Energy-saving treatment system and process method for high-cod high-ammonia-nitrogen wastewater

Abstract

The application discloses an energy-saving treatment system and process method for high-COD and high-ammonia-nitrogen wastewater, and relates to the field of high-concentration wastewater treatment. The system comprises a booster pump, a preheating device, an oxidation device and a deamination device, wherein the devices are connected through a pipe network, the oxidation device comprises an oxidation tower, a steam drum for storing steam generated by oxidation reaction residual heat in the oxidation tower, and an oxidation liquid transfer tank for storing oxidation liquid flowing out of the oxidation tower, and the steam drum and the oxidation liquid transfer tank are connected with the deamination device. The technical scheme of the application recycles and utilizes the heat generated in the oxidation stage, reduces the steam consumption required in the subsequent deamination process, realizes quantitative removal of high-COD, ammonia-nitrogen purification and reuse, and increases the economic benefits of enterprises.

Description

Technical Field

[0001] This invention relates to the field of high-concentration wastewater treatment, and more specifically, to an energy-saving treatment system and process for high-COD and high-ammonia-nitrogen wastewater. Background Technology

[0002] High-COD and high-ammonia-nitrogen wastewater mainly originates from industrial wastewater in petrochemical, pharmaceutical, and metallurgical industries. High-COD wastewater refers to wastewater with a Chemical Oxygen Demand (COD) concentration exceeding a certain threshold. It's an indicator used to measure the organic matter content in wastewater, representing the amount of chemical oxidant required for the oxidation and decomposition of organic matter. Generally, wastewater with a COD concentration exceeding 1000 mg / L can be considered high-COD wastewater. High-ammonia-nitrogen wastewater refers to wastewater with an ammonia nitrogen (AM) concentration exceeding a certain threshold. Generally, wastewater with an AM Nitrogen concentration exceeding 6000-8000 ppm can be considered high-ammonia-nitrogen wastewater. Direct discharge of large amounts of high-COD and high-ammonia-nitrogen wastewater into water bodies not only causes eutrophication and black, foul-smelling water, but also poses toxic effects on humans and other organisms. Therefore, researching and developing economical, practical, and safe methods for treating high-salinity and high-ammonia-nitrogen wastewater has become an important current issue, significant for environmental protection and human well-being.

[0003] Currently, common technologies for removing ammonia-containing wastewater include biochemical methods, air stripping, steam stripping, breakpoint chlorination, ion exchange, chemical precipitation, and membrane separation. For treating high-concentration ammonia nitrogen wastewater (500–10000 ppm) generated in industry, steam stripping is typically used. Steam stripping uses steam to convert free ammonia in the wastewater into ammonia gas, which then escapes. Steam stripping is suitable for treating high-concentration ammonia nitrogen wastewater, achieving a removal rate of over 99%, demonstrating high efficiency and technological maturity. However, traditional steam stripping ammonia removal technologies consume a large amount of steam, resulting in high energy consumption per unit of wastewater treated. Summary of the Invention

[0004] To address the shortcomings of the prior art, this invention provides two technical solutions.

[0005] The first technical solution is to provide an energy-saving treatment system for high COD and high ammonia nitrogen wastewater. The energy-saving treatment system of the present invention recovers and utilizes the excess heat generated in the high temperature and high pressure oxidation reaction stage, reduces the consumption of live steam required in the subsequent ammonia removal process, and can realize the quantitative removal of high COD and the purification and reuse of ammonia nitrogen, thereby increasing the economic benefits of enterprises.

[0006] To achieve the above objectives, the present invention provides the following technical solution: an energy-saving treatment system for high COD and high ammonia nitrogen wastewater, comprising: a booster pump for pressurizing and transporting raw water, a preheating device for preheating the raw water transported from the booster pump, an oxidation device for oxidizing the preheated raw water, and an ammonia removal device for removing ammonia from the oxidized liquid after the oxidation reaction. The above devices are connected by a pipeline network. The oxidation device includes an oxidation tower, a steam boiler for storing steam generated from the waste heat of the oxidation reaction in the oxidation tower, and an oxidation liquid transfer tank for storing the oxidized liquid flowing out of the oxidation tower. The steam boiler and the oxidation liquid transfer tank are connected to the ammonia removal device.

