High-salinity wastewater evaporation crystallization device
By using a primary and secondary preheater in the high-salt wastewater evaporation and crystallization device to preheat the influent with condensate, the problem of nozzle clogging in the ozone reactor caused by low influent temperature was solved, achieving stable operation of the device and cost reduction.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- BEIJING TDR ENVIRON TECH CO LTD
- Filing Date
- 2025-08-13
- Publication Date
- 2026-08-04
AI Technical Summary
In existing high-salt wastewater evaporation and crystallization devices, the low inlet water temperature causes sodium sulfate decahydrate crystallization to clog the nozzles inside the ozone reactor, resulting in increased operating costs.
The system employs a primary preheater and a secondary preheater to preheat the inlet water using the condensate generated by the steam heater as a heat source, thus preventing the inlet water temperature from being too low. The amount of condensate is controlled by a bypass regulating valve to ensure that the inlet water temperature is within the set range and to prevent nozzle blockage.
This effectively avoids clogging of the nozzles inside the ozone reactor, ensures stable operation of the device, reduces operating costs, and improves the whiteness of the finished salt and COD removal rate.
Smart Images
Figure CN224590818U_ABST
Abstract
Description
Technical Field
[0001] This utility model belongs to the field of high-salt wastewater crystallization technology, and more specifically, relates to a high-salt wastewater evaporation and crystallization device. Background Technology
[0002] In the high-salt wastewater evaporation and crystallization unit, the influent COD concentration is usually between 100-1000 mg / L. After subsequent evaporation and concentration of 5-20 times, the COD concentration has exceeded 10,000. The increase in COD content will increase the solution viscosity and boiling point, ultimately leading to a decrease in the treatment capacity of the evaporation and crystallization unit.
[0003] In conventional evaporation crystallization units, an additional step is required to treat the high-salinity wastewater entering the system with ozone catalytic oxidation. This reduces the COD content of the feed, resulting in a lower COD level within the evaporator separator, maintaining the system's processing capacity, and improving the purity and whiteness of the subsequently crystallized salt, thus ensuring stable operation of the evaporation crystallization unit. However, a problem arises in winter when the high-salinity wastewater reacts with ozone. Due to the low temperature of the feed solution and the high concentration of sodium sulfate in the incoming water, sodium sulfate decahydrate crystals crystallize at the nozzles inside the ozone reactor, clogging the nozzles. Unclogging the nozzles in the ozone reactor requires significant manpower and resources, increasing operating costs. Utility Model Content
[0004] The purpose of this invention is to address the shortcomings of existing technologies by providing a high-salt wastewater evaporation and crystallization device, which solves the problem of sodium sulfate decahydrate crystallizing at the nozzles of the ozone reactor and clogging the nozzles due to low inlet water temperature.
[0005] To achieve the above objectives, this utility model provides a high-salt wastewater evaporation and crystallization device, comprising: The system consists of a primary preheater, an ozone reactor, a secondary preheater, a steam heater, and an evaporator, connected in sequence. A circulation pump is installed between the steam heater and the evaporator. The condensate outlet of the steam heater is connected in sequence to the primary preheater and the secondary preheater. A bypass pipeline is connected to the condensate inlet and condensate outlet of the primary preheater, and a bypass regulating valve is installed on the bypass pipeline.
[0006] Optionally, both the primary preheater and the secondary preheater are heat exchangers, with the primary heat-absorbing medium inlet of the primary preheater connected to the feed pipeline and the primary heat-absorbing medium outlet of the primary preheater connected to the ozone reactor.
[0007] Optionally, the ozone reactor is connected to an ozone generator.
[0008] Optionally, a feed tank and a feed pump are sequentially arranged between the ozone reactor and the secondary preheater.
[0009] Optionally, the feed pump is connected to the secondary heat absorption medium inlet of the secondary preheater, and the secondary heat absorption medium outlet of the secondary preheater is connected to the steam heater.
