Integrated wastewater chroma and organic matter removal device

Abstract

The utility model discloses an integrated wastewater chroma and organic matter removal device which comprises a device body, and the device body comprises a water inlet pipeline, an ozone catalytic oxidation zone, an advanced oxidation zone, a neutralization reaction zone, a settling zone and a water outlet pipeline which are sequentially communicated along the flowing direction of wastewater, the water inlet pipeline is communicated with an ozone supply mechanism for supplying ozone to the water inlet pipeline, the catalytic ozonation zone is provided with a hydrogen peroxide adding port which is communicated with a hydrogen peroxide supply mechanism, the advanced oxidation zone is provided with a ferrous sulfate adding port which is communicated with a ferrous sulfate supply mechanism, and the neutralization reaction zone is provided with a sodium hydroxide adding port which is communicated with a sodium hydroxide supply mechanism. The sodium hydroxide feeding port is communicated with a sodium hydroxide supply mechanism, the bottom of the settling zone is provided with a downwards-sunken sediment gathering part, the bottom of the sediment gathering part is provided with a bottom mud discharge port, and the water outlet pipeline is communicated with the upper part of the settling zone, so that the organic matters in the wastewater of the non-ferrous smelting zero-discharge system are efficiently removed.

Description

Technical Field

[0001] The utility model relates to the technical field of wastewater treatment, in particular to an integrated wastewater chromaticity and organic matter removal device. Background Art

[0002] In recent years, the state has tightened the environmental protection requirements for wastewater in the non-ferrous smelting industry, and more and more companies are required to "zero discharge" of industrial wastewater. At present, most companies use the "heavy metal removal + calcium removal + membrane treatment + evaporation crystallization" process to treat production wastewater with "zero discharge". Membrane treatment usually uses the "ultrafiltration + nanofiltration + reverse osmosis" combined membrane process, which is mainly aimed at typical harmful pollutants such as heavy metals and calcium in wastewater in the non-ferrous industry, and lacks oxidation removal technology to remove organic matter. Due to the recycling of wastewater after zero discharge treatment, organic matter gradually enriches in the water system, resulting in serious fouling of the membrane system, increased energy consumption of process operation, and the inability of membrane treatment and evaporation crystallization systems to operate normally and stably. The organic matter in the wastewater system of non-ferrous smelting enterprises mainly comes from the following sources: ① Organic matter such as extractants and surfactants remaining in wet smelting waste liquid, which has the characteristics of complex composition and high organic content. ② Gas washing water, mainly from the washing and cooling process of the gas preparation process, contains a large amount of phenols, tar and suspended matter. ③ The PAM flocculant added to the heavy metal treatment system is mainly used to form easily sedimentable particles in the wastewater through coagulation, adsorption and bridging, and accelerate the precipitation of sediment in the wastewater. PAM is a high molecular polymer with a large molecular weight, stable state, and difficult to decompose naturally. The organic matter in the wastewater is complex and difficult to remove by simple conventional methods. Long-term accumulation affects the reuse of wastewater and the operation of the membrane system.

[0003] Chinese utility model patent CN201811555632.9, a process and device for electrolytic treatment of low-content organic pollutants in high-salinity rare earth hydrometallurgical wastewater, discloses a process and device for electrolytic treatment of organic pollutants in high-salinity rare earth hydrometallurgical wastewater. The patent removes organic pollutants in high-salinity rare earth hydrometallurgical wastewater by degreasing, adjusting pH coagulation and precipitation, electrolysis, adjusting pH coagulation and precipitation, and activated carbon filtration. The process is complicated and mainly removes oily organic matter that is insoluble in water. It is difficult to remove complex high-molecular organic matter in the smelting zero-emission system.

[0004] Chinese utility model patent CN202210211806.X discloses a method for treating non-ferrous metal smelting wastewater. The wastewater is treated by adjusting pH pretreatment + electrochemical oxidation. This method electrochemically oxidizes the Fe and Al ion solution at the anode end to produce easily flocculated iron hydroxide and aluminum hydroxide to remove pollutants, mainly removing heavy metal ions, and has limited effect on the removal of organic matter. Utility Model Content

[0005] The purpose of the utility model is to provide an integrated wastewater chromaticity and organic matter removal device to solve the problems existing in the above-mentioned prior art, solve the difficult problem that the organic matter composition of the wastewater of the non-ferrous smelting zero emission system in the prior art is complex and difficult to remove, and realize the efficient removal of organic matter in the wastewater of the non-ferrous smelting zero emission system.

