System for treating high-ammonia-nitrogen wastewater and recycling ammonia water resource by utilizing low-temperature heat source

Abstract

The utility model relates to a system for treating high-ammonia-nitrogen wastewater and recycling ammonia water resources by utilizing a low-temperature heat source, which comprises a steam stripping tower, a high-ammonia-nitrogen wastewater treatment device, a high-ammonia-nitrogen wastewater treatment device and a low-temperature heat source, the air blower is connected with the middle part of the steam stripping tower; the first heat exchanger exchanges heat with the material discharged from the bottom of the steam stripping tower through a production area low-grade heat source, and the material discharged from the bottom of the steam stripping tower after heat exchange flows back to the top of the steam stripping tower; a material discharged from the top of the steam stripping tower flows into the first spraying absorption tower from the bottom of the first spraying absorption tower; a material discharged from the top of the first spraying absorption tower flows into the second spraying absorption tower from the bottom of the second spraying absorption tower; a material discharged from the top of the second spraying absorption tower flows into the falling film absorption tower from the bottom of the falling film absorption tower. According to the utility model, a low-grade heat source is utilized, and the produced ammonia water can be used in a flue gas denitration process at a production end, so that the cost for ammonium salt treatment caused by acid absorption is avoided.

Description

TECHNICAL FIELD

[0001] The utility model relates to a chemical industry device technical field, concretely relates to a kind of high ammonia nitrogen wastewater and ammonia water resource recovery system using low-temperature heat source processing. BACKGROUND

[0002] With the continuous development of industrialization process, modern industry, modern animal husbandry and garbage incineration recycling and other resource recycling industries are increasingly scaled, centralized, and the resulting high ammonia nitrogen wastewater has become the second largest pollution source after COD pollutants.

[0003] High ammonia nitrogen wastewater is widely sourced, mainly from the following sources:

[0004] (1) high ammonia nitrogen wastewater of chemical industry:

[0005] ① fertilizer production plants, such as nitrogen fertilizer, compound fertilizer, etc., ammonia synthesis, urea production, etc., will produce a large amount of ammonia nitrogen-containing wastewater. For example, in the production of nitrogen fertilizer, the separation, washing, etc. of ammonia gas after reaction with other raw materials will produce high-concentration ammonia nitrogen wastewater.

[0006] ② Metallurgical industry: in the smelting process of non-ferrous metals (such as copper, zinc), especially in the wet metallurgical process, nitrogen-containing compounds in the ore will enter the wastewater in the leaching, separation, etc. step, resulting in an increase in ammonia nitrogen content.

[0007] ③ Pharmaceutical industry (new material synthesis): many drug synthesis processes involve reactions of nitrogen-containing compounds, such as the production of antibiotics, amino acids, etc. After raw material reaction, product purification, etc., high ammonia nitrogen wastewater will be produced. Like the fermentation and extraction stages in the production process of penicillin, ammonia nitrogen-containing wastewater will be discharged.

[0008] ④ Coking industry: in the high-temperature dry distillation coking process of coal, the nitrogen element in the coal will be converted into ammonia, most of which will enter the coal gas, and after cooling and washing, high ammonia nitrogen coking wastewater will be produced.

[0009] (2) Agricultural wastewater

[0010] ① Livestock and poultry breeding wastewater: the wastewater produced by livestock and poultry breeding farms contains high concentrations of organic matter and ammonia nitrogen. This is because livestock and poultry manure contains a large amount of nitrogen-containing organic matter, which will decompose to produce ammonia gas during composting or anaerobic fermentation, and then dissolve in wastewater, increasing the ammonia nitrogen content. For example, the ammonia nitrogen content in pig urine can be as high as 1000-2000 mg / L;

[0011] ② Agricultural product processing wastewater: during meat processing, aquatic product processing, etc., animal protein decomposition will produce ammonia nitrogen. For example, after slaughtering, cleaning, pickling, etc. in meat processing enterprises, wastewater will contain high concentrations of ammonia nitrogen.

