CN216445042U

CN216445042U - Ammonium nitrate wastewater treatment system

Info

Publication number: CN216445042U
Application number: CN202122325795.1U
Authority: CN
Inventors: 叶伟炳; 李琴; 王明富
Original assignee: Guangdong Wenyang Environmental Technology Co ltd
Current assignee: Guangdong Wenyang Environmental Technology Co ltd
Priority date: 2021-09-24
Filing date: 2021-09-24
Publication date: 2022-05-06
Anticipated expiration: 2031-09-24

Abstract

The utility model relates to an ammonium nitrate wastewater treatment system. The system comprises a preheating system, an evaporation system, a cooling system and a liquid discharge treatment system. Preheat ammonium nitrate waste water stoste through preheating the system to when follow-up evaporating system evaporates waste water stoste, reduce the energy consumption. Make the waste water stoste concentrate through the evaporation system, obtain the concentrate that ammonium nitrate concentration is higher to subsequent crystallization or outsourcing are handled, can effectively retrieve the nitrogen element in the ammonium nitrate waste water. In addition, distilled water with low ammonia nitrogen content and chemical oxygen demand content can be obtained through a discharged liquid treatment system, and is convenient to discharge or recycle.

Description

Ammonium nitrate wastewater treatment system

Technical Field

The utility model relates to the technical field of wastewater treatment, in particular to an ammonium nitrate wastewater treatment system.

Background

In the wastewater treatment, different kinds of wastewater are treated by different treatment processes. Among the various types of waste water, there is a waste water with ammonium nitrate, the concentration of which is about 10-30%.

At present, ammonium nitrate wastewater is treated by adopting a mode of discharging after dilution.

However, this method not only causes nitrogen loss, but also causes serious environmental pollution. Therefore, an ammonium nitrate wastewater treatment device is needed to treat the ammonium nitrate wastewater.

SUMMERY OF THE UTILITY MODEL

Therefore, it is necessary to provide an ammonium nitrate wastewater treatment device aiming at the problem of excessive nitrogen loss in the ammonium nitrate wastewater treatment process.

An ammonium nitrate wastewater treatment system comprising:

the preheating system is used for heating the wastewater stock solution;

the evaporation system comprises a heating component and a separation chamber; the liquid inlet end of the heating assembly is communicated with the preheating system, the separation chamber is provided with a liquid inlet, a liquid outlet, a backflow port and a steam outlet, the liquid inlet of the separation chamber is communicated with the liquid outlet end of the heating assembly, and the backflow port of the separation chamber is communicated with the liquid inlet end of the heating assembly; the separation chamber is used for separating the wastewater stock solution into a concentrated solution and first steam; the liquid outlet is used for discharging the concentrated solution, and the steam outlet is used for discharging the first steam;

a cooling system in communication with the vapor outlet of the separation chamber to cool the first vapor to obtain a first liquid;

and the liquid discharge treatment system is communicated with a liquid discharge end of the cooling system and is used for reducing the ammonia nitrogen content and the chemical oxygen demand content in the first liquid.

In one embodiment, the liquid discharge treatment system comprises a biochemical system or a nanofiltration system, and a liquid inlet end of the biochemical system or the nanofiltration system is communicated with a liquid discharge end of the cooling system.

In one embodiment, the liquid discharge treatment system further comprises a pH value adjusting device, wherein the liquid inlet end of the pH value adjusting device is communicated with the liquid discharge end of the cooling system, and the liquid discharge end of the pH value adjusting device is communicated with the liquid inlet end of the liquid discharge treatment system.

In one embodiment, the apparatus further comprises a crystallization device, the crystallization device is communicated with the liquid outlet of the separation chamber, and the crystallization device is used for crystallizing the concentrated solution.

In one embodiment, the device further comprises a distilled water storage device, wherein the liquid inlet end of the distilled water storage device is communicated with the liquid discharge end of the cooling system, and the liquid outlet end of the distilled water storage device is communicated with the heat source inlet end of the preheating system.