[0006] To achieve the above-mentioned purpose, the utility model provides the following scheme: The utility model provides an integrated wastewater chromaticity and organic matter removal device, including a device body, the device body includes an inlet pipe, an ozone catalytic oxidation zone, an advanced oxidation zone, a neutralization reaction zone, a precipitation zone and an outlet pipe which are sequentially connected along the flow direction of the wastewater, the inlet pipe is connected with an ozone supply mechanism for supplying ozone thereto, the ozone catalytic oxidation zone is provided with a hydrogen peroxide addition port, the hydrogen peroxide addition port is connected with the hydrogen peroxide supply mechanism, the advanced oxidation zone is provided with a ferrous sulfate addition port, the ferrous sulfate addition port is connected with the ferrous sulfate supply mechanism, the neutralization reaction zone is provided with a sodium hydroxide addition port, the sodium hydroxide addition port is connected with the sodium hydroxide supply mechanism, the bottom of the precipitation zone is provided with a downwardly concave precipitation gathering portion, the bottom of the precipitation gathering portion is provided with a bottom mud discharge port, and the outlet pipe is connected above the precipitation zone.

[0007] Preferably, the ozone supply mechanism includes an ejector and an ozone supply pipe storing ozone gas, the water inlet of the ejector is connected to a connecting pipe connected to the ozone catalytic oxidation zone, the connecting pipe is provided with a booster pump for pumping water toward the ejector, the water outlet of the ejector is connected to the water inlet pipe, and the air intake of the ejector is connected to the ozone supply pipe.

[0008] Preferably, a first partition is provided between the ozone catalytic oxidation zone and the advanced oxidation zone, the first partition extends vertically, and a first channel for wastewater circulation is opened on the top thereof.

[0009] Preferably, the first partition is connected to a second partition, the second partition extends horizontally toward a side away from the advanced oxidation zone and is spaced apart from the top of the ozone catalytic oxidation zone, and a second channel connected to the first channel is opened at a position of the second partition away from the advanced oxidation zone.

[0010] Preferably, the water outlet end of the water inlet pipe is toward and close to the bottom of the ozone catalytic oxidation zone, and close to the first baffle, the hydrogen peroxide addition port is connected to a hydrogen peroxide pipe located in the ozone catalytic oxidation zone, and the outlet of the hydrogen peroxide pipe is close to the water outlet end of the water inlet pipe and is arranged in the same direction as the water outlet end of the water inlet pipe.

[0011] Preferably, a third partition is provided between the advanced oxidation zone and the neutralization reaction zone, the third partition extends vertically and a third channel for wastewater circulation is opened at the bottom thereof, the sodium hydroxide addition port is connected to a sodium hydroxide pipeline located in the neutralization reaction zone, and the outlet of the sodium hydroxide pipeline is arranged close to the outlet of the third channel, a fourth partition is provided between the neutralization reaction zone and the precipitation zone, the fourth partition extends vertically and a fourth channel for wastewater circulation is opened at the top thereof.

[0012] Preferably, a water outlet zone is provided on the side of the sedimentation zone away from the neutralization reaction zone, a fifth partition is provided between the sedimentation zone and the water outlet zone, the fifth partition extends vertically and a fifth channel for wastewater circulation is opened at the bottom thereof, and the top of the water outlet zone is connected to the water outlet pipe.

[0013] Preferably, the advanced oxidation zone and the neutralization reaction zone are both equipped with a stirrer, and the stirrer comprises a rotating shaft rotatably connected to the advanced oxidation zone and the neutralization reaction zone respectively, and the rotating shaft is connected to a stirring blade.

[0014] Preferably, the ferrous sulfate addition port is connected to a ferrous sulfate pipeline located in the advanced oxidation zone, and the outlet of the ferrous sulfate pipeline is arranged close to the outlet of the first channel.

[0015] Preferably, the outlet of the first channel is sealed and connected to the sixth channel, the outlet of the sixth channel is arranged near the bottom of the advanced oxidation zone, the ferrous sulfate addition port is connected to a ferrous sulfate pipeline located in the advanced oxidation zone, the outlet of the ferrous sulfate pipeline is arranged near the outlet of the sixth channel, a sixth partition is provided between the first partition and the third partition, and a seventh channel for the wastewater to pass through is opened on the sixth partition.

