactor in real time and adjust the opening of the eleventh back pressure valve in real time according to the specific temperature situation, thereby controlling the flow rate of the cooling water into the fixed-bed reactor to keep the temperature in the fixed-bed reactor within a suitable range.

[0011] Preferably, a reduced nitrogen detector is connected to the fixed-bed reactor. The reduced nitrogen detector can monitor the reduced nitrogen content in the fixed-bed reactor in real time, ensuring that the reduced nitrogen in the fixed-bed reactor is completely oxidized to nitrogen dioxide. Preferably, a twelfth back pressure valve and a ninth delivery pump are installed on the pipeline between the exhaust port of the fixed-bed reactor and the second gas distributor. The ninth delivery pump is closer to the fixed-bed reactor than the twelfth back pressure valve. The ninth delivery pump can stably deliver nitrogen dioxide from the fixed-bed reactor to the second gas distributor. The twelfth back pressure valve is interlocked online with both the reduced nitrogen detector and the total nitrogen detector. By flexibly adjusting the opening size, it ensures that the nitrogen dioxide entering the second gas distributor is completely absorbed. Preferably, a thirteenth back pressure valve and a tenth delivery pump are installed on the pipeline between the oxygen source and the second gas distributor. The thirteenth back pressure valve is closer to the second gas distributor than the tenth delivery pump. The tenth delivery pump can stably deliver oxygen into the second gas distributor, thereby further and thoroughly oxidizing the residual reduced nitrogen entering the second absorption tower. The thirteenth back pressure valve is interlocked online with the twelfth back pressure valve, the fourteenth back pressure valve and the total nitrogen detector, and can be flexibly adjusted according to the reaction situation and gas pressure in the second absorption tower to ensure that the reduced nitrogen in the second absorption tower can be completely oxidized under stable gas pressure, while nitrogen dioxide can be completely absorbed by potassium hydroxide solution.

[0012] Preferably, an eleventh delivery pump and a fourteenth back pressure valve are installed on the pipeline between the third storage tank and the second atomizer. The fourteenth back pressure valve is closer to the second absorption tower than the eleventh delivery pump. The eleventh delivery pump can stably deliver potassium hydroxide solution into the second atomizer. The fourteenth back pressure valve is interlocked online with the twelfth back pressure valve and the total nitrogen detector, respectively. The amount of potassium hydroxide solution added is controlled by adjusting the opening degree to ensure that nitrogen dioxide in the second absorption tower can be completely absorbed by the potassium hydroxide solution. Preferably, a twelfth delivery pump and a sixteenth back pressure valve are installed on the pipeline between the external air and the exhaust port of the second absorption tower. The twelfth delivery pump is closer to the second absorption tower than the sixteenth back pressure valve. The twelfth delivery pump can stably discharge the treated gas that meets the standards into the external air. The sixteenth back pressure valve is interlocked online with the total nitrogen detector. Gas in the second absorption tower can only be discharged when the total nitrogen content is lower than the set value. Preferably, a fifteenth back pressure valve is installed on the pipeline between the cooling water source and the fourth temperature control jacket, and a fourth thermometer is connected to the second absorption tower. The fourth thermometer is interlocked online with the fifteenth back pressure valve. The fourth thermometer can monitor the reaction temperature in the second absorption tower in real time, and adjust the opening of the fifteenth back pressure valve in real time according to the specific temperature conditions. By controlling the flow rate of the cooling water entering the second absorption tower, the temperature in the second absorption tower is controlled within a suitable range.

[0013] Preferably, a total nitrogen detector is connected to the second absorption tower. The total nitrogen detector, the thirteenth back pressure valve, the fourteenth back pressure valve, the sixteenth back pressure valve, the twelfth back pressure valve, the reduced nitrogen detector, the ninth back pressure valve, and the tenth back pressure valve are interlocked online. The total nitrogen detector can monitor the total nitrogen content in the second absorption tower in real time. Only when the total nitrogen content reaches a first set value is discharge to the air allowed; otherwise, further processing is required until the discharge standard is met. Preferably, a thirteenth delivery pump and a seventeenth back pressure valve are installed on the pipeline between the third reactor and the discharge port of the second absorption tower. The seventeenth back pressure valve is closer to the second absorption tower than the thirteenth delivery pump. The third delivery pump can efficiently deliver the potassium nitrate solution from the second absorption tower into the third reactor. The seventeenth back pressure valve adjusts its opening according to the amount of potassium nitrate solution in the second absorption tower, ensuring timely delivery to the third reactor when the potassium nitrate solution in the second absorption tower reaches a certain level. Preferably, a fifteenth delivery pump and a nineteenth back pressure valve are installed on the pipeline between the first storage tank and the drain outlet of the third reactor. The fifteenth delivery pump is closer to the third reactor than the nineteenth back pressure valve. The fifteenth delivery pump can stably deliver the water after vacuum distillation in the third reactor to the first storage tank, allowing the water to be recycled and reused. The nineteenth back pressure valve can flexibly open and close according to the water volume in the third reactor, thereby ensuring the stable operation of the entire vacuum distillation process in the third reactor.

[0014] Preferably, an eighteenth back pressure valve and a fourteenth transfer pump are installed on the pipeline between the fourth storage tank and the drain port of the third reactor. The eighteenth back pressure valve is closer to the third reactor than the fourteenth transfer pump. The fourteenth transfer pump can efficiently deliver the potassium nitrate solid product after vacuum distillation in the third reactor into the fourth storage tank. The eighteenth back pressure valve can flexibly open and close according to the amount of potassium nitrate solid product in the third reactor, thereby ensuring the stable operation of the entire vacuum distillation process in the third reactor. Preferably, both the first and second absorption towers are equipped with trays. Both the first and second absorption towers are three-stage absorption towers with a diameter of 1000mm to 1200mm and a height of 4000mm to 4200mm. The three-stage absorption towers have better absorption efficiency and can ensure the completeness of the entire absorption process.

[0015] Preferably, the first gas distributor includes an inlet pipe, one end of which penetrates the first absorption tower and is connected to an inlet horizontal pipe. Two sets of inlet branch pipes are symmetrically connected to the outer circumference of the inlet horizontal pipe, and multiple nozzles are connected to the top of each set of inlet branch pipes. The first gas distributor also includes a primary flow splitting component and a secondary flow splitting component. The primary flow splitting component is located above the nozzles, and the secondary flow splitting component is located above the primary flow splitting component. Multiple nozzles can uniformly inject gas into the first absorption tower, allowing for maximum contact and reaction with the atomized dilute phosphoric acid solution, thus improving reaction efficiency. The primary and secondary flow splitting components can better split the gas, increasing the area of ​​uniform gas distribution and ensuring reaction efficiency.

[0016] Preferably, the primary flow splitting assembly includes multiple inverted conical first flow splitters, the number of which is equal to the number of jet nozzles. Each of the first flow splitters is located directly above a plurality of jet nozzles, and adjacent first flow splitters are connected by a first connecting rod. A first fixing ring is connected to the inner wall of the first absorption tower, and the first flow splitter closest to the first fixing ring is connected to the first fixing ring via the first connecting rod. This further splits the gas flow, maximizing reaction efficiency.

[0017] Preferably, the secondary diversion assembly includes multiple liquid storage boxes, the number of which is equal to the number of multiple first diverters. Each liquid storage box is located directly above one of the first diverters. A leakage hole is provided at the bottom of each liquid storage box. Multiple second diverters are connected in a ring shape to the top of each liquid storage box via support rods. Adjacent liquid storage boxes are connected by a second connecting rod. A second fixing ring is slidably connected to the inner wall of the first absorption tower. The liquid storage box closest to the second fixing ring is connected to the second fixing ring via a second connecting rod. When the atomizing nozzle is corroded and damaged, the atomization effect deteriorates. At this time, due to the smaller distribution area, the liquid storage box can receive more dilute phosphoric acid solution in the same amount of time. When the receiving speed exceeds the leakage speed of the leakage hole, the solution in the liquid storage box will increase, thus generating a greater pulling force on the pull rod. When the pulling force on the tension sensor exceeds a set value, it indicates that the atomizing nozzle is severely damaged. Preferably, the distance between the bottom end of the plurality of second diverters on the reservoir and the centerline of the reservoir is greater than the radius of the top surface of the first diverter located directly below the reservoir.

[0018] Preferably, the first atomizer includes multiple liquid delivery pipes equidistantly arranged at the top of the first absorption tower. One end of each liquid delivery pipe passes through the first absorption tower and is rotatably connected to a liquid delivery horizontal pipe. The liquid delivery pipe is connected to the liquid delivery horizontal pipe. Two sets of liquid delivery branch pipes are symmetrically arranged on the outer circumference of the liquid delivery horizontal pipe. Multiple atomizing nozzles are connected to the top and bottom of each set of liquid delivery branch pipes. Solenoid valves are provided on the atomizing nozzles. The atomizer also includes a drive motor and a turntable. The turntable is located inside the first absorption tower and connected to the end of the liquid delivery horizontal pipe. The second drive motor is located outside the first absorption tower and connected to the turntable. The atomization status detection component is also included. The device can uniformly atomize and spray a dilute phosphoric acid solution through multiple atomizing nozzles, ensuring that the solution fully contacts and reacts with the nitrogen-containing waste gas, thus improving the sufficiency and speed of the reaction. The drive motor can rotate the horizontal liquid delivery pipe 180 degrees, allowing a new atomizing nozzle located on the upper side to replace the damaged nozzle on the lower side for atomization spraying. This extends the replacement and maintenance cycle of the atomizing nozzles while ensuring smooth reaction, effectively improving the practicality and reliability of the device. Preferably, the atomization status detection component includes multiple sealed boxes connected in a ring to the inner wall of the first absorption tower. Each sealed box contains a tension sensor with a straight rod. The bottom end of the straight rod penetrates the bottom wall of the sealed box and is connected to a connecting plate. The connecting plate has a pull rod, the bottom end of which is connected to a second fixing ring. The tension sensor is connected to the drive motor via wired or wireless means. The tension sensor is connected to the second fixing ring by a pull rod, which allows it to monitor the weight of the entire secondary diversion assembly. When the amount of dilute phosphoric acid solution in the reservoir increases, the tension value of the tension sensor will increase, thereby enabling it to monitor the atomization effect of the atomizing nozzle and determine whether a new atomizing nozzle needs to be replaced to ensure the smooth progress of the reaction.

