Treatment system for high-salt, high-organic-matter and high-ammonia-nitrogen hazardous waste liquid

Abstract

The utility model relates to the technical field of industrial sewage treatment systems, in particular to a treatment system for high-salt, high-organic-matter and high-ammonia-nitrogen hazardous waste liquid. The system is composed of a raw water buffer tank, a low-temperature evaporation crystallizer, a distillate storage tank, an anaerobic reactor, an anaerobic water production tank, an ammonia stripping tower, an advanced oxidation reactor, a coagulation reaction sedimentation tank and a water outlet tank. The device has a good treatment effect on high-concentration dangerous waste liquid with the characteristics of high COD (Chemical Oxygen Demand) (as high as 150000 mg / L), high ammonia nitrogen (as high as 5000 mg / L), high salt and TDS (Total Dissolved Solids) as high as 180000 mg / L and mother liquor generated by an MVR (Mechanical Vapor Recompression) system, and is suitable for large, medium and small sewage treatment, and the effluent can be recycled or discharged into a municipal pipe network. The utility model solves the problems that the traditional dangerous waste liquid is difficult to treat, the direct incineration heat value is low, the atomization is difficult, the operation and maintenance are difficult, the cost is high, the environment is greatly harmed, and the like, realizes the purposes of energy conservation and high efficiency, and achieves the good combination of environmental benefits and economic benefits.

Description

Technical Field

[0001] The utility model relates to the technical field of industrial sewage treatment systems, and in particular to a treatment system for hazardous waste liquids containing high salt, high organic matter, and high ammonia nitrogen. Background Art

[0002] High-concentration hazardous waste and evaporation mother liquor produced by chemical, pharmaceutical, pesticide and other enterprises have complex sources, large fluctuations in water quality, and characteristics such as high COD, high salt, and high ammonia nitrogen. There is no very effective treatment method in traditional processes, and incineration is generally used. However, the amount of such wastewater is large, and the calorific value of direct incineration is low. It is necessary to add high calorific value materials for incineration treatment, and it is easy to cause the furnace of the incinerator to harden, affecting the normal incineration capacity of the furnace, and there is a risk of secondary pollution. Utility Model Content

[0003] The utility model aims to provide a treatment system for hazardous waste liquid with high salt, high organic matter and high ammonia nitrogen.

[0004] The utility model provides the following technical solutions:

[0005] The utility model proposes a treatment system for high-salt, high-organic-matter, high-ammonia-nitrogen hazardous waste liquid, comprising a raw water buffer tank and a low-temperature evaporation crystallizer; the outlet of the raw water buffer tank is connected to the inlet of the low-temperature evaporation crystallizer, the distillate outlet of the low-temperature evaporation crystallizer is connected to the inlet of a distillate storage tank, the outlet of the distillate storage tank is connected to the water inlet of an anaerobic reactor, the water outlet of the anaerobic reactor is connected to the inlet of an anaerobic water production pool, the outlet of the anaerobic water production pool is connected to the inlet of an ammonia stripping tower, the liquid discharge outlet of the ammonia stripping tower is connected to the inlet of an advanced oxidation reactor, the outlet of the advanced oxidation reactor is connected to the inlet of a coagulation reaction sedimentation tank, and the outlet of the coagulation reaction sedimentation tank is connected to a water outlet tank.

[0006] The residue outlet of the low-temperature evaporation crystallizer is connected to the inlet of a residue barrel; the steam condensate outlet of the low-temperature evaporation crystallizer is connected to the inlet of a condensate storage tank; the outlet of the condensate storage tank is connected to the water supply point of an external public cooling tower.

[0007] The biogas outlet of the anaerobic reactor is connected to the inlet of a steam-water separation tank, the outlet of the steam-water separation tank is connected to the inlet of a water seal tank, the outlet of the water seal tank is connected to the inlet of a biogas fan, and the outlet of the biogas fan is connected to an incinerator or an external public biogas combustion system.

[0008] The anaerobic water production tank includes an inlet channel, a first sedimentation tank and an intermediate water tank. The upper end of the inlet channel is flush with the first sedimentation tank and is not connected. The lower end of the inlet channel is connected to one side of the first sedimentation tank. The lower end of the first sedimentation tank is funnel-shaped below the lowest plane of the intermediate water tank, and a first sedimentation tank mud discharge port is provided at the bottom; the upper end of the other side of the first sedimentation tank is connected to the upper end of the intermediate water tank, and the intermediate water tank is provided with a second agitator for stirring the liquid inside the intermediate water tank. The intermediate water tank is connected to the first outlet of a first dosing barrel, and the first dosing barrel is provided with a fifth agitator.