In one embodiment, the preheating system comprises a dope inlet end, a dope outlet end, a heat source inlet end and a heat source outlet end; the raw liquid inlet end is used for inputting raw liquid of wastewater, the raw liquid output end is communicated with the liquid inlet end of the heating assembly, the heat source inlet end is communicated with the liquid outlet end of the distilled water storage device, and the heat source outlet end is communicated with the liquid inlet end of the liquid discharge treatment system.

In one embodiment, the cooling system comprises at least two cooling devices which are communicated in sequence, and the liquid outlet end of each cooling device is communicated with the distilled water storage device.

In one embodiment, the number of the evaporation systems is more than two, and in the adjacent evaporation systems, the liquid outlet of the separation chamber of the former evaporation system is communicated with the liquid inlet of the separation chamber of the latter evaporation system.

In one embodiment, the evaporation system is provided with a heating device, the heating device is connected with the heating assembly, and the heating device is used for providing a heating source for the heating assembly.

In one embodiment, the heating device is a heat transfer oil heating device or a steam heating device.

Above-mentioned ammonium nitrate effluent disposal system heats the waste water stoste through preheating the system, has the uniform temperature when making it get into vaporization system, and the heating system of being convenient for heats it with the evaporation. The wastewater stock solution is evaporated in the separation chamber to obtain a concentrated solution and first steam. The first steam is cooled by a cooling system and is subjected to subsequent treatment by a discharged liquid treatment system so as to reduce the ammonia nitrogen content and the chemical oxygen demand content in the first steam, and the first steam is conveniently discharged. The concentrated solution may be crystallized or ammonium nitrate crystals may be recovered by ex situ treatment to recover the nitrogen in the ammonium nitrate waste water.

Drawings

Fig. 1 is a schematic diagram of an ammonium nitrate wastewater treatment system according to an embodiment of the present invention.

Description of the drawings:

100. a preheating system; 110. a feed liquid delivery pump; 120. a heat exchange device; 200. an evaporation system; 210. A heating assembly; 211. a first heater; 212. second heating; 231. a third heater; 220. a separation chamber; 221. a primary separation chamber; 222. a two-effect separation chamber; 223. a triple effect separation chamber; 230. a forced circulation pump; 231. a first forced circulation pump; 232. a second forced circulation pump; 233. a third forced circulation pump; 240. A heat conducting oil heating system; 300. a crystallization device; 310. a concentrate pump; 400. a cooling system; 410. a main condenser; 420. a final condenser; 430. a vacuum pump; 440. a separation tank; 500. a distilled water storage device; 510. a distilled water tank; 520. a distilled water pump; 600. a liquid discharge treatment system.

Detailed Description

In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the utility model and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be considered limiting of the utility model.

Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.

In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature "under," "beneath," and "under" a second feature may be directly under or obliquely under the second feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

It will be understood that when an element is referred to as being "secured to" or "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. As used herein, the terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like are for purposes of illustration only and do not denote a single embodiment.

Referring to fig. 1, an ammonium nitrate wastewater treatment system according to an embodiment of the present invention includes a preheating system 100, an evaporation system 200, a crystallization apparatus 300, a cooling system 400, and a discharged liquid treatment system 600. Wherein, preheating system 100 can heat the waste water stoste for the temperature of waste water stoste promotes to some extent. The evaporation system 200 can evaporate the wastewater dope to obtain a first vapor and a concentrated solution, and the evaporation system 200 can separate the first vapor from the concentrated solution. The concentrated solution may be introduced into the crystallization apparatus 300 to crystallize ammonium nitrate, or may be subjected to an outsourcing treatment to recover ammonium nitrate. The first vapor obtained by the evaporation system 200 can be cooled by the cooling system 400 to lower the temperature of the first vapor and obtain the first liquid. The effluent treatment system 600 may treat the first liquid to reduce the ammonia nitrogen content and the chemical oxygen demand content therein to obtain distilled water.

Through above-mentioned ammonium nitrate effluent disposal system, can obtain the concentrate that contains ammonium nitrate when handling ammonium nitrate waste water, can be convenient for subsequent crystallization to carry out nitrogen recovery, reduce the loss of nitrogen. Meanwhile, distilled water with low ammonia nitrogen content and chemical oxygen demand content can be obtained, and recycling can be facilitated.