[0016] Compared with the prior art, the utility model has achieved the following technical effects:

[0017] The entire device removes organic matter from wastewater through ozone catalytic oxidation, Fenton advanced oxidation and coagulation sedimentation, and the added ferrous sulfate catalyst removes residual ferrous iron and iron ions after the reaction through subsequent coagulation sedimentation. It has the advantages of good decolorization effect, strong oxidation ability and no residue. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0019] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0020] Among them, 1-water inlet pipe, 2-second partition, 3-hydrogen peroxide addition port, 4-ferrous sulfate addition port, 5-agitator, 6-sodium hydroxide addition port, 7-water outlet pipe, 8-water outlet area, 9-fifth partition, 10-sedimentation area, 11-sludge discharge port, 12-fourth partition, 13-neutralization reaction area, 14-third partition, 15-advanced oxidation area, 16-first partition, 17-ozone catalytic oxidation area, 18-boosting pump, 19-ejector, 20-ozone supply pipe. DETAILED DESCRIPTION

[0021] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

[0022] The purpose of the utility model is to provide an integrated wastewater chromaticity and organic matter removal device to solve the problems existing in the above-mentioned prior art, solve the difficult problem that the organic matter composition of the wastewater of the non-ferrous smelting zero emission system in the prior art is complex and difficult to remove, and realize the efficient removal of organic matter in the wastewater of the non-ferrous smelting zero emission system.

[0023] In order to make the above-mentioned purposes, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below in conjunction with the accompanying drawings and specific implementation methods.

[0024] like Figure 1As shown, this embodiment provides an integrated wastewater chromaticity and organic matter removal device, including a device body, the device body includes an inlet pipe 1, an ozone catalytic oxidation zone 17, an advanced oxidation zone 15, a neutralization reaction zone 13, a precipitation zone 10 and a water outlet pipe 7 which are sequentially connected along the flow direction of the wastewater, the water inlet pipe 1 is connected to an ozone supply mechanism for supplying ozone thereto, the ozone catalytic oxidation zone 17 is provided with a hydrogen peroxide addition port 3, the hydrogen peroxide addition port 3 is connected to the hydrogen peroxide supply mechanism, the wastewater is mixed with ozone through the water inlet pipe 1, and hydrogen peroxide is added as a catalyst through the hydrogen peroxide addition port 3, the advanced oxidation zone 15 is provided with a ferrous sulfate addition port 4, the ferrous sulfate addition port 4 is connected to the ferrous sulfate supply mechanism, and the wastewater flows to the high The advanced oxidation zone 15 is provided with ferrous sulfate through the ferrous sulfate feeding port 4 at the same time. The neutralization reaction zone 13 is provided with a sodium hydroxide feeding port 6, and the sodium hydroxide feeding port 6 is connected with a sodium hydroxide supply mechanism. After the wastewater from the advanced oxidation zone 15 enters the neutralization reaction zone 13, sodium hydroxide is added to the neutralization reaction zone 13 through the sodium hydroxide feeding port 6 at the same time. A downwardly concave sedimentation gathering part is provided at the bottom of the sedimentation zone 10, and a bottom mud discharge port 11 is provided at the bottom of the sedimentation gathering part. The wastewater from the neutralization reaction zone 13 flows to the sedimentation zone 10, and the sediment sinks under the action of gravity and gathers in the sedimentation gathering part, and is discharged from the bottom mud discharge port 11. The outlet pipe 7 is connected to the top of the sedimentation zone 10 to discharge the precipitated wastewater from the outlet pipe 7. The entire device removes organic matter from wastewater through ozone catalytic oxidation, Fenton advanced oxidation and coagulation sedimentation, and the added ferrous sulfate catalyst removes residual ferrous iron and iron ions after the reaction through subsequent coagulation sedimentation. It has the advantages of good decolorization effect, strong oxidation ability and no residue.

[0025] As a preferred embodiment of the utility model, the ozone supply mechanism includes an ejector 19 and an ozone supply pipe 20 storing ozone gas, the water inlet of the ejector 19 is connected to a connecting pipe connected to the ozone catalytic oxidation zone 17, and a booster pump 18 for pumping water toward the ejector 19 is provided on the connecting pipe, the water outlet of the ejector 19 is connected to the water inlet pipe 1, and the air intake of the ejector 19 is connected to the ozone supply pipe 20. The booster pump 18 extracts part of the water in the ozone catalytic oxidation zone 17, pumps it into the ejector 19 to absorb ozone, and then flows into the water inlet pipe 1 so that the ozone and wastewater are fully mixed.