[0012] (3) Landfill leachate

[0013] In the landfill, complex biological and chemical decomposition reactions occur in the landfill process. Organic nitrogen compounds (such as proteins, amino acids, etc.) in the garbage decompose to produce ammonia under the action of microorganisms, and these ammonia dissolves in the leachate to form high ammonia-nitrogen wastewater. In the early stage of landfill, the ammonia-nitrogen concentration in the leachate can be as high as 1000-3000 mg / L.

[0014] The current high ammonia-nitrogen wastewater treatment process can be simply divided into physical and chemical methods, biological methods, membrane separation, MAP precipitation method, catalytic oxidation method, etc., each method has its own advantages and disadvantages:

[0015] 1. Whether it is "ammonia stripping (stripping) or A / O or stripping + chemical precipitation", it cannot be separated from the pretreatment process with high investment and high operating cost. The one-time investment of "ammonia stripping" is too large, and the power consumption of "stripping" is too large.

[0016] 2. When the A / O method is connected, not only the investment is high, but also the land area is large, and the requirements for the pretreated water are harsh (such as NH3-N must be less than 300 mg / l, the stripping or stripping method cannot meet this requirement for high-concentration ammonia-nitrogen wastewater of more than 5000 mg / l, so only the clean water is diluted by several times).

[0017] 3. The chemical precipitation method connected has smaller investment and land area than the A / O method, but the consumption of chemicals is too large. The chemical precipitation method mainly uses the following chemical reaction: Mg 2+ + NH 4+ + PO4 3- = MgNH4PO4. In theory, adding phosphorus salt and magnesium salt to wastewater containing high-concentration ammonia-nitrogen in a certain proportion can remove ammonia-nitrogen in water. Because the optimal dosage of the reagent is Mg:P molar ratio 1.2, N:P molar ratio 1.2-1.4, the treatment reagent cost is too high, and the water quality is complex, the dosage is often many times the theoretical dosage, and the effluent cannot meet the national first or second emission standard. Content of the utility model

[0018] The purpose of the utility model is to overcome at least one of the defects in the prior art and provide a system for treating high ammonia-nitrogen wastewater and recycling ammonia water resources by using low-temperature heat sources.

[0019] The purpose of the utility model can be achieved by the following technical solutions:

[0020] A system for treating high ammonia-nitrogen wastewater and recycling ammonia water resources by using low-temperature heat sources, comprising:

[0021] A stripping and stripping tower is arranged in the middle of the stripping and stripping tower.

[0022] a blower connected to the middle of the stripping blow tower;

[0023] a first heat exchanger, which exchanges heat with the stripping blow tower bottom discharge through a low-grade heat source in the production area, and the heat-exchanged stripping blow tower bottom discharge flows back to the top of the stripping blow tower;

[0024] a first spray absorption tower, which is connected to the top of the stripping blow tower and the bottom of the first spray absorption tower, and the stripping blow tower top discharge flows into the first spray absorption tower from the bottom of the first spray absorption tower;

[0025] a second spray absorption tower, which is connected to the top of the first spray absorption tower and the bottom of the second spray absorption tower, and the first spray absorption tower top discharge flows into the second spray absorption tower from the bottom of the second spray absorption tower;

[0026] a falling film absorption tower, which is connected to the top of the second spray absorption tower and the bottom of the falling film absorption tower, and the second spray absorption tower top discharge flows into the falling film absorption tower from the bottom of the falling film absorption tower.

[0027] Further, the first heat exchanger comprises a first heat exchange cavity and a second heat exchange cavity, and a heat-conducting partition plate is arranged between the first heat exchange cavity and the second heat exchange cavity, the stripping blow tower bottom discharge flows through the first heat exchange cavity to flow back to the stripping blow tower from the top of the stripping blow tower, and the low-grade heat source in the production area flows through the second heat exchange cavity to exchange heat with the stripping blow tower bottom discharge.