[0010] Optionally, the condensate inlet and the condensate outlet are respectively the primary heat release medium inlet and the primary heat release medium outlet of the primary preheater, the secondary preheater includes a secondary heat release medium inlet and a secondary heat release medium outlet, and the condensate outlet of the steam heater is connected in sequence to the primary heat release medium inlet, the primary heat release medium outlet and the secondary heat release medium inlet through a condensate pipeline.
[0011] Optionally, a temperature sensor is installed inside the ozone reactor.
[0012] Optionally, the steam heater is connected to the evaporator separator via a circulation pipeline, the circulation pump is installed on the circulation pipeline, and the circulation pipeline is connected to the discharge pipeline and the solid-liquid separator.
[0013] Optionally, the liquid outlet of the solid-liquid separator is connected to a reflux pipeline, and a mother liquor tank and a mother liquor pump are sequentially arranged on the reflux pipeline, and the reflux pipeline is connected to the circulation pipeline.
[0014] Optionally, the ozone generator is connected to the ozone reactor via an ozone pipeline, and a pressure gauge is installed on the ozone pipeline.
[0015] This invention provides a high-salt wastewater evaporation and crystallization device, the advantages of which are as follows: the influent of the high-salt wastewater evaporation and crystallization device first passes through a primary preheater and then enters an ozone reactor for ozone catalytic oxidation treatment. After that, it passes through a secondary preheater for further preheating before entering a steam heater and evaporation separator for evaporation and crystallization. The primary and secondary preheaters utilize the condensate generated by the steam heater as a heat source to utilize residual heat. At the same time, the primary preheater preheats the influent to prevent the influent temperature from being too low when entering the ozone reactor, thereby preventing the nozzles from being blocked by crystallized salt in the ozone reactor, ensuring the stable operation of the device. Furthermore, the amount of condensate entering the primary preheater can be controlled by adjusting the opening of the bypass regulating valve; the smaller the opening of the bypass regulating valve, the more condensate enters the primary preheater.
[0016] Other features and advantages of this invention will be described in detail in the following detailed description section. Attached Figure Description
[0017] The above and other objects, features and advantages of the present invention will become more apparent from the accompanying drawings, in which like reference numerals generally represent like parts.
[0018] Figure 1 A schematic diagram of a high-salt wastewater evaporation and crystallization apparatus according to an embodiment of the present invention is shown.
[0019] Explanation of reference numerals in the attached figures: 1. Primary preheater; 2. Ozone reactor; 3. Ozone generator; 4. Feed tank; 5. Feed pump; 6. Secondary preheater; 7. Steam heater; 8. Evaporator separator; 9. Circulation pump; 10. Discharge pump; 11. Condensate tank; 12. Condensate pump; 13. Solid-liquid separator; 14. Mother liquor tank; 15. Mother liquor pump; 16. Bypass regulating valve; 17. Temperature sensor; 18. Pressure gauge; 19. Feed line; 20. Conveying line; 21. Sodium sulfate discharge pipe; 22. Nozzle. Detailed Implementation
[0020] Preferred embodiments of the present invention will now be described in more detail. While preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided to make the present invention more thorough and complete, and to fully convey the scope of the present invention to those skilled in the art.
[0021] like Figure 1 As shown, this utility model provides a high-salt wastewater evaporation and crystallization device, comprising: The system consists of a primary preheater 1, an ozone reactor 2, a secondary preheater 6, a steam heater 7, and an evaporator separator 8 connected in sequence. A circulating pump 9 is installed between the steam heater 7 and the evaporator separator 8. The condensate outlet of the steam heater 7 is connected to the primary preheater 1 and the secondary preheater 6 in sequence. A bypass pipeline is connected to the condensate inlet and condensate outlet of the primary preheater 1, and a bypass regulating valve 16 is installed on the bypass pipeline.