[0007] By adopting the above technical solution, the energy-saving treatment system includes a booster pump, a preheating device including a raw water preheater and a thermal oil preheater, an oxidation device, and a deammoniation device, all connected by a pipeline network. High-COD, high-ammonia-nitrogen wastewater is pumped into the raw water preheater by the booster pump, then heated by the thermal oil preheater before entering the oxidation tower. Simultaneously, oxygen is introduced. The high-COD, high-ammonia-nitrogen wastewater undergoes a vigorous oxidation reaction under high temperature and high pressure in the oxidation tower, reducing the wastewater's COD. On one hand, this reaction generates a large amount of waste heat steam, which is stored in a steam drum and used for the next ammonia removal process on the batch of high-ammonia-nitrogen wastewater, significantly saving the consumption of live steam during the ammonia removal process and achieving the effect of heat energy recovery. On the other hand, the raw water obtained after the oxidation reaction of the oxidized liquid, which contains a large amount of heat energy, is again sent to the raw water preheater to preheat the new batch of high-COD, high-ammonia-nitrogen wastewater, fully utilizing the wastewater's waste heat and achieving excellent energy-saving effects.

[0008] The second technical solution provides a process method for an energy-saving treatment system for high-COD and high-ammonia-nitrogen wastewater. This method combines the oxidation and ammonia removal processes in the treatment of high-COD and high-ammonia-nitrogen wastewater, saving on live steam consumption during ammonia removal and enabling heat energy reuse. By effectively degrading COD and comprehensively utilizing ammonia nitrogen, it reduces operating costs and increases economic benefits for enterprises. To achieve the above objectives, this invention provides the following technical solution: a process method for an energy-saving treatment system for high-COD and high-ammonia-nitrogen wastewater, comprising the following steps:

[0009] a. High COD and high ammonia nitrogen wastewater is sent to the raw water preheater. The high temperature and high pressure wastewater that reacts with the oxidation tower is separated by the oxidation balance tank and then exchanged with the wastewater gas-liquid gas through rapid cooling. After that, it enters the heat transfer oil preheater for further heating.

[0010] b. After being heated by the heat transfer oil preheater, the wastewater enters from the bottom of the oxidation tower. At the same time, oxygen is introduced into the oxidation tower through the oxygen distributor, which ensures that the oxygen is fully mixed with the high COD and high ammonia nitrogen wastewater.

[0011] c. The high-temperature and high-pressure wastewater after the oxidation tower reaction is cooled to 50-60℃ after heat exchange in the raw water preheater and the heat transfer oil preheater.

[0012] d. The high-temperature and high-pressure steam generated by the oxidation tower is condensed by the tail gas condenser to obtain saturated steam, which is then fed into the steam drum through a pipeline;

[0013] e. Steam from the steam bunker is piped into the bottom heater of the tower to heat the high ammonia nitrogen wastewater to 120°C, and then the wastewater is deamed by the ammonia removal tower.

[0014] f. The ammonia gas after ammonia removal from the ammonia removal tower is cooled by an ammonia condenser. After cooling, the wastewater enters the second gas-liquid separator for gas-liquid separation, thereby recovering the more concentrated ammonia water.

[0015] g. The exhaust gas from the second gas-liquid separator enters the steam compressor for steam compression, increasing the steam outlet temperature;

[0016] h. The steam compressed by the steam compressor is then sent to the bottom heater of the tower to reheat the high ammonia nitrogen wastewater.

[0017] By adopting the above technical solution, the process method combines the oxidation process and the deammoniation process in the treatment of high COD and high ammonia nitrogen wastewater. The steam generated after the reaction in the deammoniation tower is compressed and reheated by the steam boiler input and steam compressor and sent back to the input, saving the consumption of live steam in the deammoniation process. The waste heat steam generated by oxidation and the heat energy of high temperature oxidation liquid are reused. On the basis of achieving effective degradation of COD and comprehensive utilization of ammonia nitrogen, the operating cost is reduced and the economic benefits of enterprises are increased.

[0018] The present invention is further configured such that the preheating device includes a raw water preheater and a heat transfer oil preheater.

[0019] Preferably, both the raw water preheater and the thermal oil preheater are heat exchangers.

[0020] Preferably, the raw water preheater is located between the oxidation tower and the oxidation liquid transfer tank, so that the oxidation liquid flowing out of the oxidation tower enters the raw water preheater and the oxidation liquid transfer tank in sequence, thereby preheating the raw water flowing through the raw water preheater.