[0028] Further, a forced circulation water pump is arranged between the stripping blow tower bottom discharge port and the first heat exchanger feed port.

[0029] Further, a wastewater collection tank is arranged between the forced circulation water pump and the first heat exchanger feed port.

[0030] Further, the system further comprises a high ammonia-nitrogen wastewater accumulation tank, which is connected to the high ammonia-nitrogen wastewater feed port.

[0031] Further, the system further comprises a first condensate water pump and a second heat exchanger, and the first spray absorption tower bottom discharge port is sequentially connected to the first condensate water pump and the second heat exchanger through pipelines, and the first spray absorption tower bottom discharge after heat exchange with the second heat exchanger flows back to the first spray absorption tower.

[0032] Further, the system further comprises a second condensate pump and a third heat exchanger, a bottom outlet of the second spray absorption tower is connected with the second condensate pump and the third heat exchanger in sequence through pipelines, and the bottom outlet of the second spray absorption tower is returned to the second spray absorption tower after heat exchange with the third heat exchanger.

[0033] Further, the system further comprises a first ammonia water recovery tank, the pipelines between the first condensate pump and the second heat exchanger and between the second condensate pump and the third heat exchanger are connected with the first ammonia water recovery tank through pipelines, and a first discharge valve is arranged on the connecting pipelines.

[0034] Further, the system further comprises a third condensate pump and a falling film evaporator, the bottom outlet of the falling film absorption tower is connected with the third condensate pump and the falling film evaporator in sequence through pipelines, and the bottom outlet of the falling film absorption tower is returned to the falling film absorption tower after evaporation and concentration of the falling film evaporator.

[0035] Further, the system further comprises a second ammonia water recovery tank, the pipelines between the third condensate pump and the falling film evaporator are connected with the second ammonia water recovery tank through pipelines, and a second discharge valve is arranged on the connecting pipelines.

[0036] Compared with the prior art, the utility model has the following advantages:

[0037] 1. The utility model provides a kind of high ammonia nitrogen wastewater and ammonia water resource recovery system handled by low temperature heat source, can utilize plant waste heat source, such as steam condensate, flue gas, low temperature hot water to the wastewater to be stripped for heat exchange, improve the treatment temperature of high ammonia nitrogen wastewater, can improve the stripping efficiency of ammonia nitrogen (temperature is controlled below 45 DEG C after heat exchange, reduce heat source requirement, heat exchanger area).

[0038] 2. The utility model provides a kind of high ammonia nitrogen wastewater and ammonia water resource recovery system handled by low temperature heat source, because in ammonia nitrogen stripping treatment, treatment efficiency is positively correlated with pH value and temperature, in the treatment process of stripping tower in the utility model, heat exchange is carried out by first heat exchanger, low temperature waste heat source is utilized, wastewater temperature is improved, reagent (soda) use can be reduced, 35 DEG C pH value 10 wastewater and 15 DEG C pH value 11 wastewater, same stripping efficiency, theoretical dosage is greater than 36kg per ton of water, and the acid addition amount of wastewater neutralization and adjustment after ammonia nitrogen removal is reduced, and after adjustment, meet the requirement of salt content in discharge standard, corresponding reduce circulating cooling water temperature, reduce the load of enterprise cooling water system, reduce mechanical energy consumption.

[0039] 3. The utility model provides a utilize low temperature heat source to handle high ammonia nitrogen wastewater and ammonia water resource recovery system, this system utilizes the air blower, the higher the dissolved oxygen content in wastewater, the corresponding ammonia gas content reduces, therefore the balance equation carries out to the right.

[0040] 4. The utility model provides a utilize low temperature heat source to handle high ammonia nitrogen wastewater and ammonia water resource recovery system, because ammonia gas and water have the best water solubility, this system utilizes the cold source (cooling water, 7 DEG C water) and carries out ammonia water recovery, and the recovered ammonia water can be used for producing flue gas denitration (SCR reactor) and reduces new ammonia water use.

