A high-salinity wastewater concentration device coupled with desulfurization slurry waste heat utilization and condensate water recovery

Abstract

The application discloses a high-salinity wastewater concentration device coupled with desulfurization slurry waste heat utilization and condensate water recovery, which comprises a desulfurization tower and a concentration tower. The bottom of the desulfurization tower is provided with a slurry pool. The concentration tower comprises a tower body, the bottom of the tower body is provided with a concentration pool for containing high-salinity wastewater, the top of the tower body is provided with a waste gas outlet, a filler layer is arranged above the concentration pool, a wastewater spraying layer is arranged above the filler layer, and the wastewater spraying layer and the concentration pool are connected through a wastewater circulating pump. A slurry heat exchanger is arranged below the liquid level of the high-salinity wastewater in the concentration pool. The slurry heat exchanger is provided with a medium flow channel. The inlet and outlet of the medium flow channel are connected with the slurry pool through a second slurry circulating pump and a slurry pipeline, so that the desulfurization slurry in the slurry pool is used as a heat exchange medium to form a heat exchange loop in the slurry heat exchanger and the slurry pool. A condensate water recovery assembly is arranged between the wastewater spraying layer and the waste gas outlet. The wastewater concentration device of the application is coupled with the desulfurization slurry waste heat utilization and the condensate water recovery.

Description

Technical Field

[0001] This application relates to the field of industrial waste heat recovery technology, specifically to a high-salt wastewater concentration device that couples the utilization of waste heat from desulfurization slurry with the recovery of condensate. Background Technology

[0002] In industrial sectors such as coal-fired power plants and steel smelting, the large amount of desulfurization slurry (typically maintained at 50-55℃) generated by wet desulfurization systems contains considerable low-grade heat energy. However, in existing technologies, this waste heat is mostly discharged directly through cooling towers, resulting in energy waste and environmental thermal pollution. Meanwhile, high-salinity wastewater from thermal power plants faces the industry challenge of high treatment costs due to its high salt content, complex composition, and large-scale treatment operation.

[0003] Traditional high-salinity wastewater treatment processes face multiple challenges. Mainstream multi-effect evaporation or mechanical vapor recompression technologies consume large amounts of steam or electricity, with energy consumption reaching 30-50 kWh / ton, accounting for 15%-25% of the plant's total energy consumption. When high-salinity wastewater is concentrated to 15%-20% in the evaporator, the precipitation of CaSO4, silicates, etc., leads to severe scaling on the heat exchange surfaces, and chloride ions corrode equipment, significantly shortening the system's lifespan. The secondary steam generated during the evaporation process is usually directly condensed and discharged without water recovery and reuse, exacerbating water resource pressure in water-scarce areas.

[0004] The current fragmented operation mode of desulfurization slurry waste heat utilization and high-salt wastewater treatment has the following drawbacks: (1) Low efficiency of waste heat utilization of desulfurization slurry: Although a few cases have attempted to use waste heat of desulfurization slurry for building heating or pretreatment temperature rise, the actual heat energy utilization rate is less than 20% because the heat source temperature (55-56℃) does not match the heat demand temperature (>70℃) and lacks coordinated design with wastewater treatment system; (2) High cost of treating high-salinity wastewater: Reliance on externally supplied steam or electric heat sources makes the cost of treating ton of water as high as 60-100 yuan. At the same time, frequent scaling of equipment leads to a shortened chemical cleaning cycle, and the consumption of descaling agents accounts for more than 40% of the operation and maintenance costs, further increasing the expenses; (3) High-quality condensate is not effectively recycled: The existing evaporation system only focuses on salt concentration and solidification, and lacks a targeted recycling mechanism for condensate with a purity of >98% (temperature 30-35℃), resulting in the loss of high-quality reclaimed water resources. Utility Model Content

[0005] This application provides a high-salt wastewater concentration device that couples the utilization of waste heat from desulfurization slurry and the recovery of condensate. The device recovers the waste heat from the desulfurization slurry through a slurry heat exchanger, driving the high-salt wastewater to achieve low-temperature evaporation and concentration in a concentration tower; it enhances the evaporation efficiency of wastewater by using a wastewater spraying subsystem combined with the packing material in the tower; it recovers the moisture and latent heat in the steam generated by evaporation through a steam condensation and water collection subsystem; and finally, the residual volatile gases are treated by combustion in a boiler.