[0019] The second technical solution of the present invention: a resource-based treatment method for nitrogen-containing waste gas, comprising the following steps: (a) preparing a dilute phosphoric acid solution; the preparation of the dilute phosphoric acid solution comprises the following steps: (a1) adding an appropriate amount of concentrated phosphoric acid solution to a first reaction vessel; (a2) adding an appropriate amount of deionized water to a first storage tank; (a3) ​​starting the stirrer in the first reaction vessel, adding the deionized water from step (a2) to the first reaction vessel, and diluting the concentrated phosphoric acid solution to obtain a dilute phosphoric acid solution; (b) primary absorption; (b1) inputting the dilute phosphoric acid solution from step (a3) ​​into the first atomizer at the top of the first absorption tower. In step (b1), a dilute phosphoric acid solution is sprayed downwards from the first atomizer; (b2) nitrogen-containing waste gas is transported to the first gas distributor at the bottom of the first absorption tower, and the nitrogen-containing waste gas is dispersed in the first absorption tower by the first gas distributor; (b3) the dilute phosphoric acid solution atomized in step (b1) is reacted countercurrently with the nitrogen-containing waste gas dispersed in step (b2) to generate a first mixed liquid containing a certain concentration of ammonium phosphate; (b4) the first mixed liquid in step (b3) is sent to the second reactor for vacuum distillation to obtain ammonium phosphate solid and water; (b5) the water in step (b4) is returned to the first storage tank and then... (b6) The ammonium phosphate solid from step (b4) is transported to the second storage tank; (c) Catalytic oxidation; (c1) Solid catalyst is filled into the fixed-bed reactor; (c2) The waste gas treated in step (b3) is transported to the fixed-bed reactor in step (c1); (c3) Oxygen is introduced into the fixed-bed reactor in step (c1) and catalytically oxidized with the waste gas from step (c2) in the fixed-bed reactor; (d) Secondary absorption; (d1) The remaining waste gas and oxygen after mixing in step (c3) are transported to the second gas distributor at the bottom of the second absorption tower; (d2) Add an appropriate amount of potassium hydroxide solution to the third storage tank, and input the potassium hydroxide solution in the third storage tank into the second atomizer at the top of the second absorption tower. The potassium hydroxide solution is sprayed and atomized downwards from the second atomizer, reacting countercurrently with the mixed gas in step (d1) to generate a second mixed liquid containing a certain concentration of potassium nitrate; (d3) Send the second mixed liquid into the third reaction vessel, and after vacuum distillation, obtain potassium nitrate solid and water; (d4) Return the water in step (d3) to the first storage tank for reuse; (d5) Transport the potassium nitrate solid in step (d3) to the fourth storage tank. This invention prepares a dilute phosphoric acid solution of the required concentration by first adding a concentrated phosphoric acid solution to the first reaction vessel, and then diluting the concentrated phosphoric acid solution by adding deionized water, precisely controlling the amount of deionized water added;The prepared dilute phosphate solution is atomized and sprayed into the first absorption tower from the top through the first atomizer. The nitrogen-containing waste gas to be treated is dispersed into the first absorption tower from the bottom through the first gas distributor. The nitrogen-containing waste gas rises slowly from bottom to top, while the atomized dilute phosphate solution falls slowly from top to bottom. The dilute phosphate solution and the nitrogen-containing waste gas react countercurrently. The dilute phosphate solution absorbs the inorganic ammonia in the nitrogen-containing waste gas to generate an ammonium phosphate solution. The ammonium phosphate solution is then distilled under reduced pressure to obtain ammonium phosphate solid and water. The water is returned to the first storage tank for reuse. The ammonium phosphate solid, as a compound fertilizer (nitrogen fertilizer + phosphate fertilizer), provides a certain economic source for agricultural production, further protecting the environment, improving resource utilization, and saving resources. This invention utilizes resources, resulting in a rapid reaction rate throughout the process. The dilute phosphoric acid solution exhibits high absorption efficiency for inorganic ammonia in nitrogen-containing waste gas, laying a solid foundation for subsequent treatment processes and ensuring the full absorption of inorganic ammonia. The invention further utilizes a fixed-bed reactor filled with a solid-phase catalyst, into which oxygen is introduced. This catalytic oxidation process converts nitric oxide in the waste gas into nitrogen dioxide, which can then be fully absorbed by the subsequent alkaline solution. The addition of oxygen also pressurizes the entire reaction system, providing online pressure compensation for the consumed gas and significantly improving the reaction efficiency for nitric oxide. Finally, the invention uses a second atomizer to deliver a prepared potassium hydroxide solution from the second absorption tower. The nitrogen dioxide gas to be treated is dispersed from the bottom of the second absorption tower by a second gas distributor. The nitrogen dioxide gas rises slowly from bottom to top, while the atomized potassium hydroxide solution falls slowly from top to bottom. The potassium hydroxide solution and nitrogen dioxide gas react countercurrently, and the potassium hydroxide solution absorbs the nitrogen dioxide gas to produce potassium nitrate solution. The potassium nitrate solution is then distilled under reduced pressure to obtain potassium nitrate solid and water. The water is returned to the first storage tank for reuse, and the potassium nitrate solid is used as a compound fertilizer (nitrogen fertilizer + potassium fertilizer). This effectively saves on subsequent treatment investment costs while further realizing the resource utilization of waste gas. Oxygen is introduced along with the nitrogen dioxide gas throughout the entire process. Oxygen can consistently oxidize residual nitric oxide in the waste gas, resulting in more thorough waste gas treatment. Simultaneously, oxygen replaces the waste gas in the reaction system to pressurize it, providing online pressure compensation for the waste gas consumed in the reaction, greatly improving the absorption efficiency and achieving complete absorption and zero emissions. This invention, through a primary absorption, catalytic oxidation, and secondary absorption process, enables the absorption of nitrogen from the waste gas, ultimately producing ammonium phosphate solids and potassium nitrate solids. These solids can be used as agricultural fertilizers. This treatment of nitrogen-containing waste gas not only avoids harmful secondary products but also yields agricultural waste and water, achieving safe, environmentally friendly, green, and economical treatment of nitrogen-containing waste gas.

[0020] Preferably, the method further includes the following steps: (e) online monitoring; (e1) adjusting the flow rate of deionized water in the first reactor online using a densitometer to control the concentration of the dilute phosphoric acid solution; (e2) adjusting the flow rate of cooling water in the first temperature control jacket outside the first reactor online using a first thermometer to control the temperature inside the first reactor to reach a certain set value; (e3) adjusting the flow rate of cooling water in the second temperature control jacket outside the first absorption tower online using a second thermometer to control the temperature inside the first absorption tower to reach a certain set value; (e4) adjusting the flow rate of cooling water in the fourth temperature control jacket outside the second absorption tower online using a fourth thermometer to control the temperature inside the second absorption tower to reach a certain set value; (e5) adjusting the flow rate of cooling water in the third temperature control jacket outside the fixed-bed reactor online using a third thermometer to control the temperature inside the fixed-bed reactor. The temperature inside the apparatus reaches a certain set value; (e6) An ammonia detector is connected to the first absorption tower in step (b), and the ammonia detector is online interlocked with the third back pressure valve of the dilute phosphate solution. The flow rate of the dilute phosphate solution is adjusted by adjusting the opening of the third back pressure valve online; (e7) A reduced nitrogen detector is connected to the fixed bed reactor in step (c), and the reduced nitrogen detector is online interlocked with the tenth back pressure valve of the oxygen. The flow rate of the oxygen is adjusted by adjusting the opening of the tenth back pressure valve online; (e8) A total nitrogen detector is connected to the second absorption tower in step (d), and the total nitrogen detector is online interlocked with the fourteenth back pressure valve of the potassium hydroxide solution and the thirteenth back pressure valve of the oxygen. The flow rate of the potassium hydroxide solution and the oxygen are adjusted by adjusting the opening of the fourteenth and thirteenth back pressure valves online. By interlocking the first back pressure valve of deionized water online with a densitometer, the flow rate of deionized water is adjusted to achieve precise concentration control of the concentrated phosphoric acid solution diluted into a dilute phosphoric acid solution. By interlocking the second back pressure valve of cooling water online with a first thermometer, the flow rate of cooling water is adjusted online to control the temperature inside the first reactor, allowing for better dilution of the concentrated phosphoric acid solution into a dilute solution. By interlocking the fifth back pressure valve of cooling water online with a second thermometer, the flow rate of cooling water is adjusted online to control the temperature inside the first absorption tower, ensuring that the dilute phosphoric acid solution can effectively treat nitrogen-containing waste gas. After better absorption of inorganic ammonia, an ammonium phosphate solution is generated. The cooling water's fifteenth back pressure valve is interlocked online via a fourth thermometer. By adjusting the opening of the fifteenth back pressure valve online, the cooling water flow rate is regulated, thereby controlling the temperature within the second absorption tower online. This allows the potassium hydroxide solution to better absorb nitrogen dioxide gas, resulting in a potassium nitrate solution. The cooling water's eleventh back pressure valve is interlocked online via a third thermometer. By adjusting the opening of the eleventh back pressure valve online, the cooling water flow rate is regulated, thereby controlling the temperature within the fixed-bed reactor online. This enables the catalytic oxidation of nitric oxide in the waste gas, converting it more efficiently into nitrogen dioxide gas.The ammonia detector is online-interlocked with the third back pressure valve of the dilute phosphate solution. By adjusting the opening of the third back pressure valve online, the flow rate of the dilute phosphate solution is regulated, ensuring that the ammonia content detected by the ammonia detector in the first absorption tower is always within the set value. This guarantees that the inorganic ammonia in the waste gas can be absorbed by the dilute phosphate solution as completely as possible. Similarly, the reduced nitrogen detector is online-interlocked with the tenth back pressure valve of the oxygen system. By adjusting the opening of the tenth back pressure valve online, the oxygen flow rate is regulated, ensuring that the reduced nitrogen content detected by the reduced nitrogen detector in the fixed-bed reactor is always within the set value. This guarantees that the reduced nitrogen in the waste gas... The original nitrogen can be oxidized to nitrogen dioxide by oxygen as completely as possible. The total nitrogen detector is online-interlocked with the fourteenth back pressure valve of the potassium hydroxide solution and the thirteenth back pressure valve of the oxygen. By adjusting the opening of the fourteenth back pressure valve online, the flow rate of the potassium hydroxide solution is regulated, ensuring that the nitrogen dioxide in the second absorption tower is reacted with the potassium hydroxide solution as completely as possible. Similarly, by adjusting the opening of the thirteenth back pressure valve online, the flow rate of oxygen is regulated, ensuring that the reduced nitrogen in the second absorption tower is oxidized to nitrogen dioxide as completely as possible. Overall, the total nitrogen detector detects the total nitrogen content in the second absorption tower. The nitrogen content is consistently maintained at a set value, ensuring that the nitrogen in the exhaust gas is absorbed as completely as possible, guaranteeing that the final discharged gas will not pollute the air. The temperature and nitrogen content in the exhaust gas during the mixing and reaction process are monitored in real time, and the opening of corresponding valves is interlocked. Online thermometers and online interlocking cooling water valves allow for online adjustment of valve openings and cooling water flow, thereby controlling the mixing and reaction temperature online. This precise temperature control during gas mixing and reaction lays a solid foundation for efficient exhaust gas treatment. Online ammonia and nitrogen oxide detectors are used to test the concentration of inorganic ammonia and nitrogen oxides in the reactor in real time. Online interlocking of the first absorption tower, second absorption tower, fixed-bed reactor, dilute phosphate solution, potassium hydroxide solution, and nitrogen-containing exhaust gas valves ensures the controllability of the reaction process by adjusting valve openings online. This successfully achieves high-efficiency and fully closed-loop exhaust gas treatment, ensuring that nitrogen-containing exhaust gas meets emission requirements. It effectively reduces costs and avoids the harm to personnel caused by exhaust gas overflow due to intermittent sampling operations, demonstrating significant practical value and economic benefits.

