A method and system for resource utilization of neutralization method deacidification salt-containing wastewater

Abstract

The application provides a neutralization method for resource utilization of deacidification salt-containing wastewater, which is characterized in that the deacidification wastewater is naturally cooled in a cooling tank, so that the use of electric power resources is reduced; the closed heat exchange coil is connected with circulating cooling water, and the deacidification wastewater is atomized and sprayed in the cooler, so that the deacidification wastewater at a low temperature is indirectly cooled and exchanged with the cooling water at a high temperature in the heat exchange coil, the water vapor in the deacidification wastewater is evaporated, and the salt concentration of the deacidification wastewater is increased; the closed heat exchange coil can ensure that the cooling water and the deacidification wastewater are not mixed, so that the cooling water in the technical scheme of the application can be used for the high-temperature liquid which needs to be heat-exchanged in the system at the same time, so that the deacidification wastewater is heated and evaporated, and the liquid in the heat exchange coil is cooled, and the overall energy consumption of the system is further reduced.

Description

Technical Field

[0001] This invention relates to the field of deacidification wastewater resource utilization technology, specifically a method and system for the resource utilization of deacidification saline wastewater using a neutralization method. Background Technology

[0002] In waste gas purification processes, alkaline solutions are typically used to neutralize acidic gases in the waste gas, thereby purifying the acidic gases. However, this wet deacidification process generates a large amount of saline wastewater. Existing technologies usually employ methods such as membrane filtration, membrane concentration, indirect steam evaporation concentration, or flue gas drying to treat saline wastewater from wet deacidification. For example, the technology disclosed in patent application number CN201910306601.8 uses flue gas drying to dry the deacidification wastewater and then achieve brine separation. However, these methods require the consumption of large amounts of high-quality energy sources such as steam and electricity, resulting in high system energy consumption, inability to achieve resource utilization, and high investment costs. Summary of the Invention

[0003] To address the high energy and water consumption issues in existing wet desulfurization wastewater treatment processes, this invention provides a method for the resource utilization of desulfurized wastewater treated by neutralization. This method reduces energy consumption during wet desulfurization wastewater treatment, thereby lowering the overall operating cost of the system. This application also discloses a system for the resource utilization of desulfurized wastewater treated by neutralization.

[0004] The technical solution of this invention is as follows: a method for the resource utilization of deacidified saline wastewater by neutralization, characterized by comprising the following steps:

[0005] S1: Cooling of deacidification wastewater;

[0006] The deacidification wastewater is transferred to a cooling tank for storage until it is cooled to a preset temperature before being sent to a cooler; some of the crystalline salts that precipitate during the cooling process are recovered.

[0007] S2: Heat exchange and evaporation of deacidification wastewater;

[0008] A closed heat exchange coil is installed in the cooler; after the deacidification wastewater is cooled down, it is sent into the cooler and then atomized and sprayed to indirectly exchange heat with the circulating cooling water with a higher temperature in the heat exchange coil. The atomized deacidification wastewater exchanges heat with the circulating cooling water with a higher temperature, and the water in the deacidification wastewater is evaporated to obtain a higher concentration of deacidification wastewater.

[0009] S3: Precipitation of mixed salts;

[0010] A wastewater concentration section is set below the heat exchange coil in the cooler. The higher concentration of deacidified wastewater after heat exchange falls into the salt-containing wastewater concentration section for cooling, and crystallized salt precipitates at the bottom.

[0011] S4: Brine separation;

[0012] The high-concentration crystalline salt mixture at the bottom of the wastewater concentration section is sent out of the cooler for solid-liquid separation. The separated solid crystalline salt is reused, and the separated waste liquid is sent back to the cooling tank.

[0013] S5: Repeat steps S1~S4, gradually increasing the salt concentration of the deacidification wastewater in the cooling tank, and reusing the precipitated solid crystalline salt.