In some embodiments, the preheating system 100 includes a feed liquid delivery pump 110 and a heat exchange device 120, the feed liquid delivery pump 110 can deliver the wastewater raw liquid into the heat exchange device 120, and the heat exchange device 120 is used for heating the wastewater raw liquid.

Specifically, the heat exchanging device 120 may be a plate heat exchanger or the like. The heat exchanging device 120 includes a raw liquid inlet end, a raw liquid outlet end, a heat source inlet end, and a heat source outlet end. Wherein, the stock solution inlet end is communicated with the stock solution outlet end, and the heat source inlet end is communicated with the heat source outlet end. The wastewater dope can enter the heat exchange device 120 along the dope inlet end under the pumping of the feed liquid transfer pump 110, and exchange heat with the heat source entering in the heat source inlet end to increase the temperature of the wastewater dope. Wherein, the heat source can be liquid heat source or gas heat source, such as hot water, hot oil or hot air with temperature higher than 80 deg.C. The dope output may be in communication with the vaporization system 200.

In some embodiments, the vaporization system 200 includes a separation chamber and a heating assembly 210. Wherein, heating element 210 is used for heating waste water stoste, and the separator is used for separating first steam and concentrate.

The heating assembly 210 may include a heater. The heating heat source of the heater can be a liquid heat source or a gas heat source. Such as hot oil or air, etc.

In some embodiments, the heat source may be hot oil. The heating assembly 210 further includes a heat transfer oil heating system 240 and an oil transfer pump. The conduction oil heating system 240 may heat the oil by means of electric heating, etc. The oil transfer pump is used for transferring the heated heat transfer oil into the heater so as to heat the wastewater stock solution.

The heat conducting oil heating system 240 includes an oil inlet and an oil outlet, and the heater includes a heat source inlet and a heat source outlet. The oil enters the heat conduction oil heating system 240 for heating, and the heat conduction oil obtained after heating enters the heat source inlet of the heater from the oil outlet of the heat conduction oil heating system 240 so as to carry out heat exchange on the wastewater stock solution and further improve the temperature of the wastewater stock solution. And the temperature of the heat-exchanged heat conduction oil is reduced, and the heat conduction oil flows out from the heat source outlet of the heater and flows back to the oil inlet of the heat conduction oil heating system 240, so that the heat conduction oil can be heated circularly.

The heater also comprises a liquid inlet end and a liquid outlet end, wherein the liquid inlet end of the heater can be communicated with the stock solution output end of the preheating system 100 so as to heat the stock solution. The liquid outlet end of the heater is communicated with the separation chamber. The liquid inlet end and the liquid outlet end of the heater are communicated through a heat exchange tube (not shown in the figure). The number of the heat exchange pipes may be plural. The heat exchange tube can be bent and folded in the heater, and other arrangement modes can be adopted, so that the contact area and the contact time of the waste water stock solution in the heat exchange tube and the heat exchange of the heating source are increased. The flow velocity of the waste water stock solution in the heat exchange tube can be controlled to be 1.5-3.0 m/s, and the waste water stock solution can be prevented from scaling on the surface of the heat exchange tube to affect the heat exchange efficiency.

In some embodiments, the vaporization system 200 is a cyclical vaporization system 200. That is, the evaporation system 200 further comprises a forced circulation pump 230, and the forced circulation pump 230 is used for pumping the liquid obtained from the separation chamber 220 back to the heater for reheating and separation.

Specifically, the separation chamber 220 may include a liquid inlet, a liquid outlet, a liquid return, and a vapor outlet. The inlet of the separation chamber 220 may be in communication with the raw liquid outlet of the preheating system 100, that is, the inlet of the heater is in communication with the raw liquid outlet of the preheating system 100 through the separation chamber 220. The liquid outlet of the separation chamber 220 is communicated with a forced circulation pump, the forced circulation pump 230 has a liquid outlet and a reflux port, and the liquid outlet of the forced circulation pump 230 is communicated with another evaporation system 200 or with the crystallization apparatus 300. The return port of the forced circulation pump 230 communicates with the liquid inlet end of the heater. The liquid outlet end of the heater is communicated with the reflux port of the separation chamber 220. While a steam outlet at the top of the separation chamber 220 may allow water vapor to exit the evaporation system 200.