[0021] The oxidized liquid flowing out of the oxidation tower after the oxidation reaction has a large amount of residual heat, which is injected sequentially into the raw water preheater and the oxidized liquid transfer tank to preheat the raw water flowing through the raw water preheater.

[0022] The present invention is further configured such that: an oxidation liquid cooler is provided in front of the oxidation liquid transfer tank for reducing the temperature of the oxidation liquid flowing out of the oxidation tower.

[0023] The present invention is further configured such that the oxidation tower is also connected to an oxygen distributor that fully mixes oxygen with the preheated raw water.

[0024] The present invention is further configured such that: the ammonia removal device includes an ammonia removal tower for removing ammonia from the steam package and the material in the oxidation liquid transfer tank, an ammonia condenser for condensing the ammonia removed from the ammonia removal tower, and a steam compressor connected to the ammonia condenser and / or the steam package for compressing the steam and reheating it for sending it back to the ammonia removal tower.

[0025] Oxidizing liquid and steam are the reactants in the deammoniation process. The oxidizing liquid flows into the deammoniation tower through the oxidation tower, raw water preheater, oxidizing liquid cooler and oxidizing liquid transfer tank. There are three sources of steam: live steam from the external pipeline network, steam from the steam drum and steam from the steam compressor. The latter two types of steam input can save on the live steam consumption in the deammoniation process.

[0026] Preferably, the deammoniation tower further includes a bottom heater disposed at its bottom.

[0027] The present invention is further configured such that a first gas-liquid separator and a tail gas condenser are provided between the oxidation tower and the steam package.

[0028] In summary, compared with the prior art, the above-described technical solutions conceived by this invention can achieve the following beneficial effects:

[0029] 1. The high-temperature and high-pressure oxidation reaction that occurs in the oxidation tower generates a large amount of heat energy. This reaction is accompanied by the generation of a large amount of waste heat steam and high-temperature oxidizing liquid. The waste heat steam is passed into a steam boiler for storage and used for the continued ammonia removal of this batch of wastewater. This can save the consumption of live steam during the ammonia removal process and achieve the effect of continuing to reuse heat energy. In addition, the high-temperature oxidizing liquid is passed back into the raw water preheater to preheat the new batch of wastewater.

[0030] 2. The high-concentration ammonia water obtained from the ammonia removal reaction in the deammoniation tower is reheated by a steam compressor and sent back to the bottom heater of the tower, realizing the recycling of steam. Combined with the oxidation unit, this significantly reduces the consumption of live steam. The technical and economic comparison of this energy-saving treatment system for high-COD, high-ammonia nitrogen wastewater with traditional deammoniation units is shown in the table below:

[0031]

[0032] 3. This energy-saving treatment system can effectively degrade COD and comprehensively utilize ammonia nitrogen in high COD and high ammonia nitrogen wastewater, resulting in low operating costs and increased economic benefits for enterprises. Attached Figure Description

[0033] Appendix Figure 1 This is a flowchart of the process flow of the present invention;

[0034] Appendix Figure 2 This is a schematic diagram of the system structure of the present invention;

[0035] The labels in the diagram represent the following: 1. Booster pump; 2-1. Raw water preheater; 2-2. Heat transfer oil preheater; 2-3. Oxidation liquid cooler; 3. Oxidation liquid pressure reducing separator; 4. Oxidation liquid transfer tank; 5. Oxidation liquid transfer pump; 6. Oxidation balance tank; 7. Oxidation tower; 7-1. Oxygen distributor; 8. First gas-liquid separator; 9-1. Tail gas condenser; 9-2. Tail gas cooler; 10. Steam drum; 11. Water circulation tank; 11-1. Water circulation pump; 12. Ammonia removal outlet pump; 13. Ammonia removal tower; 14. Condensate tank; 15. Condensate discharge pump; 16. Ammonia water reflux pump; 17. Ammonia condenser; 18. Second gas-liquid separator; 19. Steam compressor; 20. Tower bottom heater; 21. Vacuum pump. Detailed Implementation

[0036] The specific embodiments of the present invention are described in detail below with reference to the accompanying drawings, so that those skilled in the art can more clearly understand how to practice the present invention. Although the present invention has been described in conjunction with its preferred embodiments, these embodiments are merely illustrative and not intended to limit the scope of the invention.