[0014] Its further features are:

[0015] In step S1, when the deacidification waste liquid in the cooling tank is cooled to 20°C, it is sent to the subsequent steps;

[0016] In step S2, the circulating cooling water in the heat exchange coil is the high-temperature cooling water output from the cooling equipment of the rotating shaft or mechanical seal of the large equipment in the same system after heat exchange.

[0017] In steps S2 and S3, the water vapor generated after the deacidification wastewater exchanges heat with the cooling circulating water in the heat exchange coil, as well as the water vapor generated by the deacidification wastewater cooled in the salt-containing wastewater concentration section, are all recycled as clean condensate and reused.

[0018] The cold water at the bottom of the cooling pool is sent to the cooler;

[0019] In step S3, the deacidified wastewater after heat exchange stored in the wastewater concentration section, and the deacidified wastewater with lower salt concentration in the upper part are sent to the cooling tank through the overflow port for further cooling.

[0020] A system for the resource utilization of deacidified saline wastewater by neutralization includes: a cooler shell and an atomizing spray device, characterized in that it further includes: a heat exchange coil, a salt scraper, a centrifuge, and a cooling tank;

[0021] The atomizing spray device, the heat exchange coil, and the salt scraper are arranged in the inner cavity of the cooler shell in a top-to-bottom order; the salt scraper is located at the bottom of the inner cavity of the cooler shell; and a steam exhaust port is provided at the top of the cooler shell.

[0022] The cooling pool is located outside the cooler shell and is connected to the liquid supply equipment for deacidification wastewater;

[0023] The atomizing spray equipment includes: a deacidification wastewater inlet and a spray nozzle; the cooling tank is connected to the deacidification wastewater inlet of the atomizing spray equipment via a circulating pump;

[0024] The heat exchange coil includes an inlet and an outlet for circulating cooling water. The inlet is located below the outlet, and the inlet and outlet are respectively connected to the circulating water supply equipment.

[0025] The bottom of the cooler housing is provided with a crystallization salt discharge port, which is connected to the centrifuge, and the liquid discharge port of the centrifuge is connected to the cooling pool.

[0026] Its further features are:

[0027] The salt scraper includes a scraper and a drive motor, wherein the scraper is mounted on the output shaft of the drive motor.

[0028] The bottom of the cooler housing is a bowl-shaped structure with a central concave shape. The curvature of the scraper blade is adapted to the curvature of the bottom of the cooler housing, and the blade faces the bottom of the cooler housing when installed, close to the bottom end face of the cooler. Through holes are evenly opened on the back of the scraper.

[0029] An air inlet and a deacidification wastewater overflow outlet are provided from top to bottom on the cooler shell between the salt scraper and the heat exchange coil; the deacidification wastewater overflow outlet is connected to the cooling tank;

[0030] It also includes: a water collector and a demisting packing layer, wherein the water collector is disposed between the atomizing spray device and the exhaust fan; and the demisting packing layer is disposed between the water collector and the exhaust fan.

[0031] The water collector includes a liner plate and a vent cap. The liner plate has a through hole, and a cylinder is disposed on the through hole. The vent cap is mounted above the through hole by a support structure, and the size of the vent cap is larger than the size of the through hole. One end of the liner plate has a recessed water collection trough, which is connected to a condensate recovery device.