[0041] 5. The utility model provides a utilize low temperature heat source to handle high ammonia nitrogen wastewater and ammonia water resource recovery system, utilizes the process that spray tower absorption tower and falling film absorption tower are combined, guarantees timely absorption to improve ammonia gas concentration while ammonia gas volatilizes. Spray tower (its water flow form is liquid drop) is advantageous to ammonia nitrogen absorption, falling film absorption (exhibits liquid film) is advantageous to cooling, can rapidly reduce system temperature (the volatility of recovery liquid greatly reduces), reduces technological process.

[0042] 6, the effective combination of the two technologies can utilize a large amount of low-grade heat source in power plants, chemical plants and the like, and the produced ammonia water can be used in flue gas denitration process in the production end, thereby completely eliminating the process cost required for ammonium salt treatment and disposal caused by acid absorption. BRIEF DESCRIPTION OF DRAWINGS

[0043] Figure 1 It is the flow chart of the system for utilizing low temperature heat source to handle high ammonia nitrogen wastewater and ammonia water resource recovery system in example 1.

[0044] Figure 2 It is the graph showing the relationship between the existing form of ammonia nitrogen in aqueous solution and pH value and temperature.

[0045] The reference signs in the figure are shown as follows: 1-air blower; 2-high ammonia nitrogen wastewater storage tank; 4-stripping blow-off tower; 5-forced circulation water pump; 6-wastewater collection tank; 9-first heat exchanger; 10-first spray absorption tower; 11-first condensate pump; 12-second heat exchanger; 13-first discharge valve; 14-first ammonia water recovery tank; 15-second spray absorption tower; 16-third heat exchanger; 17-second condensate pump; 18-falling film absorption tower; 19-second ammonia water recovery tank; 20-third condensate pump; 21-falling film evaporator; and 22-second discharge valve. DETAILED DESCRIPTION

[0046] The utility model will be described in detail in combination with the drawings and specific embodiments. The embodiment is implemented on the premise of the technical scheme of the utility model, and detailed implementation mode and specific operation process are given, but the protection scope of the utility model is not limited to the following examples.

[0047] Embodiment 1

[0048] A high ammonia-nitrogen wastewater treatment system using a low-temperature heat source and an ammonia water resource recovery system, the specific structure of which is shown in Figure 1 , comprising:

[0049] A stripping blow-off tower 4, a high ammonia-nitrogen wastewater inlet is arranged in the middle of the stripping blow-off tower 4;

[0050] A blower 1, which is connected to the middle of the stripping blow-off tower 4;

[0051] A first heat exchanger 9, which exchanges heat with the stripping blow-off tower 4 bottom discharge through a low-grade heat source in the production area, and the stripping blow-off tower 4 bottom discharge after heat exchange flows back to the top of the stripping blow-off tower 4; in the ammonia-nitrogen blow-off treatment, the treatment efficiency is positively correlated with pH value and temperature, and in the treatment process of the stripping blow-off tower 4 in the embodiment, heat exchange is realized through the first heat exchanger 9, low-temperature waste heat source is utilized, wastewater temperature is increased, reagent (soda) use is reduced, the theoretical dosage of 35℃ pH value 10 wastewater is greater than 36 kg, and the same blow-off efficiency, the amount of acid added for neutralization and adjustment after ammonia-nitrogen removal is reduced, and the adjusted wastewater meets the salt requirement in the discharge standard, the circulating cooling water temperature is correspondingly reduced, the load of the enterprise cooling water system is reduced, and the mechanical energy consumption is reduced, see Figure 2 .