[0009] The feeding port of the distillate storage tank is connected to the second outlet of the first dosing barrel.

[0010] The ammonia gas outlet of the ammonia stripping tower is connected to the air inlet of an ammonia adsorption tower, the outlet of the ammonia adsorption tower is connected to the inlet of an ammonia liquid recovery tank, and the outlet of the ammonia liquid recovery tank is connected to an external ammonia water recovery system.

[0011] The liquid outlet of the ammonia stripping tower is connected to the inlet of a deammoniation water production tank, and the outlet of the deammoniation water production tank is connected to the inlet of the advanced oxidation reactor.

[0012] The first feed port of the advanced oxidation reactor is connected to the outlet of a second dosing barrel, and the second dosing barrel is provided with a sixth agitator; the second feed port of the advanced oxidation reactor is connected to the outlet of a third dosing barrel.

[0013] The coagulation reaction sedimentation tank comprises a first reaction tank, a second reaction tank and a second sedimentation tank; the second reaction tank is between the first reaction tank and the second sedimentation tank, the lower end of the first reaction tank is connected to the lower end of the second reaction tank, the upper end of the second reaction tank is connected to the upper end of one side of the second sedimentation tank, and the upper end of the other side of the second sedimentation tank is connected to the upper end of an outlet channel; the upper end of the first reaction tank, the upper end of the second reaction tank, the upper end of the second sedimentation tank and the upper end of the outlet channel are at the same height, the lower end of the first reaction tank, the lower end of the second reaction tank and the lower end of the outlet channel are at the same height, and the lower end of the second sedimentation tank is lower than The lower end of the second reaction tank is funnel-shaped, and a second sedimentation tank mud discharge port is opened at the bottom; an inclined plate filler for solid-liquid separation is arranged in the middle of the second sedimentation tank; the first reaction tank is provided with a third agitator for stirring the liquid in the first reaction tank, and the second reaction tank is provided with a fourth agitator for stirring the liquid in the second reaction tank, the feeding port of the first reaction tank is connected to the outlet of a fifth dosing barrel, and the fifth dosing barrel is provided with an eighth agitator; the feeding port of the first reaction tank is also connected to the third outlet of the first dosing pump; the feeding port of the second reaction tank is connected to the outlet of a fourth dosing barrel, and the fourth dosing barrel is provided with a seventh agitator.

[0014] The distillation liquid storage tank is provided with a first agitator for agitating the liquid in the distillation liquid storage tank.

[0015] Compared with the prior art, the utility model has the following beneficial effects: for high-concentration hazardous waste liquids with high COD (up to 150,000 mg / L), high ammonia nitrogen (up to 5,000 mg / L), high salt, TDS up to 180,000 mg / L and the mother liquor produced by the MVR system, the treatment effect is good, the effluent can be recycled or discharged into the municipal pipe network, and it is suitable for large, medium and small sewage treatment. The treatment system provided by the utility model solves the problems of traditional hazardous waste liquids being difficult to treat, low calorific value of direct incineration, difficult atomization, difficult operation and maintenance, high cost, and great harm to the environment, achieving the purpose of energy saving and high efficiency, and achieving a good combination of environmental benefits and economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 This is a schematic diagram of the main process flow of the utility model.

[0017] Figure 2 This is a connection diagram of the raw water buffer tank, low-temperature evaporation crystallizer and distillate storage tank.

[0018] Figure 3 This is a schematic diagram of the connection between the anaerobic reactor and the anaerobic water production tank.

[0019] Figure 4 This is a connection diagram of the ammonia stripping tower, ammonia adsorption tower and deammoniation water production tank.

[0020] Figure 5 This is a schematic diagram of the connection between the advanced oxidation reactor and the coagulation reaction sedimentation tank.

