Ammonia-containing wastewater and LSR wastewater treatment system

Abstract

The utility model relates to the technical field of wastewater treatment, and provides an ammonia-containing wastewater and LSR wastewater treatment system which comprises a heat exchanger, and a first pH regulating tank, an inclined plate sedimentation tank, a second pH regulating tank and an ammonia nitrogen stripping system which are communicated in sequence, the second pH regulating tank is communicated with a liquid inlet of the ammonia nitrogen stripping system through a wastewater conveying pipe; a liquid outlet of the ammonia nitrogen stripping system is connected with a drain pipe; the waste water conveying pipe is connected with the heat exchanger as a cold source, and the drainage pipe is connected with the heat exchanger as a heat source. The wastewater treatment system provided by the utility model can prevent the pipeline of the heat exchanger from being blocked in the treatment process.

Description

Technical Field

[0001] The utility model relates to the technical field of wastewater treatment, in particular to a treatment system for ammonia-containing wastewater and LSR wastewater. Background Art

[0002] The scrubber washing wastewater of the machine tool is recycled to the machine tool as washing water after removing cations and anions through the 3B3T process. Among them, in addition to the high ammonia nitrogen concentration in the regenerated wastewater of the 3B3T cation tower (which needs to be discharged after being treated in the ammonia nitrogen stripping system), the metal ions Ca 2+ , Fe 3+ also have relatively high contents. The pH of this wastewater is acidic, and metal ions will dissolve in the wastewater under acidic conditions. Before the regenerated wastewater of the cation tower enters the ammonia nitrogen stripping system, the pH needs to be adjusted to 10-11 so that ammonium ions can be converted into ammonia gas and absorbed by sulfuric acid to form ammonium sulfate. However, due to the adjustment of alkalinity, OH - reacts with metal ions Ca 2+ , Fe 3+ , Mg 2+ in the wastewater to generate precipitation, which will block the plate heat exchanger in the ammonia nitrogen stripping system, greatly affecting the removal efficiency of the system. And if the precipitation is not removed, after the heat exchanger is blocked, it needs to be manually disassembled and cleaned, and the frequency of occurrence is frequent.

[0003] In view of this, this application is specifically proposed. Content of the Utility Model

[0004] The purpose of the utility model is to provide a treatment system for ammonia-containing wastewater and LSR wastewater to improve at least one problem mentioned in the background art.

[0005] In the first aspect, the utility model provides a treatment system for ammonia-containing wastewater, including: a heat exchanger, a first pH adjustment tank, an inclined plate sedimentation tank, a second pH adjustment tank and an ammonia nitrogen stripping system connected in sequence;

[0006] The second pH adjustment tank is connected to the liquid inlet of the ammonia nitrogen stripping system through a wastewater delivery pipe;

[0007] The liquid discharge port of the ammonia nitrogen stripping system is connected to a drain pipe;

[0008] The wastewater delivery pipe is connected to the heat exchanger as a cold source, and the drain pipe is connected to the heat exchanger as a heat source.

[0009] In an optional embodiment, a stirrer for uniformly mixing the added alkali agent and water is arranged in the first pH adjustment tank.

[0010] In an alternative embodiment, the first pH adjustment tank includes an inlet pipe, a first outlet pipe, a first reaction chamber, and a first buffer chamber. An overflow partition is provided between the first reaction chamber and the first buffer chamber. The inlet pipe communicates with the first reaction chamber, and the upper part of the first buffer chamber communicates with the inclined plate sedimentation tank through the first outlet pipe.

[0011] In an alternative embodiment, the number of agitators is 2, and the 2 agitators are respectively arranged in the first reaction chamber and the first buffer chamber.

[0012] In an alternative embodiment, the bottom of the inclined plate sedimentation tank is connected to a sludge discharge pipe, and the upper part of the inclined plate sedimentation tank communicates with the second pH adjustment tank through a second outlet pipe.

[0013] In an alternative embodiment, the second pH adjustment tank has a second reaction chamber and a second buffer chamber. An overflow partition is provided between the second reaction chamber and the second buffer chamber. The second outlet pipe communicates with the second reaction chamber, and the lower part of the second buffer chamber communicates with the ammonia nitrogen stripping system through a wastewater transfer pipe.

[0014] In an alternative embodiment, an agitator is arranged in the second reaction chamber.