[0032] This application provides a method for the resource utilization of deacidification wastewater using a neutralization process. The method utilizes a cooling tank to naturally cool the wastewater, reducing electricity consumption. A closed heat exchange coil connects to circulating cooling water. The wastewater enters the cooler and is atomized and sprayed, allowing the lower-temperature wastewater to indirectly exchange heat with the higher-temperature cooling water in the coil. This achieves water vapor evaporation in the wastewater, increasing its salt concentration. The closed heat exchange coil ensures that the cooling water and wastewater do not mix. Therefore, the cooling water in this solution can simultaneously be the high-temperature liquid requiring heat exchange in the system, achieving both heating and evaporation of the wastewater and cooling of the liquid in the heat exchange coil, further reducing overall system energy consumption. Even if industrial water is used as cooling water, the lack of mixing with the wastewater ensures efficient energy utilization. The mixed acid wastewater can be reused, reducing water waste. A wastewater concentration section is set at the bottom of the inner cavity of the cooler shell. The high-concentration deacidification wastewater after heat exchange is further naturally cooled in the wastewater concentration section. The water vapor generated during the natural cooling process is discharged from the top of the cooler shell and reused. The mixture of precipitated crystal salt and wastewater is separated into solid and liquid. The separated low-salt liquid is sent to the cooling tank for further cooling and then circulated again. In the technical solution of this application, the salt concentration of the deacidification wastewater is increased and crystal salt is extracted by cyclically executing the steps of deacidification wastewater cooling, heat exchange evaporation, precipitation of impurities and salt water separation. Most of the process is based on natural cooling and the cooling water can be repeatedly recycled. There is no need to use a lot of electrical energy, which greatly reduces the energy consumption in the wet deacidification saline wastewater treatment process, thereby reducing the overall operating cost of the system. Attached Figure Description

[0033] Figure 1 This is a schematic diagram of the structure of a system for the resource utilization of acid-removing wastewater by neutralization.

[0034] Figure 2 This is a schematic diagram of the water collector.

[0035] Figure 3 This is a schematic diagram of the salt scraper from the front view.

[0036] Figure 4 This is a top view of the salt scraper. Detailed Implementation

[0037] like Figures 1-4 As shown, this application includes a system for the resource utilization of deacidified saline wastewater by neutralization, which includes: a cooler shell 1, an atomizing spray device 2, a heat exchange coil 3, a salt scraper 4, a centrifuge 5, a cooling tank 6, a circulating pump 7, a precision filter 8, a water collector 9, a demisting packing layer 10, and a heat exhaust fan 11.

[0038] The atomizing spray device 2, heat exchange coil 3, and salt scraper 4 are arranged in a top-to-bottom order within the inner cavity of the cooler shell 1; the salt scraper 4 is located at the bottom of the inner cavity of the cooler shell 1; and a steam exhaust port 102 is located at the top of the cooler shell 1. A cooling tank 6 is located outside the cooler shell 1 and is connected to the deacidification wastewater supply equipment (not marked in the figure). The atomizing spray device 2 includes a spray pipe and nozzles 202. One end of the spray pipe is the deacidification wastewater inlet 201, and the nozzles 202 are located on the body of the spray pipe. The cooling tank 6 is connected to the deacidification wastewater inlet 201 of the atomizing spray device 2 via a circulating pump 7. A heat exhaust fan 11 is located below the exhaust port 102 at the top of the cooler shell 1. The heat exhaust fan 11 promptly discharges the hot air and steam mixture inside the cooler, and the clean condensed mist droplets generated during the cooling process are collected and reused through the demisting packing layer 10.

[0039] In this application, the deacidification wastewater is cooled to approximately 20°C in cooling tank 6 and then fed into the spray pipes in cooler shell 1 for atomized spraying, achieving indirect cooling of the circulating cooling water coil and heating and evaporation of the deacidification wastewater. Specifically, the heat exchange coil is made of titanium to prevent corrosion and to prevent the deacidification wastewater from contaminating the clean circulating cooling water. A cooling fan 601 is installed at the top of cooling tank 6 to cool the deacidification wastewater containing salt before recycling. After the deacidification wastewater enters the cooling tank, the saturated solubility of salt decreases during the cooling process, and the high-concentration salt water falls to the bottom of the tank, further precipitating crystallized salt.

[0040] The inlet of the circulating pump 7 is located at the bottom of the cooling pool 6; the outlet of the circulating pump 7 is equipped with a liquid precision filter 8.

[0041] The deacidification wastewater in the cooling pool 6 is pumped into the cooler by the circulating pump 7 to exchange heat and cool the circulating cooling water. A precision filter 8 is installed at the outlet of the circulating pump 7. The precision filter 8 has a 300-mesh filtration aperture, which is mainly used to further recover the crystallized salt that may precipitate during the cooling process for subsequent resource utilization of salt, while preventing the crystallized salt from clogging the spray pipe of the atomizing spray device 2 in the cooler.