[0021] (The non-numerical arrows in the figure indicate the direction of material flow)

[0022] In the figure, 1-raw water buffer tank; 21-low temperature evaporation crystallizer; 22-residue barrel; 23-condensate storage tank; 24-condensate lifting pump; 3-distillate storage tank; 31-first agitator; 32-distillate lifting pump; 41-anaerobic reactor; 43-steam-water separation tank; 44-water seal tank; 45-biogas fan; 5-anaerobic water production tank; 50-inlet channel; 51-first sedimentation tank; 52-intermediate water tank; 53-second agitator; 54-anaerobic water production lifting pump; 61-ammonia stripping tower; 66-ammonia adsorption tower; 611-ammonia liquid recovery tank; 612-ammonia liquid recovery lifting pump; 7-deammonification water production tank; 71-deammonification water production lifting pump; 81-advanced oxidation reactor; 9-coagulation Reaction sedimentation tank; 91-first reaction tank; 92-second reaction tank; 93-second sedimentation tank; 94-third agitator; 95-fourth agitator; 96-exit channel; 97-inclined plate filler; 10-water outlet tank; 121-first dosing barrel; 122-fifth agitator; 123-first dosing pump; 124-second dosing pump; 125-third dosing pump; 131-second dosing barrel; 132-sixth agitator; 133-fourth dosing pump; 141-third dosing barrel; 142-fifth dosing pump; 151-fourth dosing barrel; 152-seventh agitator; 153-sixth dosing pump; 161-fifth dosing barrel; 162-eighth agitator; 163-seventh dosing pump. DETAILED DESCRIPTION

[0023] The utility model is further described below in conjunction with the accompanying drawings.

[0024] The utility model provides an embodiment:

[0025] The raw water buffer tank used in this example: 10m 3 ; Low temperature evaporation crystallizer: LT-ZQ500, processing capacity 500L / h; Distillate storage tank: 10m 3 ; Anaerobic reactor: ZM-UASB500, processing capacity 500L / h; Ammonia stripping tower: ZM-AN500, processing capacity 500L / h; Ammonia adsorption tower: M-TN500, processing capacity 500L / h; Advanced oxidation reactor: ZM-FEO500, processing capacity 500L / h; Steam-water separation tank: Φ500×800mm; Water seal tank: Φ500×1200mm; Biogas blower: HC-20S.

[0026] See also Figure 1-Figure 5In one embodiment of the utility model, a treatment system for high-salt, high-organic-matter, high-ammonia-nitrogen hazardous waste liquid includes a raw water buffer tank 1 and a low-temperature evaporation crystallizer 21; the outlet of the raw water buffer tank 1 is connected to the inlet of the low-temperature evaporation crystallizer 21, the distillate outlet of the low-temperature evaporation crystallizer 21 is connected to the inlet of a distillate storage tank 3, the outlet of the distillate storage tank 3 is connected to the water inlet of an anaerobic reactor 41, the water outlet of the anaerobic reactor 41 is connected to the inlet of an anaerobic water production pool 5, the outlet of the anaerobic water production pool 5 is connected to the inlet of an ammonia stripping tower 61, the liquid discharge outlet of the ammonia stripping tower 61 is connected to the inlet of an advanced oxidation reactor 81, the outlet of the advanced oxidation reactor 81 is connected to the inlet of a coagulation reaction sedimentation tank 9, and the outlet of the coagulation reaction sedimentation tank 9 is connected to a water outlet tank 10.

[0027] See also Figure 2 and Figure 3 In the above embodiment, a distillate boost pump is provided between the outlet of the distillate storage tank 3 and the water inlet of the anaerobic reactor 41 to facilitate flow control.

[0028] See also Figure 3 and Figure 4 In the above embodiment, an anaerobic water production lift pump is provided between the outlet of the anaerobic water production pool 5 and the inlet of the ammonia stripping tower to control the flow rate.

[0029] See also Figure 2 In one embodiment of the utility model, the residue outlet of the low-temperature evaporation crystallizer 21 is connected to the inlet of a residue barrel 22; the steam condensate outlet of the low-temperature evaporation crystallizer 21 is connected to the inlet of a condensate storage tank 23; the outlet of the condensate storage tank 23 is connected to the water supply point of an external public cooling tower.

[0030] Please continue reading Figure 2 In the above embodiment, a condensate lift pump 24 is connected to the outlet of the condensate storage tank 23 to facilitate the control of the discharge of water in the condensate storage tank 23.

[0031] See also Figure 3 In one embodiment of the utility model, the biogas outlet of the anaerobic reactor 41 is connected to the inlet of a steam-water separation tank 43, the outlet of the steam-water separation tank 43 is connected to the inlet of a water seal tank 44, the outlet of the water seal tank 44 is connected to the inlet of a biogas fan 45, and the outlet of the biogas fan 45 is connected to an incinerator or an external public biogas combustion system.

