CN112979071A

CN112979071A - Industrial wastewater treatment standard-reaching direct-discharge system and process method

Info

Publication number: CN112979071A
Application number: CN202110206697.8A
Authority: CN
Inventors: 宋金成; 虞彤; 赵方金; 乌力更
Original assignee: Beijing Qiyuan Huitong Water Technology Co ltd
Current assignee: Beijing Qiyuan Huitong Water Technology Co ltd
Priority date: 2021-02-24
Filing date: 2021-02-24
Publication date: 2021-06-18

Abstract

The invention provides a standard-reaching direct-discharging system and a process method for industrial wastewater treatment. Wherein, the system of directly discharging up to standard of industrial waste water treatment includes: a gravity oil remover; a regulating tank; an air flotation oil remover; the system comprises an activated sludge pretreatment biochemical system, a sewage treatment system and a sewage treatment system, wherein the activated sludge pretreatment biochemical system is used for pretreating the wastewater; the primary A-O biochemical treatment system is used for carrying out primary A-O biochemical treatment on the pretreated wastewater; the secondary A-O biochemical treatment system carries out secondary A-O biochemical treatment on the wastewater after the primary A-O biochemical treatment; the chemical coagulating sedimentation system is used for carrying out chemical coagulating sedimentation treatment on the wastewater after the secondary A-O biochemical treatment; the electromagnetic strong oxidation advanced treatment system carries out electromagnetic strong oxidation advanced treatment on the wastewater after chemical coagulation and precipitation treatment. The invention solves the problem that the industrial wastewater treatment process in the prior art can not meet the requirement of direct discharge standard.

Description

Industrial wastewater treatment standard-reaching direct-discharge system and process method

Technical Field

The invention relates to the technical field of industrial wastewater treatment, in particular to a standard-reaching direct-discharging system and a process method for industrial wastewater treatment.

Background

Industrial wastewater has the characteristics of large water quality change, poor biodegradability, difficult degradation, complex and various pollutants and the like, generally, according to the actual wastewater quality, a proper pretreatment method, such as flocculation, micro electricity, adsorption, photocatalysis and other processes are adopted to destroy organic matters difficult to degrade in the wastewater and improve the biodegradability of the wastewater, then, biological methods, such as ABR, SBR, A-O and other processes are combined to treat the industrial wastewater, and the common advanced treatment process of the coking wastewater mainly comprises two types: the first is physical adsorption method, including biological fluidized bed technology and active carbon adsorption regeneration technology, and the second is chemical oxidation method, Fenton (Fenton reagent) catalytic oxidation method, ozone oxidation method, electrolytic multi-element catalysis method, etc. The current research on the industrial wastewater treatment process tends to adopt a combined process of a plurality of methods.

However, the advanced treatment of the coking wastewater by adopting the combined process is still difficult to stably meet the requirements of the discharge standard of pollutants for coking chemical industry (GB16171-2012) special discharge limit value table 3 direct discharge standard.

Disclosure of Invention

The invention mainly aims to provide a standard-reaching direct-discharging system and a process method for industrial wastewater treatment, so as to solve the problem that the industrial wastewater treatment process in the prior art cannot meet the requirement of direct discharge standard.

In order to achieve the above objects, according to one aspect of the present invention, there is provided an industrial wastewater treatment standard direct discharge system comprising: the gravity oil remover can remove part of oil condensate and floating oil in the wastewater; the adjusting tank is communicated with the gravity oil remover and can be used for quenching and tempering and mixing the wastewater; the air floatation oil remover is communicated with the regulating tank and can remove oil in the wastewater; the activated sludge pretreatment biochemical system is communicated with the air floatation oil remover and is used for pretreating the wastewater from the air floatation oil remover; the primary A-O biochemical treatment system is communicated with the activated sludge pretreatment biochemical system and carries out primary A-O biochemical treatment on the pretreated wastewater; the secondary A-O biochemical treatment system is communicated with the primary A-O biochemical treatment system and carries out secondary A-O biochemical treatment on the wastewater after the primary A-O biochemical treatment; the chemical coagulating sedimentation system is communicated with the second-stage A-O biochemical treatment system and is used for carrying out chemical coagulating sedimentation treatment on the wastewater after the second-stage A-O biochemical treatment; the electromagnetic strong oxidation advanced treatment system is communicated with the chemical coagulating sedimentation system and carries out electromagnetic strong oxidation advanced treatment on the wastewater after the chemical coagulating sedimentation treatment.