[0022] Specifically, to address the problem in existing technologies where low influent water temperature leads to sodium sulfate decahydrate crystallization at nozzle 22 of ozone reactor 2, causing nozzle 22 blockage, the high-salt wastewater evaporation crystallization device provided by this invention first passes through a primary preheater 1 before entering ozone reactor 2 for ozone catalytic oxidation treatment. Afterward, it passes through a secondary preheater 6 for further preheating before entering steam heater 7 and evaporation separator 8 for evaporation crystallization. The primary and secondary preheaters 1 and 6 utilize the condensate generated by steam heater 7 as a heat source to utilize residual heat. Simultaneously, the primary preheater preheats the influent water, preventing excessively low influent temperature entering ozone reactor 2, thus preventing salt crystallization at nozzle 22 from blocking it and ensuring stable operation of the device. Furthermore, the amount of condensate entering primary preheater 1 can be controlled by adjusting the opening of bypass regulating valve 16; a smaller opening of bypass regulating valve 16 results in more condensate entering primary preheater 1.
[0023] Optionally, both the primary preheater 1 and the secondary preheater 6 are heat exchangers. The primary heat absorption medium inlet of the primary preheater is connected to the feed pipeline 19, and the primary heat absorption medium outlet of the primary preheater is connected to the ozone reactor 2.
[0024] Specifically, both the primary preheater 1 and the secondary preheater 6 utilize the sensible heat of the condensate from the steam heater 7 to heat the inlet water and the liquid before it enters the steam heater 7 through heat exchange.
[0025] Optionally, the ozone reactor 2 is connected to an ozone generator 3.
[0026] Specifically, ozone generator 3 provides ozone to ozone reactor 2, and ozone catalytic oxidation is performed on high-salt wastewater in ozone reactor 2 to reduce the COD content of the feed.
[0027] Optionally, a feed tank 4 and a feed pump 5 are sequentially arranged between the ozone reactor 2 and the secondary preheater 6.
[0028] Specifically, the wastewater treated by ozone catalytic oxidation enters the feed tank 4 through the feed pipeline 20, and the liquid in the feed tank 4 is pumped by the feed pump 5.
[0029] Optionally, the feed pump 5 is connected to the secondary heat absorption medium inlet of the secondary preheater 6, and the secondary heat absorption medium outlet of the secondary preheater 6 is connected to the steam heater 7.
[0030] Specifically, the liquid pumped by the feed pump 5 first enters the secondary preheater 6 for heating, and the heated liquid enters the steam heater 7. The steam heater 7 uses steam for heating, and the condensate from the steam conversion enters the primary preheater 1 and the secondary preheater 6 as a heat source.
[0031] Optionally, the condensate inlet and condensate outlet are the primary heat release medium inlet and primary heat release medium outlet of the primary preheater 1, respectively, and the secondary preheater 6 includes a secondary heat release medium inlet and a secondary heat release medium outlet. The condensate outlet of the steam heater 7 is connected in sequence to the primary heat release medium inlet, the primary heat release medium outlet and the secondary heat release medium inlet through a condensate pipeline.
[0032] Specifically, the condensate pipeline includes a first condensate pipeline and a second condensate pipeline. The condensate outlet of the steam heater 7 is first connected to the primary heat release medium inlet through the first condensate pipeline. The primary heat release medium outlet is then connected to the secondary heat release medium inlet through the second condensate pipeline. The two ends of the bypass pipeline are connected to the first condensate pipeline and the second condensate pipeline, respectively. The condensate output from the secondary heat release medium outlet is discharged through the external discharge pipeline.
[0033] In this embodiment, a condensate tank 11 and a condensate pump 12 are sequentially installed on the condensate pipeline.
[0034] Optionally, a temperature sensor 17 is installed inside the ozone reactor 2.
[0035] Specifically, the temperature sensor 17 is configured to detect the temperature information inside the ozone reactor 2 in real time, and adjust the opening of the bypass regulating valve 16 according to the temperature information, thereby adjusting the amount of condensate entering the primary preheater 1 to ensure that the temperature of the inlet water is within the set temperature threshold range.
