Electric evaporative crystallization and biochemical comprehensive treatment system for high-salinity wastewater
By combining electroevaporation crystallization and biochemical treatment technology in the high-salt wastewater treatment system, the problems of high-salt wastewater disposal cost and strict water quality requirements in the existing technology are solved, and efficient wastewater removal and economical operation of the system are achieved.
Patent Information
- Application Number
- CN202421882019.9
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-08-06
- Publication Date
- 2025-06-24
- Estimated Expiration
- 2034-08-06
AI Technical Summary
When disposing of high-salt wastewater, the operating costs are high, the inlet water quality is demanding, and it is difficult to economically and effectively remove pollutants in high-salt wastewater.
The high-salt wastewater electroevaporation crystallization and biochemical comprehensive disposal system is used to remove pollutants such as salt, total nitrogen and COD in high-salt wastewater through physical and chemical neutralization, and the evaporated water is reasonably matched with biochemical hydration to reduce the concentration of pollutants entering the biochemical system.
It effectively improves the system operation stability, reduces the power consumption of the evaporative crystallization device, optimizes the operating temperature of the biochemical system, improves microbial activity, ensures that wastewater meets the standards, and has low overall operating cost of the system.
Smart Images
Figure CN223016657U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of industrial wastewater treatment, in particular to an electro-evaporation crystallization and biochemical comprehensive treatment system for high-salt wastewater. Background Technique
[0002] With the continuous development of industries such as chemical engineering, pharmaceuticals, pesticides, and coking, the composition of the high-salt wastewater generated by them is becoming more and more complex, and the treatment difficulty is also increasing continuously. Such wastewater not only has a high salt content and high COD, but also has the characteristics of complex chemical components, strong acidity and alkalinity, high toxicity, and poor biodegradability. During the treatment process, after conventional physical and chemical neutralization, the concentrations of various pollutants are still relatively high, especially the salt content, and both the treatment energy consumption and the treatment difficulty are continuously increasing.
[0003] At present, the main methods for treating high-salt wastewater include electro-despherization method, membrane permeation method, evaporation concentration method, salt-tolerant bacteria biochemical method, etc. Among them, the evaporation concentration method has relatively stable operation and high automation, but the operation cost is relatively high. The salt-tolerant bacteria biochemical method has a low treatment cost, but has strict requirements for the influent water quality, poor shock resistance, and a long acclimation period. Therefore, there is an urgent need for a comprehensive treatment system that can treat high-salt wastewater more economically and effectively. Content of the Utility Model
[0004] The technical problem to be solved by the utility model is to provide an electro-evaporation crystallization and biochemical comprehensive treatment system for high-salt wastewater, aiming to solve the technical problems of high operation cost, high requirements for influent water quality, and inability to treat high-salt wastewater economically and effectively existing in the prior art.
[0005] The technical solution of the utility model is: an electro-evaporation crystallization and biochemical comprehensive treatment system for high-salt wastewater, including a raw water tank, an intermediate water tank connected to the raw water tank, the intermediate water tank is respectively connected to an adjustment tank and an evaporation crystallization device, the adjustment tank is also sequentially connected to A tank I, O tank I, A tank II, O tank II, and a secondary sedimentation tank, O tank I and O tank II are connected to an aeration system, a first heat exchanger is connected between the intermediate water tank and the evaporation crystallization device, and the first heat exchanger is connected to the aeration system for preheating the evaporation influent; the evaporation crystallization device is respectively connected to a condenser and a crystal salt collection device, the condenser is connected to the adjustment tank for sending the evaporated water back to the adjustment tank; the condenser is also connected to a circulating water type vacuum pump, the circulating water type vacuum pump is also connected to the secondary sedimentation tank and O tank II, and a second heat exchanger is arranged in the circulating water type vacuum pump, and the second heat exchanger, the condenser, and the secondary sedimentation tank are sequentially connected to form a circulation loop.
[0006] Further, in the utility model, the aeration system includes an aeration blower and aeration devices respectively installed in O tank I and O tank II, and the first heat exchanger is connected between the aeration blower and the aeration devices.
[0007] Furthermore, an electric heating component is provided inside the evaporation and crystallization device of the present utility model, heat insulation cotton is provided outside, and a circulation pump is connected to the evaporation and crystallization device.
[0008] Furthermore, a sewage discharge valve is installed at the bottom of the evaporation and crystallization device of the present utility model, and the sewage discharge valve is connected to the crystal salt collection device.