In the evaporation system 200, the wastewater raw liquid can enter the separation chamber 220 through a liquid inlet of the separation chamber 220, and exit the separation chamber 220 through a liquid outlet of the separation chamber 220, and then enter the heater through a return port of the forced circulation pump 230 to be heated under the conveying of the forced circulation pump 230. The heated wastewater stock solution can enter the separation chamber 220 through a return port of the separation chamber 220. Because the pressure in the separation chamber 220 is lower than the pressure in the heater, the wastewater raw liquid does not boil in the heater, and after entering the separation chamber 220, the wastewater raw liquid is flashed in the separation chamber 220 due to the reduction of the pressure to obtain a concentrated liquid and a first steam, the first steam is discharged out of the separation chamber 220 from a steam outlet of the separation chamber 220, the concentrated liquid is discharged to the forced circulation pump 230 from a liquid outlet of the separation chamber 220, and enters the heater again to be heated, and the above process is repeated to perform cyclic evaporation. When the obtained concentrated solution after flash evaporation reaches the corresponding concentration multiple, that is, the concentration of ammonium nitrate in the concentrated solution reaches the predetermined standard, the concentrated solution can be discharged through the liquid outlet of the forced circulation pump 230.

In some embodiments, the number of the evaporation systems 200 is plural, for example, two or more are selected. And the evaporation systems 200 are connected in sequence to enable the wastewater stock solution to carry out multi-effect evaporation. The heating temperature in the heaters in the vaporization system 200 may be sequentially reduced in the flow pattern along the wastewater dope.

For example, in the illustrated embodiment, the number of the evaporation systems 200 is three, and the evaporation systems are respectively the first evaporation system 200, the second evaporation system 200, and the third evaporation system 200, which are connected in sequence.

The first evaporation system 200 includes a first heater 211, a first effect separation chamber 221, and a first forced circulation pump 231. The second evaporation system 200 comprises a second heater 212, a two-effect separation chamber 222 and a second forced circulation pump 232. The third evaporation system 200 includes a third heater 231, a three-effect separation chamber 223, and a third forced circulation pump 233. The liquid outlet of the first forced circulation pump 231 is communicated with the liquid inlet of the two-effect separation chamber 222, and the liquid outlet of the second forced circulation pump 232 is communicated with the liquid inlet of the three-effect separation chamber 223.

In the illustrated embodiment, the heating source of the first heater 211 is thermal oil. Therefore, in the first evaporation system 200, the aforementioned thermal oil heating system 240 is further included. The heating sources of the second heater 212 and the third heater 231 may be selected from steam, and the first steam obtained by the previous evaporation system 200 may be selected. That is, the steam outlet of the primary separation chamber 221 is communicated with the heat source inlet of the second heater 212, and the heat source outlet of the second heater 212 is communicated with the cooling system 400; the steam outlet of the two-effect separation chamber 222 is communicated with the heat source inlet of the third heater 231, and the heat source outlet of the third heater 231 is communicated with the cooling system 400. The steam outlet of the primary separation chamber 221 may be in direct communication with the cooling system 400.

The arrangement can recycle the heat in the first steam obtained by the previous evaporation system 200, reduce energy consumption and increase energy recovery.

In addition, in the third evaporation system 200, the liquid outlet of the three-effect separation chamber 223 can be directly communicated with the third forced circulation pump 233, the third forced circulation pump 233 comprises the aforementioned reflux port and liquid outlet, and the liquid outlet can be communicated with the crystallization apparatus 300. In other embodiments, the liquid outlets of the three-way separation chamber 223 can be connected by a tee, an opening of the tee is connected with the third forced circulation pump 233, and the third forced circulation pump 233 has only a return opening. The other opening of the tee can be connected to a concentrate pump 310 so that concentrate can enter the crystallization device 300 through the concentrate pump 310 for crystallization or can be output for outsourcing.