[0032] Please continue reading Figure 3In one embodiment of the utility model, the anaerobic water production tank 5 includes an inlet channel 50, a first sedimentation tank 51 and an intermediate water tank 52. The upper end of the inlet channel 50 is flush with the first sedimentation tank 51 and is not connected. The lower end of the inlet channel 50 is connected to one side of the first sedimentation tank 51. The lower end of the first sedimentation tank 51 is funnel-shaped below the lowest plane of the intermediate water tank, and a first sedimentation tank mud discharge port is provided at the bottom; the upper end of the other side of the first sedimentation tank 51 is connected to the upper end of the intermediate water tank 52, and the intermediate water tank 52 is provided with a second agitator 53 for stirring the liquid inside the intermediate water tank. The intermediate water tank 52 is connected to the first outlet of a first dosing barrel 121, and the first dosing barrel 121 is provided with a fifth agitator 122.

[0033] Please continue reading Figure 3 In the above embodiment, a second dosing pump 124 is provided between the intermediate water pool 52 and the first outlet of the first dosing barrel 121 .

[0034] See also Figure 2 In one embodiment of the present invention, the feeding port of the distillate storage tank 3 is connected to the second outlet of the first dosing barrel 121 .

[0035] Please continue reading Figure 2 In the above embodiment, a first dosing pump is provided between the feed port of the distillate storage tank 3 and the second outlet of the first dosing barrel 121 .

[0036] See also Figure 4 In one embodiment of the utility model, the ammonia gas outlet of the ammonia stripping tower 61 is connected to the air inlet of an ammonia adsorption tower 66, the outlet of the ammonia adsorption tower 66 is connected to the inlet of an ammonia liquid recovery tank 611, and the outlet of the ammonia liquid recovery tank 611 is connected to an external ammonia water recovery system.

[0037] See also Figure 4 and Figure 5 In one embodiment of the utility model, the liquid outlet of the ammonia stripping tower 61 is connected to the inlet of a deammoniation water production tank 7, and the outlet of the deammoniation water production tank 7 is connected to the inlet of the advanced oxidation reactor 81; it is convenient to control the flow rate.

[0038] Please continue reading Figure 4 and Figure 5 In the above embodiment, a deamination water production lift pump is provided between the outlet of the deamination water production tank 7 and the inlet of the advanced oxidation reactor 81 to control the flow rate.

[0039] See also Figure 5 In one embodiment of the utility model, the first feeding port of the advanced oxidation reactor 81 is connected to the outlet 131 of a second dosing barrel, and the second dosing barrel 131 is provided with a sixth agitator 132; the second feeding port of the advanced oxidation reactor 81 is connected to the outlet of a third dosing barrel 141.

[0040] Please continue reading Figure 5 In the above embodiment, a fourth dosing pump 133 is provided between the first feed port of the advanced oxidation reactor 81 and the outlet 131 of the second dosing barrel; a fifth dosing pump is provided between the second feed port of the advanced oxidation reactor 81 and the outlet of the third dosing barrel 141.

[0041] Please continue reading Figure 5 In one embodiment of the utility model, the coagulation reaction sedimentation tank 9 includes a first reaction tank 91, a second reaction tank 92 and a second sedimentation tank 93; the second reaction tank 92 is between the first reaction tank 91 and the second sedimentation tank 93, the lower end of the first reaction tank 91 is connected to the lower end of the second reaction tank 92, the upper end of the second reaction tank 92 is connected to the upper end of one side of the second sedimentation tank 93, and the upper end of the other side of the second sedimentation tank 93 is connected to the upper end of an outlet channel 96; the upper end of the first reaction tank 91, the upper end of the second reaction tank 92, the upper end of the second sedimentation tank 93 and the upper end of the outlet channel 96 are at the same height, the lower end of the first reaction tank 91, the lower end of the second reaction tank 92 and the lower end of the outlet channel 96 are at the same height, and the second sedimentation tank 93 The lower end of the second reaction tank 93 is lower than the lower end of the second reaction tank 92 and is funnel-shaped, and a second sedimentation tank mud discharge port is opened at the bottom; an inclined plate filler 97 for solid-liquid separation is arranged in the middle of the second sedimentation tank 93; the first reaction tank 91 is provided with a third agitator 94 for stirring the liquid in the first reaction tank 91, and the second reaction tank 92 is provided with a fourth agitator 95 for stirring the liquid in the second reaction tank, and the feeding port of the first reaction tank 91 is connected to the outlet of a fifth dosing barrel 161, and the fifth dosing barrel 161 is provided with an eighth agitator 162; the feeding port of the first reaction tank is also connected to the third outlet of the first dosing pump 121, and the feeding port of the second reaction tank 92 is connected to the outlet of a fourth dosing barrel 151, and the fourth dosing barrel 151 is provided with a seventh agitator 152.