[0021] Preferably, the process also includes step (f) discharging the waste gas; by observing the reading of the total nitrogen detector in step (e8), it is determined whether the total nitrogen content in the waste gas meets the standard; if the total nitrogen content in the waste gas is lower than the emission standard, the waste gas is discharged into the atmosphere through a pipeline; if the total nitrogen content in the waste gas is higher than the emission standard, the waste gas continues to remain in the second absorption tower, and the sixteenth back pressure valve is closed by the online total nitrogen detector, while the opening of the fourteenth back pressure valve of the potassium hydroxide solution and the thirteenth back pressure valve of the oxygen are increased to continue treatment until the waste gas meets the standard and is discharged into the atmosphere. The total nitrogen detector is online interlocked to the sixteenth back pressure valve, so that the waste gas can only be discharged into the atmosphere through a pipeline when the total nitrogen content in the waste gas is lower than the emission standard. If the total nitrogen content in the waste gas is higher than the emission standard, the nitrogen-containing gaseous compounds in it need to be further treated until they meet the standard before being discharged, thereby ensuring that the finally discharged gas is a gas that will not pollute the air. Preferably, the mass concentration of the concentrated phosphoric acid solution in step (a1) is 50% to 70%. More preferably, the mass concentration of the concentrated phosphoric acid solution in step (a1) is 55% to 65%. More preferably, the mass concentration of the concentrated phosphoric acid solution in step (a1) is 60%. The mass concentration of the concentrated phosphoric acid solution is limited by adjusting the required concentration of the dilute phosphoric acid solution, which is determined by the content of inorganic ammonia in the nitrogen-containing waste gas to be treated. The purpose is to absorb the inorganic ammonia in the nitrogen-containing waste gas as completely as possible into an ammonium phosphate solution.

[0022] Preferably, the temperature of the dilute phosphate solution in step (a3) ​​is 20°C to 40°C. More preferably, the temperature of the dilute phosphate solution in step (a3) ​​is 25°C to 35°C. Even more preferably, the temperature of the dilute phosphate solution in step (a3) ​​is 30°C. This temperature limitation is to allow the concentrated phosphate solution to be better diluted into a dilute phosphate solution. Preferably, the mass concentration of the dilute phosphate solution in step (a3) ​​is 30% to 35%. More preferably, the mass concentration of the dilute phosphate solution in step (a3) ​​is 32% to 34%. Even more preferably, the mass concentration of the dilute phosphate solution in step (a3) ​​is 33%. This limitation on the mass concentration of the dilute phosphate solution is determined based on the content of inorganic ammonia in the nitrogen-containing waste gas to be treated, with the aim of maximizing the absorption of inorganic ammonia in the nitrogen-containing waste gas into an ammonium phosphate solution. Preferably, the flow rate of the dilute phosphate solution in step (b1) is 60 mL / min to 80 mL / min. More preferably, the flow rate of the dilute phosphate solution in step (b1) is 65 mL / min to 75 mL / min. More preferably, the flow rate of the dilute phosphate solution in step (b1) is 70 mL / min. This limitation on the flow rate of the dilute phosphate solution is determined based on the content of inorganic ammonia in the nitrogen-containing waste gas to be treated, which better ensures that the inorganic ammonia in the waste gas can be absorbed as completely as possible by the dilute phosphate solution.

[0023] Preferably, the flow rate of the nitrogen-containing waste gas in step (b2) is 15 mL / min to 25 mL / min. More preferably, the flow rate of the nitrogen-containing waste gas in step (b2) is 18 mL / min to 22 mL / min. Even more preferably, the flow rate of the nitrogen-containing waste gas in step (b2) is 20 mL / min. The flow rate limit for the nitrogen-containing waste gas is determined based on the entire treatment system. Within this flow rate range, the nitrogen-containing waste gas can be completely treated while ensuring a good treatment rate. Preferably, the reaction time in step (b3) is 30 min to 90 min. More preferably, the reaction time in step (b3) is 40 min to 80 min. Even more preferably, the reaction time in step (b3) is 50 min to 70 min. Even more preferably, the reaction time in step (b3) is 55 min to 65 min. Even more preferably, the reaction time in step (b3) is 60 min. The limitation on the reaction time here is to ensure that the inorganic ammonia in the nitrogen-containing waste gas is absorbed as completely as possible into an ammonium phosphate solution, while also considering timeliness. Preferably, the reaction temperature in step (b3) is 30℃~40℃. More preferably, the reaction temperature in step (b3) is 33℃~38℃. Even more preferably, the reaction temperature in step (b3) is 35℃. Within this temperature range, the inorganic ammonia in the nitrogen-containing waste gas can be absorbed more efficiently by the dilute phosphate solution.

[0024] Preferably, the reaction pressure in the step (b3) is 1 MPa to 4 MPa. More preferably, the reaction pressure in the step (b3) is 1.5 MPa to 3.5 MPa. More preferably, the reaction pressure in the step (b3) is 2 MPa to 3 MPa. More preferably, the reaction pressure in the step (b3) is 2.2 MPa to 2.8 MPa. More preferably, the reaction pressure in the step (b3) is 2.5 MPa. Within this reaction pressure range, the inorganic ammonia in the nitrogen-containing waste gas can be more efficiently absorbed by the dilute phosphoric acid solution; wherein the inorganic ammonia in the waste gas can come into contact with the dilute phosphoric acid solution more fully, and thus, while ensuring the absorption effect, the absorption efficiency of the inorganic ammonia in the waste gas is improved. Preferably, the solid-phase catalyst in the step (c1) is a transition metal compound. The transition metal compound can more rapidly catalyze the reaction of the reduced nitrogen in the waste gas into nitrogen dioxide; under the action of the solid-phase catalyst, the nitrogen-containing waste gas and oxygen are catalytically oxidized, achieving the purpose of oxidizing the nitrogen-containing compound into nitrogen oxides. The operation is simple and easy to control. While improving the oxidation treatment efficiency, the treatment cost and energy consumption are also reduced. Preferably, the transition metal compound is at least one of Ce2O3, CeO2, Ce2(CO3)3, xCe2O3∙(1 - x)CuO, Ce-Cu, Ce-Fe, Ce-Mn, Ce-Cr, MnO2, MnO, xMn2O3∙(1 - x)CuO, xMnO∙(1 - x)CuO, Mn3O4, Mn(OH)2, MnCO3, xFe2O3∙(1 - x)MnO2, xFe2O3 ∙(1 - x)CuO, Fe(OH)3, Fe2O3, Fe3O4, CuO, Cu(OH)2, CuMn2O4, Cr2O3, Cr(OH)3, xCr2O3∙(1 - x)CuO, xCr2O3∙(1 - x)MnO2 or CuCr2O4, where 0 < x < 1. The selection of transition metal compounds is relatively diverse, and selecting the defined compounds as catalysts can have a better catalytic effect on the reduced nitrogen in the waste gas.

[0025] Preferably, the particle size of the solid-phase catalyst in step (c1) is 0.25 mm to 10 mm. More preferably, the particle size of the solid-phase catalyst in step (c1) is 0.5 mm to 8 mm. More preferably, the particle size of the solid-phase catalyst in step (c1) is 1 mm to 6 mm. More preferably, the particle size of the solid-phase catalyst in step (c1) is 2 mm to 5 mm. More preferably, the particle size of the solid-phase catalyst in step (c1) is 3 mm to 4 mm. More preferably, the particle size of the solid-phase catalyst in step (c1) is 3.5 mm. Solid-phase catalyst particle sizes within these defined ranges can form a good porosity, thereby achieving a suitable catalytic effect on the reaction. Preferably, the porosity of the fixed-bed reactor after filling with solid-phase catalyst in step (c1) is 30% to 50%. More preferably, the porosity of the fixed-bed reactor after filling with solid-phase catalyst in step (c1) is 35% to 45%. More preferably, the porosity of the fixed-bed reactor after filling with solid catalyst in step (c1) is 40%. A porosity within this defined range ensures good gas passage while also providing a good catalytic effect for the oxidation of reduced nitrogen. Preferably, the fixed-bed reactor contains a solid catalyst support, which is selected from at least one of activated carbon, molecular sieves, or montmorillonite. The selected solid catalyst support effectively supports the solid catalyst, providing a larger contact area between the solid catalyst and the reacting gas, resulting in a better catalytic effect for the rapid degradation of nitrogen-containing waste gas by oxygen.

[0026] Preferably, the flow rate of the waste gas in step (c2) is 20 mL / min to 40 mL / min. More preferably, the flow rate of the waste gas in step (c2) is 25 mL / min to 35 mL / min. Even more preferably, the flow rate of the waste gas in step (c2) is 30 mL / min. This limitation on the waste gas flow rate is determined based on the content of reduced nitrogen in the nitrogen-containing waste gas to be treated, which better ensures that the reduced nitrogen in the waste gas can be catalytically oxidized by oxygen as completely as possible. Preferably, the flow rate of oxygen in step (c3) is 30 mL / min to 60 mL / min. More preferably, the flow rate of oxygen in step (c3) is 35 mL / min to 55 mL / min. Even more preferably, the flow rate of oxygen in step (c3) is 40 mL / min to 50 mL / min. Even more preferably, the flow rate of oxygen in step (c3) is 45 mL / min. The oxygen flow rate limit here is determined based on the content of reduced nitrogen in the nitrogen-containing waste gas to be treated. This ensures that the reduced nitrogen in the waste gas is catalytically oxidized as completely as possible, and also maintains the pressure in the fixed-bed reactor at a good level.

[0027] Preferably, the reaction temperature in step (c3) is 210℃~280℃. More preferably, the reaction temperature in step (c3) is 220℃~270℃. More preferably, the reaction temperature in step (c3) is 230℃~260℃. More preferably, the reaction temperature in step (c3) is 240℃~250℃. More preferably, the reaction temperature in step (c3) is 245℃. Within this temperature range, reduced nitrogen in nitrogen-containing waste gas can be more efficiently catalytically oxidized to nitrogen dioxide by oxygen. Preferably, the reaction pressure in step (c3) is 5MPa~8MPa. More preferably, the reaction pressure in step (c3) is 5.5MPa~7.5MPa. More preferably, the reaction pressure in step (c3) is 6MPa~7MPa. More preferably, the reaction pressure in step (c3) is 6.5MPa. Within this reaction pressure range, reduced nitrogen in nitrogen-containing waste gas can be more efficiently catalytically oxidized by oxygen; this allows the reduced nitric oxide in the waste gas to come into more complete contact with oxygen and catalyst, thereby improving the catalytic oxidation efficiency of reduced nitric oxide in the waste gas while ensuring absorption effect.