[0052] A first spray absorption tower 10, the top of the stripping blow-off tower 4 is connected to the bottom of the first spray absorption tower 10, and the stripping blow-off tower 4 top discharge flows into the first spray absorption tower 10 from the bottom of the first spray absorption tower 10;

[0053] A second spray absorption tower 15, the top of the first spray absorption tower 10 is connected to the bottom of the second spray absorption tower 15, and the first spray absorption tower 10 top discharge flows into the second spray absorption tower 15 from the bottom of the second spray absorption tower;

[0054] A falling film absorption tower 18, the top of the second spray absorption tower 15 is connected to the bottom of the falling film absorption tower 18, and the second spray absorption tower 15 top discharge flows into the falling film absorption tower 18 from the bottom of the falling film absorption tower 18.

[0055] In the embodiment, the first heat exchanger 9 includes a first heat exchange cavity and a second heat exchange cavity, a heat-conducting partition is arranged between the first heat exchange cavity and the second heat exchange cavity, the stripping blow-off tower 4 bottom discharge flows through the first heat exchange cavity to flow back to the stripping blow-off tower 4 from the top of the stripping blow-off tower 4, and the low-grade heat source in the production area flows through the second heat exchange cavity to exchange heat with the stripping blow-off tower 4 bottom discharge.

[0056] In the embodiment, a forced circulation water pump 5 is arranged between the stripping blow-off tower 4 bottom outlet and the first heat exchanger 9 inlet; and a waste water collecting tank 6 is arranged between the forced circulation water pump 5 and the first heat exchanger 9 inlet.

[0057] In the embodiment, the system further comprises a high ammonia-nitrogen waste water storage tank 2, which is connected to the high ammonia-nitrogen waste water inlet.

[0058] In the embodiment, the system further comprises a first condensate water pump 11 and a second heat exchanger 12, and the first spray absorption tower 10 bottom outlet is sequentially connected to the first condensate water pump 11 and the second heat exchanger 12 through pipelines, and the first spray absorption tower 10 bottom outlet backflow after heat exchange with the second heat exchanger 12 returns to the first spray absorption tower 10.

[0059] In the embodiment, the system further comprises a second condensate water pump 17 and a third heat exchanger 16, and the second spray absorption tower 15 bottom outlet is sequentially connected to the second condensate water pump 17 and the third heat exchanger 16 through pipelines, and the second spray absorption tower 15 bottom outlet backflow after heat exchange with the third heat exchanger 16 returns to the second spray absorption tower 15.

[0060] In the embodiment, the system further comprises a first ammonia water recovery tank 14, and the pipelines between the first condensate water pump 11 and the second heat exchanger 12 and the pipelines between the second condensate water pump 17 and the third heat exchanger 16 are connected to the first ammonia water recovery tank 14 through pipelines, and a first discharge valve 13 is arranged on the connecting pipelines.

[0061] In the embodiment, the system further comprises a third condensate water pump 20 and a falling film evaporator 21, and the falling film absorption tower 18 bottom outlet is sequentially connected to the third condensate water pump 20 and the falling film evaporator 21 through pipelines, and the falling film absorption tower 18 bottom outlet backflow after evaporation and concentration by the falling film evaporator 21 returns to the falling film absorption tower 18.

[0062] In the embodiment, the system further comprises a second ammonia water recovery tank 19, and the pipelines between the third condensate water pump 20 and the falling film evaporator 21 are connected to the second ammonia water recovery tank 19 through pipelines, and a second discharge valve 22 is arranged on the connecting pipelines.

[0063] Application Example 1

[0064] The anaerobic membrane effluent of a landfill leachate in Shanghai is treated by stripping with a filter blowdown water heat source as heat source, heat exchange to 35-40°C, pH adjustment to 10, gas-liquid ratio same as pH adjustment to 11. After comparison, the ammonia nitrogen removal efficiency is roughly the same. The raw water is 1570 mg / L, the ammonia nitrogen content of the treated wastewater is 290 mg / L in scheme 1, and the ammonia nitrogen content of the treated wastewater is 266 mg / L in scheme 2. The alkali dosage of the raw water is reduced by about 37% (the organic matter in the wastewater can react with the alkali). According to the system provided in example 1, the daily treatment capacity is 200 tons / day, about 12% of ammonia water is recovered by using a multi-stage spray absorption tower and a falling film absorption tower, about 2 tons, which is reused in the denitration process to reduce the ammonia water dosage of the customer.