[0042] The inlet of the circulating pump 7 is located at the bottom of the cooling pool 6. On the one hand, it can effectively collect the crystallized salt deposited at the bottom of the cooling pool 6. On the other hand, it utilizes the difference in density between cold and hot water, with the cold water at the bottom, to pump the cold water back to the cooler for recycling, while the hot water continues to cool down. This prevents the circulating cooling water in the cooler from failing to meet the heat exchange conditions, which would lead to problems such as high operating power and high energy consumption of the exhaust fan 11.

[0043] The heat exchange coil 3 includes an inlet 301 and an outlet 302 for circulating cooling water. The inlet 301 is located below the outlet 302, and both the inlet 301 and outlet 302 are connected to the cooling circulating water supply equipment (not marked in the figure). Higher-temperature circulating cooling water enters from bottom to top, with the temperature of the coil increasing towards the bottom. Lower-temperature deacidification wastewater spray falls from top to bottom, and the water in the wastewater gradually evaporates upon heating. As the deacidification wastewater spray descends, it encounters the increasingly hot heat exchange coil, effectively increasing the evaporation rate of water in the deacidification wastewater and thus increasing the salt concentration of the deacidification wastewater falling to the bottom.

[0044] In this embodiment, the circulating cooling water in the heat exchange coil uses high-temperature cooling water output from the cooling equipment of the rotating shaft or mechanical seal of the large equipment in the same system, with a temperature of approximately 30-40°C. The 20°C deacidification wastewater from the cooling pool is atomized and encounters the higher-temperature heat exchange coil. The water in the wastewater atomization evaporates upon heating, increasing the salt concentration of the wastewater. The high-concentration salt wastewater then flows into the wastewater concentration section 105 below the cooler shell. After cooling, the high-temperature cooling water is returned to the cooling equipment of the rotating shaft or mechanical seal, eliminating the need for additional water resources and reducing the overall system cost.

[0045] After heat exchange with the circulating cooling water, the salty wastewater evaporates and concentrates, falling into the wastewater concentration section 105 at the bottom of the inner cavity of the cooler shell 1. Some of the wastewater absorbs heat and evaporates, and is carried out by the exhaust fan at the top of the cooler. Therefore, the deacidification wastewater collected at the bottom of the cooler will be concentrated, and the salt content will further increase. After a long period of operation, the crystallized salt precipitated at the bottom of the cooler is discharged outside the tower through the rotary salt scraper 4 set at the bottom of the cooler for collection and utilization.

[0046] An air inlet 102 and a deacidification wastewater overflow outlet 101 are provided from top to bottom on the cooler shell 1 between the salt scraper 4 and the heat exchange coil 3; the deacidification wastewater overflow outlet 101 is connected to the cooling pool 6.

[0047] An air inlet 102 is provided above the wastewater concentration section 105. In specific applications, the air inlet 102 is set based on louvers to introduce natural air and improve the cooling efficiency of the brine stored in the wastewater concentration section 105. The mist of high-salt wastewater sprayed by the nozzle 202 exchanges heat with the heat exchange coil 3 and continues to fall downwards to the wastewater concentration section 105 at the bottom of the cooler housing 1. During the dripping process, the natural air introduced by the air inlet 102 cools the falling wastewater, which greatly improves the cooling efficiency of the wastewater and does not require the use of electricity or other energy sources, thus reducing the system energy consumption.

[0048] The wastewater stored in the wastewater concentration section 105 after heat exchange has a higher salt concentration in the lower part and a lower salt concentration in the upper part. When the height of the wastewater reaches the height of the overflow port 10, it will flow through the overflow port 10 into the cooling tank 6 for circulation, cooling, and concentration. The overflow port 10 at the bottom of the cooler controls the amount of wastewater stored in the wastewater concentration section 105, preventing excessive wastewater from affecting the heat exchange process above the cooler due to blockages or other reasons. At the same time, it introduces the low-salt wastewater in the wastewater concentration section 105 into the cooling tank for recirculation and impurity salt refining.