Furthermore, an adjusting submersible stirrer is arranged in the adjusting tank, and the adjusting submersible stirrer is used for conditioning and mixing the wastewater in the adjusting tank.

Further, the activated sludge pretreatment biochemical system comprises: the aeration tank is communicated with the air floatation oil remover, and a pretreatment aerator is arranged in the aeration tank to carry out aeration treatment on the wastewater in the aeration tank; the sedimentation tank is communicated with the aeration tank, solid-liquid separation is carried out on the wastewater from the aeration tank, and the supernatant obtained by the separation flows into the primary A-O biochemical treatment system; and the pretreatment return pipeline is communicated with the sedimentation tank and the aeration tank, and at least part of sludge in the sedimentation tank flows back to the aeration tank through the pretreatment return pipeline.

Further, the sludge reflux ratio of the pretreatment reflux pipeline is 100%.

Further, still be provided with the fan that is used for the air feed in the aeration tank, be used for detecting dissolved oxygen detecting instrument, the PH detector that is used for detecting the PH value, be used for the temperature-detecting appearance of temperature.

Furthermore, the bottom of the sedimentation tank is provided with a conical structure, and the pretreatment return pipeline is communicated with the bottom of the sedimentation tank.

Further, be provided with elevator pump and defoaming pump in the sedimentation tank, elevator pump drive mud gets into the preliminary treatment return line and flows back to the aeration tank in, and the defoaming pump can spray the defoaming.

Further, the primary A-O biochemical treatment system comprises: the primary facultative tank is communicated with the activated sludge pretreatment biochemical system and is used for carrying out denitrification treatment on the pretreated wastewater; the primary aerobic tank is communicated with the primary facultative tank, and a primary aerator is arranged in the primary aerobic tank; the primary nitrification liquid return pipeline is communicated with the primary facultative tank and the primary aerobic tank, and the nitrification liquid in the primary aerobic tank flows back to the primary facultative tank through the primary nitrification liquid return pipeline; the primary sedimentation tank is communicated with the primary aerobic tank and is used for carrying out sedimentation separation on the wastewater from the primary aerobic tank; the primary sludge return pipeline is communicated with the primary sedimentation tank and the primary facultative tank, and sludge in the primary sedimentation tank flows back to the primary facultative tank through the primary sludge return pipeline; and the middle water tank is communicated with the primary sedimentation tank, and supernatant separated from the primary sedimentation tank enters the middle water tank.

Furthermore, the nitrifying liquid reflux ratio of the primary nitrifying liquid reflux pipeline is 300%, and the sludge reflux ratio of the primary sludge reflux pipeline is 100%.

Further, a fan for supplying air, a dissolved oxygen detection instrument for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value and a temperature detector for detecting the temperature are arranged in the primary aerobic tank, the PH value in the primary aerobic tank is 7.5-8.5, the dissolved oxygen is below 0.5mg/L, and the temperature is 30-40 ℃.

Furthermore, a mud scraper and a lifting pump are arranged in the primary sedimentation tank, the bottom of the primary sedimentation tank is provided with a conical structure, the mud scraper concentrates the mud in the conical structure, a primary sludge return pipeline is communicated with the bottom of the primary sedimentation tank, and the lifting pump drives the mud to enter the primary sludge return pipeline and return to the primary facultative tank.

Further, a defoaming pump for spraying defoaming is arranged in the middle water tank.

