CN213387880U - Wastewater treatment system - Google Patents
Wastewater treatment system Download PDFInfo
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- CN213387880U CN213387880U CN202022217744.2U CN202022217744U CN213387880U CN 213387880 U CN213387880 U CN 213387880U CN 202022217744 U CN202022217744 U CN 202022217744U CN 213387880 U CN213387880 U CN 213387880U
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Abstract
The application provides a wastewater treatment system, relates to waste water treatment technical field. The wastewater treatment system comprises an MVR evaporation crystallization subsystem and a deamination subsystem; the MVR evaporation crystallization subsystem comprises an MVR evaporation crystallization unit and a distilled water treatment unit, and a distilled water drainage port of the MVR evaporation crystallization unit is connected with the distilled water treatment unit; the deamination subsystem comprises a deamination tower and a combined preheating heat exchanger, the deamination tower is connected with the MVR evaporation crystallization unit, and the combined preheating heat exchanger is connected with the distilled water treatment unit; and a wastewater stock solution conveying pipeline for conveying the wastewater stock solution is connected with a combined preheating heat exchanger, and the combined preheating heat exchanger is connected with a wastewater stock solution inlet end at the top of the deamination tower. Waste water stock solution subjected to primary heat exchange through the combined preheating heat exchanger is treated by the deamination tower again to obtain deamination waste water back solution meeting the temperature required by the MVR evaporative crystallization unit, so that secondary heat exchange is not needed, the heat exchange times are reduced, the utilization rate of heat energy is improved, and the cost is saved.
Description
Technical Field
The application relates to the technical field of wastewater treatment, in particular to a wastewater treatment system.
Background
High ammonia and high salt wastewater is one of common wastewater in chemical industry, and the common wastewater treatment mode is a deamination tower device + MVR (Mechanical Vapor Recompression) evaporative crystallization device.
In the deamination tower device, deamination liquid and low-temperature wastewater stock solution enter the MVR evaporative crystallization device after primary heat exchange through a stock solution preheating heat exchanger; in MVR evaporation crystallization device, the liquid after the deamination carries out twice heat transfer through liquid preheat heat exchanger and steam preheater after the deamination and MVR evaporation crystallization device distilled water in proper order again, receives the heat transfer efficiency influence, and the heat energy waste rate is higher.
SUMMERY OF THE UTILITY MODEL
In order to overcome the not enough among the prior art, the application provides a effluent disposal system for receive heat transfer efficiency influence among the solution prior art heat transfer process many times, lead to the higher technical problem of heat energy waste rate.
In order to achieve the purpose, the application provides a wastewater treatment system which is applied to the treatment of high-ammonia and high-salt wastewater and comprises an MVR evaporation crystallization subsystem and a deamination subsystem;
the MVR evaporative crystallization subsystem comprises an MVR evaporative crystallization unit and a distilled water treatment unit, and a distilled water drainage port of the MVR evaporative crystallization unit is connected with the distilled water treatment unit;
the deamination subsystem comprises a deamination tower and a combined preheating heat exchanger, the deamination tower is connected with the MVR evaporation crystallization unit, and the combined preheating heat exchanger is connected with the distilled water treatment unit;
the combined preheating heat exchanger is connected with a wastewater stock solution inlet end at the top of the deamination tower.
In a possible embodiment mode, the deamination tower further comprises a heating kettle at the bottom, and the heating kettle is connected with a saturated steam supply pipeline.
In a possible embodiment mode, the discharge port of the heating kettle is connected with a first discharge pump, and the first discharge pump is respectively connected with the feed port of the heating kettle and the MVR evaporative crystallization unit.
In a possible embodiment mode, the discharge port of the heating kettle is connected with two first discharge pumps, one of the first discharge pumps is connected with the MVR evaporative crystallization unit, and the other first discharge pump is connected with the feed port of the heating kettle.
In a feasible embodiment mode, the deamination subsystem further comprises an ammonia gas collecting unit, the ammonia gas collecting unit comprises an ammonia gas condenser and a cold water loop connected with the ammonia gas condenser, the ammonia gas inlet end of the ammonia gas condenser is connected with the ammonia gas outlet end at the top of the deamination tower, and the ammonia water outlet end of the ammonia gas condenser is connected with an ammonia water collecting pipe.