In some embodiments, the crystallization device 300 may be a storage barrel or the like, temporarily stores the concentrated solution, and dissipates heat through air, so that ammonium nitrate is separated out after the temperature of the concentrated solution is reduced, and the subsequent outsourcing treatment may be performed.

In some implementations, the cooling system 400 may include at least two cooling devices in serial communication. The cooling device may cool the first vapor obtained by the evaporation system 200 to obtain the first liquid.

In the illustrated embodiment, the number of cooling devices is two, a main condenser 410 and a final condenser 420.

Wherein the air inlet of the main condenser 410 may be in communication with a steam outlet within the evaporation system 200, i.e. with a steam outlet of the three-way separation chamber 223, for a first cooling of the first vapor. The first liquid obtained from the main condenser 410 may be collected by the distilled water storage device 500 and then uniformly processed. The distilled water storage device 500 may be a distilled water tank 510. Since the first steam contains water vapor and non-condensable gas, part of the non-condensed water vapor and non-condensable gas can enter the final condenser 420 through the gas outlet of the main condenser 410 for further cooling treatment.

The final condenser 420 may receive the water vapor and the non-condensable gas discharged from the outlet of the main condenser 410, and the final condenser 420 may receive the first vapor as a heat source in the evaporation apparatus. That is, the first vapor discharged from the heat source outlet of the second heater 212 and the heat source outlet of the third heater 231 may be introduced into the final condenser 420 to be condensed.

The first liquid condensed by the final condenser 420 may be introduced into the distilled water storage apparatus 500 together with the first liquid condensed by the main condenser 410, or may be introduced into another distilled water storage apparatus 500. The non-condensable gas can be discharged out of the ammonium nitrate wastewater treatment system by arranging a vacuum pump 430 and a separation tank 440 which are arranged in sequence.

The cooling system 400 may then exchange heat with the condensate to cause condensation of the water vapor. In the illustrated embodiment, the condensate may enter the main condenser 410 and the final condenser 420 through different pipes for heat exchange, and after heat exchange, the condensate may be discharged through the same pipe or different pipes and cooled for recycling.

In the illustrated embodiment, the distilled water condensed by the final condenser 420 and the first liquid condensed by the main condenser 410 enter the same distilled water storage device 500, and in addition, in the evaporation system 200, when the heater heats, a part of the first vapor forms the first liquid, and the part of the distilled water also enters the distilled water storage device 500 together. The first liquid stored in the distilled water storage device 500 has a temperature higher than the normal temperature, and therefore, can be used as a heat source of the preheating system 100 to recycle heat.

In the distilled water storage device 500, a portion of the distilled water in the first liquid may form water vapor, and the water vapor may enter the main condenser 410 through the air outlet of the distilled water storage device 500 for condensation.

In some embodiments, the distilled water pump 520 is connected to the outlet of the distilled water storage device 500, the distilled water pump 520 can deliver the first liquid with higher temperature in the distilled water storage device 500 to the heat source inlet end of the heat exchange device 120, and after the first liquid is subjected to heat exchange, the temperature of the first liquid is reduced, and the first liquid is discharged from the heat source outlet end to enter the discharged liquid treatment system 600 for treatment, so as to reduce the ammonia nitrogen content and the chemical oxygen demand content in the first liquid, and obtain distilled water which can be recycled or discharged.

In some embodiments, the liquid waste treatment system 600 may be a biochemical system or a nanofiltration system. Wherein, the biochemical system can select an anaerobic tank, an anoxic tank and an aerobic tank which are arranged in sequence. Impurities in the first solution are removed by a biochemical system. The nanofiltration system is provided with a nanofiltration membrane which can separate the distilled water in the first solution. The liquid inlet end of the biochemical system or the nanofiltration system is communicated with the liquid discharge end of the cooling system 400.