Further, the secondary A-O biochemical treatment system comprises: the secondary facultative tank is communicated with the primary A-O biochemical treatment system and is used for carrying out denitrification treatment on the wastewater subjected to the primary A-O biochemical treatment; the secondary aerobic tank is communicated with the secondary facultative tank, and a secondary aerator is arranged in the secondary aerobic tank; the secondary sedimentation tank is communicated with the secondary aerobic tank and is used for carrying out sedimentation separation on the wastewater from the secondary aerobic tank; and the secondary sludge return pipeline is communicated with the secondary sedimentation tank and the secondary facultative tank, and sludge in the secondary sedimentation tank flows back to the secondary facultative tank through the secondary sludge return pipeline.

Further, the sludge reflux ratio of the secondary sludge reflux pipeline is 100%.

Further, a fan for supplying air, a dissolved oxygen detection instrument for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value and a temperature detector for detecting the temperature are arranged in the secondary aerobic tank, the PH value in the secondary aerobic tank is 7.5-8.5, the dissolved oxygen is below 0.5mg/L, and the temperature is 30-40 ℃.

Furthermore, a lifting pump is arranged in the secondary sedimentation tank, the bottom of the secondary sedimentation tank is provided with a conical structure, a secondary sludge return pipeline is communicated with the bottom of the secondary sedimentation tank, and the lifting pump drives sludge to enter the secondary sludge return pipeline and return to the secondary facultative tank.

Further, the chemical coagulation sedimentation system comprises: the coagulating sedimentation equipment is communicated with the secondary A-O biochemical treatment system, and the wastewater after the secondary A-O biochemical treatment and the FeSO in the coagulating sedimentation equipment₄、H₂O₂CaO mixing reaction, and a mechanical stirring device, an aeration stirring device and a PH detector are arranged in the coagulating sedimentation equipmentTable; the mixed reaction tank is communicated with the coagulating sedimentation equipment, the wastewater treated by the coagulating sedimentation equipment enters the mixed reaction tank, and a stirring device and an aeration stirring device are arranged in the mixed reaction tank; the coagulating sedimentation tank is communicated with the mixing reaction tank and is used for precipitating and separating the wastewater from the mixing reaction tank, a mud scraper and a lifting pump are arranged in the coagulating sedimentation tank, and the sludge at the bottom enters a sludge concentration tank through the lifting pump; the air flotation coagulating sedimentation equipment, air flotation coagulating sedimentation equipment and coagulating sedimentation tank intercommunication, during the supernatant fluid after the coagulating sedimentation tank separation got into air flotation coagulating sedimentation equipment, be provided with circulating water pump in the air flotation coagulating sedimentation equipment and scrape the sediment machine, oil material and the suspended solid in the waste water scraped the sediment machine and got into the scum groove and get into crude benzol recovery system, and the supernatant fluid gets into the strong oxidation deep treatment system of electromagnetism.

Further, the electromagnetic strong oxidation advanced treatment system comprises an acid regulation dosing tank, an electromagnetic strong oxidation system, an advanced reaction system, a neutralization flocculation device, a final sedimentation tank and a sand filter which are sequentially communicated.