In a possible embodiment, the MVR evaporative crystallization unit includes an MVR crystallization separator, an MVR forced circulation heat exchanger, and a forced circulation pump, and the MVR crystallization separator, the MVR forced circulation heat exchanger, and the forced circulation pump are connected to form a circulation loop, wherein:
the MVR crystallization separator is also connected with the deamination tower;
and a distilled water discharge port of the MVR forced circulation heat exchanger is connected with the distilled water treatment unit.
In a possible embodiment, the MVR evaporative crystallization unit further comprises a vapor compressor, and the vapor compressor is connected to the MVR crystallization separator and the MVR forced circulation heat exchanger, respectively.
In a possible embodiment, the wastewater treatment system further includes a salt discharge subsystem, and the salt discharge subsystem includes a second discharge pump and a centrifugal drying device, and the second discharge pump is connected to the MVR crystal separator and the centrifugal drying device, respectively.
In a possible embodiment mode, the distilled water treatment unit comprises a third discharge pump, the water inlet end of the third discharge pump is connected with the distilled water discharge port, and the water outlet end of the third discharge pump is connected with the combined preheating heat exchanger.
In a possible embodiment, the distilled water treatment unit further comprises a distilled water storage container, and the distilled water storage container is respectively connected with the distilled water discharge port and the water inlet end of the third discharge pump.
Compared with the prior art, the beneficial effects of the application are that:
the application provides a wastewater treatment system, which comprises an MVR evaporation crystallization subsystem and a deamination subsystem; the MVR evaporation crystallization subsystem comprises an MVR evaporation crystallization unit and a distilled water treatment unit, and a distilled water drainage port of the MVR evaporation crystallization unit is connected with the distilled water treatment unit; the deamination subsystem comprises a deamination tower and a combined preheating heat exchanger, the deamination tower is connected with the MVR evaporation crystallization unit, and the combined preheating heat exchanger is connected with the distilled water treatment unit; the combined preheating heat exchanger is connected with a wastewater stock solution inlet end at the top of the deamination tower. The application provides a wastewater treatment system, the low temperature waste water stoste of carrying in the high temperature distilled water that utilizes the distilled water processing unit to provide and the waste water stoste conveying pipeline carries out a heat transfer through jointly preheating the heat exchanger, the high temperature waste water stoste that obtains after the heat transfer gets into the deamination tower again and carries out the deamination processing, the deamination waste water back liquid that obtains, because, the temperature of deamination waste water back liquid can reach the required temperature of MVR evaporation crystallization unit, can directly carry deamination waste water back liquid to MVR evaporation crystallization unit and carry out the evaporation crystallization processing, need not again through the heat transfer, and then reduced the heat transfer number of times, the utilization ratio of heat energy has been improved.
In addition, because this application has reduced the heat transfer number of times, and then has reduced indirect heating equipment's input, save the cost.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention, and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic diagram illustrating a modular configuration of a wastewater treatment system according to an embodiment of the present disclosure;
FIG. 2 is a schematic diagram illustrating a wastewater treatment system according to an embodiment of the present disclosure;
FIG. 3 shows a schematic diagram of a deamination tower in a wastewater treatment system provided by an embodiment of the present application;
FIG. 4 shows a schematic structural diagram of an MVR evaporative crystallization subsystem in a wastewater treatment system provided by an embodiment of the present application.
Description of the main element symbols:
100-MVR evaporative crystallization subsystem; 110-MVR evaporative crystallization unit; 111-MVR forced circulation heat exchanger; 1110-distilled water discharge; 112-MVR crystallization separator; 113-forced circulation pump; 114-a vapor compressor; 120-distilled water treatment unit; 121-a third discharge pump; 122-distilled water storage container;
200-a deamination subsystem; 210-combined preheat exchanger; 210 a-a wastewater stock solution conveying pipeline; 220-a deamination tower; 221-a first discharge pump; 222-heating the kettle; 223-a laminar flow configuration; 224-ammonia outlet port; 225-wastewater bulk inlet end; 226-discharge port; 227-feed port; 230-an ammonia gas collection unit; 231-ammonia gas condenser; 232-cold water circuit; 233-ammonia collecting pipe; 240-saturated steam supply line;
300-salt discharge subsystem; 310-a second discharge pump; 320-centrifugal drying equipment.