[0015] In an alternative embodiment, the ammonia nitrogen stripping system includes a heater, a first stripping tower, a second stripping tower, and an absorption tower;

[0016] The wastewater transfer pipe communicates with the liquid inlet of the first stripping tower. The liquid outlet of the first stripping tower communicates with the liquid inlet of the second stripping tower. The gas outlet of the first stripping tower communicates with the gas inlet of the second stripping tower. The liquid outlet of the second stripping tower is the liquid discharge port of the ammonia nitrogen stripping system. The liquid outlet of the second stripping tower communicates with a drain pipe. The gas outlet of the second stripping tower communicates with the gas inlet of the absorption tower. The gas outlet of the absorption tower communicates with the gas inlet of the first stripping tower. A blower is arranged on the pipe connecting the gas outlet of the absorption tower and the gas inlet of the first stripping tower. The upper liquid discharge port of the absorption tower is connected to an ammonium sulfate solution discharge pipe;

[0017] The heater is arranged on the wastewater transfer pipe, between the heat exchanger and the first stripping tower.

[0018] In an alternative embodiment, the number of blowers is 2, and the 2 blowers are arranged in parallel.

[0019] In a second aspect, the present utility model provides a treatment system for LSR wastewater, including a 3B3T ion removal system and the treatment system according to any one of the foregoing embodiments;

[0020] The 3B3T ion removal system includes a weakly basic anion exchanger, a cation exchanger, and a strongly basic anion exchanger connected in series in sequence. The weakly basic anion exchanger communicates with the wastewater inlet pipe, and the strongly basic anion exchanger communicates with the product water pipe;

[0021] The wastewater drain outlet of the cation exchanger communicates with the inlet pipe of the first pH adjustment tank.

[0022] The wastewater treatment system provided by the present utility model sets a first pH adjustment tank and an inclined plate sedimentation tank before the second pH adjustment tank. First, an alkali agent is added to the first pH adjustment tank to precipitate metal ions such as calcium and magnesium in the wastewater. Then, the wastewater is transported to the inclined plate sedimentation tank, and the precipitated substances generated in the wastewater precipitate under the action of gravity. After that, the wastewater treated by the inclined plate sedimentation tank is introduced into the second pH adjustment tank, and an alkali agent is added to the wastewater again in the second pH adjustment tank. After the pH of the wastewater meets the requirements for entering the ammonia stripping system, it is transported to the ammonia stripping system through a wastewater delivery pipe, and the wastewater is heated by a heat exchanger during the transportation process. Due to the setting of the first pH adjustment tank and the inclined plate sedimentation tank, the easily precipitable metals in the wastewater can be precipitated and removed in advance, so that the blockage of the heat exchanger pipeline due to the generation of precipitation when the wastewater passes through the heat exchanger can be avoided. Brief Description of the Drawings

[0023] In order to more clearly illustrate the specific embodiments of the present utility model or the technical solutions in the prior art, the following will briefly introduce the drawings required for use in the description of the specific embodiments or the prior art. Obviously, the following drawings are some embodiments of the present utility model. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts.

[0024] Figure 1 It is a structural diagram of the treatment system for LSR wastewater provided by an embodiment of the present utility model.

[0025] Icons: 101 - agitator; 110 - first pH adjustment tank; 111 - first reaction chamber; 112 - first buffer chamber; 113 - water inlet pipe; 114 - first water outlet pipe; 120 - inclined plate sedimentation tank; 121 - sludge scraper; 122 - second water outlet pipe; 130 - second pH adjustment tank; 131 - wastewater delivery pipe; 132 - second reaction chamber; 133 - second buffer chamber; 140 - ammonia stripping system; 141 - heater; 142 - first stripping tower; 143 - second stripping tower; 144 - absorption tower; 145 - drain pipe; 146 - ammonium sulfate solution discharge pipe; 147 - fan; 150 - heat exchanger; 200 - 3B3T ion removal system; 201 - weak anion bed; 202 - cation bed; 203 - strong anion bed; 204 - product water pipe; 205 - wastewater inlet pipe; 10 - LSR wastewater treatment system. Detailed Embodiments

[0026] To make the objectives, technical solutions, and advantages of the embodiments of the present utility model clearer, the technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model. Obviously, the described embodiments are some, but not all, of the embodiments of the present utility model. The components of the embodiments of the present utility model usually described and illustrated in the drawings here can be arranged and designed in various different configurations.