[0028] Preferably, the reaction time in step (c3) is 20 min to 60 min. More preferably, the reaction time in step (c3) is 25 min to 55 min. More preferably, the reaction time in step (c3) is 30 min to 50 min. More preferably, the reaction time in step (c3) is 35 min to 45 min. More preferably, the reaction time in step (c3) is 40 min. This limitation on the reaction time is to ensure the most complete catalytic oxidation of reduced nitric oxide in the nitrogen-containing waste gas while also considering timeliness. Preferably, the oxygen flow rate in step (d1) is 40 mL / min to 50 mL / min. More preferably, the oxygen flow rate in step (d1) is 42 mL / min to 47 mL / min. More preferably, the oxygen flow rate in step (d1) is 45 mL / min. The oxygen flow rate limit here is determined based on the content of reduced nitrogen in the nitrogen-containing waste gas to be treated. This ensures that the reduced nitrogen in the waste gas is catalytically oxidized as completely as possible, and also maintains the pressure in the second absorption tower at a good level. Preferably, the waste gas flow rate in step (d1) is 30 mL / min to 60 mL / min. More preferably, the waste gas flow rate in step (d1) is 35 mL / min to 55 mL / min. More preferably, the waste gas flow rate in step (d1) is 40 mL / min to 50 mL / min. More preferably, the waste gas flow rate in step (d1) is 45 mL / min. This limit on the waste gas flow rate is determined based on the content of nitrogen dioxide and residual reduced nitric oxide to be treated. This ensures that the nitrogen dioxide in the waste gas is absorbed as completely as possible, and that the residual reduced nitric oxide in the waste gas is also oxidized to nitrogen dioxide by oxygen before absorption.

[0029] Preferably, the mass concentration of the potassium hydroxide solution in step (d2) is 13% to 18%. More preferably, the mass concentration of the potassium hydroxide solution in step (d2) is 15% to 17%. Even more preferably, the mass concentration of the potassium hydroxide solution in step (d2) is 16%. This limitation on the mass concentration of the potassium hydroxide solution is determined based on the required nitrogen dioxide content to be absorbed, with the aim of maximizing the absorption of nitrogen dioxide into potassium nitrate solution. Preferably, the flow rate of the potassium hydroxide solution in step (d2) is 60 mL / min to 160 mL / min. More preferably, the flow rate of the potassium hydroxide solution in step (d2) is 70 mL / min to 150 mL / min. Even more preferably, the flow rate of the potassium hydroxide solution in step (d2) is 80 mL / min to 140 mL / min. Even more preferably, the flow rate of the potassium hydroxide solution in step (d2) is 90 mL / min to 130 mL / min. More preferably, the flow rate of the potassium hydroxide solution in step (d2) is 100 mL / min to 120 mL / min. More preferably, the flow rate of the potassium hydroxide solution in step (d2) is 105 mL / min to 115 mL / min. More preferably, the flow rate of the potassium hydroxide solution in step (d2) is 110 mL / min. The flow rate limit for the potassium hydroxide solution here is determined based on the required nitrogen dioxide content to be absorbed, with the aim of maximizing the absorption of nitrogen dioxide into potassium nitrate solution.

[0030] Preferably, the reaction temperature in step (d2) is 20°C to 35°C. More preferably, the reaction temperature in step (d2) is 25°C to 30°C. Even more preferably, the reaction temperature in step (d2) is 28°C. Within this temperature range, nitrogen dioxide can be absorbed more efficiently by the potassium hydroxide solution. Preferably, the reaction pressure in step (d2) is 2.5 MPa to 5 MPa. More preferably, the reaction pressure in step (d2) is 3 MPa to 4.5 MPa. Even more preferably, the reaction pressure in step (d2) is 3.5 MPa to 4 MPa. Even more preferably, the reaction pressure in step (d2) is 3.8 MPa. Within this reaction pressure range, nitrogen dioxide can be absorbed more efficiently by the potassium hydroxide solution; wherein nitrogen dioxide can come into more complete contact with the potassium hydroxide solution, thereby improving the absorption efficiency of nitrogen dioxide while ensuring the absorption effect. Preferably, the reaction time in step (d2) is 30 min to 45 min. More preferably, the reaction time in step (d2) is 35 min to 40 min. More preferably, the reaction time in step (d2) is 38 min. This limitation on the reaction time is to ensure that nitrogen dioxide is absorbed into potassium nitrate solution as completely as possible while also considering timeliness. Preferably, the emission standard in step (f) is that the total nitrogen concentration in the exhaust gas does not exceed 5 × 10⁻⁶. -4 mg / L. If the total nitrogen content in nitrogen-containing waste gas is controlled below this standard, it will not cause air pollution.

[0031] The present invention has the following beneficial effects: (1) By setting up a first storage tank to store deionized water for precise dilution of concentrated phosphoric acid solution, by setting up a first reaction vessel to carry out the preparation process from concentrated phosphoric acid solution to dilute phosphoric acid solution, by setting up a first temperature control jacket on the outer periphery of the first reaction vessel, and by using cooling water to precisely control the temperature during the preparation process of dilute phosphoric acid solution, the heat during the dilution process is cooled down as soon as possible to prevent the phosphoric acid solution from decomposing; (2) By setting up a first absorption tower, the dilute phosphoric acid solution can completely absorb inorganic ammonia in nitrogen-containing waste gas; by setting up a first atomizer at the top of the first absorption tower, the dilute phosphoric acid solution is atomized and sprayed from the top of the first absorption tower to the first absorption tower. Inside the first absorption tower, the dilute phosphate solution can react more fully with the inorganic ammonia in the nitrogen-containing waste gas; by setting a first gas distributor at the bottom of the first absorption tower, the nitrogen-containing waste gas is well distributed in the first absorption tower, so that it can be fully reacted with the falling dilute phosphate solution in a countercurrent manner, so that the dilute phosphate solution absorbs the inorganic ammonia in the nitrogen-containing waste gas to generate ammonium phosphate solution; by setting a second temperature control jacket on the outer circumference of the first absorption tower, cooling water is used to precisely control the temperature in the entire countercurrent contact reaction process, so as to ensure the full reaction and absorption of inorganic ammonia; (3) by setting a second reaction vessel to receive the ammonium phosphate solution generated after the reaction, the ammonium phosphate solution is further dissolved. The liquid is separated into ammonium phosphate solid and water; the separated ammonium phosphate solid is stored in a second storage tank; the water is returned to the first storage tank for reuse. The ammonium phosphate solid provides a certain economic source for agricultural production as a compound fertilizer, which not only further protects the environment, but also improves the resource utilization rate and saves resources. The reaction rate of the whole process is relatively fast. The dilute phosphate solution has a high absorption efficiency for inorganic ammonia in nitrogen-containing waste gas, which lays a good foundation for subsequent treatment processes and technology, and ensures that inorganic ammonia in nitrogen-containing waste gas is fully absorbed; (4) the reduced nitric oxide in the waste gas is catalytically oxidized into nitrogen dioxide gas by setting up a fixed bed reactor; the fixed bed reactor The internal solid catalyst is filled to make the oxidation process of reduced nitric oxide faster; by installing a third temperature control jacket on the outer periphery of the fixed bed reactor, cooling water is used to precisely control the temperature of the entire catalytic oxidation reaction process, so that the reduced nitric oxide is more fully converted into nitrogen dioxide gas; the addition of oxygen can also pressurize the entire reaction system, and can compensate the gas consumed in the reaction online, which greatly improves the reaction efficiency of nitric oxide; (5) by setting up a second absorption tower, on the one hand, the potassium hydroxide solution absorbs the nitrogen dioxide after the reaction and becomes potassium nitrate solution, and on the other hand, the residual reduced nitric oxide can be re-reacted;By installing a second gas distributor at the bottom of the second absorption tower, the mixed gas is well distributed within the tower, allowing for sufficient countercurrent contact and reaction with the falling potassium hydroxide solution. This enables the potassium hydroxide solution to absorb nitrogen dioxide from the mixed gas, generating potassium nitrate solution. A second atomizer at the top of the second absorption tower atomizes and sprays the potassium hydroxide solution into the tower, further enhancing its contact and reaction with nitrogen dioxide. A third storage tank stores the potassium hydroxide solution. A fourth temperature-controlled jacket is fitted onto the outer surface of the second absorption tower, using cooling water to precisely control the temperature throughout the reaction process, ensuring more complete and efficient absorption of nitrogen dioxide. The solution is potassium nitrate; oxygen is introduced along with nitrogen dioxide gas throughout the process. Oxygen can always oxidize the residual nitrogen monoxide in the waste gas, making the treatment of the waste gas more thorough. At the same time, oxygen replaces the waste gas to pressurize the reaction system, which can compensate the waste gas consumed by the reaction online, greatly improving the absorption efficiency of the waste gas, and achieving complete absorption and zero emission of the waste gas; (6) A third reaction vessel is set up to receive the potassium nitrate solution generated after the reaction, thereby further separating the potassium nitrate solution into potassium nitrate solid and water; a fourth storage tank is set up to hold the separated potassium nitrate solid; among which, potassium nitrate solid is used as compound fertilizer, which effectively saves the investment cost of subsequent treatment and further realizes the resource treatment of waste gas. Attached Figure Description

[0032] Figure 1 This is a schematic diagram of the process modules of the present invention; Figure 2 yes Figure 3 Enlarged view of point A in the middle; Figure 3 This is a schematic diagram of the structure of the first absorption tower in this invention; Figure 4 yes Figure 3 Enlarged view of point B in the middle; Figure 5 This is a schematic diagram of the structure of the liquid delivery horizontal tube in this invention; Figure 6 This is a schematic diagram of the structure at the second shunt in this invention; Figure 7 This is a schematic diagram of the structure at the first shunt in this invention; Figure 8 This is a schematic diagram of the structure of the horizontal intake pipe in this invention.

[0033] The labels in the attached diagram are as follows: 100-First absorption tower, 101-First atomizer, 1011-Liquid delivery pipe, 1012-Liquid delivery horizontal pipe, 1013-Liquid delivery branch pipe, 1014-Atomizing nozzle, 1015-Drive motor, 1016-Turntable, 1017-Atomization status detection component, 10171-Sealed box, 10172-Tension sensor, 10173-Straight rod, 10174-Connecting plate, 10175-Pull rod, 102-First volume distributor, 1021-Inlet pipe, 1022-Inlet horizontal pipe, 1023-Inlet branch pipe, 1024-Air nozzle, 1025-First-stage diversion component, 10251-First diverter, 10252-First Connecting rod, 10253-First fixing ring, 1026-Secondary diversion assembly, 10261-Liquid storage box, 10262-Leakage hole, 10263-Support rod, 10264-Second diverter, 10265-Second connecting rod, 10266-Second fixing ring, 103-Second temperature control jacket, 104-Third transfer pump, 105-Fourth back pressure valve, 106-Ammonia detector, 107-Fifth back pressure valve, 108-Second thermometer, 109-Fourth transfer pump, 110-Sixth back pressure valve, 111-Seventh transfer pump, 112-Ninth back pressure valve, 200-First storage tank, 300-First reaction vessel, 301-First temperature control jacket, 302-First 303-First back pressure valve, 304-Density meter, 305-Second back pressure valve, 306-First thermometer, 307-Second transfer pump, 308-Third back pressure valve, 400-Second reactor, 401-Fifth transfer pump, 402-Seventh back pressure valve, 403-Eighth back pressure valve, 404-Sixth transfer pump, 500-Second storage tank, 600-Fixed bed reactor, 601-Solid phase catalyst, 602-Third temperature control jacket, 603-Eighth transfer pump, 604-Tenth back pressure valve, 605-Eleventh back pressure valve, 606-Third thermometer, 607-Reduced nitrogen detector, 700-Second absorption tower, 701-Second gas distributor, 70 2-Second atomizer, 703-Fourth temperature control jacket, 704-Twelfth back pressure valve, 705-Ninth delivery pump, 706-Thirteenth back pressure valve, 707-Tenth delivery pump, 708-Eleventh delivery pump, 709-Fourteenth back pressure valve, 710-Twelfth delivery pump, 711-Sixteenth back pressure valve, 712-Fifteenth back pressure valve, 713-Fourth thermometer, 714-Total nitrogen detector, 715-Thirteenth delivery pump, 716-Seventeenth back pressure valve, 800-Third storage tank, 900-Third reaction vessel, 901-Fifteenth delivery pump, 902-Nineteenth back pressure valve, 903-Eighteenth back pressure valve, 904-Fourteenth delivery pump, 1000-Fourth storage tank. Detailed Implementation

[0034] The present invention will be further described below with reference to the accompanying drawings and embodiments, but this should not be construed as limiting the present invention.