[0036] In this embodiment, the temperature threshold is set to 32-45℃.
[0037] In this embodiment, a control unit is also included. The control unit is electrically connected to the temperature sensor 17 and the bypass regulating valve 16. The control unit controls the opening degree of the bypass regulating valve 16 according to the detection result of the temperature sensor 17. When the detection result of the temperature sensor 17 is lower than the set temperature, the control unit controls the bypass regulating valve 16 to reduce its opening degree.
[0038] Optionally, the steam heater 7 is connected to the evaporator separator 8 via a circulation pipeline, and the circulation pump 9 is installed on the circulation pipeline, which is connected to the discharge pipeline and the solid-liquid separator 13.
[0039] Specifically, the circulation pipeline includes a first circulation pipeline and a second circulation pipeline. The first circulation pipeline is connected to the upper end of the steam heater 7, and the second circulation pipeline is connected to the lower end of the evaporator separator 8 and the lower end of the steam heater 7. The circulation pump 9 is installed on the second circulation pipeline, and the discharge pipeline is connected to the second circulation pipeline.
[0040] In this embodiment, a discharge pump 10 is installed on the discharge pipeline.
[0041] In this embodiment, the secondary heat absorption medium outlet of the secondary preheater 6 is connected to the circulation pipeline between the steam heater 7 and the circulation pump 9.
[0042] Optionally, the liquid outlet of the solid-liquid separator 13 is connected to a return pipeline, on which a mother liquor tank 14 and a mother liquor pump 15 are sequentially installed, and the return pipeline is connected to the circulation pipeline.
[0043] Specifically, the liquid evaporates and crystallizes sodium sulfate in the evaporator separator 8. The crystal slurry is pumped to the solid-liquid separator 13 by the discharge pump 10 for solid-liquid separation. The centrifugal mother liquor is returned to the second circulation pipeline by the mother liquor pump 15, and the sodium sulfate is discharged through the sodium sulfate discharge pipe 21.
[0044] Optionally, the ozone generator 3 is connected to the ozone reactor 2 via an ozone pipeline, and a pressure gauge 18 is installed on the ozone pipeline.
[0045] Specifically, the pressure gauge 18 is set to help determine whether the nozzle 22 inside the ozone reactor 2 is blocked.
[0046] Furthermore, the clogging status of the nozzles 22 in the ozone reactor 2 can be assessed from multiple perspectives, such as the fluctuation of the pressure gauge 18 reading, the change in COD content of wastewater in the feed line 19 and the conveying line 20, and the product salinity.
[0047] In summary, when using the high-salt wastewater evaporation and crystallization device provided by this utility model, taking a single operation as an example: in the initial state, the bypass regulating valve 16 is fully open; in winter, the temperature detected by the temperature sensor 17 inside the ozone reactor 2 is between 0-10℃; the pressure fluctuation of the pressure gauge 18 on the ozone pipeline is between 10% and 60%; after testing and analysis of the COD content of the wastewater in the feed pipeline 19 and the conveying pipeline 20, the COD removal rate is between 2-5%; the whiteness of the finished sodium sulfate in the sodium sulfate discharge pipe 21 is below 50; based on this, it can be determined that the nozzle 22 inside the ozone reactor 2 has been blocked by crystallized sodium sulfate decahydrate. At this point, adjusting the opening of the bypass regulating valve 16 to reduce its opening and controlling the valve opening at 72-82%, the temperature inside the ozone reactor 2 is controlled at 32-35℃, and the ozone pipeline pressure is almost stable at 0.1 MPa. After testing and analysis of the COD content of the wastewater in the feed pipeline 19 and the conveying pipeline 20, the COD removal rate is 30-50%. The whiteness of the finished sodium sulfate in the sodium sulfate discharge pipe 21 is between 65-75. It can be determined that there is no problem of sodium sulfate decahydrate clogging the nozzle 22 in the ozone reactor 2. Furthermore, by further reducing the opening of the bypass regulating valve 16 to 52-72%, the temperature inside the ozone reactor 2 was controlled at 35-40℃, and the ozone pipeline pressure was almost stable at 0.1 MPa. After testing and analysis of the COD content of the wastewater in the feed pipeline 19 and the conveying pipeline 20, the COD removal rate was 30-50%. The whiteness of the finished sodium sulfate salt in the sodium sulfate discharge pipe 21 was between 65-75. It can be determined that there was no problem of crystallized sodium sulfate decahydrate clogging the nozzle 22 in the ozone reactor 2. Continue to reduce the opening of the bypass regulating valve 16. When its opening is between 23% and 52%, the temperature inside the ozone reactor 2 is controlled at 40-45℃, and the pressure of the ozone pipeline is almost stable at 0.1 MPa. After testing and analysis of the COD content of the wastewater in the feed pipeline 19 and the conveying pipeline 20, the COD removal rate is 30-50%. The whiteness of the finished sodium sulfate salt in the sodium sulfate discharge pipe 21 is between 65-75%. It can be determined that there is no problem of sodium sulfate decahydrate clogging the nozzle 22 in the ozone reactor 2.