In addition, in some embodiments, the discharged liquid treatment system 600 further includes a pH adjusting device, and an inlet end of the pH adjusting device is communicated with the discharged liquid end of the cooling system 400, or is communicated with a liquid outlet of the distilled water storage device 500, or is communicated with a heat source discharge end of the heat exchanging device 120, and can be adjusted according to actual situations. The liquid discharge end of the pH value adjusting device is communicated with the liquid inlet end of the biochemical system or the liquid inlet end of the nanofiltration system. The pH value adjusting device can adjust the pH value of the first liquid.

The pH value adjusting device can enable the first liquid to be acidic, so that ammonia nitrogen in the first liquid exists in the first liquid in an ammonium salt form, a subsequent biochemical system or a nanofiltration system can conveniently process the first liquid, and the quality of outlet water of obtained distilled water is improved.

In an embodiment, the treatment capacity of the ammonium nitrate wastewater raw liquid is 10T/D, the ammonium nitrate concentration of the wastewater raw liquid is 24.3%, when the ammonium nitrate treatment system of the illustrated embodiment is used for treating the wastewater raw liquid, after the evaporation system 200 evaporates, the concentration of ammonium nitrate in the obtained concentrated liquid containing ammonium nitrate reaches 81%, so that the subsequent crystallization treatment is facilitated.

Through above-mentioned ammonium nitrate effluent disposal system, can preheat ammonium nitrate waste water and circulation evaporation, obtain the higher ammonium nitrate solution of concentration, later crystallize it through crystallizer 300 to obtain ammonium nitrate crystal, so that recycle. In addition, in the ammonium nitrate wastewater treatment process, water vapor can be recycled, and the water vapor is used as a heat source for heat exchange, so that the heat loss is reduced, and the process is more green and environment-friendly.

The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.

The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the utility model. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.

Claims

1. An ammonium nitrate wastewater treatment system, comprising:

the preheating system is used for heating the wastewater stock solution;

2. The ammonium nitrate wastewater treatment system according to claim 1, wherein the liquid discharge treatment system comprises a biochemical system or a nanofiltration system, and a liquid inlet end of the biochemical system or the nanofiltration system is communicated with a liquid discharge end of the cooling system.

3. The ammonium nitrate wastewater treatment system according to claim 1, wherein the discharged liquid treatment system further comprises a pH value adjusting device, wherein a liquid inlet end of the pH value adjusting device is communicated with a liquid outlet end of the cooling system, and a liquid outlet end of the pH value adjusting device is communicated with a liquid inlet end of the discharged liquid treatment system.

4. The ammonium nitrate wastewater treatment system of claim 1, further comprising a crystallization device in communication with the liquid outlet of the separation chamber, the crystallization device being configured to crystallize the concentrate.

5. The ammonium nitrate wastewater treatment system according to claim 1, further comprising a distilled water storage device, wherein a liquid inlet end of the distilled water storage device is communicated with a liquid discharge end of the cooling system, and a liquid outlet end of the distilled water storage device is communicated with a heat source inlet end of the preheating system.

6. The ammonium nitrate wastewater treatment system according to claim 5, wherein the preheating system includes a raw liquid inlet end, a raw liquid outlet end and a heat source discharge end; the stoste inlet end is used for inputting a wastewater stoste, the stoste output end is communicated with the liquid inlet end of the heating assembly, and the heat source discharge end is communicated with the liquid inlet end of the liquid discharge treatment system.

7. The ammonium nitrate wastewater treatment system according to claim 5, wherein the cooling system comprises at least two cooling devices which are communicated in sequence, and the liquid outlet end of each cooling device is communicated with the distilled water storage device.

8. The ammonium nitrate wastewater treatment system according to claim 1, wherein the number of the evaporation systems is two or more, and in the adjacent evaporation systems, the liquid outlet of the separation chamber of the former evaporation system is communicated with the liquid inlet of the separation chamber of the latter evaporation system.

9. The ammonium nitrate wastewater treatment system of claim 1, wherein the evaporation system is provided with a heating device connected to the heating assembly, the heating device being configured to provide a heating source to the heating assembly.

10. The ammonium nitrate wastewater treatment system according to claim 9, wherein the heating device is a conduction oil heating device or a steam heating device.