According to another aspect of the invention, the industrial wastewater treatment standard-reaching direct-discharge process method is provided, and by adopting the industrial wastewater treatment standard-reaching direct-discharge system, the industrial wastewater treatment standard-reaching direct-discharge process method comprises the following steps: after the wastewater is subjected to heat collection and simultaneous temperature reduction pretreatment by a heat exchanger, the wastewater enters a gravity oil remover, the retention time of the wastewater in the gravity oil remover is more than or equal to 5 hours, oil condensate and floating oil with high density are removed by gravity oil removal, and supernatant flows into a regulating tank; the adjusting tank fully adjusts and mixes the wastewater, and the retention time of the wastewater in the adjusting tank is more than or equal to 24 hours; conveying the wastewater flowing out of the regulating tank to an air flotation oil remover, wherein the retention time of the wastewater in the air flotation oil remover is more than or equal to 1.5 hours, adding an aluminum sulfate coagulant and a polyacrylamide coagulant aid into the air flotation oil remover, floating and condensing more than 95% of oil of floating oil, emulsified oil, dissolved oil and dispersed oil in the wastewater, performing solid-liquid separation through a slag scraper arranged on the air flotation oil remover, and collecting and recycling scum; the wastewater treated by the air floatation oil remover automatically flows into an activated sludge pretreatment biochemical system, aeration and sedimentation are carried out in the activated sludge pretreatment biochemical system, and the treated supernatant flows into a primary A-O biochemical treatment system; the wastewater treated by the activated sludge pretreatment biochemical system automatically flows into a primary A-O biochemical treatment system, anaerobic and aerobic treatment is carried out in the primary A-O biochemical treatment system, and the treated supernatant flows into a secondary A-O biochemical treatment system; the wastewater treated by the primary A-O biochemical treatment system automatically flows into a secondary A-O biochemical treatment system, anaerobic and aerobic treatment is carried out in the secondary A-O biochemical treatment system, and the treated supernatant flows into a chemical coagulating sedimentation system; the wastewater treated by the secondary A-O biochemical treatment system automatically flows into a chemical coagulating sedimentation system, chemical coagulating sedimentation treatment is carried out in the chemical coagulating sedimentation system, and the treated supernatant flows into an electromagnetic strong oxidation advanced treatment system; the wastewater treated by the chemical coagulation sedimentation system automatically flows into an electromagnetic strong oxidation advanced treatment system, the electromagnetic strong oxidation advanced treatment is carried out in the electromagnetic strong oxidation advanced treatment system, the treated sludge enters a sludge treatment system, and finally the effluent reaches the requirement of direct discharge standard.

Further, in an activated sludge pretreatment biochemical system, the wastewater treated by the air floatation oil remover flows automatically and is mixed with the return sludge of the sedimentation tank and then flows into the foremost end of the aeration tank, and the retention time of the mixed liquid in the aeration tank is more than or equal to 13 hours; the mixed liquid in the aeration tank automatically flows into a sedimentation tank for mud-water separation, the retention time of the wastewater in the sedimentation tank is more than or equal to 6.5 hours, the activated sludge in the conical structure at the bottom of the sedimentation tank flows back to the foremost end of the aeration tank through a lift pump, and the supernatant of the sedimentation tank automatically flows into a first-level A-O biochemical treatment system.

Further, the concentration of dissolved oxygen in the aeration tank is 0.5mg/L, and the online monitoring is carried out through a dissolved oxygen detection instrument, the PH in the aeration tank is 7.5, the temperature is 30 ℃, and the supernatant in the sedimentation tank is sprayed and defoamed on the foam generated in the aeration tank through a defoaming pump.

Furthermore, in the primary A-O biochemical treatment system, effluent of the biochemical system is pretreated by activated sludge, return sludge of the primary sedimentation tank and return nitrifying liquid of the primary aerobic tank are mixed and then flow into the foremost end of the primary facultative tank, the retention time of the mixed liquid in the primary facultative tank is more than or equal to 36 hours, nitrifying bacteria carried by the nitrifying liquid ammoniate ammonia nitrogen and organic nitrogen in the wastewater into ammonia nitrogen, and the ammonia nitrogen is converted into nitrate through biological nitrification, and in an anoxic section, the nitrate brought by the return nitrifying liquid is converted into nitrogen through biological denitrification by the denitrifying bacteria; effluent of the primary facultative tank automatically flows into the primary aerobic tank, the retention time of wastewater in the primary aerobic tank is more than or equal to 100 hours, and nitrified liquid at the tail end of the primary aerobic tank flows back to the foremost end of the primary facultative tank; the mixed liquid of the first-stage aerobic tank automatically flows to a first-stage sedimentation tank for mud-water separation, the retention time of the wastewater in the first-stage sedimentation tank is more than or equal to 7.6 hours, a mud scraper in the first-stage sedimentation tank collects activated sludge and concentrates the activated sludge in a conical structure at the bottom of the first-stage sedimentation tank, the activated sludge in the conical structure flows back to the foremost end of the first-stage facultative tank through a lifting pump, and the supernatant of the first-stage sedimentation tank automatically flows into a middle water tank; supernatant in the first-stage sedimentation tank automatically flows into an intermediate water tank, the retention time of wastewater in the intermediate water tank is more than or equal to 2 hours, the supernatant in the intermediate water tank sprays and clears up foam generated by aeration in the first-stage aerobic tank through a defoaming pump, and water in the intermediate water tank enters a second-stage A-O biochemical treatment system through a lifting pump.