[0035] A method for resource-based treatment of nitrogen-containing waste gas includes the following steps: (a) preparing a dilute phosphoric acid solution; the preparation of the dilute phosphoric acid solution includes the following steps: (a1) adding an appropriate amount of concentrated phosphoric acid solution to a first reaction vessel; the mass concentration of the concentrated phosphoric acid solution in step (a1) is 50%–70%; the concentration of the concentrated phosphoric acid solution is adjusted according to the concentration of the dilute phosphoric acid solution; (a2) adding an appropriate amount of deionized water to a first storage tank; (a3) ​​starting the stirrer in the first reaction vessel, adding the deionized water from step (a2) to the first reaction vessel, and diluting the concentrated phosphoric acid solution to obtain the dilute phosphoric acid solution; the temperature of the dilute phosphoric acid solution in step (a3) ​​is 20℃–40℃; the mass concentration of the dilute phosphoric acid solution in step (a3) ​​is 30%–35%;

[0036] (b)Primary absorption; (b1) Input the dilute phosphoric acid solution in step (a3) into the first atomizer at the top of the first absorption tower, and the dilute phosphoric acid solution is sprayed downward and atomized from the first atomizer; the flow rate of the dilute phosphoric acid solution in step (b1) is 60 mL / min to 80 mL / min; (b2) Transport the nitrogen-containing waste gas to the first gas distributor at the bottom of the first absorption tower, and the nitrogen-containing waste gas is dispersed in the first absorption tower by the first gas distributor; the flow rate of the nitrogen-containing waste gas in step (b2) is 15 mL / min to 25 mL / min; (b3) Make the atomized dilute phosphoric acid solution in step (b1) contact and react with the dispersed nitrogen-containing waste gas in step (b2) in countercurrent to generate a first mixed solution containing a certain concentration of ammonium phosphate salt; the reaction time in step (b3) is 30 min to 90 min; the reaction temperature in step (b3) is 30 °C to 40 °C; the reaction pressure in step (b3) is 1 MPa to 4 MPa; so that the nitrogen in the waste gas can contact the dilute phosphoric acid solution more fully, and then, while ensuring the absorption effect, the absorption efficiency of nitrogen in the waste gas is improved; (b4) Send the first mixed solution in step (b3) into the second reaction kettle, and after vacuum distillation, obtain ammonium phosphate salt solid and water; (b5) Return the water in step (b4) to the first storage tank for reuse; (b6) Transport the ammonium phosphate salt solid in step (b4) to the second storage tank; (c) Catalytic oxidation; (c1) Fill the solid-phase catalyst into the fixed-bed reactor; the solid-phase catalyst in step (c1) is a transition metal compound; the transition metal compound is at least one of Ce2O3, CeO2, Ce2(CO3)3, xCe2O3∙(1-x)CuO, Ce-Cu, Ce-Fe, Ce-Mn, Ce-Cr, MnO2, MnO, xMn2O3∙(1-x)CuO, xMnO∙(1-x)CuO, Mn3O4, Mn(OH)2, MnCO3, xFe2O3∙(1-x)MnO2, xFe2O3 ∙(1-x)CuO, Fe(OH)3, Fe2O3, Fe3O4, CuO, Cu(OH)2, CuMn2O4, Cr2O3, Cr(OH)3, xCr2O3∙(1-x)CuO, xCr2O3∙(1-x)MnO2 or CuCr2O4, where 0 < x < 1; the particle size of the solid-phase catalyst in step (c1) is 0.25mm~10mm; the porosity of the fixed-bed reactor after being filled with solid catalyst in step (c1) is 30%~50%. In this process, organic nitrogen-containing waste gas and oxygen are catalytically oxidized under the action of a solid-phase catalyst, achieving the purpose of oxidizing organic nitrogen-containing compounds into nitrogen oxides. The operation is simple and easy to control, improving the oxidation treatment efficiency while reducing the treatment cost and energy consumption. The fixed-bed reactor is equipped with a solid-phase catalyst support, which is selected from at least one of activated carbon, molecular sieve, or montmorillonite. It has a good catalytic effect on the rapid degradation of organic nitrogen-containing waste gas by oxygen. (c2) The waste gas treated in step (b3) is transported to the fixed-bed reactor in step (c1). The flow rate of the waste gas in step (c2) is 20 mL / min to 40 mL / min. (c3) Oxygen is introduced into the fixed-bed reactor in step (c1) and undergoes catalytic oxidation reaction with the waste gas in step (c2) in the fixed-bed reactor. The flow rate of oxygen in step (c3) is 30 mL / min to 60 mL / min. The reaction temperature in step (c3) is 210℃ to 280℃. The reaction pressure in step (c3) is 5 MPa to 8 MPa. The reaction time in step (c3) is 20 min to 60 min; (d) secondary absorption; (d1) the remaining waste gas and oxygen after mixing in step (c3) are transported to the second gas distributor at the bottom of the second absorption tower; the oxygen flow rate in step (d1) is 40 mL / min to 50 mL / min; the waste gas flow rate in step (d1) is 30 mL / min to 60 mL / min; (d2) an appropriate amount of potassium hydroxide solution is added to the third storage tank, and the potassium hydroxide solution in the third storage tank is transported... The potassium hydroxide solution is introduced into the second atomizer at the top of the second absorption tower. It is sprayed downwards and atomized, reacting counter-currently with the mixed gas from step (d1) to generate a second mixed solution containing a certain concentration of potassium nitrate. The mass concentration of the potassium hydroxide solution in step (d2) is 13%–18%. The flow rate of the potassium hydroxide solution in step (d2) is 60 mL / min–160 mL / min. The reaction temperature in step (d2) is 20℃–35℃. The reaction pressure in step (d2) is 2.5MPa~5MPa; the reaction time in step (d2) is 30min~45min; (d3) the second mixture is sent to the third reactor for vacuum distillation to obtain potassium nitrate solid and water; (d4) the water in step (d3) is returned to the first storage tank for reuse; (d5) the potassium nitrate solid in step (d3) is transferred to the fourth storage tank; (e) online monitoring; (e1) the flow rate of deionized water in the first reactor is adjusted online using a densitometer to control the concentration of the dilute phosphoric acid solution; (e2) the flow rate of cooling water in the first temperature control jacket outside the first reactor is adjusted online using a first thermometer to control the concentration of the solution. (e3) The temperature inside the first reactor reaches a certain set value; (e4) The cooling water flow rate inside the second temperature control jacket outside the first absorption tower is adjusted online using the second thermometer to control the temperature inside the first absorption tower to reach a certain set value; (e5) The cooling water flow rate inside the third temperature control jacket outside the fixed bed reactor is adjusted online using the third thermometer to control the temperature inside the fixed bed reactor to reach a certain set value; (e6) An ammonia detector is connected to the first absorption tower in step (b). The ammonia detector is online interlocked with the third back pressure valve of the dilute phosphate solution. The flow rate of the dilute phosphate solution is adjusted by adjusting the opening of the third back pressure valve online. (e7) A reduced nitrogen detector is connected to the fixed bed reactor in step (c). The reduced nitrogen detector is online interlocked with the tenth back pressure valve of the oxygen. The flow rate of the oxygen is adjusted by adjusting the opening of the tenth back pressure valve online. (e8) A total nitrogen detector is connected to the second absorption tower in step (d). The total nitrogen detector is online interlocked with the fourteenth back pressure valve of the potassium hydroxide solution and the thirteenth back pressure valve of the oxygen. The flow rate of the potassium hydroxide solution is adjusted by adjusting the opening of the fourteenth and thirteenth back pressure valves online. Liquid flow rate and oxygen flow rate; (f) Discharge of waste gas; By observing the reading of the total nitrogen detector in step (e8), determine whether the total nitrogen content in the waste gas meets the standard; If the total nitrogen content in the waste gas is lower than the emission standard, the waste gas is discharged into the atmosphere through the pipeline; If the total nitrogen content in the waste gas is higher than the emission standard, the waste gas continues to remain in the second absorption tower, and the sixteenth back pressure valve for venting is closed by the online total nitrogen detector, and the opening of the fourteenth back pressure valve for potassium hydroxide solution and the thirteenth back pressure valve for oxygen is increased to continue treatment until the waste gas meets the standard and is discharged into the atmosphere; The emission standard in step (f) is that the mass concentration of total nitrogen in the waste gas does not exceed 5×10. -4 mg / L.