[0006] A high-salt wastewater concentration device that couples desulfurization slurry waste heat utilization and condensate recovery includes a desulfurization tower and a concentration tower. The bottom of the desulfurization tower has a slurry pool, and a desulfurization spray layer is provided above the slurry pool. The desulfurization spray layer and the first slurry outlet of the slurry pool are connected by a first slurry circulation pump. The concentration tower includes: The tower body has a thickening tank at the bottom for containing high-salt wastewater and an exhaust gas outlet at the top. A packing layer is installed above the thickening tank, and a wastewater spraying layer is installed above the packing layer. The wastewater spraying layer and the thickening tank are connected by a wastewater circulation pump. The slurry heat exchanger is located below the liquid surface of the high-salt wastewater in the thickening tank. The slurry heat exchanger has a medium flow channel. The inlet and outlet of the medium flow channel are connected to the slurry tank through a second slurry circulation pump and a slurry circulation pipe. It is used to form a heat exchange circuit between the slurry heat exchanger and the slurry tank by using the desulfurization slurry in the slurry tank as the heat exchange medium. And a condensate recovery component, which is installed between the wastewater spray layer and the exhaust gas outlet.

[0007] In the concentration tower, high-salt wastewater is pumped to the wastewater spray layer via a wastewater circulation pump and evenly sprayed onto the surface of the packing layer to accelerate evaporation. This application addresses the slow evaporation rate of low-temperature wastewater by utilizing the desulfurization slurry at the bottom of the desulfurization tower for heating. This not only improves the evaporation and concentration efficiency of the wastewater but also lowers the temperature of the desulfurization slurry, helping to maintain a constant temperature. The steam generated by evaporation has high humidity and contains a large amount of latent heat. As the steam rises and passes through the condensate recovery component, it is condensed, recovering the moisture and latent heat. The condensate is collected via a liquid guide pipe and can be reused. The condensed steam still contains some volatile components, which can be extracted by a fan and transported to the boiler inlet for combustion in the furnace. This process recovers waste heat and saves on the cost of volatile gas treatment.

[0008] Several alternative methods are provided below, but they are not intended as additional limitations on the overall solution above. They are merely further additions or optimizations. Provided there are no technical or logical contradictions, each alternative method can be combined individually with respect to the overall solution above, or multiple alternative methods can be combined with each other.

[0009] Optionally, the slurry heat exchanger is a shell-and-tube slurry heat exchanger, and the diameter of the medium flow channel is 40~60mm.

[0010] Optionally, the inlet of the slurry circulation pump is connected to the second slurry outlet of the slurry tank through a slurry circulation pipe, and the outlet is connected to the inlet of the medium flow channel through a slurry circulation pipe; the outlet of the medium flow channel is connected to the slurry return port of the slurry tank through a slurry circulation pipe.

[0011] Optionally, the filler layer is filled with multifaceted hollow spheres made of polyvinylidene fluoride, with a filling height of 2.5~3.5m.

[0012] Optionally, the spray head of the wastewater spray layer is a conical spray head.

[0013] Optionally, the condensate recovery assembly includes a condensate layer arranged vertically and used to capture condensate from steam and a liquid guiding layer for collecting the condensate.

[0014] Optionally, a condensate tank is also included, which is connected to the outlet of the condensate layer via a condensate drain pipe. After the flue gas rises and passes through the condensate layer, the resulting condensate is collected in the condensate layer and then guided into the condensate tank through the condensate drain pipe.

[0015] Optionally, the condensation layer adopts a baffle demister structure, which consists of a series of zigzag or wavy baffles with an included angle of 45° between adjacent planar sections. When steam passes through, the mist droplets are separated due to inertial impact on the baffles.

[0016] Optionally, the liquid guiding layer mainly adopts a structure of several parallel strip guiding channels with a slight guiding slope (1-2°) on the surface. The material is corrosion-resistant FRP (fiberglass reinforced plastic), and the gap between adjacent strip guiding channels allows steam to pass through.

[0017] Optionally, the fluid guide tube is installed at a 15° downward angle.

[0018] Optionally, the exhaust gas outlet is connected to the boiler air inlet via a pipeline; an exhaust fan is installed at the exhaust gas outlet.