[0037] like Figure 1 , Figure 2 As shown, an energy-saving treatment system for high COD and high ammonia nitrogen wastewater includes a booster pump 1 for pressurizing and transporting raw water.

[0038] A preheating device for preheating the raw water delivered from the booster pump 1, the preheating device including a raw water preheater 2-1 and a heat transfer oil preheater 2-2, both of which are heat exchangers;

[0039] An oxidation device is used to oxidize preheated raw water. The reactants of the oxidation device are high-COD and high-ammonia nitrogen wastewater that has been pressurized and preheated by booster pump 1 and preheating device, as well as liquid oxygen input from the outside. The oxidation tower 7 is connected to an oxygen distributor 7-1 that fully mixes oxygen with preheated raw water. To ensure that the reactant oxygen does not react with the oxygen distributor 7-1, the oxygen distributor 7-1 is made of titanium alloy with ceramic lining.

[0040] The oxidation device mainly includes an oxidation tower 7, where the reaction products have two flow directions. It includes a steam package 10 for storing steam generated from the waste heat of the oxidation reaction in the oxidation tower 7, and an oxidation liquid transfer tank 4 for storing the oxidation liquid flowing out of the oxidation tower 7.

[0041] The raw water preheater 2-1 is located between the oxidation tower 7 and the oxidation liquid transfer tank 4, so that the oxidation liquid flowing out of the oxidation tower 7 enters the raw water preheater 2-1 and the oxidation liquid transfer tank 4 in sequence, thereby preheating the raw water flowing through the raw water preheater 2-1. An oxidation liquid cooler 2-3 is also provided in front of the oxidation liquid transfer tank 4 to reduce the temperature of the oxidation liquid flowing out of the oxidation tower 7, so as to cool down the high temperature oxidation liquid.

[0042] A first gas-liquid separator 8 and a tail gas condenser 9-1 are also provided between the oxidation tower 7 and the steam package 10 to separate and condense the gas and liquid products after the oxidation reaction.

[0043] An ammonia removal device for removing ammonia from oxidized liquid after oxidation reaction includes an ammonia removal tower 13 for removing ammonia from materials in steam package 10 and oxidized liquid transfer tank 4, an ammonia condenser 17 for condensing ammonia removed from the ammonia removal tower 13, and a steam compressor 19 connected to the ammonia condenser 17 and / or steam package 10 for compressing and reheating the steam and sending it back to the ammonia removal tower 13. Oxidized liquid and steam are the reactants in the ammonia removal process. The oxidized liquid flows into the ammonia removal tower 13 through the oxidation tower 7, raw water preheater 2-1, oxidized liquid cooler 2-3 and oxidized liquid transfer tank 4. There are three sources of steam: live steam input from the external pipeline network, steam input from steam package 10 and steam compressor 19. The latter two types of steam input can save the live steam consumption in the ammonia removal process.

[0044] The ammonia removal tower 13 also includes a bottom heater 20 disposed at its bottom;

[0045] The steam compressor 19 compresses and reheats the deammoniation-treated steam and sends it back to the bottom heater 20 at the bottom of the deammoniation tower 13. The remaining cleaner wastewater is discharged through the deammoniation effluent pump 12.

[0046] In addition, such as Figure 2 An oxidation liquid pressure reducing separator 3 is connected between the raw water preheater 2-1 and the oxidation liquid cooler 2-3. The oxidation liquid transfer tank 4 transports the cooled oxidation liquid to the deammoniation unit via the oxidation liquid transfer pump 5. An oxidation balance tank 6 is also provided in the middle of the pipeline from the oxidation tower 7 to the raw water preheater 2-1 after the oxidation reaction. The first gas-liquid separator 8 is also connected to a tail gas cooler 9-2 to transport the condensate after the oxidation reaction to the oxidation liquid transfer tank 4. The tail gas condenser 9-1 is also provided with a water circulation device including a water circulation tank 11 and a water circulation pump 11-1. The tower bottom heater 20 is also connected in sequence to a condensate tank 14 and a condensate discharge pump 15 to discharge the condensed steam. The deammoniation tower 13 is also connected to an ammonia water reflux pump 16, an ammonia condenser 17, and a second gas-liquid separator 18 to realize the gas-liquid separation and reflux of steam during the deammoniation process. The steam compressor 19 is also provided with a vacuum pump 21.