[0037] like Figure 1The nitrogen-containing waste gas treatment equipment shown considers both resource utilization and cost, including a first storage tank 200. The drain outlet of the first storage tank is connected to a first reaction vessel 300 via a pipeline. A first temperature control jacket 301 is fitted onto the outer circumference of the first reaction vessel, and the inlet of the first temperature control jacket is connected to a cooling water source. The drain outlet of the first reaction vessel is connected to a... Figure 3The first absorption tower 100 shown has a first atomizer 101 at its top, which is connected to the drain port of a first reactor via a pipeline. A first gas distributor 102 is located at the bottom of the first absorption tower and is connected to a nitrogen-containing waste gas source via a pipeline. A second temperature control jacket 103 is fitted onto the outer periphery of the first absorption tower, and its inlet is connected to a cooling water source. The drain port of the first absorption tower is connected to a second reactor 400 via a pipeline, and the drain outlet of the second reactor is connected to a first storage tank via a pipeline. The solid product outlet of the second reactor is connected to a second storage tank 500 via a pipeline. The exhaust port of the first absorption tower is connected to a fixed-bed reactor 600 via a pipeline, and the inlet of the fixed-bed reactor is connected to an oxygen source via a pipeline. The fixed-bed reactor is filled with a solid-phase catalyst 601. A third temperature control jacket 60 is fitted onto the outer periphery of the fixed-bed reactor. 2. The inlet of the third temperature control jacket is connected to a cooling water source via a pipeline; it also includes a second absorption tower 700, with a second gas distributor 701 at the bottom of the second absorption tower, which is connected to the exhaust port of the fixed-bed reactor via a pipeline and to an oxygen source via a pipeline; a second atomizer 702 is installed at the top of the second absorption tower, which is connected to a third storage tank 800 via a pipeline, the third storage tank being located outside the second absorption tower and containing potassium hydroxide solution; the exhaust port of the second absorption tower is connected to the outside air via a pipeline; a fourth temperature control jacket 703 is fitted on the outer circumference of the second absorption tower, with its inlet connected to a cooling water source; the drain port of the second absorption tower is connected to a third reaction vessel 900 via a pipeline, the drain port of the third reaction vessel is connected to a first storage tank via a pipeline, and the drain port of the third reaction vessel is connected to a fourth storage tank 1000 via a pipeline. A first delivery pump 302 and a first back pressure valve 303 are installed on the pipeline between the first storage tank and the first reactor. The first back pressure valve is closer to the first reactor than the first delivery pump. A density meter 304 is connected to the first reactor, and the density meter is interlocked online with the first back pressure valve. A second back pressure valve 305 is installed on the pipeline between the inlet of the first temperature control jacket and the cooling water source. A first thermometer 306 is connected to the first reactor, and the first thermometer is interlocked online with the second back pressure valve. A second delivery pump 304 is installed on the pipeline between the first reactor and the first absorption tower. 07 and the third back pressure valve 308, the third back pressure valve is closer to the first absorption tower than the second delivery pump; the pipeline between the nitrogen-containing waste gas source and the first gas distributor is equipped with a third delivery pump 104 and a fourth back pressure valve 105, the fourth back pressure valve is closer to the first absorption tower than the third delivery pump; an ammonia detector 106 is connected to the first absorption tower; a fifth back pressure valve 107 is installed on the pipeline between the inlet of the second temperature control jacket and the cooling water source; a second thermometer 108 is connected to the first absorption tower, the second thermometer and the fourth back pressure valve are interlocked online;A fourth transfer pump 109 and a sixth back pressure valve 110 are installed on the pipeline between the second reactor and the first absorption tower. The fourth transfer pump is closer to the first absorption tower than the sixth back pressure valve. The sixth back pressure valve, the fourth back pressure valve, the ammonia detector, and the third back pressure valve are interlocked online. A fifth transfer pump 401 and a seventh back pressure valve 402 are installed on the pipeline between the first storage tank and the drain outlet of the second reactor. The fifth transfer pump is closer to the second reactor than the seventh back pressure valve. An eighth back pressure valve 403 and a sixth transfer pump 404 are installed on the pipeline between the second storage tank and the solid product discharge outlet of the second reactor. The eighth back pressure valve is closer to the second reactor than the sixth transfer pump. A fourth back pressure valve 403 and a sixth transfer pump 404 are installed on the pipeline between the fixed bed reactor and the exhaust outlet of the first absorption tower. A seventh delivery pump 111 and a ninth back pressure valve 112 are installed, with the ninth back pressure valve being closer to the fixed-bed reactor than the seventh delivery pump. An eighth delivery pump 603 and a tenth back pressure valve 604 are installed on the pipeline between the oxygen source and the fixed-bed reactor inlet, with the tenth back pressure valve being closer to the fixed-bed reactor than the eighth delivery pump. An eleventh back pressure valve 605 is installed on the pipeline between the cooling water source and the third temperature control jacket. A third thermometer 606 is connected to the fixed-bed reactor, and the third thermometer is interlocked online with the eleventh back pressure valve. A reduced nitrogen detector 607 is connected to the fixed-bed reactor. A twelfth back pressure valve 704 and a ninth delivery pump 705 are installed on the pipeline between the fixed-bed reactor exhaust port and the second gas distributor. The 12th back pressure valve is closer to the fixed-bed reactor than the 12th back pressure valve; a 13th back pressure valve 706 and a 10th transfer pump 707 are installed on the pipeline between the oxygen source and the second gas distributor, with the 13th back pressure valve closer to the second gas distributor than the 10th transfer pump; an 11th transfer pump 708 and a 14th back pressure valve 709 are installed on the pipeline between the third storage tank and the second atomizer, with the 14th back pressure valve closer to the second absorption tower than the 11th transfer pump; a 12th transfer pump 710 and a 16th back pressure valve 711 are installed on the pipeline between the external air and the exhaust port of the second absorption tower, with the 12th transfer pump closer to the second absorption tower than the 16th back pressure valve; a 15th back pressure valve 712 is installed on the pipeline between the cooling water source and the fourth temperature control jacket, and the second absorption... A fourth thermometer 713 is connected to the tower, and the fourth thermometer is interlocked online with the fifteenth back pressure valve; a total nitrogen detector 714 is connected to the second absorption tower, and the total nitrogen detector, the thirteenth back pressure valve, the fourteenth back pressure valve, the sixteenth back pressure valve, the twelfth back pressure valve, the reduced nitrogen detector, the ninth back pressure valve, and the tenth back pressure valve are interlocked online; a thirteenth transfer pump 715 and a seventeenth back pressure valve 716 are installed on the pipeline between the third reactor and the discharge port of the second absorption tower, with the seventeenth back pressure valve being closer to the second absorption tower than the thirteenth transfer pump; a fifteenth transfer pump 901 and a nineteenth back pressure valve 902 are installed on the pipeline between the first storage tank and the discharge port of the third reactor, with the fifteenth transfer pump being closer to the third reactor than the nineteenth back pressure valve;An eighteenth back pressure valve 903 and a fourteenth delivery pump 904 are installed on the pipeline between the fourth storage tank and the drain port of the third reactor. The eighteenth back pressure valve is closer to the third reactor than the fourteenth delivery pump. The first gas distributor includes an inlet pipe 1021, one end of which passes through the first absorption tower and is connected to an inlet horizontal pipe 1022. Two sets of inlet branch pipes 1023 are symmetrically connected to the outer circumference of the inlet horizontal pipe. The top of each set of inlet branch pipes is connected to multiple... Figure 8 The jet nozzle 1024 shown; the first gas distributor also includes, as shown in the figure Figure 4 The primary flow splitter assembly 1025 and the secondary flow splitter assembly 1026 are shown. The primary flow splitter assembly is located above the nozzle, and the secondary flow splitter assembly is located above the primary flow splitter assembly. The primary flow splitter assembly includes multiple inverted conical shapes, such as... Figure 7 The first diverter 10251 shown has the same number of diverters as the number of nozzles. Multiple first diverters are located directly above multiple nozzles, and adjacent first diverters are connected by a first connecting rod 10252. A first fixing ring 10253 is connected to the inner wall of the first absorption tower, and the first diverter near the first fixing ring is connected to the first fixing ring via the first connecting rod. The secondary diverting assembly includes multiple liquid storage boxes 10261, the number of which is equal to the number of first diverters. Multiple liquid storage boxes are located directly above multiple first diverters, and each liquid storage box has a leakage hole 10262 at its bottom. Multiple liquid storage boxes are connected in a ring shape to their tops via support rods 10263. Figure 6 The second distributor 10264 shown has two adjacent liquid storage boxes connected by a second connecting rod 10265. A second fixing ring 10266 is slidably connected to the inner wall of the first absorption tower. The liquid storage box near the second fixing ring is connected to the second fixing ring by the second connecting rod. The distance between the bottom end of the multiple second distributors on the liquid storage box and the center line of the liquid storage box is greater than the top surface radius of the first distributor located directly below the liquid storage box. The second gas distributor has the same structure as the first gas distributor.

[0038] The first atomizer 101 includes a plurality of liquid delivery pipes 1011 equidistantly disposed at the top of the first absorption tower, one end of which passes through the first absorption tower and is rotatably connected to a plurality of liquid delivery pipes such as... Figure 5 The liquid delivery horizontal pipe 1012 shown is connected to the liquid delivery pipe. Two sets of liquid delivery branch pipes 1013 are symmetrically arranged on the outer circumference of the liquid delivery horizontal pipe. Multiple atomizing nozzles 1014 are connected to the top and bottom of both sets of liquid delivery branch pipes. Solenoid valves are installed on the atomizing nozzles. The system also includes a drive motor 1015 and a turntable 1016. The turntable is located inside the first absorption tower and connected to the end of the liquid delivery horizontal pipe. A second drive motor is located outside the first absorption tower and connected to the turntable. Other components include... Figure 2The atomization state detection component 1017 shown includes multiple sealed boxes 10171 connected in a ring to the inner wall of the first absorption tower. Each sealed box contains a tension sensor 10172, with a straight rod 10173 attached to it. The bottom end of the straight rod penetrates the bottom wall of the sealed box and is connected to a connecting plate 10174. A pull rod 10175 is mounted on the connecting plate, with its bottom end connected to a second fixing ring. The tension sensor is connected to a drive motor via wired or wireless means. The second atomizer has the same structure as the first atomizer.

[0039] The working principle of this invention is as follows: After being powered on, gas is injected upward into the first absorption tower 100 and the second absorption tower 700 through the air inlet pipe 1021, the horizontal air inlet pipe 1022, the air inlet branch pipe 1023, and the nozzle 1024. Then, the gas is initially dispersed by the first distributor 10251 directly above the nozzle. The initially dispersed gas then continues to flow upward and collides with multiple second distributors 10264, where it is dispersed again. At this point, the gas is fully and evenly distributed inside the first and second absorption towers. Simultaneously, the solution is atomized and sprayed into the first and second absorption towers through the liquid delivery pipe 1011, the liquid delivery horizontal pipe 1012, the liquid delivery branch pipe 1013, and the atomizing nozzle 1014, until it reacts with the thoroughly dispersed and evenly distributed gas to form a mixed liquid. As the atomizing nozzle 1014 operates for an extended period, it becomes corroded and damaged by the solution. This results in a decreased atomization effect, making it difficult to evenly distribute the dilute phosphoric acid and sodium hydroxide solutions within the first absorption tower 100 and the second absorption tower 700. Consequently, the downward-sprayed solution becomes more concentrated, leading to an increase in the amount of solution falling into the storage box 10261 within the same timeframe. When the velocity of the solution entering the storage box exceeds the velocity of the solution exiting through the drain hole 10262, the amount of solution in the storage box continues to increase, causing the pull rod 1017 to... When the tension of the tension sensor 10172 increases, and the tension reaches the set value, the drive motor 1015 is started, which drives the liquid delivery horizontal pipe 1012 to rotate 180 degrees through the turntable 1016 and the liquid delivery pipe 1011. This causes the brand-new atomizing nozzle that was originally located on the upper side to be put into operation, while the damaged atomizing nozzle rotates to the upper side and closes the solenoid valve on it to stop working. In this way, the replacement and maintenance cycle of the atomizing nozzle can be extended without affecting the atomizing spray effect, which effectively improves the practicality and reliability of the first atomizer and the second atomizer.