Further, in the secondary A-O biochemical treatment system, the effluent of the primary A-O biochemical treatment system is mixed with the return sludge of the secondary sedimentation tank and then automatically flows into the secondary facultative tank, the retention time of the mixed liquid in the secondary facultative tank is more than or equal to 36 hours, and the mixed liquid is stirred by a submersible stirrer; the effluent of the secondary facultative tank automatically flows into a secondary aerobic tank, and the retention time of the wastewater in the secondary aerobic tank is more than or equal to 18 hours; the mixed liquid of the second-stage aerobic pool automatically flows to the second-stage sedimentation pool to carry out mud-water separation, the retention time of the mixed liquid in the second-stage sedimentation pool is more than or equal to 9 hours, sludge is deposited in a conical structure at the bottom of the second-stage sedimentation pool and flows back to the front end of the second-stage facultative aerobic pool through a lifting pump, meanwhile, the supernatant in the second-stage sedimentation pool is sprayed and digested on foam generated in the second-stage aerobic pool through a defoaming pump, and the supernatant in the second-stage sedimentation pool automatically flows into a chemical coagulation sedimentation system.

Further, in the chemical coagulating sedimentation system, the effluent of the secondary A-O biochemical treatment system automatically flows into coagulating sedimentation equipment and is added at the same timeFeSO₄、H₂O₂CaO, the retention time of the wastewater in the coagulating sedimentation equipment is more than or equal to 0.5 hour; enabling effluent of the coagulating sedimentation equipment to automatically flow into a mixing reaction tank, enabling the retention time of the mixed liquid in the mixing reaction tank to be more than or equal to 0.5 hour, adding polyacrylamide into the mixing reaction tank, stirring by using a stirring device and an aeration stirring device, and enabling the treated mixed liquid to automatically flow into the coagulating sedimentation tank; the mixed liquid from the mixing reaction tank is statically precipitated for more than or equal to 8 hours in a coagulating sedimentation tank, sludge in the coagulating sedimentation tank is concentrated by an arranged sludge scraper and enters a sludge concentration tank through a lifting pump, and supernatant automatically flows into air floatation coagulating sedimentation equipment; the supernatant from the coagulating sedimentation tank stays in the air-flotation coagulating sedimentation equipment for more than or equal to 1.5 hours, oil substances and suspended matters in the wastewater float upwards in the equipment, are scraped into a scum trough through a scum scraper and enter a crude benzene recovery system, and the supernatant enters an electromagnetic strong oxidation advanced treatment system.

Further, in the electromagnetic strong oxidation advanced treatment system, the supernatant of the chemical coagulation sedimentation system passes through a regulating tank and then enters the electromagnetic strong oxidation system and the advanced reaction system, the supernatant stays for more than or equal to 1.8 hours, then the supernatant enters a neutralization flocculation device, a final sedimentation tank and a sand filter for solid-liquid separation, the produced sludge enters a sludge treatment system, and the produced supernatant can be directly discharged.