[0019] Optionally, the thickening tank has a high-salinity wastewater inlet and a high-salinity wastewater outlet, which are respectively connected to a high-salinity wastewater inlet pipe and a high-salinity wastewater outlet pipe.

[0020] Optionally, the water pipe connecting the wastewater circulation pump is connected to a height of 2 / 5 of the effective liquid level in the thickening tank.

[0021] Compared with the prior art, this application has the following beneficial effects: (1) This application provides a solution for efficiently utilizing the low-grade waste heat of desulfurization slurry. The waste heat of the 55°C desulfurization slurry is used to drive the evaporation of wastewater, replacing the externally supplied steam or electric drive heat source. The overall energy consumption of the system is reduced by more than 60%, and the traditional waste low-grade heat energy is converted into effective driving force. At the same time, the temperature of the desulfurization slurry is kept stable, ensuring the desulfurization efficiency.

[0022] (2) This application provides a steam condensate recovery scheme. During the steam condensation process, water is recovered and latent heat is released. The heat energy is recycled through the design of the condensation layer, thereby improving the thermal efficiency of the system. The purity of the recovered condensate is >98%, the temperature is 30-35℃, and the water resource recovery rate is >85%, thus avoiding the waste of freshwater resources.

[0023] (3) This application provides a solution to effectively reduce the volume and treatment cost of high-salt wastewater. After high-salt concentration, the salt content of the wastewater is 15%-20%, and the volume is reduced by 80%-85%, which greatly reduces the cost and difficulty of treating high-salt wastewater.

[0024] (4) This application provides a tail gas purification solution in which the evaporated volatile organic compounds are directly sent to the boiler for high-temperature combustion and decomposition, eliminating the waste gas treatment process, saving waste gas treatment costs, and avoiding secondary pollution. Attached Figure Description

[0025] Figure 1 This is a schematic diagram of the high-salt wastewater concentration device of this application.

[0026] The reference numerals in the figure are as follows: 1-Desulfurization tower: 11-Slurry pool, 12-Flue gas inlet, 13-Desulfurization spray layer, 14-Condensation and demisting layer, 15-Flue gas outlet; 2-First slurry circulation pump; 3-Second slurry circulation pump; 4-Slurry heat exchanger; 5-Concentration tower: 51-Concentration tank, 52-High salinity wastewater inlet pipe, 53-High salinity wastewater outlet pipe, 54-Packing layer, 55-Wastewater spray layer, 56-Liquid guiding layer, 57-Condensation layer, 58-Liquid guiding pipe; 6- Wastewater circulation pump; 7-Condensate tank; 8-Exhaust fan; 9. Slurry circulation pipe. Detailed Implementation

[0027] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0028] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application.

[0029] A high-salt wastewater concentration device, such as Figure 1 As shown, the structure includes a desulfurization tower 1 and a concentration tower 5. The desulfurization tower 1 includes a tower body, with a slurry pool 11 at the bottom of the tower body. A flue gas inlet 12 is provided on the tower wall above the slurry pool 11. A desulfurization spray layer 13 is provided inside the tower body and above the flue gas inlet. The desulfurization spray layer 13 is connected to the first slurry outlet of the slurry pool 11 through a first slurry circulation pump 2. A condensation and demisting layer 14 is provided above the desulfurization spray layer 13. A flue gas outlet 15 is provided at the top of the tower body.

[0030] The thickening tower 5 includes a tower body, with a thickening tank 51 at the bottom of the tower body. A packing layer 54 is arranged above the thickening tank 51, and a wastewater spray layer 55 is arranged above the packing layer 54. The wastewater spray layer 55 is connected to the thickening tank 51 through a wastewater circulation pump 6. A condensate recovery component is arranged above the wastewater spray layer 55. In some embodiments, the condensate recovery component includes a condensate layer 57 and a liquid guiding layer 56 arranged vertically. The liquid guiding layer 56 is located above the wastewater spray layer 55 and is connected to a condensate tank 7 externally through a condensate liquid guiding pipe 58. The condensate layer is located above the liquid guiding layer. The top of the tower body has an exhaust port.