[0040] Example 1: A method for resource treatment of nitrogen-containing waste gas, comprising the following steps: (a) preparing a dilute phosphoric acid solution; the preparation of the dilute phosphoric acid solution includes the following steps: (a1) adding an appropriate amount of phosphoric acid concentrated solution with a mass concentration of 50% into the first reaction kettle; (a2) adding an appropriate amount of deionized water into the first storage tank; (a3) starting the stirrer in the first reaction kettle, adding the deionized water in step (a2) into the first reaction kettle, and diluting the phosphoric acid concentrated solution at a temperature of 20 °C to obtain a dilute phosphoric acid solution with a mass concentration of 30%; (b) primary absorption; (b1) inputting the dilute phosphoric acid solution in step (a3) into the first atomizer at the top of the first absorption tower at a flow rate of 60 mL / min, and the dilute phosphoric acid solution is sprayed and atomized downward from the first atomizer; (b2) transporting the nitrogen-containing waste gas to the first gas distributor at the bottom of the first absorption tower at a flow rate of 15 mL / min, and the nitrogen-containing waste gas is dispersed in the first absorption tower by the first gas distributor; (b3) making the atomized dilute phosphoric acid solution in step (b1) and the dispersed nitrogen-containing waste gas in step (b2) contact and react countercurrently at a temperature of 30 °C and a pressure of 1 MPa for 30 min to generate a first mixed solution containing a certain concentration of ammonium phosphate; (b4) sending the first mixed solution in step (b3) into the second reaction kettle, and performing vacuum distillation to obtain ammonium phosphate solid and water; (b5) returning the water in step (b4) to the first storage tank for reuse; (b6) transporting the ammonium phosphate solid in step (b4) to the second storage tank; (c) catalytic oxidation; (c1) filling a solid-phase catalyst into a fixed-bed reactor; the solid-phase catalyst in step (c1) is a transition metal compound; the transition metal compound is at least one of Ce2O3, CeO2, Ce2(CO3)3, xCe2O3∙(1-x)CuO, Ce-Cu, Ce-Fe, Ce-Mn, Ce-Cr, MnO2, MnO, xMn2O3∙(1-x)CuO, xMnO∙(1-x)CuO, Mn3O4, Mn(OH)2, MnCO3, xFe2O3∙(1-x)MnO2, xFe2O3 ∙(1-x)CuO, Fe(OH)3, Fe2O3, Fe3O4, CuO, Cu(OH)2, CuMn2O4, Cr2O3, Cr(OH)3, xCr2O3∙(1-x)CuO, xCr2O3∙(1-x)MnO2 or CuCr2O4, where 0 < x < 1; the particle size of the solid-phase catalyst in step (c1) is 0.25mm; the porosity of the fixed-bed reactor after filling with solid catalyst in step (c1) is 30%. Under the action of solid catalyst, organic nitrogen-containing waste gas and oxygen are catalytically oxidized, realizing the purpose of oxidizing organic nitrogen-containing compounds into nitrogen oxides. The operation is simple and easy to control, improving the oxidation treatment efficiency while reducing the treatment cost and energy consumption; the fixed-bed reactor is equipped with a solid catalyst support, which is selected from at least one of activated carbon, molecular sieve or montmorillonite; the catalytic effect on the rapid degradation of organic nitrogen-containing waste gas by oxygen is good; (c2) the waste gas treated in step (b3) is transported to the fixed-bed reactor in step (c1) at a flow rate of 20mL / min; (c3) oxygen is introduced into the fixed-bed reactor in step (c1) at a flow rate of 30mL / min, and the step (c2) The waste gas in the fixed bed reactor undergoes catalytic oxidation for 20 min at a temperature of 210℃ and a pressure of 5MPa; (d) Secondary absorption; (d1) The remaining waste gas after mixing in step (c3) is transported to the second gas distributor at the bottom of the second absorption tower at a flow rate of 30 mL / min and oxygen at a flow rate of 40 mL / min; (d2) An appropriate amount of potassium hydroxide solution with a mass concentration of 13% is added to the third storage tank, and the potassium hydroxide solution in the third storage tank is fed into the second atomizer at the top of the second absorption tower at a flow rate of 60 mL / min. The potassium hydroxide solution is sprayed and atomized downward from the second atomizer, and mixed with the gas in step (d1) at a temperature of 20℃ and a pressure of 2.The reaction was carried out countercurrently for 30 minutes under a pressure of 5 MPa to generate a second mixture containing a certain concentration of potassium nitrate; (d3) the second mixture was sent to a third reactor for vacuum distillation to obtain solid potassium nitrate and water; (d4) the water from step (d3) was returned to the first storage tank for reuse; (d5) the solid potassium nitrate from step (d3) was transferred to a fourth storage tank; (e) online monitoring; (e1) the flow rate of deionized water in the first reactor was adjusted online using a densitometer to control the concentration of the dilute phosphoric acid solution; (e2) the cooling water flow in the first temperature control jacket outside the first reactor was adjusted online using a first thermometer. (e3) ... The ammonia detector is online interlocked with the third back pressure valve of the dilute phosphate solution. The flow rate of the dilute phosphate solution is adjusted by adjusting the opening of the third back pressure valve online. (e7) A reduced nitrogen detector is connected to the fixed bed reactor in step (c). The reduced nitrogen detector is online interlocked with the tenth back pressure valve of the oxygen. The flow rate of the oxygen is adjusted by adjusting the opening of the tenth back pressure valve online. (e8) A total nitrogen detector is connected to the second absorption tower in step (d). The total nitrogen detector is online interlocked with the fourteenth back pressure valve of the potassium hydroxide solution and the thirteenth back pressure valve of the oxygen. The flow rate of the potassium hydroxide solution is adjusted by adjusting the opening of the fourteenth and thirteenth back pressure valves online. Solution flow rate and oxygen flow rate; (f) Discharge of waste gas; By observing the reading of the total nitrogen detector in step (e8), determine whether the total nitrogen content in the waste gas meets the standard; If the total nitrogen content in the waste gas is lower than the emission standard, the waste gas is discharged into the atmosphere through the pipeline; If the total nitrogen content in the waste gas is higher than the emission standard, the waste gas continues to remain in the second absorption tower, and the sixteenth back pressure valve for venting is closed by the online total nitrogen detector, and the opening of the fourteenth back pressure valve for potassium hydroxide solution and the thirteenth back pressure valve for oxygen is increased to continue treatment until the waste gas meets the standard and is discharged into the atmosphere; The emission standard in step (f) is that the mass concentration of total nitrogen in the waste gas does not exceed 5×10. -4 mg / L.

[0041] Example 2: A method for resource treatment of nitrogen-containing waste gas, comprising the following steps: (a) preparing a dilute phosphoric acid solution; the preparation of the dilute phosphoric acid solution includes the following steps: (a1) adding an appropriate amount of phosphoric acid concentrated solution with a mass concentration of 70% into the first reaction kettle; (a2) adding an appropriate amount of deionized water into the first storage tank; (a3) starting the stirrer in the first reaction kettle, adding the deionized water in step (a2) into the first reaction kettle, and diluting the phosphoric acid concentrated solution at a temperature of 40°C to obtain a dilute phosphoric acid solution with a mass concentration of 35%; (b) primary absorption; (b1) inputting the dilute phosphoric acid solution in step (a3) into the first atomizer at the top of the first absorption tower at a flow rate of 80 mL / min, and the dilute phosphoric acid solution is sprayed and atomized downward from the first atomizer; (b2) transporting the nitrogen-containing waste gas to the first gas distributor at the bottom of the first absorption tower at a flow rate of 25 mL / min, and the nitrogen-containing waste gas is dispersed in the first absorption tower by the first gas distributor; (b3) making the atomized dilute phosphoric acid solution in step (b1) and the dispersed nitrogen-containing waste gas in step (b2) contact and react countercurrently at a temperature of 40°C and a pressure of 4 MPa for 90 min to generate a first mixed solution containing a certain concentration of ammonium phosphate; (b4) sending the first mixed solution in step (b3) into the second reaction kettle, and performing vacuum distillation to obtain ammonium phosphate solid and water; (b5) returning the water in step (b4) to the first storage tank for reuse; (b6) transporting the ammonium phosphate solid in step (b4) to the second storage tank; (c) catalytic oxidation; (c1) filling a solid-phase catalyst into a fixed-bed reactor; the solid-phase catalyst in step (c1) is a transition metal compound; the transition metal compound is at least one of Ce2O3, CeO2, Ce2(CO3)3, xCe2O3∙(1-x)CuO, Ce-Cu, Ce-Fe, Ce-Mn, Ce-Cr, MnO2, MnO, xMn2O3∙(1-x)CuO, xMnO∙(1-x)CuO, Mn3O4, Mn(OH)2, MnCO3, xFe2O3∙(1-x)MnO2, xFe2O3 ∙(1-x)CuO, Fe(OH)3, Fe2O3, Fe3O4, CuO, Cu(OH)2, CuMn2O4, Cr2O3, Cr(OH)3, xCr2O3∙(1-x)CuO, xCr2O3∙(1-x)MnO2 or CuCr2O4, where 0 < x < 1; the particle size of the solid-phase catalyst in step (c1) is 10 mm; the porosity of the fixed-bed reactor after filling the solid-phase catalyst in step (c1) is 50%.The organic nitrogen-containing waste gas and oxygen are catalytically oxidized under the action of a solid-phase catalyst, realizing the oxidation of organic nitrogen-containing compounds into nitrogen oxides. The operation is simple and easy to control, improving the oxidation treatment efficiency while reducing the treatment cost and energy consumption. The fixed-bed reactor is equipped with a solid-phase catalyst support, which is selected from at least one of activated carbon, molecular sieve or montmorillonite. It has a good catalytic effect on the rapid degradation of organic nitrogen-containing waste gas by oxygen. (c2) The waste gas treated in step (b3) is transported to the fixed-bed reactor in step (c1) at a flow rate of 40 mL / min. (c3) Oxygen is introduced into the fixed-bed reactor in step (c1) at a flow rate of 60 mL / min, and the waste gas in step (c2) undergoes catalytic oxidation reaction with the waste gas in step (c2) in the fixed-bed reactor at a temperature of 280℃ and a pressure of 8 MPa for 60 min. (d) Secondary absorption; (d1) The remaining gas after mixing in step (c3) The waste gas is delivered at a flow rate of 60 mL / min, and the oxygen is delivered at a flow rate of 50 mL / min to the second gas distributor at the bottom of the second absorption tower; (d2) An appropriate amount of potassium hydroxide solution with a mass concentration of 18% is added to the third storage tank, and the potassium hydroxide solution in the third storage tank is fed into the second atomizer at the top of the second absorption tower at a flow rate of 160 mL / min. The potassium hydroxide solution is sprayed and atomized downward from the second atomizer and reacts countercurrently with the mixed gas in step (d1) at a temperature of 35°C and a pressure of 5 MPa for 45 min to generate a second mixed liquid containing a certain concentration of potassium nitrate; (d3) The second mixed liquid is sent to the third reaction vessel and distilled under reduced pressure to obtain potassium nitrate solid and water; (d4) The water in step (d3) is returned to the first storage tank for reuse; (d5) The potassium nitrate solid in step (d3) is transported to the fourth storage tank; other contents are partially the same as in Example 1.