Detailed Description
Reference will now be made in detail to embodiments of the present application, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present application and are not to be construed as limiting the present application.
In the description of the present application, it is to be understood that the terms "center," "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 present application and for simplicity in description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the present application.
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 one or more of that feature. In the description of the present application, "a plurality" means two or more unless specifically limited otherwise.
In this application, unless expressly stated or limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can include, for example, fixed connections, removable connections, or integral parts; can be mechanically or electrically connected; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art as appropriate.
In this application, unless expressly stated or limited otherwise, 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 intervening media. 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 being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
Examples
Referring to fig. 1, the wastewater treatment system provided in this embodiment is applied to the treatment of high-ammonia and high-salt wastewater, which is referred to as wastewater stock solution hereinafter.
The effluent disposal system that this embodiment provided includes MVR evaporation crystallization subsystem 100 and deamination subsystem 200, and wherein, deamination subsystem 200 is arranged in the ammonia of desorption waste water stoste, and the solution behind the waste water stoste desorption ammonia forms the back liquid of deamination waste water, and the back liquid of deamination waste water is high salt waste water. The MVR evaporative crystallization subsystem 100 is used for realizing evaporative crystallization of the deamination waste water back liquid, namely concentrating the deamination waste water back liquid, and separating water and salt in the deamination waste water back liquid.
Referring to fig. 1 and fig. 2, in detail, the MVR evaporative crystallization subsystem 100 includes an MVR evaporative crystallization unit 110 and a distilled water treatment unit 120, and a distilled water discharge port 1110 of the MVR evaporative crystallization unit 110 is connected to the distilled water treatment unit 120. The deamination subsystem 200 comprises a deamination tower 220 and a combined preheating heat exchanger 210, wherein the deamination tower 220 is connected with the MVR evaporation crystallization unit 110, the distilled water treatment unit 120 is connected with the combined preheating heat exchanger 210, a wastewater stock solution conveying pipeline 210a is connected with the combined preheating heat exchanger 210, and the combined preheating heat exchanger 210 is connected with a wastewater stock solution inlet end 225 at the top of the deamination tower 220.
It can be understood that waste water stoste pipeline 210a is used for carrying the waste water stoste, specifically carry the waste water stoste to jointly preheat the high temperature distilled water that heat exchanger 210 and distilled water processing unit 120 carried and carry out a heat transfer, promptly, obtain the waste water stoste of high temperature after preheating microthermal waste water stoste, in the waste water stoste of high temperature is carried to deamination tower 220 by waste water stoste pipeline 210a again, deamination processing is accomplished to the waste water stoste of high temperature in deamination tower 220.
Referring to fig. 2 and fig. 3, the deammoniation tower 220 is a vertically arranged tower structure, the bottom of the deammoniation tower 220 is a heating kettle 222, and a predetermined number of laminar flow structures 223 are disposed at the upper end of the deammoniation tower 220 far away from the heating kettle 222. The wastewater stock solution conveying pipeline 210a is connected to a wastewater stock solution inlet end 225 at the top of the deamination tower 220 through the combined preheating heat exchanger 210, a heating kettle 222 at the bottom of the deamination tower 220 is connected with a saturated steam supply pipeline 240, and the saturated steam supply pipeline 240 is used for conveying high-temperature saturated steam into the heating kettle 222.
It can be understood that, the high temperature waste water stoste that obtains through the heat transfer of joint preheating heat exchanger 210 gets into in the deammoniation tower 220 from the waste water stoste entrance point 225 at deammoniation tower 220 top, subsequently the waste water stoste flows into in the heating cauldron 222 of deammoniation tower 220 bottom along the laminar flow structure 223 in the deammoniation tower 220, ammonia is deviate from at this in-process that the waste water stoste falls into the heating cauldron 222 of deammoniation tower 220 bottom, and saturated steam supply line 240 combines with the ammonia in the deammoniation tower 220 to the saturated steam of carrying high temperature in heating cauldron 222, and take out the ammonia from the ammonia exit end 224 at deammoniation tower 220 top, and simultaneously, the saturated steam of high temperature can also carry out secondary heating with the deammoniation waste water back liquid in the deammoniation tower 220, be used for guaranteeing that.