[0065] Application Example 2

[0066] A medical chemical pharmaceutical industry in Taizhou, Zhejiang, urea wastewater treatment, urea hydrolysis products are ammonia and carbon dioxide in the evaporation process. Low-temperature heat source is used for heating and stripping to recover ammonia water. It can be directly returned to the production line, and the treated wastewater is treated by biochemical treatment. The system provided in example 1 is used for treatment, the treatment capacity is 50 tons / day, the steam condensate tank water is used for heat exchange, the raw water is reduced from 1200 mg / L to 240 mg / L, and mixed into a comprehensive water tank to enter the biochemical system for treatment and discharge. Urea under high temperature conditions, will reduce the production of biuret, which is not conducive to hydrolysis.

[0067] Application Example 3

[0068] A new material company in Shandong, in the synthesis of epoxy resin products research and development, in which the curing agent of various amine series intermediates, produce a large amount of dimethylamine, trimethylamine and a large amount of ammonia nitrogen small molecule wastewater (content about 3% ~ 5%). Because dimethylamine, trimethylamine and ammonia nitrogen are excessive in the reaction, therefore a certain concentration of dimethylamine, trimethylamine and ammonia nitrogen can be used in the production line. The system provided in example 1 is used, under alkaline conditions (under waste heat recovery), the temperature after heat exchange is controlled at about 35°C (the effect is obvious in winter), the pH value is controlled at about 10, and the hydrolysis of dimethylamine and trimethylamine can be inhibited under alkaline conditions. And can recover dimethylamine, trimethylamine, ammonia nitrogen under this condition, recovery rate > 96.5%, ammonia nitrogen content of the produced water < 103 mg / L, according to the wastewater amount of 120 t / d, more than 95% recovery rate, more than 4.5 tons of dimethylamine, trimethylamine and ammonia nitrogen are recovered every day, and the treated wastewater is mixed with the domestic sewage in the factory area, which can be completely treated by the biochemical system to meet the discharge standard. The wastewater treatment is changed into the extension of the production line, realizes the win-win of wastewater treatment and resource recovery, and brings real benefits to the enterprise.

[0069] Application Example 4

[0070] A certain chemical factory in Cangzhou, Hebei province, is a pesticide intermediate, a salted cyanide wastewater, 80 tons per day, containing 4% to 9% of ammonium chloride, weak alkaline pH, containing ammonia 1.8%, ethanol 1.5%, cyanoethyl 0.3%, toluene trace amount, using appropriate temperature preheating, alkaline stripping, ammonia is absorbed by 5% dilute hydrochloric acid, ammonium chloride salt is generated with the original water to evaporate crystallization as byproduct, ethanol, trace amount of toluene into the evaporation water, can be used as carbon source directly into the biochemical system for treatment. The system provided in example 1 can realize ammonia nitrogen (solvent stripping recovery) at low temperature, water evaporation, salt crystallization (high boiling point) separation at high temperature by using low temperature heat source preheating.

[0071] The above is only the preferred embodiment of the present application, and is not intended to limit the present application in other forms. Any skilled person in the art can modify or change the above disclosed technical content to equivalent embodiments. However, any simple modification, equivalent change and modification of the above embodiments without departing from the technical scheme of the present application, according to the technical essence of the present application, still belongs to the protection scope of the technical scheme of the present application.