[0042] Example 3: A method for resource-based treatment of nitrogen-containing waste gas, comprising the following steps: (a) preparing a dilute phosphoric acid solution; the preparation of the dilute phosphoric acid solution comprises the following steps: (a1) adding an appropriate amount of concentrated phosphoric acid solution with a mass concentration of 60% to the first reaction vessel; (a2) adding an appropriate amount of deionized water to the first storage tank; (a3) ​​starting the stirrer in the first reaction vessel, adding the deionized water from step (a2) to the first reaction vessel, and diluting the concentrated phosphoric acid solution at a temperature of 30°C to obtain a dilute phosphoric acid solution with a mass concentration of 32.5%. (a) Liquid; (b) Primary absorption; (b1) The dilute phosphoric acid solution from step (a3) ​​is fed into the first atomizer at the top of the first absorption tower at a flow rate of 70 mL / min, and the dilute phosphoric acid solution is sprayed and atomized downward from the first atomizer; (b2) The nitrogen-containing waste gas is conveyed to the first gas distributor at the bottom of the first absorption tower at a flow rate of 20 mL / min, and the nitrogen-containing waste gas is dispersed in the first absorption tower by the first gas distributor; (b3) The dilute phosphoric acid solution atomized in step (b1) and the nitrogen-containing waste gas dispersed in step (b2) are mixed together. The reaction was carried out in a countercurrent manner at 35°C and 2.5 MPa for 60 min to generate a first mixture containing a certain concentration of ammonium phosphate; (b4) The first mixture from step (b3) was sent to the second reactor and subjected to vacuum distillation to obtain solid ammonium phosphate and water; (b5) The water from step (b4) was recycled to the first storage tank for reuse; (b6) The solid ammonium phosphate from step (b4) was transferred to the second storage tank; (c) Catalytic oxidation; (c1) Solid catalyst was packed into the fixed bed reactor. In the apparatus; the solid-phase catalyst in step (c1) is a transition metal compound; the transition metal compound is Ce2O3, CeO2, Ce2(CO3)3, xCe2O3∙(1-x)CuO, Ce-Cu, Ce-Fe, Ce-Mn, Ce-Cr, MnO2, MnO, xMn2O3∙(1-x)CuO, xMnO∙(1-x)CuO, Mn3O4, Mn(OH)2, MnCO3, xFe2O3∙(1-x)MnO2, xFe2O3 ∙At least one of (1-x)CuO, Fe(OH)3, Fe2O3, Fe3O4, CuO, Cu(OH)2, CuMn2O4, Cr2O3, Cr(OH)3, xCr2O3∙(1-x)CuO, xCr2O3∙(1-x)MnO2 or CuCr2O4, wherein 0

Claims

1. A nitrogen-containing waste gas treatment device that balances resource utilization and cost, characterized by: It includes a first storage tank (200), the drain outlet of the first storage tank is connected to a first reaction vessel (300) through a pipeline, a first temperature control jacket (301) is fitted on the outer peripheral surface of the first reaction vessel, and the water inlet of the first temperature control jacket is connected to a cooling water source; The drain port of the first reactor is connected to the first absorption tower (100) through a pipeline. The top of the first absorption tower is equipped with a first atomizer (101), which is connected to the drain port of the first reactor through a pipeline. The bottom of the first absorption tower is equipped with a first gas distributor (102), which is connected to a nitrogen-containing waste gas source through a pipeline. A second temperature control jacket (103) is fitted on the outer circumference of the first absorption tower, and the inlet of the second temperature control jacket is connected to a cooling water source. The drain outlet of the first absorption tower is connected to the second reactor (400) via a pipeline, the drain outlet of the second reactor is connected to the first storage tank via a pipeline, and the solid product outlet of the second reactor is connected to the second storage tank (500) via a pipeline. The exhaust port of the first absorption tower is connected to a fixed bed reactor (600) via a pipeline. The inlet of the fixed bed reactor is connected to an oxygen source via a pipeline. The interior of the fixed bed reactor is filled with a solid catalyst (601). A third temperature control jacket (602) is fitted on the outer circumference of the fixed bed reactor. The inlet of the third temperature control jacket is connected to a cooling water source via a pipeline. It also includes a second absorption tower (700), a second gas distributor (701) at the bottom of the second absorption tower, the second gas distributor being connected to the exhaust port of the fixed bed reactor via a pipeline, and the second gas distributor being connected to an oxygen source via a pipeline; a second atomizer (702) at the top of the second absorption tower, the second atomizer being connected to a third storage tank (800) via a pipeline, the third storage tank being located outside the second absorption tower, and the third storage tank containing potassium hydroxide solution; the exhaust port of the second absorption tower being connected to the outside air via a pipeline; a fourth temperature control jacket (703) being fitted on the outer circumference of the second absorption tower, the inlet of the fourth temperature control jacket being connected to a cooling water source; The drain outlet of the second absorption tower is connected to the third reaction vessel (900) via a pipeline. The drain outlet of the third reaction vessel is connected to the first storage tank via a pipeline. The drain outlet of the third reaction vessel is connected to the fourth storage tank (1000) via a pipeline.

2. The nitrogen-containing waste gas treatment equipment according to claim 1, which balances resource utilization and cost, is characterized in that: The first gas distributor includes an inlet pipe (1021), one end of which passes through the first absorption tower and is connected to an inlet horizontal pipe (1022). Two sets of inlet branch pipes (1023) are symmetrically connected on the outer circumferential surface of the inlet horizontal pipe. The top of each set of inlet branch pipes is connected to multiple jet nozzles (1024). The first gas distributor also includes a primary flow splitting assembly (1025) and a secondary flow splitting assembly (1026). The primary flow splitting assembly is located above the jet nozzles, and the secondary flow splitting assembly is located above the primary flow splitting assembly.

3. The nitrogen-containing waste gas treatment equipment according to claim 2, which balances resource utilization and cost, is characterized in that: The primary diversion assembly includes multiple inverted conical first diverters (10251), the number of which is equal to the number of nozzles. The multiple first diverters are located directly above the multiple nozzles, and adjacent first diverters are connected by a first connecting rod (10252). A first fixing ring (10253) is connected to the inner wall of the first absorption tower, and the first diverter near the first fixing ring is connected to the first fixing ring by the first connecting rod. The secondary diversion assembly includes multiple liquid storage boxes (10261), the number of which is equal to the number of multiple first diverters. The multiple liquid storage boxes are located directly above the multiple first diverters. Each liquid storage box has a leakage hole (10262) at its bottom. Multiple second diverters (10264) are connected to the top of the liquid storage box in a ring shape by a support rod (10263). Adjacent liquid storage boxes are connected by a second connecting rod (10265). A second fixing ring (10266) is slidably connected to the inner wall of the first absorption tower. The liquid storage box near the second fixing ring is connected to the second fixing ring by the second connecting rod.

4. The nitrogen-containing waste gas treatment equipment according to claim 3, which balances resource utilization and cost, is characterized in that: The distance between the bottom of the multiple second distributors on the liquid storage box and the centerline of the liquid storage box is greater than the radius of the top surface of the first distributor located directly below the liquid storage box.

5. The nitrogen-containing waste gas treatment equipment according to claim 3, which balances resource utilization and cost, is characterized in that: The first atomizer includes multiple liquid delivery pipes (1011) equidistantly arranged at the top of the first absorption tower. One end of each liquid delivery pipe passes through the first absorption tower and is rotatably connected to a liquid delivery horizontal pipe (1012). The liquid delivery pipe is connected to the liquid delivery horizontal pipe. Two sets of liquid delivery branch pipes (1013) are symmetrically arranged on the outer circumference of the liquid delivery horizontal pipe. Multiple atomizing nozzles (1014) are connected to the top and bottom of the two sets of liquid delivery branch pipes. Solenoid valves are provided on the atomizing nozzles.

6. The nitrogen-containing waste gas treatment equipment according to claim 5, which balances resource utilization and cost, is characterized in that: It also includes a drive motor (1015) and a turntable (1016), the turntable being located inside the first absorption tower and connected to the end of the liquid delivery horizontal pipe, and the drive motor being located outside the first absorption tower and connected to the turntable.

7. The nitrogen-containing waste gas treatment equipment according to claim 6, which balances resource utilization and cost, is characterized in that: It also includes an atomization state detection component (1017); the atomization state detection component includes multiple sealed boxes (10171) connected in a ring on the inner side wall of the first absorption tower, each sealed box is equipped with a tension sensor (10172), the tension sensor is equipped with a straight rod (10173), the bottom end of the straight rod penetrates the bottom wall of the sealed box and is connected to a connecting plate (10174), the connecting plate is equipped with a pull rod (10175), the bottom end of the pull rod is connected to a second fixing ring, and the tension sensor is connected to the drive motor by wired or wireless means.

8. The nitrogen-containing waste gas treatment equipment according to claim 1, which balances resource utilization and cost, is characterized in that: A first delivery pump (302) and a first back pressure valve (303) are provided on the pipeline between the first storage tank and the first reactor. The first back pressure valve is closer to the first reactor than the first delivery pump. A densitometer (304) is connected to the first reactor. The densitometer is interlocked online with the first back pressure valve. A second back pressure valve (305) is provided on the pipeline between the inlet of the first temperature control jacket and the cooling water source. A first thermometer (306) is connected to the first reactor. The first thermometer is interlocked online with the second back pressure valve. A second delivery pump (307) and a third back pressure valve (308) are provided on the pipeline between the first reactor and the first absorption tower. The third back pressure valve is closer to the first absorption tower than the second delivery pump.

9. The nitrogen-containing waste gas treatment equipment according to claim 1, which balances resource utilization and cost, is characterized in that: A third delivery pump (104) and a fourth back pressure valve (105) are provided on the pipeline between the nitrogen-containing waste gas source and the first gas distributor. The fourth back pressure valve is closer to the first absorption tower than the third delivery pump. An ammonia detector (106) is connected to the first absorption tower. A fifth back pressure valve (107) is provided on the pipeline between the inlet of the second temperature control jacket and the cooling water source. A second thermometer (108) is connected to the first absorption tower. The second thermometer and the fourth back pressure valve are interlocked online. A fourth delivery pump (109) and a sixth back pressure valve (110) are provided on the pipeline between the second reactor and the first absorption tower. The fourth delivery pump is closer to the first absorption tower than the sixth back pressure valve. The sixth back pressure valve, the fourth back pressure valve, the ammonia detector, and the third back pressure valve are interlocked online.

10. The nitrogen-containing waste gas treatment equipment according to claim 1, which balances resource utilization and cost, is characterized in that: A fifth transfer pump (401) and a seventh back pressure valve (402) are installed on the pipeline between the drain outlets of the first storage tank and the second reactor. The fifth transfer pump is closer to the second reactor than the seventh back pressure valve. An eighth back pressure valve (403) and a sixth transfer pump (404) are installed on the pipeline between the solid product outlets of the second storage tank and the second reactor. The eighth back pressure valve is closer to the second reactor than the sixth transfer pump. A seventh transfer pump (111) and a ninth back pressure valve (112) are installed on the pipeline between the fixed bed reactor and the exhaust outlet of the first absorption tower. The ninth back pressure valve is closer to the fixed bed reactor than the seventh delivery pump; the pipeline between the oxygen source and the air inlet of the fixed bed reactor is equipped with an eighth delivery pump (603) and a tenth back pressure valve (604), the tenth back pressure valve being closer to the fixed bed reactor than the eighth delivery pump; the pipeline between the cooling water source and the third temperature control jacket is equipped with an eleventh back pressure valve (605), a third thermometer (606) is connected to the fixed bed reactor, the third thermometer being interlocked online with the eleventh back pressure valve; a reduced nitrogen detector (607) is connected to the fixed bed reactor.

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