[0027] Therefore, the following detailed description of the embodiments of the present utility model provided in the drawings is not intended to limit the scope of the claimed present utility model, but merely represents selected embodiments of the present utility model. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present utility model without creative efforts belong to the scope of protection of the present utility model.

[0028] It should be noted that similar reference numerals and letters denote similar items in the following drawings. Therefore, once an item is defined in one drawing, it does not need to be further defined and explained in subsequent drawings.

[0029] In the description of the present utility model, it should be noted that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship in which the utility model product is usually placed during use. It is only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present utility model. In addition, the terms "first", "second", "third", etc. are only used for descriptive distinction and cannot be understood as indicating or implying relative importance.

[0030] In addition, the terms "horizontal", "vertical", "hanging", etc. do not mean that the components are required to be absolutely horizontal or hanging, but can be slightly inclined. For example, "horizontal" only means that its direction is more horizontal relative to "vertical", and does not mean that the structure must be completely horizontal, but can be slightly inclined.

[0031] In the description of the present utility model, it should also be noted that unless otherwise clearly specified and defined, the terms "set", "installed", "connected", "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present utility model can be understood according to specific circumstances.

[0032] The following will describe in detail some embodiments of the present utility model with reference to the accompanying drawings. Without conflict, the following embodiments and the features in the embodiments can be combined with each other.

[0033] As Figure 1 shown, an embodiment of the present utility model provides a treatment system for ammonia-containing wastewater, including: a heat exchanger 150, a first pH adjustment tank 110, an inclined plate sedimentation tank 120, a second pH adjustment tank 130, and an ammonia stripping system 140 that are connected in sequence;

[0034] The second pH adjustment tank 130 is connected to the liquid inlet of the ammonia stripping system 140 through a wastewater delivery pipe 131;

[0035] The liquid discharge port of the ammonia stripping system 140 is connected to a drain pipe 145;

[0036] The wastewater delivery pipe 131 is connected to the heat exchanger 150 as a cold source, and the drain pipe 145 is connected to the heat exchanger 150 as a heat source.

[0037] The LSR wastewater treated by the 3B3T ion removal system 200 has a high content of ammonium ions and free ammonia, as well as some metal ions such as magnesium ions and calcium ions that are prone to precipitation under alkaline conditions. Since the wastewater will be adjusted to alkaline and heat-exchanged by the heat exchanger 150 before entering the ammonia stripping system 140, metal ions such as calcium and magnesium in the wastewater are likely to form precipitates and block the pipes of the heat exchanger 150 after the pH adjustment.

[0038] In this application, a first pH adjustment tank 110 and an inclined plate sedimentation tank 120 are provided before the second pH adjustment tank 130. By adding an alkali agent to the first pH adjustment tank 110 first to precipitate metal ions such as calcium and magnesium in the wastewater, and then transporting the wastewater to the inclined plate sedimentation tank 120, the precipitated substances in the wastewater are precipitated under the action of gravity. After that, the wastewater treated by the inclined plate sedimentation tank 120 is introduced into the second pH adjustment tank 130. In the second pH adjustment tank 130, an alkali agent is added to the wastewater again to make the pH of the wastewater meet the requirements for entering the ammonia stripping system 140, and then it is transported to the ammonia stripping system 140 through the wastewater delivery pipe 131. The wastewater is heated by the heat exchanger 150 during the transportation process. Due to the setting of the first pH adjustment tank 110 and the inclined plate sedimentation tank 120, the easily precipitated metals in the wastewater can be precipitated and removed in advance, so that the pipes of the heat exchanger 150 can be prevented from being blocked due to the generation of precipitates when the wastewater passes through the heat exchanger 150.

[0039] Optionally, a stirrer 101 for uniformly mixing the added alkali agent and water is provided in the first pH adjustment tank 110.

[0040] Optionally, the first pH adjustment tank 110 includes a water inlet pipe 113, a first water outlet pipe 114, a first reaction chamber 111, and a first buffer chamber 112. An overflow partition is provided between the first reaction chamber 111 and the first buffer chamber 112. The water inlet pipe 113 communicates with the first reaction chamber 111, and the upper part of the first buffer chamber 112 communicates with the inclined plate sedimentation tank 120 through the first water outlet pipe 114.