[0026] Furthermore, a first partition 16 is provided between the ozone catalytic oxidation zone 17 and the advanced oxidation zone 15. The first partition 16 extends vertically, and a first channel for wastewater circulation is provided on the top thereof, wherein the first channel is preferably the interval between the first partition 16 and the top of the ozone catalytic oxidation zone 17. By providing the first partition 16, it is convenient to set the outlet end of the water inlet pipe 1 at the bottom of the ozone catalytic oxidation zone 17, so that the wastewater flows upward from the bottom of the ozone catalytic oxidation zone 17 until it overflows out of the ozone catalytic oxidation zone 17 through the first channel and enters the advanced oxidation zone 15, which can increase the reaction time of ozone catalytic oxidation.

[0027] As a preferred embodiment of the utility model, the first partition 16 is connected to the second partition 2, the second partition 2 extends horizontally toward the side away from the advanced oxidation zone 15, and is spaced apart from the top of the ozone catalytic oxidation zone 17. The second partition 2 is provided with a second channel connected to the first channel at a position away from the advanced oxidation zone 15, wherein the preferred second channel is the interval between the second partition 2 and the side wall of the ozone catalytic oxidation zone 17. By providing the second partition 2, it is convenient to set the outlet end of the water inlet pipe 1 close to the first partition 16, so that the wastewater flows from the side of the ozone catalytic oxidation zone 17 close to the advanced oxidation zone 15 to the other side, further increasing the reaction time of the ozone catalytic oxidation.

[0028] Furthermore, the water outlet end of the water inlet pipe 1 is oriented toward and close to the bottom of the ozone catalytic oxidation zone 17, and close to the first partition 16. The hydrogen peroxide addition port 3 is connected to a hydrogen peroxide pipe located in the ozone catalytic oxidation zone 17. The outlet of the hydrogen peroxide pipe is close to the water outlet end of the water inlet pipe 1 and is arranged in the same direction as the water outlet end, so that the depth of the hydrogen peroxide pipe outlet is consistent with the depth of the water outlet end of the water inlet pipe 1, thereby ensuring the best mixing effect of hydrogen peroxide and wastewater inlet.

[0029] As a preferred embodiment of the utility model, a third partition 14 is provided between the advanced oxidation zone 15 and the neutralization reaction zone 13. The third partition 14 extends vertically and has a third channel for wastewater circulation at its bottom. The preferred third channel is the interval between the third partition 14 and the bottom of the advanced oxidation zone 15. The sodium hydroxide addition port 6 is connected to a sodium hydroxide pipeline located in the neutralization reaction zone 13. The outlet of the sodium hydroxide pipeline is arranged close to the outlet of the third channel. A fourth partition 12 is provided between the neutralization reaction zone 13 and the precipitation zone 10. The fourth partition 12 extends vertically and has a fourth channel for wastewater circulation at its top. The preferred fourth channel is the interval between the fourth partition 12 and the top of the neutralization reaction zone 13. The wastewater from the advanced oxidation zone 15 enters the neutralization reaction zone 13 through the third channel, and sodium hydroxide is added to the neutralization reaction zone 13 through the outlet of the sodium hydroxide pipeline. The outlet depth of the sodium hydroxide pipeline is consistent with the depth of the third channel, ensuring the best mixing effect of sodium hydroxide and wastewater inflow. And because the fourth channel is located at the top, the wastewater is mixed with sodium hydroxide and then overflows from the top to the neutralization reaction zone 13, thereby increasing the reaction time.

[0030] Preferably, a water outlet zone 8 is provided on the side of the sedimentation zone 10 away from the neutralization reaction zone 13, and a fifth partition plate 9 is provided between the sedimentation zone 10 and the water outlet zone 8. The fifth partition plate 9 extends vertically and a fifth channel for wastewater circulation is opened at the bottom thereof. The top of the water outlet zone 8 is connected with the water outlet pipe 7. The wastewater flows to the water outlet zone 8 through the fifth channel, and then flows upward until it overflows from the water outlet pipe 7, so as to fully ensure the sedimentation time of the wastewater.

[0031] Furthermore, both the advanced oxidation zone 15 and the neutralization reaction zone 13 are equipped with a stirrer 5, which includes a rotating shaft rotatably connected to the advanced oxidation zone 15 and the neutralization reaction zone 13, respectively, and a stirring blade is connected to the rotating shaft to ensure sufficient mixing of the reagent and the wastewater.