[0031] A slurry heat exchanger 4 is installed in the thickening tank 51. The slurry heat exchanger 4 is located below the liquid surface in the thickening tank. The slurry heat exchanger has a medium flow channel with an inlet and an outlet. The inlet and outlet of the medium flow channel are connected to the slurry pool 11 of the desulfurization tower through a second slurry circulation pump 3 and a slurry circulation pipe. The desulfurization slurry in the desulfurization pool is driven by the second slurry circulation pump to be sent into the slurry heat exchanger as a heat exchange medium. The waste heat of the desulfurization slurry is used to exchange heat and concentrate with the high-salt wastewater in the thickening tank.

[0032] The thickening tank 51 has a high-salinity wastewater inlet and a high-salinity wastewater outlet. The high-salinity wastewater inlet is connected to a high-salinity wastewater inlet pipe 52, and the high-salinity wastewater outlet is connected to a high-salinity wastewater outlet pipe 53. Both the high-salinity wastewater inlet and outlet pipes are made of rigid polyvinyl chloride (UPVC) pipes with excellent corrosion resistance. Low-concentration high-salinity wastewater with a concentration of approximately 3% enters the thickening tank through the high-salinity wastewater inlet pipe. After thickening, high-concentration wastewater with a concentration of 15-20% is discharged through the high-salinity wastewater outlet pipe 53 at the bottom of the tank for further treatment.

[0033] The second slurry circulation pump 3 has an inlet and an outlet. In some embodiments, the inlet of the second slurry circulation pump 3 is connected to the second slurry outlet of the slurry tank 11 through a slurry circulation pipe 9, and the outlet of the second slurry circulation pump is connected to the inlet of the medium flow channel of the slurry heat exchanger 4 through the slurry circulation pipe 9. The outlet of the medium flow channel of the slurry heat exchanger 4 is connected to the slurry return port of the slurry tank 11 through the slurry circulation pipe 9. Driven by the second slurry circulation pump, the desulfurization slurry circulates between the slurry heat exchanger and the slurry tank as a heat exchange medium. The inlet temperature of the heat exchanger is approximately 55-56℃, the outlet temperature is 45-50℃, and the slurry flow velocity in the pipe is controlled within 2.0-3.0 m / s. In some embodiments, the slurry heat exchanger 4 is a shell-and-tube heat exchanger with an inner diameter of 40-60 mm.

[0034] In some embodiments, the height of the packing layer is set to 22.5~3.5m, preferably 3m, and can be filled with multifaceted hollow spheres made of polyvinylidene fluoride (PVDF). The wastewater spray layer 55 is located above the packing layer 54 and sprays towards the packing layer. The spray layer includes spray pipes and spray heads evenly distributed on the spray pipes. The spray heads can be conical spray heads. The wastewater circulation pump 6 drives the high-salt wastewater in the thickening tank to circulate and spray onto the packing layer. The flow velocity in the pipe of the high-salt wastewater spray system is 1.5-2.5 m / s. The wastewater circulation pump is made of duplex stainless steel. In some embodiments, the condensation layer 57 adopts a baffle demister structure, consisting of a series of zigzag or wavy baffles with an included angle of 45° between adjacent planar sections. When steam passes through, the mist droplets are separated due to inertial impact on the baffles. The liquid guiding layer 56 mainly adopts a structure of several parallel strip-shaped guiding channels with a slight guiding slope (1-2°) on the surface. The material is corrosion-resistant FRP (fiberglass reinforced plastic), and steam passes through the gaps between adjacent strip-shaped guiding channels.

[0035] After the flue gas rises and passes through the condensation layer, the condensate produced is collected in the liquid guiding layer and introduced into the condensate tank through the condensate liquid guiding pipe. The condensate liquid guiding pipe is inclined downward at a 15° angle, and the condensate flows to the condensate tank 7 by gravity.

[0036] An exhaust fan 8 is installed at the exhaust port at the top of the tower. The exhaust port is connected to the boiler air supply pipe through a pipeline. After passing through the condensation layer, the temperature of the flue gas drops to 30-35℃ and is drawn out by the exhaust fan 8 at the top of the tower and sent to the boiler for combustion.