[0009] The present utility model has the following advantages compared with the prior art:
[0010] 1) The present utility model combines the evaporation and concentration method with the biochemical method. After the high-salt wastewater is physicochemically neutralized, most of the pollutants such as salts, total nitrogen, and COD in the high-salt wastewater are removed through electro-evaporation and crystallization. The evaporated water is then rationally formulated with the biochemical influent and enters the biochemical system, reducing the concentrations of pollutants such as salts, total nitrogen, and COD entering the biochemical system, thereby effectively improving the operation stability of the system and finally achieving qualified discharge.
[0011] 2) In the present utility model, the waste heat of the aeration pipeline of the biochemical system is used to preheat the inlet water of the evaporation and crystallization device, reducing the power consumption of the evaporation and crystallization device, optimizing the operation temperature of the biochemical system, and enhancing the microbial activity.
[0012] 3) In the present utility model, the effluent from the secondary sedimentation tank of the biochemical system is used as the circulating water of the vacuum pump, the circulating water of the vacuum pump heat exchanger and the condenser, which can reduce the water temperature in the water-ring vacuum pump and can minimize the influence of volatile small-molecule organic compounds on the vacuum stability during the evaporation process, ensuring the evaporation efficiency, energy conservation and environmental protection.
[0013] 4) The present utility model can adjust the operation load of the biochemical system by reasonably controlling the compatibility of the electro-evaporation and crystallization and the biochemical system according to the concentration of the influent pollutants, ensuring the system stability, enabling the wastewater to finally meet the discharge standards, with low comprehensive operation cost of the system, and remarkable environmental and economic benefits. Description of the Drawings
[0014] Figure 1 It is a schematic diagram of the system structure of the present utility model.
[0015] Wherein: 1, raw water tank; 2, intermediate water tank; 3, regulating tank; 4, evaporation and crystallization device; 4a, heat insulation cotton; 4b, circulation pump; 4c, sewage discharge valve; 5, A tank I; 6, O tank I; 7, A tank II; 8, O tank II; 9, secondary sedimentation tank; 10, aeration blower; 11, aeration device; 12, first heat exchanger; 13, condenser; 14, crystal salt collection device; 15, water-ring vacuum pump; 16, second heat exchanger. Detailed Embodiments
[0016] The following specifically describes the detailed embodiments of the present utility model with reference to the drawings.
[0017] Embodiment:
[0018] The specific implementation manner of a high-salt wastewater electro-evaporation crystallization and biochemical comprehensive treatment system of the present utility model is shown in combination with the attached drawings. As Figure 1 , it mainly includes a raw water tank 1, an intermediate water tank 2 connected to the raw water tank 1. The intermediate water tank 2 is respectively connected to an adjustment tank 3 and an evaporation crystallization device 4. The adjustment tank 3 is also sequentially connected to an A tank I 5, an O tank I 6, an A tank II 7, an O tank II 8, and a secondary sedimentation tank 9.
[0019] Aeration devices 11 are respectively installed in the O tank I 6 and the O tank II 8, and the aeration devices 11 are connected to an aeration blower 10. A first heat exchanger 12 is connected between the intermediate water tank 2 and the evaporation crystallization device 4. The first heat exchanger 12 is arranged between the aeration blower 10 and the aeration devices 11 and is used for preheating the evaporation inlet water.
[0020] The evaporation crystallization device 4 is respectively connected to a condenser 13 and a crystal salt collection device 14. The condenser 13 is connected to the adjustment tank 3 to send the evaporated water back to the adjustment tank 3. An electric heating component is arranged inside the evaporation crystallization device 4, and a heat preservation cotton 4a is arranged outside the evaporation crystallization device 4. A circulation pump 4b is connected to the evaporation crystallization device 4, and a drain valve 4c is installed at the bottom of the evaporation crystallization device 4. The drain valve 4c is connected to the crystal salt collection device 14.
[0021] The condenser 13 is also connected to a circulating water type vacuum pump 15. The circulating water type vacuum pump 15 is also connected to the secondary sedimentation tank 9 and the O tank II 8. A second heat exchanger 16 is arranged inside the circulating water type vacuum pump 15. The second heat exchanger 16, the condenser 13, and the secondary sedimentation tank 9 are sequentially connected to form a circulation loop.
[0022] When this embodiment works specifically:
[0023] (1) After the high-salt wastewater is subjected to physical and chemical neutralization in the raw water tank 1, the effluent enters the intermediate water tank 2. The wastewater in the intermediate water tank 2 enters the evaporation crystallization device 4 and the adjustment tank 3 respectively according to a ratio. Under the automatic control of the electric heating component and the circulating water type vacuum pump 15, the evaporation crystallization device 4 maintains the evaporation temperature at about 60 °C and the negative pressure above -0.9 kPa, and uses the circulation pump 4b for circulating evaporation. The heat preservation cotton 4a outside the evaporation crystallization device 4 can reduce heat loss. When the evaporation is concentrated to near the crystallization state (water content < 20%), the drain valve 4c is started to discharge the crystal salt to the crystal salt collection device 14 for regular external disposal.