[0049] A crystallization salt discharge port 106 is provided at the bottom of the cooler housing 1. The crystallization salt discharge port is connected to the centrifuge 5, and the liquid discharge port of the centrifuge 5 is connected to the cooling pool 6.

[0050] like Figure 3 and 4 As shown, the salt scraper 4 includes a scraper 401 and a drive motor 402. The scraper 401 is mounted on the output shaft 404 of the drive motor 402. The bottom of the cooler housing is a bowl-shaped structure with a central depression. The crystallized salt discharge port 106 is located near the bottom of the bowl, ensuring that the denser crystallized salt mixture can naturally deposit and concentrate near the crystallized salt discharge port. The curvature of the scraper 401's blade is adapted to the curvature of the bottom of the cooler housing 1, and when installed, the blade faces the bottom of the cooler housing and is positioned close to the bottom end face of the cooling surface. In this embodiment, the bottom cross-section of the cooler housing is circular, the rotation axis of the scraper 401 is located at the center of the circle, and the length of the scraper 401 is adapted to the radius of the bottom of the cooler housing.

[0051] When the drive motor 402 starts, it drives the scraper 401 to slowly rotate along the bottom of the cooler housing 1, scraping the crystallized salt that has precipitated at the bottom of the housing. The mixed solution of the scraped crystallized salt and concentrated hydrochloric acid is discharged into the centrifuge 5 through the crystallized salt discharge port at the bottom. In this embodiment, four scrapers 401 are provided in a cross arrangement to ensure that the crystallized salt at the bottom can be scraped off evenly and without dead angles.

[0052] The scraper 401 has evenly spaced through holes 403 on its back. This not only reduces the overall weight of the scraper, but also prevents the scraper 401 from causing excessive agitation of the deacidified wastewater stored in the wastewater concentration section 105 when it rotates. This ensures that the high-density crystalline salt mixture can naturally flow to the bottom of the bowl-shaped structure based on its high density and be discharged from the crystalline salt discharge port.

[0053] Crystallized salt discharged from the bottom of the cooler via a rotating salt scraper 4 undergoes solid-liquid separation via a high-salt concentrate centrifuge 5. The salt after solid-liquid separation can be further utilized as a resource. The low-salt water discharged from the high-salt concentrate centrifuge 5 after solid-liquid separation is recycled into a cooling tank.

[0054] A water collector 9 is positioned between the atomizing spray device 2 and the exhaust fan 11; a demisting packing layer 10 is positioned between the water collector 9 and the exhaust fan 11. For example... Figure 2 As shown, the water collector 9 includes: a liner plate 901 and a vent 903. The liner plate 901 is provided with a through hole 902, and a cylinder 904 is provided on the through hole 902. The vent 903 is installed above the through hole 902 through a rod-shaped support structure (not marked in the figure), and the size of the vent 903 is larger than the size of the through hole 902. A recessed water collection trough 905 is provided at one end of the liner plate 901, and the water collection trough 905 is connected to a condensate recovery device (not marked in the figure).

[0055] The steam generated from the heat exchange between the deacidification wastewater and the cooling circulating water in the heat exchange coil 3, as well as the steam generated from the deacidification wastewater cooled in the saline wastewater concentration section, rises from the through-hole 902 to above the support plate 901. The vent 903, larger than the through-hole 902, guides and disperses the steam. Simultaneously, if the steam condenses and drips from the vent 903 during its ascent, it will not fall into the through-hole 902 below, but will drip onto the support plate 901. A water collection tank 905 is provided on one side of the support plate 901 to send the collected condensate to a condensate recovery device. In this application, the water collector 9 prevents the condensate collected by the demisting packing from falling to the bottom of the cooler, achieving separate collection of clean condensate.

[0056] The method for utilizing deacidification wastewater based on the above-mentioned neutralization deacidification wastewater resource utilization system includes the following steps.