Because the wastewater stock solution is preheated by the combined preheating heat exchanger 210 before entering the deamination tower 220, the high-temperature wastewater stock solution entering the deamination tower 220 can ensure a certain temperature in the deamination tower 220, and the temperature can ensure that high-temperature saturated steam can smoothly flow from the heating kettle 222 at the bottom of the deamination tower 220 to the ammonia outlet 224 at the top in a gaseous form.
Further, a discharge port 226 of the heating kettle 222 is connected to a first discharge pump 221, and the first discharge pump 221 is connected to the feed port 227 of the heating kettle 222 and the MVR evaporative crystallization unit 110 through a pipeline respectively. That is to say, first discharge pump 221 divides the deamination waste water back liquid in heating kettle 222 into two, and wherein a part of deamination waste water back liquid passes through pipeline entering MVR evaporation crystallization unit 110, and another part of deamination waste water back liquid gets back to and circulates once more in heating kettle 222, and the deamination waste water back liquid of once more circulated is heated by the saturated steam of the high temperature in heating kettle 222 again for the temperature of deamination waste water back liquid accords with the temperature of MVR evaporation crystallization unit 110 demand, and heat utilization rate is high. It can be understood that the temperature of the deamination waste water back liquid that comes out through heating kettle 222 can reach about 100 ℃, and the deamination waste water back liquid of this temperature can directly input MVR evaporation crystallization unit 110 and carry out the evaporation crystallization processing, need not to carry out heat transfer again and handles, reduces heat energy loss, improves heat utilization rate. In addition, because the heat exchange times are reduced, the investment of heat exchange equipment is reduced, and the cost is saved.
In some specific embodiments, the discharge port 226 of the heating kettle 222 may be connected with two first discharge pumps 221, wherein one of the first discharge pumps 221 is connected to the MVR evaporative crystallization unit 110 through a pipeline, and is configured to convey the deamination wastewater post-liquid in the heating kettle 222 to the MVR evaporative crystallization unit 110 for evaporative crystallization treatment; another first discharging pump 221 is connected to the feeding port 227 of the heating kettle 222 through a pipeline, so that the deamination wastewater in the heating kettle 222 is returned to the heating kettle 222 for recycling, and is heated again by the high-temperature saturated steam in the heating kettle 222.
Referring to fig. 2 and fig. 3, further, in order to avoid secondary pollution to the environment caused by the emission of ammonia gas in the deamination tower 220, in the embodiment, the deamination subsystem 200 further includes an ammonia gas collecting unit 230, and the ammonia gas collecting unit 230 is configured to collect ammonia gas and steam exhausted from an ammonia gas outlet 224 at the top of the deamination tower 220. Specifically, the ammonia gas collecting unit 230 includes an ammonia gas condenser 231 and a cold water loop 232 connected to the ammonia gas condenser 231, wherein an ammonia gas inlet end of the ammonia gas condenser 231 is connected to an ammonia gas outlet end 224 at the top of the deamination tower 220 through a pipeline, and an ammonia water outlet end of the ammonia gas condenser 231 is connected to an ammonia water collecting pipe 233.
The principle that ammonia water is collected to ammonia collection unit 230 is that, the saturated steam of high temperature carries the ammonia and carries out the heat transfer with the low temperature water that cold water return circuit 232 carried in ammonia condenser 231, meets and condenses into liquid aqueous ammonia after the cold, and the aqueous ammonia outlet end that the aqueous ammonia flowed into ammonia condenser 231 again is connected to aqueous ammonia collecting pipe 233 and collects, and then the effectual ammonia of avoiding is arranged outward and is caused secondary pollution to the environment.
Referring to fig. 2 and fig. 4, the MVR evaporative crystallization unit 110 includes an MVR crystallization separator 112, an MVR forced circulation heat exchanger 111, a forced circulation pump 113 and a vapor compressor 114, wherein the MVR crystallization separator 112, the MVR forced circulation heat exchanger 111 and the forced circulation pump 113 are connected to form a circulation loop. The vapor compressor 114 is connected to the MVR crystallization separator 112 and the MVR forced circulation heat exchanger 111, and more specifically, an air inlet of the vapor compressor 114 is connected to the top of the MVR crystallization separator 112, and an air outlet of the vapor compressor 114 is connected to the MVR forced circulation heat exchanger 111.