[0041] Optionally, the number of agitators 101 is 2, and the two agitators 101 are respectively arranged in the first reaction chamber 111 and the first buffer chamber 112.

[0042] The ammonia-containing wastewater coming from the upstream is discharged into the first reaction chamber 111 through the water inlet pipe 113. An alkali agent is added to the first reaction chamber 111. Under the action of the agitator 101, the alkali agent, calcium ions, and magnesium ions are fully contacted and mixed evenly to form hydroxide precipitates. The mixed waste liquid in the upper part of the first reaction chamber 111 overflows into the first buffer chamber 112. Under the action of the agitator 101 in the first buffer chamber 112, the alkali agent and calcium and magnesium ions further fully react to form precipitates. The wastewater treated by the first buffer chamber 112 is discharged from the first water outlet pipe 114 and enters the inclined plate sedimentation tank 120.

[0043] Optionally, the bottom of the inclined plate sedimentation tank 120 is connected to a sludge discharge pipe, and the sludge obtained after sedimentation is discharged from the sludge discharge pipe; the upper part of the inclined plate sedimentation tank 120 communicates with the second pH adjustment tank 130 through a second water outlet pipe 122, and the clear water in the upper part of the inclined plate sedimentation tank 120 enters the second pH adjustment tank 130 through the second water outlet pipe 122.

[0044] Optionally, a sludge scraper 121 is further arranged in the inclined plate sedimentation tank 120. The sludge scraper 121 is used to scrape the sludge at the bottom of the sedimentation tank towards the sludge discharge pipe for convenient unified discharge.

[0045] Optionally, the second pH adjustment tank 130 has a second reaction chamber 132 and a second buffer chamber 133. An overflow partition is provided between the second reaction chamber 132 and the second buffer chamber 133. The second water outlet pipe 122 communicates with the second reaction chamber 132, and the lower part of the second buffer chamber 133 communicates with the ammonia nitrogen stripping system through a wastewater delivery pipe 131.

[0046] Optionally, an agitator 101 is arranged in the second reaction chamber 132.

[0047] The wastewater entering the second pH adjustment tank 130 first enters the second reaction chamber 132. An alkali agent is added to the second reaction chamber 132, and under the action of the agitator 101, the alkali agent and the wastewater are fully mixed. Then the mixed wastewater overflows into the second buffer chamber 133, and the pH of the wastewater is stabilized at about 11 in the second buffer chamber 133. Then the wastewater with adjusted pH is transported to the ammonia nitrogen stripping system 140 through the wastewater delivery pipe 131.

[0048] Optionally, the alkali agent added in some embodiments of the present application is sodium hydroxide.

[0049] Optionally, the ammonia nitrogen stripping system includes a heater 141, a first stripping tower 142, a second stripping tower 143, and an absorption tower 144;

[0050] The wastewater delivery pipe 131 communicates with the liquid inlet of the first stripping tower 142. The liquid outlet of the first stripping tower 142 communicates with the liquid inlet of the second stripping tower 143. The gas outlet of the first stripping tower 142 communicates with the gas inlet of the second stripping tower 143. The liquid outlet of the second stripping tower 143 is the liquid discharge port of the ammonia nitrogen stripping system 140. The liquid outlet of the second stripping tower 143 communicates with the drain pipe 145. The gas outlet of the second stripping tower 143 communicates with the gas inlet of the absorption tower 144. The gas outlet of the absorption tower 144 communicates with the gas inlet of the first stripping tower 142. A fan 147 is provided on the pipeline where the gas outlet of the absorption tower 144 communicates with the gas inlet of the first stripping tower 142. The upper liquid discharge port of the absorption tower 144 is connected to the ammonium sulfate solution discharge pipe 146;

[0051] The heater 141 is provided on the wastewater delivery pipe 131, between the heat exchanger 150 and the first stripping tower 142.

[0052] Optionally, the number of fans 147 provided is 2, and the 2 fans 147 are arranged in parallel.