[0057] S1: Cooling of deacidification wastewater;

[0058] The deacidification wastewater is transferred to cooling tank 6 for storage until it is cooled to a preset temperature before being sent to a cooler; some of the crystalline salt precipitated during the cooling process in cooling tank 6 is recovered.

[0059] S2: Heat exchange and evaporation of deacidification wastewater to increase the salt concentration of deacidification wastewater;

[0060] A closed heat exchange coil 3 is installed in the cooler; after the deacidification wastewater is cooled down, it is sent into the cooler and then atomized and sprayed to indirectly exchange heat with the circulating cooling water in the heat exchange coil 3; the atomized deacidification wastewater exchanges heat with the circulating cooling water at a higher temperature, and the water in the deacidification wastewater is evaporated to obtain a higher concentration of deacidification wastewater.

[0061] S3: Precipitation of mixed salts;

[0062] A wastewater concentration section 105 is installed below the heat exchange coil 3 in the cooler. The deacidified wastewater after heat exchange falls into the salt-containing wastewater concentration section 105 for cooling, and crystallized salt precipitates at the bottom.

[0063] In steps S2 and S3, the steam generated after the deacidification wastewater exchanges heat with the cooling circulating water in the heat exchange coil 3, as well as the steam generated from the deacidification wastewater cooled in the salt wastewater concentration section, are all recovered and reused.

[0064] S4: Brine separation;

[0065] The high-concentration crystalline salt mixture at the bottom of the wastewater concentration section is sent to the cooler for solid-liquid separation. The separated low-salt waste liquid is sent back to the cooling tank 6, and the separated solid crystalline salt is reused for resource recovery.

[0066] S5: Repeat steps S1~S4, gradually increasing the salt concentration of the deacidification wastewater in the cooling tank, and reusing the precipitated solid crystalline salt.

[0067] Desulfurization wastewater typically contains about 5% of a mixed salt primarily composed of sodium chloride and sodium sulfate. Because brine has a relatively low specific heat capacity (4.18 J / (g℃) for conventional water and 3.47 J / (g℃) for 10% brine), it absorbs less heat than conventional low-hardness and low-salinity process water, allowing for the consumption of a larger volume of desulfurization wastewater.

[0068] In existing cooling equipment, a packing layer is set under the spray pipe. In this application, indirect cooling with coils is used, and no packing layer is set under the spray pipe. Compared with the prior art, the arrangement of this application increases the gas-liquid contact area and is less prone to clogging, thereby ensuring that the separation of salt and water is easier to achieve in the cooler of this application.

[0069] The saturated solubility of sodium chloride at 20℃ is 36.0 g / 100 g water, and the saturated solubility of sodium sulfate at 20℃ is 19.5 g / 100 g water. When the deacidification wastewater is cooled by about 10℃, every 1 kg of circulating cooling water can evaporate 17 g of water from the saline wastewater. After 5 cycles, 0.1 kg of saline deacidification wastewater can increase the salt concentration to more than 33.33%, thereby allowing the salt to precipitate and separate.

Claims

1. A method for the resource utilization of deacidified saline wastewater via neutralization, characterized in that, It includes the following steps: S1: Cooling of deacidification wastewater; The deacidification wastewater is sent to a cooling tank for natural cooling until it reaches a preset temperature, after which it is sent to a cooler; some of the crystalline salts that precipitate during the cooling process are recovered. In step S1, when the deacidification waste liquid in the cooling tank is cooled to 20°C, it is sent to the subsequent steps; S2: Heat exchange and evaporation of deacidification wastewater; A closed heat exchange coil is installed in the cooler; after the deacidification wastewater is cooled, it is sent into the cooler and then atomized and sprayed to indirectly exchange heat with the circulating cooling water with a higher temperature in the heat exchange coil. The atomized deacidification wastewater exchanges heat with the circulating cooling water with a higher temperature, and the water in the deacidification wastewater is evaporated to obtain a higher concentration of deacidification wastewater. S3: Precipitation of mixed salts; A wastewater concentration section is set below the heat exchange coil in the cooler. The higher concentration of deacidified wastewater after heat exchange falls into the salt-containing wastewater concentration section for cooling, and crystallized salt precipitates at the bottom. In step S3, the deacidified wastewater after heat exchange stored in the wastewater concentration section, and the deacidified wastewater with lower salt concentration in the upper part are sent to the cooling tank through the overflow port for further cooling. S4: Brine separation; The high-concentration crystalline salt mixture at the bottom of the wastewater concentration section is sent out of the cooler and undergoes a solid-liquid separation process by a centrifuge. The separated solid crystalline salt is reused, and the separated waste liquid is sent back to the cooling tank. The inlet of the circulating pump is located at the bottom of the cooling pool, and a precision filter is installed at the outlet of the circulating pump to recover the crystallized salt that precipitates during the cooling process. S5: Repeat steps S1~S4, gradually increasing the salt concentration of the deacidification wastewater in the cooling tank, and reusing the precipitated solid crystalline salt.