[0048] The various embodiments of the present invention have been described above. These descriptions are exemplary and not exhaustive, nor are they limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.
Claims
1. A high-salinity wastewater evaporation crystallization device, characterized in that, include: The system consists of a primary preheater, an ozone reactor, a secondary preheater, a steam heater, and an evaporator, connected in sequence. A circulation pump is installed between the steam heater and the evaporator. The condensate outlet of the steam heater is connected in sequence to the primary preheater and the secondary preheater. A bypass pipeline is connected to the condensate inlet and condensate outlet of the primary preheater, and a bypass regulating valve is installed on the bypass pipeline.
2. The high-salinity wastewater evaporative crystallization device of claim 1, wherein, Both the primary preheater and the secondary preheater are heat exchangers. The primary heat-absorbing medium inlet of the primary preheater is connected to the feed pipeline, and the primary heat-absorbing medium outlet of the primary preheater is connected to the ozone reactor.
3. The high-salinity wastewater evaporative crystallization device of claim 1, wherein, The ozone reactor is connected to an ozone generator.
4. The high-salinity wastewater evaporative crystallization device of claim 2, wherein, A feed tank and a feed pump are sequentially arranged between the ozone reactor and the secondary preheater.
5. The high-salinity wastewater evaporative crystallization device of claim 4, wherein, The feed pump is connected to the inlet of the secondary heat absorption medium of the secondary preheater, and the outlet of the secondary heat absorption medium of the secondary preheater is connected to the steam heater.
6. The high-salinity wastewater evaporative crystallization device of claim 2, wherein, The condensate inlet and the condensate outlet are respectively the primary heat release medium inlet and the primary heat release medium outlet of the primary preheater. The secondary preheater includes a secondary heat release medium inlet and a secondary heat release medium outlet. The condensate outlet of the steam heater is connected in sequence to the primary heat release medium inlet, the primary heat release medium outlet and the secondary heat release medium inlet through a condensate pipeline.
7. The high-salinity wastewater evaporative crystallization device of claim 1, wherein, The ozone reactor is equipped with a temperature sensor.
8. The high-salinity wastewater evaporative crystallization device of claim 1, wherein, The steam heater is connected to the evaporator separator via a circulation pipeline, the circulation pump is installed on the circulation pipeline, and the circulation pipeline is connected to the discharge pipeline and the solid-liquid separator.
9. The high-salinity wastewater evaporative crystallization device of claim 8, wherein, The liquid outlet of the solid-liquid separator is connected to a reflux pipeline, on which a mother liquor tank and a mother liquor pump are sequentially installed, and the reflux pipeline is connected to the circulation pipeline.
10. The high-salinity wastewater evaporative crystallization device of claim 3, wherein, The ozone generator is connected to the ozone reactor via an ozone pipeline, and a pressure gauge is installed on the ozone pipeline.