[0047] The above-mentioned devices are connected through a pipeline network and various valves on the pipeline network.

[0048] In summary, the wastewater energy-saving treatment system and process of the present invention are as follows:

[0049] Oxidation Process: High-COD, high-ammonia-nitrogen wastewater is pumped into raw water preheater 2-1 via booster pump 1, then heated in heat transfer oil preheater 2-2 before entering oxidation tower 7. Oxygen is simultaneously introduced. The high-COD, high-ammonia-nitrogen wastewater undergoes a vigorous oxidation reaction under high temperature and pressure in oxidation tower 7, reducing the wastewater's COD. On one hand, this reaction generates a large amount of waste heat steam, which is stored in steam package 10 and used for the next ammonia removal process on this batch of high-ammonia-nitrogen wastewater, significantly saving the consumption of live steam during ammonia removal and achieving heat energy recovery. On the other hand, the raw water obtained after the oxidation reaction of the oxidized liquid, which contains a large amount of heat energy, is again sent to raw water preheater 2-1 to preheat new batches of high-COD, high-ammonia-nitrogen wastewater, fully utilizing the wastewater's waste heat and achieving excellent energy-saving effects.

[0050] Deammoniation process: Oxidizing liquid and steam are the reactants in the deammoniation process. The oxidizing liquid flows into the deammoniation tower through the oxidation tower 7, the raw water preheater 2-1, the oxidizing liquid cooler 2-3 and the oxidizing liquid transfer tank 4. There are three sources of steam: live steam input from the external pipeline network, steam input from the steam package 10 and steam compressor 19, which compresses and reheats the steam generated after the reaction in the deammoniation tower 13 and sends it back to the input. The latter two types of steam input can save the live steam consumption in the deammoniation process.

[0051] Operating method of wastewater energy-saving treatment system: a. High COD and high ammonia nitrogen wastewater is sent to raw water preheater 2-1. After the high temperature and high pressure wastewater reacting with oxidation tower 7 is separated by oxidation balance tank 6, it is rapidly cooled and exchanged with wastewater gas and liquid before entering heat transfer oil preheater 2-2 for further heating.

[0052] b. After being heated by the heat transfer oil preheater 2-2, the wastewater enters from the bottom of the oxidation tower 7. At the same time, oxygen is introduced into the oxidation tower 7 through the oxygen distributor 7-1, which fully mixes the oxygen with the high COD and high ammonia nitrogen wastewater.

[0053] c. The high-temperature and high-pressure wastewater after the reaction in oxidation tower 7 is cooled to 50-60℃ after heat exchange with raw water preheater 2-1 and heat transfer oil preheater 2-2.

[0054] d. The high-temperature and high-pressure steam generated by the oxidation tower 7 is condensed by the tail gas condenser 9-1 to obtain saturated steam, which is then fed into the steam drum 10 through a pipeline;

[0055] e. Steam from steam package 10 is fed into bottom heater 20 via pipeline to heat the high ammonia nitrogen wastewater to 120°C, and then the wastewater is deamed by ammonia removal tower 13.

[0056] f. The ammonia gas after ammonia removal in the ammonia removal tower 13 is cooled by the ammonia condenser 17. After cooling, the wastewater enters the second gas-liquid separator 18 for gas-liquid separation, thereby recovering the more concentrated ammonia water.

[0057] g. The exhaust gas from the second gas-liquid separator 18 enters the steam compressor 19 for steam compression, thereby increasing the steam outlet temperature;

[0058] h. The steam compressed by the steam compressor 19 is then sent to the bottom heater 20 to reheat the high ammonia nitrogen wastewater.

[0059] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the invention by those skilled in the art. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the invention should be included within the scope of protection of the invention.