[0042] Continue reading Figure 5 In the above embodiment, a third dosing pump 125 is arranged between the feeding port of the first reaction tank and the third outlet of the first dosing pump 121, a seventh dosing pump is arranged between the feeding port of the first reaction tank 91 and the outlet of the fifth dosing barrel 161, and a sixth dosing pump 153 is arranged between the feeding port of the second reaction tank 92 and the outlet of the fourth dosing barrel 151.

[0043] See also Figure 2 In one embodiment of the present invention, the distillation liquid storage tank 3 is provided with a first agitator 31 for stirring the liquid in the distillation liquid storage tank.

[0044] In practical applications, after the hazardous waste liquid enters the raw water buffer tank 1 and is averaged, it enters the low-temperature evaporation crystallizer 21. The low-temperature evaporation crystallization will produce steam condensed water, which is pumped into the external municipal public water system as cooling water replenishment through a pump; the distillate obtained by the low-temperature evaporation crystallization enters the distillate storage tank 3, and liquid alkali is added to the distillate storage tank 3; the obtained solution enters the anaerobic reactor 41 for anaerobic reaction, and organic matter such as COD in the wastewater is converted into small molecular inorganic matter and carbon dioxide and other substances; the anaerobic circulation pump of the anaerobic reactor is controlled to control the internal rising flow rate of the anaerobic reactor to be 0.5-1.0m / h; the biogas generated by the anaerobic reaction is connected to the external municipal public biogas combustion system for combustion treatment; the liquid after the anaerobic reaction enters the anaerobic water production tank 5 through the inlet channel 50, and solid-liquid separation is carried out in the first sedimentation tank 51, and alkali is added to the central water tank 52 Liquid, controlling the pH at 11-12, the liquid with controlled pH enters the ammonia stripping tower 61 for ammonia stripping treatment, the ammonia gas stripped from the ammonia stripping tower 61 enters the ammonia adsorption tower 66 for ammonia adsorption to become ammonia water or saturated ammonium sulfate solution, and the ammonia water or saturated ammonium sulfate solution is recovered; the liquid discharged from the ammonia stripping tower 61 enters the advanced oxidation reactor 81, the second dosing barrel 131 is filled with sulfuric acid and ferrous sulfate, and the third dosing barrel 141 is filled with hydrogen peroxide, sulfuric acid, ferrous sulfate and hydrogen peroxide are added to the advanced oxidation reactor 81, and the hydroxyl free radicals with strong oxidizing property generated by them oxidize the pollutants in the wastewater into harmless substances such as inorganic substances and carbon dioxide, and the oxidized wastewater enters the coagulation reaction tank 9, alkali and PAC are added to the first reaction tank 91, and PAM is added to the second reaction tank 92, and then enters the second sedimentation tank 93 for solid-liquid separation, and the obtained liquid is the produced water.

[0045] After the above treatment, the produced water meets the water quality limit value of Class B in Table 1 of the "Water Quality Standard for Sewage Discharge into Urban Sewers" (GB / T 31962-2015), COD≤500 mg / L, ammonia nitrogen≤45 mg / L, TDS≤2000 mg / L, Cl - ≤800mg / L.

[0046] The implementation modes of the present invention are provided for the purpose of illustration and description. Although the embodiments of the present invention have been shown and described above, it can be understood that the above embodiments are exemplary and cannot be understood as limitations of the present invention. Ordinary technicians in this field can change, modify, replace and modify the above embodiments within the scope of the present invention.

Claims

1. A system for treating hazardous waste liquid with high salt content, high organic matter content and high ammonia nitrogen content, characterized by: It includes a raw water buffer tank and a low-temperature evaporation crystallizer; the outlet of the raw water buffer tank is connected to the inlet of the low-temperature evaporation crystallizer, the distillate outlet of the low-temperature evaporation crystallizer is connected to the inlet of a distillate storage tank, the outlet of the distillate storage tank is connected to the water inlet of an anaerobic reactor, the water outlet of the anaerobic reactor is connected to the inlet of an anaerobic water production tank, the outlet of the anaerobic water production tank is connected to the inlet of an ammonia stripping tower, the liquid discharge outlet of the ammonia stripping tower is connected to the inlet of an advanced oxidation reactor, the outlet of the advanced oxidation reactor is connected to the inlet of a coagulation reaction sedimentation tank, and the outlet of the coagulation reaction sedimentation tank is connected to a water outlet tank.