Claims

1. A system for treating high ammonia-nitrogen wastewater and ammonia water resource recovery using a low-temperature heat source, characterized by, The system comprises: a stripping blow-off tower (4) provided with a high-ammonia-nitrogen wastewater inlet in the middle part; a blower (1) connected with the middle part of the stripping blow-off tower (4); a first heat exchanger (9) which exchanges heat with the bottom discharge of the stripping blow-off tower (4) through a low-grade heat source in a production area, and the bottom discharge of the stripping blow-off tower (4) after heat exchange flows back to the top of the stripping blow-off tower (4); a first spray absorption tower (10) connected with the top of the stripping blow-off tower (4) and the bottom of the first spray absorption tower (10), and the top discharge of the stripping blow-off tower (4) flows into the first spray absorption tower (10) from the bottom of the first spray absorption tower (10); a second spray absorption tower (15) connected with the top of the first spray absorption tower (10) and the bottom of the second spray absorption tower (15), and the top discharge of the first spray absorption tower (10) flows into the second spray absorption tower (15) from the bottom of the second spray absorption tower (15); a falling-film absorption tower (18) connected with the top of the second spray absorption tower (15) and the bottom of the falling-film absorption tower (18), and the top discharge of the second spray absorption tower (15) flows into the falling-film absorption tower (18) from the bottom of the falling-film absorption tower (18).

2. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 1, characterized in that, The first heat exchanger (9) comprises a first heat exchange cavity and a second heat exchange cavity, and a heat-conducting partition plate is arranged between the first heat exchange cavity and the second heat exchange cavity, the bottom discharge of the stripping blow-off tower (4) flows through the first heat exchange cavity to flow back to the top of the stripping blow-off tower (4), and the low-grade heat source in the production area flows through the second heat exchange cavity to exchange heat with the bottom discharge of the stripping blow-off tower (4).

3. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 1, characterized in that, A forced circulation water pump (5) is arranged between the bottom discharge inlet of the stripping blow-off tower (4) and the feed inlet of the first heat exchanger (9).

4. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 3, characterized in that, A wastewater collection tank (6) is arranged between the forced circulation water pump (5) and the feed inlet of the first heat exchanger (9).

5. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 1, characterized in that, The system further comprises a high-ammonia-nitrogen wastewater storage tank (2) which is connected with the high-ammonia-nitrogen wastewater inlet.

6. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 1, characterized in that, The system further comprises a first condensate water pump (11) and a second heat exchanger (12), and the bottom discharge outlet of the first spray absorption tower (10) is sequentially connected with the first condensate water pump (11) and the second heat exchanger (12) through pipelines, and the bottom discharge of the first spray absorption tower (10) after heat exchange with the second heat exchanger (12) flows back to the first spray absorption tower (10).

7. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 6, characterized in that, The system further comprises a second condensate water pump (17) and a third heat exchanger (16), and the bottom discharge outlet of the second spray absorption tower (15) is sequentially connected with the second condensate water pump (17) and the third heat exchanger (16) through pipelines, and the bottom discharge of the second spray absorption tower (15) after heat exchange with the third heat exchanger (16) flows back to the second spray absorption tower (15).

8. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 7, characterized in that, The system further comprises a first ammonia water recovery tank (14), the pipes between the first condensate pump (11) and the second heat exchanger (12), and the pipes between the second condensate pump (17) and the third heat exchanger (16) are communicated with the first ammonia water recovery tank (14) through pipes, and a first discharge valve (13) is arranged on the communication pipes.

9. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 1, characterized in that, The system further comprises a third condensate pump (20) and a falling film evaporator (21), and the falling film absorption tower (18) bottom discharge is communicated with the third condensate pump (20) and the falling film evaporator (21) through pipes in turn, and the falling film absorption tower (18) bottom discharge concentrated by evaporation in the falling film evaporator (21) is returned to the falling film absorption tower (18).

10. The system for treating high ammonia-nitrogen wastewater and recovering ammonia water resource by using low-temperature heat source according to claim 9, characterized in that, The system further comprises a second ammonia water recovery tank (19), and the pipes between the third condensate pump (20) and the falling film evaporator (21) are communicated with the second ammonia water recovery tank (19) through pipes, and a second discharge valve (22) is arranged on the communication pipes.

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