[0024] (2) The aeration blower 10 provides aeration for the O tank I 6 and the O tank II 8. When the compressed air passes through the aeration pipeline, high temperature will be generated. Heat exchange is carried out between the aeration pipeline and the inlet pipeline of the evaporation crystallization device 4 through the first heat exchanger 12 on the aeration pipeline to preheat the evaporation inlet water, which can reduce the power consumption of the evaporation crystallization device 4.
[0025] (3) The water vapor generated by heating and evaporating the wastewater in the evaporation and crystallization device 4 forms evaporated water after passing through the condenser 13, enters the regulation tank 3, and is rationally mixed with the biochemical influent and enters the biochemical system. The effluent from the secondary sedimentation tank 9 of the biochemical system is, on the one hand, circulated through the second heat exchanger 16 and the condenser 13 in sequence for heat exchange, reducing the water temperature in the circulating water type vacuum pump 15 to ensure the vacuum pumping effect, and at the same time condensing the water vapor generated by evaporation to form evaporated water. On the other hand, the effluent from the secondary sedimentation tank 9 also serves as the circulating water in the circulating water type vacuum pump 15. As the evaporation process progresses, it is regularly supplemented, replaced, and discharged to the O tank II 8 to reduce the impact of volatile small molecule organic substances on the vacuum degree during the evaporation process and ensure the evaporation efficiency.
[0026] (4) Regularly detect the water quality data of the wastewater in the intermediate water tank 2, the evaporated water, and the regulation tank 3, and adjust the proportion of the wastewater fed into the evaporation and crystallization device 4 in real time to control the concentrations of pollutants such as the salt content, total nitrogen, and COD in the wastewater in the regulation tank 3, ensuring the stability of the biochemical influent.
[0027] (5) The wastewater in the regulation tank 3 enters the biochemical system, passes through the secondary AO system in sequence, and then enters the secondary sedimentation tank 9, and finally is discharged up to standard.
[0028] Of course, the above embodiments are only for illustrating the technical concept and features of the present invention, and their purpose is to enable those who are familiar with this technology to understand the content of the present invention and implement it accordingly, and cannot be used to limit the protection scope of the present invention. All modifications made according to the spirit and essence of the main technical solution of the present invention should be covered within the protection scope of the present invention.
Claims
1. A high-salinity wastewater electric evaporation crystallization and biochemical comprehensive treatment system, characterized by: The invention comprises a raw water tank (1), an intermediate water tank (2) connected to the raw water tank (1), the intermediate water tank (2) being connected to a regulating tank (3) and an evaporation crystallization device (4), respectively, the regulating tank (3) being connected to an A tank I (5), an O tank I (6), an A tank II (7), an O tank II (8), and a secondary sedimentation tank (9) in sequence, the O tank I (6) and the O tank II (8) being connected to an aeration system, a first heat exchanger (12) being connected between the intermediate water tank (2) and the evaporation crystallization device (4), the first heat exchanger (12) being connected to the aeration system for preheating the evaporation inlet water; The evaporation and crystallization device (4) is respectively connected to a condenser (13) and a crystallized salt collection device (14); the condenser (13) is connected to the regulating tank (3) for returning evaporated water to the regulating tank (3); the condenser (13) is also connected to a circulating water vacuum pump (15); the circulating water vacuum pump (15) is also connected to the secondary sedimentation tank (9) and the O tank II (8); a second heat exchanger (16) is provided in the circulating water vacuum pump (15); the second heat exchanger (16), the condenser (13) and the secondary sedimentation tank (9) are sequentially connected to form a circulation loop.
2. The high-salinity wastewater electric evaporation crystallization and biochemical comprehensive treatment system according to claim 1 is characterized by: The aeration system comprises an aeration fan (10) and an aeration device (11) respectively installed in the O tank I (6) and the O tank II (8), and the first heat exchanger (12) is connected between the aeration fan (10) and the aeration device (11).
3. The high-salinity wastewater electric evaporation crystallization and biochemical comprehensive treatment system according to claim 1 is characterized by: The evaporation crystallization device (4) is provided with an electric heating component inside and a heat-insulating cotton (4a) outside. The evaporation crystallization device (4) is connected to a circulation pump (4b).
4. The high-salinity wastewater electric evaporation crystallization and biochemical comprehensive treatment system according to claim 1 is characterized by: A drain valve (4c) is installed at the bottom of the evaporation crystallization device (4), and the drain valve (4c) is connected to the crystallized salt collection device (14).