[0037] The slurry tank 11, the second slurry circulation pump 3, the slurry heat exchanger 4, and the thickening tank 51 together constitute the desulfurization slurry waste heat utilization subsystem: The second slurry circulation pump 3 transports the desulfurization slurry at 55-56℃ to the tubular heat exchanger in the thickening tank, where it exchanges heat with the high-salt wastewater. The slurry after heat exchange is returned to the desulfurization tower slurry tank for recycling. Driven by the second slurry circulation pump, the 55-56℃ desulfurization slurry enters the slurry heat exchanger 4 at a flow rate of 2.0-3.0 m / s, where it undergoes liquid-liquid indirect heat exchange with the 40℃ high-salt wastewater. After heat exchange, the desulfurization slurry temperature drops to 45-50℃ and is returned to the slurry tank by the second slurry circulation pump for continued use in high-temperature flue gas desulfurization. Simultaneously, the high-salt wastewater temperature rises to 40-45℃ and enters the high-salt wastewater spraying subsystem.

[0038] The wastewater circulation pump 6, the spray pipes and spray heads of the wastewater spray layer 55, and the packing layer 54 constitute the high-salt wastewater spraying subsystem: the wastewater circulation pump 6 transports the wastewater from the thickener 11 to the wastewater spray layer 55, and sprays it evenly onto the surface of the PVDF multifaceted hollow spherical packing through the conical spray heads. The volatile components and water in the wastewater evaporate upon heating, forming saturated water vapor that rises. The unevaporated concentrated wastewater flows back to the thickener through the packing layer for further concentration.

[0039] The effective liquid level of the high-salinity wastewater thickening tank is 2.5m, and the outlet pipe connected to the wastewater circulation pump 6 is 1m below the effective liquid level. Under the action of water evaporation and gravity, salt gradually accumulates, and the heavier, high-concentration liquid and salt gradually sink, resulting in a higher salt concentration at the bottom of the tank than at the top. The concentrated high-concentration, high-salinity wastewater is discharged through the concentrated wastewater drain pipe at the bottom of the tank. The lower-concentration high-salinity wastewater in the upper part of the thickening tank 11 is lifted by the wastewater circulation pump 6 to the wastewater spray layer 55 at the top of the thickening tower, and is evenly sprayed onto the surface of the packing material through the spray nozzles, significantly increasing the contact area between the wastewater and the air. The system utilizes the humidity difference between the two to enhance the mass and heat transfer process, accelerate water evaporation, and generate saturated steam at about 40-45℃ that flows upward. As water continues to evaporate from the surface of the packing material, when the salt concentration reaches saturation, it will precipitate in the form of crystals, fall off the surface of the packing material, and finally settle at the bottom of the thickening tank.

[0040] The condenser layer 57, the liquid guiding layer 56, the condensate guiding pipe 58, and the condensate tank 7 constitute a steam condensation and water collection subsystem: As rising saturated steam passes through the condenser layer 57, it is cooled, and water condenses and precipitates on the surface of the condenser layer packing. The condensate is collected through the liquid guiding layer 56 and flows by gravity along the condensate guiding pipe 58 to the condensate tank 7 for recovery. During its flow through the condenser layer, the saturated steam at 40-45°C exchanges heat with the cooling medium, releasing latent heat of phase change, and its temperature drops to 30-35°C. The steam completes its phase change and condenses into liquid water during its ascent, at which point the condensate temperature remains at 30-35°C. After being collected by the liquid guiding layer, the condensate is discharged through the condensate guiding pipe and collected in the condensate tank.

[0041] The flue gas extracted by exhaust fan 8 contains harmful substances such as VOCs, ammonium salts, and nitrogen-containing pollutants. Direct emission of these substances would cause air pollution. Introducing them into the boiler furnace for combustion avoids additional treatment costs and allows for resource utilization.

[0042] The process flow of the above-mentioned device is as follows: (1) Inside the desulfurization tower, the desulfurization slurry at 55~56℃, driven by the second slurry circulation pump 3, enters the slurry heat exchanger 4 at a flow rate of 2.0~3.0 m / s, and exchanges liquid-liquid heat with the high-salt wastewater at 40℃. After the heat exchange, the slurry temperature drops to 50~55℃, and is returned to the slurry pool 11 driven by the second slurry circulation pump, continuing to be used for high-temperature flue gas desulfurization. At the same time, the temperature of the high-salt wastewater rises to 40~45℃.