Wherein, MVR crystal separator 112 still connects deamination tower 220, and specifically MVR crystal separator 112 and the pipe connection of first discharge pump 221 conveying deamination waste water back liquid are used for realizing carrying out the evaporation crystallization in carrying out the deamination waste water back liquid to MVR crystal separator 112.
It can also be understood that vapor in the MVR crystallization separator 112 is extracted by the vapor compressor 114 to carry out secondary heating, and high-temperature vapor to be heated is conveyed to the MVR forced circulation heat exchanger 111 to carry out heat exchange, and the forced circulation pump 113 pumps the concentrated deamination waste water back liquid of the MVR crystallization separator 112 into the MVR forced circulation heat exchanger 111 to carry out heat exchange with the high-temperature vapor conveyed by the vapor compressor 114, so that the deamination waste water back liquid is heated up again, and the efficiency of evaporative crystallization of the MVR crystallization separator 112 is improved.
Enters the MVR forced circulation heat exchanger 111 to exchange heat with the deamination wastewater back liquid, is condensed into high-temperature distilled water, and is discharged into the distilled water treatment unit 120 from a distilled water discharge port 1110 on the MVR forced circulation heat exchanger 111.
In this embodiment, the distilled water processing unit 120 includes a third discharging pump 121, a water inlet end of the third discharging pump 121 is connected to the distilled water discharging port 1110, and a water outlet end of the third discharging pump 121 is connected to the combined preheating heat exchanger 210. That is to say, the third discharging pump 121 delivers the high-temperature distilled water from the distilled water discharge port 1110 to the combined preheating heat exchanger 210 to exchange heat with the wastewater stock solution in the wastewater stock solution delivery pipeline 210a for the first time, so as to preheat the wastewater stock solution entering the deamination tower 220.
Further, the distilled water after heat exchange by the combined preheating heat exchanger 210 can be discharged to the environment or collected for reuse through a pipeline.
In some embodiments, considering that the distilled water discharged from the distilled water discharging port 1110 has a relatively large amount, the distilled water treating unit 120 further includes a distilled water storing container 122, and the distilled water storing container 122 is used for buffering distilled water. Wherein, the distilled water storage container 122 is disposed between the MVR crystal separator 112 and the third discharging pump 121, and the distilled water storage container 122 is connected to the distilled water discharge port 1110 and the water inlet end of the third discharging pump 121 respectively.
In some embodiments, the distilled water storage container 122 is a tank structure.
Further, it can be understood that the content of salt in the deamination wastewater post-liquid after deamination treatment is high, and the deamination wastewater post-liquid after deamination treatment is concentrated by the MVR crystal separator 112 to obtain a high-concentration deamination wastewater post-liquid, i.e. a high-concentration salt solution.
Referring to fig. 1 and fig. 2, in order to avoid secondary pollution to the environment caused by discharge of the high-concentration salt solution, the wastewater treatment system provided in this embodiment further includes a salt discharge subsystem 300, the salt discharge subsystem 300 includes a second discharge pump 310 and a centrifugal drying device 320, the second discharge pump 310 is respectively connected to the MVR crystal separator 112 and the centrifugal drying device 320, that is, the second discharge pump 310 delivers the high-concentration salt solution in the MVR crystal separator 112 to the centrifugal drying device 320 for centrifugal drying and packaging.
The effluent disposal system that this embodiment provided compares prior art, has reduced the heat transfer number of times, has greatly improved the utilization ratio of heat energy. In addition, the heat exchange times of the deamination wastewater back liquid are reduced, so that the investment of heat exchange equipment is reduced, and the cost is saved.
Further, it can be understood that the ammonia tower device and the MVR evaporative crystallization device in the prior art are two sets of independent devices, the two sets of devices operate independently, the structure is complex, and the heat exchange efficiency is low. And because the wastewater treatment capacity of the two sets of equipment is designed differently, a large transfer pool is usually required to be built between the two sets of equipment for caching the deamination wastewater back liquid, the transfer pool increases the floor area and the cost investment.