2. A system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1, characterized in that: The residue outlet of the low-temperature evaporation crystallizer is connected to the inlet of a residue barrel; the steam condensate outlet of the low-temperature evaporation crystallizer is connected to the inlet of a condensate storage tank; the outlet of the condensate storage tank is connected to the water supply point of an external public cooling tower.

3. A system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1, characterized in that: The biogas outlet of the anaerobic reactor is connected to the inlet of a steam-water separation tank, the outlet of the steam-water separation tank is connected to the inlet of a water seal tank, the outlet of the water seal tank is connected to the inlet of a biogas fan, and the outlet of the biogas fan is connected to an incinerator or an external public biogas combustion system.

4. A system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1, characterized in that: The anaerobic water production tank includes an inlet channel, a first sedimentation tank and an intermediate water tank. The upper end of the inlet channel is flush with the first sedimentation tank and is not connected. The lower end of the inlet channel is connected to one side of the first sedimentation tank. The lower end of the first sedimentation tank is funnel-shaped below the lowest plane of the intermediate water tank, and a first sedimentation tank mud discharge port is provided at the bottom; the upper end of the other side of the first sedimentation tank is connected to the upper end of the intermediate water tank, and the intermediate water tank is provided with a second agitator for stirring the liquid inside the intermediate water tank; the intermediate water tank is connected to the first outlet of a first dosing barrel, and the first dosing barrel is provided with a fifth agitator.

5. A system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 4, characterized in that: The feeding port of the distillate storage tank is connected to the second outlet of the first dosing barrel.

6. A system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1, characterized in that: The ammonia gas outlet of the ammonia stripping tower is connected to the air inlet of an ammonia adsorption tower, the outlet of the ammonia adsorption tower is connected to the inlet of an ammonia liquid recovery tank, and the outlet of the ammonia liquid recovery tank is connected to an external ammonia water recovery system.

7. The system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1, characterized in that: The liquid outlet of the ammonia stripping tower is connected to the inlet of a deammoniation water production tank, and the outlet of the deammoniation water production tank is connected to the inlet of the advanced oxidation reactor.

8. The system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1 is characterized by: The first feed port of the advanced oxidation reactor is connected to the outlet of a second dosing barrel, and the second dosing barrel is provided with a sixth agitator; the second feed port of the advanced oxidation reactor is connected to the outlet of a third dosing barrel.

9. A system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 4, characterized in that: The coagulation reaction sedimentation tank comprises a first reaction tank, a second reaction tank and a second sedimentation tank; the second reaction tank is between the first reaction tank and the second sedimentation tank, the lower end of the first reaction tank is connected to the lower end of the second reaction tank, the upper end of the second reaction tank is connected to the upper end of one side of the second sedimentation tank, and the upper end of the other side of the second sedimentation tank is connected to the upper end of an outlet channel; the upper end of the first reaction tank, the upper end of the second reaction tank, the upper end of the second sedimentation tank and the upper end of the outlet channel are at the same height, the lower end of the first reaction tank, the lower end of the second reaction tank and the lower end of the outlet channel are at the same height, and the lower end of the second sedimentation tank is lower than The lower end of the second reaction tank is funnel-shaped, and a second sedimentation tank mud discharge port is opened at the bottom; an inclined plate filler for solid-liquid separation is arranged in the middle of the second sedimentation tank; the first reaction tank is provided with a third agitator for stirring the liquid in the first reaction tank, and the second reaction tank is provided with a fourth agitator for stirring the liquid in the second reaction tank, the feeding port of the first reaction tank is connected to the outlet of a fifth dosing barrel, and the fifth dosing barrel is provided with an eighth agitator; the feeding port of the first reaction tank is also connected to the third outlet of the first dosing barrel; the feeding port of the second reaction tank is connected to the outlet of a fourth dosing barrel, and the fourth dosing barrel is provided with a seventh agitator.

10. The system for treating hazardous waste liquid containing high salt, high organic matter and high ammonia nitrogen according to claim 1, characterized in that: The distillate storage tank is provided with a first stirrer for stirring the liquid in the distillate storage tank.

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