By applying the technical scheme of the invention, the coking wastewater is pretreated firstly, namely is mechanically and physically treated by the gravity oil remover, the regulating reservoir and the air flotation oil remover, and then is biochemically treated, namely is subjected to chemical coagulating sedimentation treatment and electromagnetic strong oxidation advanced treatment by the activated sludge pretreatment biochemical system, the primary A-O biochemical treatment system and the secondary A-O biochemical treatment system, so that the treated wastewater meets the discharge standard. The setting mode has reasonable process composition and clear and concise route, combines biochemical treatment and physicochemical treatment orderly and organically, and optimally combines and supports each main body unit. By adopting the system and the process method of the embodiment, the removal rate of the integral COD is more than or equal to 98 percent, the removal rate of organic characteristic pollutants is more than or equal to 98 percent, the removal rate of refractory components such as benzopyrene, cyanide, polycyclic aromatic hydrocarbon and the like is far greater than the three-emission limit value, and individual indexes cannot be detected, so that the high-efficiency recycling of refractory industrial wastewater such as coking wastewater and the like becomes practical, and a technical and process basis is provided for the high-efficiency recycling, energy conservation and emission reduction; the operation management is convenient; the process is stable; the investment and operation cost is low; the method overcomes the problem of high treatment cost of the highly-refractory organic pollutants, breaks through the technical and technological bottlenecks which cannot be solved by the highly-refractory organic pollutants, and has remarkable social, economic and environmental benefits.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:

FIG. 1 shows a schematic diagram of the industrial wastewater treatment standard direct discharge system of the present invention.

Wherein the figures include the following reference numerals:

10. a gravity oil remover; 20. a regulating tank; 30. an air flotation oil remover; 40. an activated sludge pretreatment biochemical system; 41. an aeration tank; 42. a sedimentation tank; 43. pre-treating a return pipeline; 50. a primary A-O biochemical treatment system; 51. a first-stage facultative tank; 52. a primary aerobic tank; 53. a first-stage nitration liquid return pipeline; 54. a primary sedimentation tank; 55. a primary sludge return line; 56. a middle water tank; 60. a secondary A-O biochemical treatment system; 61. a secondary facultative tank; 62. a secondary aerobic tank; 63. a secondary sedimentation tank; 64. a secondary sludge return line; 70. a chemical coagulation sedimentation system; 71. coagulating sedimentation equipment; 72. a mixing reaction tank; 73. a coagulating sedimentation tank; 74. air flotation coagulating sedimentation equipment; 80. an electromagnetic strong oxidation advanced treatment system; 81. an acid regulation dosing tank; 82. an electromagnetic strong oxidation system; 83. a deep reaction system; 84. a neutralization flocculation device; 85. a final sedimentation tank; 86. a sand filter; 90. a heat exchanger.

Detailed Description

It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.

It is noted that, unless otherwise indicated, 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.

In the present invention, unless specified to the contrary, use of the terms of orientation such as "upper, lower, top, bottom" or the like, generally refer to the orientation as shown in the drawings, or to the component itself in a vertical, perpendicular, or gravitational orientation; likewise, for ease of understanding and description, "inner and outer" refer to the inner and outer relative to the profile of the components themselves, but the above directional words are not intended to limit the invention.

In order to solve the problem that the industrial wastewater treatment process in the prior art cannot meet the requirement of the direct discharge standard, the invention provides a standard-reaching direct discharge system and a process method for industrial wastewater treatment.

As shown in FIG. 1, the industrial wastewater treatment standard-reaching direct discharging system comprises a gravity oil remover 10, a regulating tank 20, an air flotation oil remover 30, an activated sludge pretreatment biochemical system 40, a primary A-O biochemical treatment system 50, a secondary A-O biochemical treatment system 60, a chemical coagulation sedimentation system 70 and an electromagnetic strong oxidation advanced treatment system 80, wherein the gravity oil remover 10 can remove part of oil condensate and floating oil in wastewater; the regulating tank 20 is communicated with the gravity oil remover 10 and can be used for quenching and tempering and mixing the wastewater; the air floatation oil remover 30 is communicated with the regulating tank 20, and the air floatation oil remover 30 can remove oil in the wastewater; the activated sludge pretreatment biochemical system 40 is communicated with the air floatation oil remover 30 and is used for pretreating the wastewater from the air floatation oil remover 30; the primary A-O biochemical treatment system 50 is communicated with the activated sludge pretreatment biochemical system 40, and primary A-O biochemical treatment is carried out on the pretreated wastewater; the secondary A-O biochemical treatment system 60 is communicated with the primary A-O biochemical treatment system 50, and carries out secondary A-O biochemical treatment on the wastewater after the primary A-O biochemical treatment; the chemical coagulating sedimentation system 70 is communicated with the secondary A-O biochemical treatment system 60, and the wastewater after the secondary A-O biochemical treatment is subjected to chemical coagulating sedimentation treatment; the electromagnetic strong oxidation advanced treatment system 80 is communicated with the chemical coagulating sedimentation system 70, and carries out electromagnetic strong oxidation advanced treatment on the wastewater after the chemical coagulating sedimentation treatment.