[0032] As a preferred embodiment of the utility model, the ferrous sulfate addition port 4 is connected to a ferrous sulfate pipeline located in the advanced oxidation zone 15, and the outlet of the ferrous sulfate pipeline is arranged close to the outlet of the first channel. The wastewater overflows to the advanced oxidation zone 15 through the first channel. At the same time, ferrous sulfate is added through the ferrous sulfate addition port 4 and the ferrous sulfate pipeline. The outlet depth of the ferrous sulfate pipeline is consistent with the depth of the water outlet end of the first channel, which can ensure that the ferrous sulfate is mixed with the wastewater entering the advanced oxidation zone 15 as soon as possible.

[0033] As another preferred embodiment of the utility model, the outlet of the first channel is sealed and connected with the sixth channel, the sixth channel is a pipeline structure, and its water inlet section is adapted to the outlet structure of the first channel. The outlet of the sixth channel is arranged near the bottom of the advanced oxidation zone 15, and the ferrous sulfate addition port 4 is connected with the ferrous sulfate pipeline located in the advanced oxidation zone 15, and the outlet of the ferrous sulfate pipeline is arranged near the outlet of the sixth channel. A sixth partition is provided between the first partition 16 and the third partition 14, and a seventh channel for wastewater to pass through is provided on the sixth partition. The preferred seventh channel is the interval between the sixth partition and the bottom of the advanced oxidation zone 15, so that the wastewater first flows to the bottom of the advanced oxidation zone 15 through the sixth channel, and then overflows through the seventh channel, and then flows downward and flows into the third channel to fully extend the reaction time of ferrous sulfate and wastewater. And the stirring blades in the advanced oxidation zone 15 are located between the sixth partition and the first partition 16.

[0034] When implementing:

[0035] For example, if the COD in the wastewater is 350mg / L, then the ozone dosage is 420mg / L (the ozone dosage is ozone: COD mass ratio = 1.2:1), the residence time in the ozone reaction tower is 45min, the hydrogen peroxide dosage in the ozone oxidation tower is 252mg / L (hydrogen peroxide: ozone mass ratio = 0.6:1), and the COD of the effluent after the reaction is 165mg / L. The ferrous sulfate configuration concentration is 10%, the dosage is 100.8mg / L (hydrogen peroxide: ferrous sulfate mass ratio = 2.5:1), the residence time in the catalytic oxidation tower is 60min, and 4% sodium hydroxide is added to control the neutralization reaction pH to 8. The COD of the effluent from the neutralization sedimentation tank is 45mg / L, and the COD removal effect is obvious.

[0036] For example, the COD in the wastewater is 500 mg / L, the ozone dosage is 750 mg / L (the ozone dosage is ozone: COD mass ratio = 1.5:1), the residence time in the ozone reaction tower is 30 minutes, the hydrogen peroxide dosage in the ozone oxidation tower is 450 mg / L (hydrogen peroxide: ozone mass ratio = 0.6:1), and the COD of the effluent after the reaction is 210 mg / L. The ferrous sulfate concentration is 10%, the dosage is 70 mg / L (hydrogen peroxide: ferrous sulfate mass ratio = 3:1), the residence time in the catalytic oxidation tower is 60 minutes, 4% sodium hydroxide is added to control the neutralization reaction pH to 8.5, and the COD of the effluent from the neutralization sedimentation tank is 30 mg / L.

[0037] Both embodiments can ensure sufficient reaction in the entire device body without causing excessive dosage of various drugs.

[0038] Adaptive changes made according to actual needs are all within the protection scope of this utility model.

[0039] It should be noted that it is obvious to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or basic features of the present invention. Therefore, no matter from which point of view, the embodiments should be regarded as exemplary and non-restrictive, and the scope of the present invention is defined by the appended claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims are included in the present invention. Any reference numerals in the claims should not be regarded as limiting the claims involved.

[0040] The present invention uses specific examples to illustrate the principle and implementation of the present invention. The above examples are only used to help understand the method and core idea of ​​the present invention. At the same time, for those skilled in the art, according to the idea of ​​the present invention, there will be changes in the specific implementation and application scope. In summary, the content of this specification should not be understood as limiting the present invention.