Claims

1. An energy-saving treatment system for high COD and high ammonia nitrogen wastewater, characterized in that, include: A booster pump (1) for pressurizing and transporting raw water, a preheating device for preheating the raw water transported from the booster pump (1), an oxidation device for oxidizing the preheated raw water, and an ammonia removal device for removing ammonia from the oxidized liquid after the oxidation reaction are connected by a pipeline network. The oxidation device includes an oxidation tower (7), a steam package (10) for storing the steam generated from the waste heat of the oxidation reaction in the oxidation tower (7), and an oxidation liquid transfer tank (4) for storing the oxidized liquid flowing out of the oxidation tower (7). The steam package (10) is used to... The oxidation liquid transfer tank (4) is connected to the deammoniation device; the deammoniation device includes a deammoniation tower (13) for deammoniating the steam package (10) and the materials in the oxidation liquid transfer tank (4), an ammonia condenser (17) for condensing the ammonia gas removed from the deammoniation tower (13), and a steam compressor (19) connected to the ammonia condenser (17) and / or the steam package (10) for compressing the steam and reheating it to send it back to the deammoniation tower (13); the deammoniation tower (13) also includes a bottom heater (20) located at its bottom.

2. The energy-saving treatment system for high COD and high ammonia nitrogen wastewater according to claim 1, characterized in that: The preheating device includes a raw water preheater (2-1) and a heat transfer oil preheater (2-2).

3. The energy-saving treatment system for high COD and high ammonia nitrogen wastewater according to claim 2, characterized in that: Both the raw water preheater (2-1) and the thermal oil preheater (2-2) are heat exchangers.

4. The energy-saving treatment system for high COD and high ammonia nitrogen wastewater according to claim 2, characterized in that: The raw water preheater (2-1) is located between the oxidation tower (7) and the oxidation liquid transfer tank (4), so that the oxidation liquid flowing out of the oxidation tower (7) enters the raw water preheater (2-1) and the oxidation liquid transfer tank (4) in sequence, thereby preheating the raw water flowing through the raw water preheater (2-1).

5. The energy-saving treatment system for high COD and high ammonia nitrogen wastewater according to any one of claims 1-4, characterized in that: An oxidizing liquid cooler (2-3) is also provided in front of the oxidizing liquid transfer tank (4) to reduce the temperature of the oxidizing liquid flowing out of the oxidizing tower (7).

6. The energy-saving treatment system for high COD and high ammonia nitrogen wastewater according to any one of claims 1-4, characterized in that: The oxidation tower (7) is also connected to an oxygen distributor (7-1) that thoroughly mixes oxygen with the preheated raw water.

7. The energy-saving treatment system for high COD and high ammonia nitrogen wastewater according to any one of claims 1-4, characterized in that: A first gas-liquid separator (8) and a tail gas condenser (9-1) are also provided between the oxidation tower (7) and the steam package (10).

8. A process method for treating high-COD, high-ammonia nitrogen wastewater using the energy-saving system according to any one of claims 1-7, characterized in that, Includes the following steps: a. High COD and high ammonia nitrogen wastewater is sent to the raw water preheater (2-1). The high temperature and high pressure wastewater that reacts with the oxidation tower (7) is separated by the oxidation balance tank (6) and then rapidly cooled and heated by the wastewater gas-liquid exchange before entering the heat transfer oil preheater (2-2) for further heating. b. After the heat transfer oil preheater (2-2) heats the wastewater, it enters from the bottom of the oxidation tower (7). At the same time, oxygen is introduced into the oxidation tower (7) through the oxygen distributor (7-1). The oxygen distributor (7-1) makes the oxygen fully mixed with the high COD and high ammonia nitrogen wastewater. c. The high-temperature and high-pressure wastewater after the reaction in the oxidation tower (7) is cooled to 50-60℃ after heat exchange with the raw water preheater (2-1) and the heat transfer oil preheater (2-2); d. The high-temperature and high-pressure steam generated by the oxidation tower (7) is condensed by the tail gas condenser (9-1) to obtain saturated steam, which is then fed into the steam drum (10) through a pipeline. e. Steam from the steam package (10) is fed into the bottom heater (20) of the tower through a pipeline to heat the high ammonia nitrogen wastewater to a temperature of 120°C, and then deammoniated through the deammoniation tower (13); f. The ammonia gas after ammonia removal (13) is cooled by the ammonia condenser (17). After cooling, the wastewater enters the second gas-liquid separator (18) for gas-liquid separation, thereby recovering the more concentrated ammonia water. g. The exhaust gas from the second gas-liquid separator (18) enters the steam compressor (19) for steam compression to increase the steam outlet temperature; h. The steam compressed by the steam compressor (19) is then sent to the bottom heater (20) to reheat the high ammonia nitrogen wastewater.

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