[0053] Ammonia nitrogen in wastewater mainly exists in the forms of ammonium ions (NH 4+ ) and free ammonia (NH3), and its equilibrium relationship is affected by the pH value. When the pH value increases, the equilibrium shifts to the left, and the proportion of free ammonia increases. At room temperature, when the pH value is about 7, most of the ammonia nitrogen exists in the form of ammonium ions, while when the pH is about 11, free ammonia accounts for approximately 98%. Free ammonia is easily released from water. By aeration, ammonia can be promoted to escape from water. The ammonia nitrogen stripping tower generally operates in series with two towers to increase the recovery concentration of ammonia, and an ammonia nitrogen absorption tower 144 is installed behind the stripping tower to make the ammonia nitrogen waste gas discharged through the absorption tower 144 meet the standards. The ammonia nitrogen stripping system 140 generally uses the produced water of the system to preheat the system inlet water through the heat exchanger 150 to achieve the effect of energy conservation and consumption reduction.

[0054] The wastewater transported to the ammonia stripping system 140 is first heated by the heater 141 and then enters the first stripping tower 142. Since the temperature of the wastewater increases, after entering the first stripping tower 142, under the stripping action of the air blown in by the blower 147, most of the ammonia nitrogen in the wastewater overflows in the form of ammonia gas and enters the second stripping tower 143. The wastewater with most of the ammonia nitrogen removed enters the second stripping tower 143, and the remaining ammonia nitrogen in the wastewater in the second stripping tower 143 further overflows under the stripping action of the gas entering the second stripping tower 143. The water after ammonia nitrogen removal is discharged through the drain pipe 145. Since the water after ammonia nitrogen removal contains relatively high heat, it is used as the heat source of the heat exchanger 150 to preheat the wastewater entering the ammonia stripping system 140, thus achieving the energy-saving effect. The ammonia gas generated in the first stripping tower 142 enters the second stripping tower 143, and together with the ammonia gas generated in the second stripping tower 143, it enters the absorption tower 144 and is absorbed by the sulfuric acid solution sprayed in the absorption tower 144 to generate ammonium sulfate solution, and the generated ammonium sulfate solution is discharged through the ammonium sulfate solution discharge pipe 146. Some of the unabsorbed ammonia gas in the absorption tower 144 returns to the first ammonia stripping tower again.

[0055] A treatment system 10 for LSR wastewater provided by an embodiment of the present invention includes a 3B3T ion removal system 200 and a treatment system for ammonia-containing wastewater provided by an embodiment of the present invention.

[0056] The 3B3T ion removal system 200 includes a weakly basic anion exchanger 201, a cation exchanger 202, and a strongly basic anion exchanger 203 connected in series in sequence. The weakly basic anion exchanger 201 is communicated with the wastewater inlet pipe 205, and the strongly basic anion exchanger 203 is communicated with the product water pipe 204;

[0057] The wastewater drain outlet of the cation exchanger 202 is communicated with the inlet pipe 113 of the first pH adjustment tank 110.

[0058] LSR (Local scrubber reclaim) wastewater is the wastewater generated by the scrubber machine in the semiconductor. After removing the cations and anions in the wastewater by the 3B3T process, it is recycled and used as the supply fluid of the scrubber machine to dissolve the waste gas.

[0059] The 3B3T is composed of a weakly basic anion exchanger 201, a cation exchanger 202, and a strongly basic anion exchanger 203 connected in series. The core treatment process is the (resin) ion exchange technology. Its main purpose is to remove the cations and anions in the wastewater. Since ion exchange requires the regeneration of the resin to ensure the durable use of the resin, reduce environmental pollution and waste of resources, and improve production efficiency and economic benefits. Since the 3B3T already belongs to the prior art, no more details will be described here.

[0060] Due to the relatively high ammonia nitrogen concentration in the LSR wastewater, after being adsorbed by the 3B3T resin through ion exchange, the produced water is recycled and supplied to the machine tool. However, during the resin regeneration process, ammonia nitrogen (concentration about 600 ppm) and metal ions (Ca 2+ , Mg 2+ concentration about 20 ppm) are present in the regeneration waste liquid and go to the ammonia nitrogen stripping system 140 for treatment and discharge after reaching the standard. When the ammonia nitrogen wastewater enters the stripping system, NaOH is added to adjust the pH to about 11 before entering the stripping system to facilitate the escape of ammonia gas from the water. At the same time, the metal ions (Ca 2+ , Mg 2+ ) in the wastewater will form Ca(OH)2 and Mg(OH)2 precipitates with NaOH, which will clog the heat exchanger 150. The present utility model adds a first pH adjustment tank 110 and an inclined plate sedimentation tank 120 to remove Ca(OH)2 and Mg(OH)2 before the ammonia nitrogen wastewater enters the ammonia nitrogen stripping system 140. The supernatant is then adjusted to a pH of about 11 through a second pH adjustment tank 130 and enters the ammonia nitrogen stripping system 140 to ensure the stable operation of the ammonia nitrogen stripping system 140.