[0043] (2) Low-concentration, high-salt wastewater (approximately 40-45°C) from the upper part of the thickener 51 is pumped by the wastewater circulation pump 6 to the wastewater spray layer at the top of the thickener tower. The wastewater is then evenly sprayed onto the surface of the packing material through spray nozzles, significantly increasing the contact area between the wastewater and the air. The system utilizes the humidity difference between the two to drive the mass and heat transfer processes, promoting water evaporation and generating saturated steam at 40-45°C that flows upwards. As the moisture on the packing surface continues to evaporate, crystals precipitate when the salt concentration reaches saturation, detaching from the packing surface and eventually settling at the bottom of the thickener.

[0044] (3) When saturated steam at 40~45℃ flows through the condenser layer 57, it exchanges heat with the cooling medium, releases the latent heat of phase change, and then its temperature drops to 30~35℃, condensing into liquid water. The condensate is collected through the liquid guide layer and then discharged through the liquid guide pipe 58 and collected in the condensate tank 7.

[0045] (4) The flue gas extracted by the exhaust fan 8 contains harmful substances such as VOCs, ammonium salts and nitrogen-containing pollutants, and is directly sent into the boiler furnace for combustion treatment.

[0046] The above embodiments merely illustrate several implementation methods of this application, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the invention patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this application, and these all fall within the protection scope of this application. Therefore, the protection scope of this patent application should be determined by the appended claims.

Claims

1. A high-salinity wastewater concentration device coupling desulfurization slurry waste heat utilization and condensate recovery, comprising a desulfurization tower and a concentration tower, wherein the bottom of the desulfurization tower has a slurry pool, a desulfurization spray layer is provided above the slurry pool, and the desulfurization spray layer is connected to a first slurry outlet of the slurry pool via a first slurry circulation pump; characterized in that, The concentration tower includes: The tower body has a thickening tank at the bottom for containing high-salt wastewater and an exhaust gas outlet at the top. A packing layer is installed above the thickening tank, and a wastewater spraying layer is installed above the packing layer. The wastewater spraying layer and the thickening tank are connected by a wastewater circulation pump. The slurry heat exchanger is located below the liquid surface of the high-salt wastewater in the thickening tank. The slurry heat exchanger has a medium flow channel. The inlet and outlet of the medium flow channel are connected to the slurry tank through a second slurry circulation pump and a slurry circulation pipe. It is used to form a heat exchange circuit between the slurry heat exchanger and the slurry tank by using the desulfurization slurry in the slurry tank as the heat exchange medium. And a condensate recovery component, which is installed between the wastewater spray layer and the exhaust gas outlet.

2. The high-salinity wastewater concentration device according to claim 1, characterized in that, The slurry heat exchanger is a shell-and-tube slurry heat exchanger with a medium flow channel diameter of 40~60mm.

3. The high-salinity wastewater concentration device according to claim 1, characterized in that, The inlet of the slurry circulation pump is connected to the second slurry outlet of the slurry tank through a slurry circulation pipe, and the outlet is connected to the inlet of the medium flow channel through a slurry circulation pipe; the outlet of the medium flow channel is connected to the slurry return port of the slurry tank through a slurry circulation pipe.

4. The high-salinity wastewater concentration device according to claim 1, characterized in that, The filler layer is filled with multifaceted hollow spheres made of polyvinylidene fluoride, with a filling height of 2.5~3.5m.

5. The high-salinity wastewater concentration device according to claim 1, characterized in that, The spray head of the wastewater spray layer is a conical spray head.

6. The high-salinity wastewater concentration device according to claim 1, characterized in that, The condensate recovery assembly includes a condensate layer arranged vertically and used to capture condensate from steam, and a liquid guiding layer for collecting the condensate.

7. The high-salinity wastewater concentration device according to claim 5, characterized in that, It also includes a condensate tank, which is connected to the outlet of the liquid guiding layer via a condensate guide pipe.

8. The high-salinity wastewater concentration device according to claim 1, characterized in that, The exhaust gas outlet is connected to the boiler air inlet via a pipeline; an exhaust fan is installed at the exhaust gas outlet.

9. The high-salinity wastewater concentration device according to claim 1, characterized in that, The thickening tank has a high-salinity wastewater inlet and a high-salinity wastewater outlet, which are respectively connected to a high-salinity wastewater inlet pipe and a high-salinity wastewater outlet pipe.

10. The high-salinity wastewater concentration device according to claim 1, characterized in that, The water pipe connecting the wastewater circulation pump is connected to the concentration tank at 2 / 5 of the effective liquid level.

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