2. The method for resource utilization of neutralized deacidified saline wastewater according to claim 1, characterized in that: In step S2, the circulating cooling water in the heat exchange coil is the high-temperature cooling water output from the cooling equipment of the rotating shaft or mechanical seal of the large equipment in the same system after heat exchange.

3. The method for resource utilization of neutralized deacidified saline wastewater according to claim 1, characterized in that: In steps S2 and S3, the water vapor generated after the deacidification wastewater exchanges heat with the circulating cooling water in the heat exchange coil, as well as the water vapor generated by the deacidification wastewater cooled in the salt-containing wastewater concentration section, are all recycled as clean condensate for reuse.

4. A system for the resource utilization of saline wastewater treated by neutralization, comprising: The cooler shell and atomizing spray equipment are characterized in that they further include: heat exchange coils, salt scrapers, centrifuges, and cooling tanks; The atomizing spray device, the heat exchange coil, and the salt scraper are arranged in the inner cavity of the cooler shell in a top-to-bottom order; the salt scraper is located at the bottom of the inner cavity of the cooler shell; and a steam exhaust port is provided at the top of the cooler shell. The cooling pool is located outside the cooler shell and is connected to the liquid supply equipment for deacidification wastewater; The atomizing spray equipment includes: a deacidification wastewater inlet and a spray nozzle; the cooling pool is connected to the deacidification wastewater inlet of the atomizing spray equipment via a circulating pump; the circulating pump inlet is located at the bottom of the cooling pool and a precision filter is installed at the outlet of the circulating pump. The heat exchange coil includes an inlet and an outlet for circulating cooling water. The inlet is located below the outlet, and the inlet and outlet are respectively connected to the circulating cooling water supply equipment. The bottom of the cooler housing is provided with a crystallization salt discharge port, which is connected to the centrifuge, and the liquid discharge port of the centrifuge is connected to the cooling pool; The salt scraper includes a scraper and a drive motor, wherein the scraper is mounted on the output shaft of the drive motor. The bottom of the cooler housing is a bowl-shaped structure with a central depression, and the crystallized salt discharge port is located near the bottom of the bowl; The curvature of the scraper blade is adapted to the curvature of the bottom of the cooler housing, and the blade faces the bottom of the cooler housing during installation, and is set close to the bottom end face of the cooler housing; through holes are evenly opened on the back of the scraper blade; An air inlet and a deacidification wastewater overflow outlet are provided on the cooler shell between the salt scraper and the heat exchange coil, from top to bottom; the deacidification wastewater overflow outlet is connected to the cooling tank.

5. The neutralization-based deacidification and saline wastewater resource utilization system according to claim 4, characterized in that: It also includes: a water collector and a demisting packing layer, wherein the water collector is disposed between the atomizing spray device and the exhaust fan; and the demisting packing layer is disposed between the water collector and the exhaust fan. The water collector includes a liner plate and a vent cap. The liner plate has a through hole, and a cylinder is disposed on the through hole. The vent cap is mounted above the through hole by a support structure, and the size of the vent cap is larger than the size of the through hole. One end of the liner plate has a recessed water collection trough, which is connected to a condensate recovery device.

Images