[0061] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present utility model and are not intended to limit them; although the present utility model has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements for some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present utility model.

Claims

1. A treatment system for ammonia-containing wastewater, characterized in that, Comprising: A heat exchanger, a first pH adjustment tank, an inclined plate sedimentation tank, a second pH adjustment tank, and an ammonia nitrogen stripping system connected in sequence; The second pH adjustment tank is connected to the liquid inlet of the ammonia nitrogen stripping system through a waste water delivery pipe; The liquid discharge port of the ammonia nitrogen stripping system is connected to a drain pipe; The waste water delivery pipe is connected to the heat exchanger as a cold source, and the drain pipe is connected to the heat exchanger as a heat source.

2. The processing system according to claim 1, wherein A stirrer for uniformly mixing the added alkali agent and water is provided in the first pH adjustment tank.

3. The processing system according to claim 2, wherein The first pH adjustment tank includes a water inlet pipe, a first water outlet pipe, a first reaction chamber, and a first buffer chamber. An overflow partition is provided between the first reaction chamber and the first buffer chamber. The water inlet pipe is connected to the first reaction chamber, and the upper part of the first buffer chamber is connected to the inclined plate sedimentation tank through the first water outlet pipe.

4. The processing system according to claim 3, characterized in that, The number of the stirrers is 2, and the 2 stirrers are respectively arranged in the first reaction chamber and the first buffer chamber.

5. The processing system according to claim 4, wherein The bottom of the inclined plate sedimentation tank is connected to a sludge discharge pipe, and the upper part of the inclined plate sedimentation tank is connected to the second pH adjustment tank through a second water outlet pipe.

6. The processing system according to claim 5, characterized in that, The second pH adjustment tank has a second reaction chamber and a second buffer chamber. An overflow partition is provided between the second reaction chamber and the second buffer chamber. The second water outlet pipe is connected to the second reaction chamber, and the lower part of the second buffer chamber is connected to the ammonia nitrogen stripping system through a waste water delivery pipe.

7. The processing system according to claim 6, wherein A stirrer is provided in the second reaction chamber.

8. The processing system according to claim 7, wherein The ammonia nitrogen stripping system includes a heater, a first stripping tower, a second stripping tower, and an absorption tower; The waste water delivery pipe is connected to the liquid inlet of the first stripping tower. The liquid outlet of the first stripping tower is connected to the liquid inlet of the second stripping tower. The gas outlet of the first stripping tower is connected to the gas inlet of the second stripping tower. The liquid outlet of the second stripping tower is the liquid discharge port of the ammonia nitrogen stripping system. The liquid outlet of the second stripping tower is connected to the drain pipe. The gas outlet of the second stripping tower is connected to the gas inlet of the absorption tower. The gas outlet of the absorption tower is connected to the gas inlet of the first stripping tower. A fan is provided on the pipe connecting the gas outlet of the absorption tower and the gas inlet of the first stripping tower. The upper part liquid discharge port of the absorption tower is connected to an ammonium sulfate solution discharge pipe; The heater is provided on the waste water delivery pipe, between the heat exchanger and the first stripping tower.

9. The processing system according to claim 8, wherein The number of the fans provided is 2, and the 2 fans are connected in parallel.

10. A treatment system for LSR wastewater, characterized in that, Comprising a 3B3T ion removal system and the treatment system according to any one of claims 1 to 9; The 3B3T ion removal system includes a weakly basic anion exchanger, a cation exchanger, and a strongly basic anion exchanger connected in series. The weakly basic anion exchanger is connected to a waste water inlet pipe, and the strongly basic anion exchanger is connected to a product water pipe; The waste water discharge port of the cation exchanger is connected to the water inlet pipe of the first pH adjustment tank.

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