Claims

1. An integrated wastewater chromaticity and organic matter removal device, characterized in that: The device body comprises a water inlet pipe, an ozone catalytic oxidation zone, an advanced oxidation zone, a neutralization reaction zone, a precipitation zone and a water outlet pipe which are sequentially connected along the flow direction of the wastewater, the water inlet pipe is connected with an ozone supply mechanism for supplying ozone thereto, the ozone catalytic oxidation zone is provided with a hydrogen peroxide injection port, the hydrogen peroxide injection port is connected with the hydrogen peroxide supply mechanism, the advanced oxidation zone is provided with a ferrous sulfate injection port, the ferrous sulfate injection port is connected with the ferrous sulfate supply mechanism, the neutralization reaction zone is provided with a sodium hydroxide injection port, the sodium hydroxide injection port is connected with the sodium hydroxide supply mechanism, the bottom of the precipitation zone is provided with a downwardly concave precipitation gathering portion, the bottom of the precipitation gathering portion is provided with a bottom mud discharge port, and the water outlet pipe is connected with the top of the precipitation zone.

2. The integrated wastewater chromaticity and organic matter removal device according to claim 1 is characterized in that: The ozone supply mechanism includes an ejector and an ozone supply pipe storing ozone gas, the water inlet of the ejector is connected to a connecting pipe connected to the ozone catalytic oxidation zone, the connecting pipe is provided with a booster pump for pumping water toward the ejector, the water outlet of the ejector is connected to the water inlet pipe, and the air intake of the ejector is connected to the ozone supply pipe.

3. The integrated wastewater chromaticity and organic matter removal device according to claim 1 or 2, characterized in that: A first partition is arranged between the ozone catalytic oxidation zone and the advanced oxidation zone. The first partition extends vertically and a first channel for wastewater to flow is opened on the top.

4. The integrated wastewater chromaticity and organic matter removal device according to claim 3 is characterized in that: The first partition is connected to a second partition, which extends horizontally toward a side away from the advanced oxidation zone and is spaced apart from the top of the ozone catalytic oxidation zone. A second channel connected to the first channel is opened at a position of the second partition away from the advanced oxidation zone.

5. The integrated wastewater chromaticity and organic matter removal device according to claim 4 is characterized in that: The water outlet end of the water inlet pipe faces and is close to the bottom of the ozone catalytic oxidation zone, and is close to the first partition. The hydrogen peroxide addition port is connected to a hydrogen peroxide pipe located in the ozone catalytic oxidation zone, and the outlet of the hydrogen peroxide pipe is close to the water outlet end of the water inlet pipe and is arranged in the same direction as the water outlet end of the water inlet pipe.

6. The integrated wastewater chromaticity and organic matter removal device according to claim 5, characterized in that: A third partition is provided between the advanced oxidation zone and the neutralization reaction zone, the third partition extends vertically and a third channel for wastewater circulation is provided at the bottom thereof, the sodium hydroxide addition port is connected to a sodium hydroxide pipeline located in the neutralization reaction zone, and an outlet of the sodium hydroxide pipeline is arranged close to an outlet of the third channel, a fourth partition is provided between the neutralization reaction zone and the precipitation zone, the fourth partition extends vertically and a fourth channel for wastewater circulation is provided at the top thereof.

7. The integrated wastewater chromaticity and organic matter removal device according to claim 6, characterized in that: A water outlet zone is provided on the side of the precipitation zone away from the neutralization reaction zone, a fifth partition is provided between the precipitation zone and the water outlet zone, the fifth partition extends vertically and a fifth channel for wastewater circulation is opened at the bottom thereof, and the top of the water outlet zone is connected to the water outlet pipe.

8. The integrated wastewater chromaticity and organic matter removal device according to claim 7, characterized in that: The advanced oxidation zone and the neutralization reaction zone are both equipped with a stirrer, and the stirrer comprises a rotating shaft rotatably connected to the advanced oxidation zone and the neutralization reaction zone respectively, and the rotating shaft is connected with a stirring blade.

9. The integrated wastewater chromaticity and organic matter removal device according to claim 8, characterized in that: The ferrous sulfate addition port is connected to a ferrous sulfate pipeline located in the advanced oxidation zone, and the outlet of the ferrous sulfate pipeline is arranged close to the outlet of the first channel.

10. The integrated wastewater chromaticity and organic matter removal device according to claim 8, characterized in that: The outlet of the first channel is sealed and connected to the sixth channel, and the outlet of the sixth channel is arranged near the bottom of the advanced oxidation zone. The ferrous sulfate addition port is connected to a ferrous sulfate pipeline located in the advanced oxidation zone, and the outlet of the ferrous sulfate pipeline is arranged near the outlet of the sixth channel. A sixth partition is arranged between the first partition and the third partition, and a seventh channel for the wastewater to pass through is opened on the sixth partition.

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