And this application is through structural reasonable setting, integrates MVR evaporation crystallization subsystem 100 and deamination subsystem 200 into the integral structure, and the integrated nature is high, and is structural simpler, and compacter, and it is more convenient to maintain. In addition, in the whole process, the matching of the processing amount of the MVR evaporative crystallization subsystem 100 and the deamination subsystem 200 is realized, the running mode of immediate processing is realized, a transfer pool does not need to be additionally arranged, and the occupied area and the cost input are further reduced.
Moreover, after the wastewater treatment system continuously operates, only the deamination tower 220 in the deamination subsystem 200 needs saturated steam provided from the outside, so that the consumption of the saturated steam is reduced, and the cost is saved.
In the description herein, reference to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the application. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present application, and that variations, modifications, substitutions and alterations may be made to the above embodiments by those of ordinary skill in the art within the scope of the present application.
Claims (10)
1. A wastewater treatment system is characterized by being applied to the treatment of high-ammonia and high-salt wastewater, and the wastewater treatment system comprises an MVR evaporation crystallization subsystem and a deamination subsystem;
the MVR evaporative crystallization subsystem comprises an MVR evaporative crystallization unit and a distilled water treatment unit, and a distilled water drainage port of the MVR evaporative crystallization unit is connected with the distilled water treatment unit;
the deamination subsystem comprises a deamination tower and a combined preheating heat exchanger, the deamination tower is connected with the MVR evaporation crystallization unit, and the combined preheating heat exchanger is connected with the distilled water treatment unit;
the combined preheating heat exchanger is connected with a wastewater stock solution inlet at the top of the deamination tower.
2. The wastewater treatment system of claim 1, wherein the deamination tower further comprises a heating still at the bottom, the heating still being connected to a saturated steam supply line.
3. The wastewater treatment system according to claim 2, wherein the discharge port of the heating kettle is connected with a first discharge pump, and the first discharge pump is respectively connected with the feed port of the heating kettle and the MVR evaporative crystallization unit.
4. The wastewater treatment system according to claim 2, wherein the discharge port of the heating kettle is connected with two first discharge pumps, one of the first discharge pumps is connected with the MVR evaporative crystallization unit, and the other first discharge pump is connected with the feed port of the heating kettle.
5. The wastewater treatment system of any one of claims 1-4, wherein the ammonia removal subsystem further comprises an ammonia gas collection unit, the ammonia gas collection unit comprises an ammonia gas condenser and a cold water loop connected with the ammonia gas condenser, an ammonia gas inlet end of the ammonia gas condenser is connected with an ammonia gas outlet end at the top of the ammonia removal tower, and an ammonia water outlet end of the ammonia gas condenser is connected with an ammonia water collection pipe.
6. The wastewater treatment system of claim 1, wherein the MVR evaporative crystallization unit comprises an MVR crystallization separator, an MVR forced circulation heat exchanger and a forced circulation pump, the MVR crystallization separator, the MVR forced circulation heat exchanger and the forced circulation pump are connected to form a circulation loop, wherein:
the MVR crystallization separator is also connected with the deamination tower;
and a distilled water discharge port of the MVR forced circulation heat exchanger is connected with the distilled water treatment unit.
7. The wastewater treatment system of claim 6, wherein the MVR evaporative crystallization unit further comprises a vapor compressor, and the vapor compressor is respectively connected with the MVR crystallization separator and the MVR forced circulation heat exchanger.
8. The wastewater treatment system of claim 6, further comprising a salt discharge subsystem, wherein the salt discharge subsystem comprises a second discharge pump and a centrifugal drying device, and the second discharge pump is connected to the MVR crystal separator and the centrifugal drying device, respectively.
9. The wastewater treatment system according to claim 1, wherein the distilled water treatment unit comprises a third discharge pump, a water inlet end of the third discharge pump is connected with the distilled water discharge port, and a water outlet end of the third discharge pump is connected with the combined preheating heat exchanger.
10. The wastewater treatment system of claim 9, wherein the distilled water treatment unit further comprises a distilled water storage tank connected to the distilled water discharge port and the water inlet end of the third discharge pump, respectively.
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