In the embodiment, the coking wastewater is pretreated firstly, namely mechanically and physically treated by the gravity oil remover 10, the regulating tank 20 and the air flotation oil remover 30, and then biochemically treated, namely treated by the activated sludge pretreatment biochemical system 40, the primary A-O biochemical treatment system 50 and the secondary A-O biochemical treatment system 60, and then subjected to chemical coagulation sedimentation treatment and electromagnetic strong oxidation advanced treatment, so that the treated wastewater meets the discharge standard. The setting mode has reasonable process composition and clear and concise route, combines biochemical treatment and physicochemical treatment orderly and organically, and optimally combines and supports each main body unit. By adopting the system and the process method of the embodiment, the removal rate of the integral COD is more than or equal to 98 percent, the removal rate of organic characteristic pollutants is more than or equal to 98 percent, the removal rate of refractory components such as benzopyrene, cyanide, polycyclic aromatic hydrocarbon and the like is far greater than the three-emission limit value, and individual indexes cannot be detected, so that the high-efficiency recycling of refractory industrial wastewater such as coking wastewater and the like becomes practical, and a technical and process basis is provided for the high-efficiency recycling, energy conservation and emission reduction; the operation management is convenient; the process is stable; the investment and operation cost is low; the method overcomes the problem of high treatment cost of the highly-refractory organic pollutants, breaks through the technical and technological bottlenecks which cannot be solved by the highly-refractory organic pollutants, and has remarkable social, economic and environmental benefits.

The system and the process method of the embodiment are suitable for but not limited to treatment of industrial wastewater containing refractory organic characteristic pollutants, such as coking wastewater, and have the advantages that COD (chemical oxygen demand), refractory organic pollutants, benzopyrene, polycyclic aromatic hydrocarbons, total nitrogen and the like in the wastewater are efficiently removed, and finally, the discharged water can stably meet the requirements of the discharge standard of coking chemical industry pollutants (GB16171-2012) special discharge limit table 3. The A-O biochemical treatment is anaerobic-aerobic biochemical treatment.

In this embodiment, a regulating submersible mixer is arranged in the regulating reservoir 20, and the regulating submersible mixer is used for mixing the wastewater in the regulating reservoir 20 to perform conditioning mixing.

In this embodiment, the activated sludge pretreatment biochemical system 40 includes an aeration tank 41, a sedimentation tank 42 and a pretreatment return line 43, the aeration tank 41 is communicated with the air flotation degreaser 30, and a pretreatment aerator is arranged in the aeration tank 41 to perform aeration treatment on the wastewater in the aeration tank 41; the sedimentation tank 42 is communicated with the aeration tank 41, and carries out solid-liquid separation on the wastewater from the aeration tank 41, and the supernatant obtained by the separation flows into the first-stage A-O biochemical treatment system 50; the pretreatment return line 43 communicates the sedimentation tank 42 and the aeration tank 41, and at least a part of sludge in the sedimentation tank 42 is returned to the aeration tank 41 via the pretreatment return line 43.

Preferably, the sludge reflux ratio of the pretreatment return line 43 is 100%.

Optionally, a blower for supplying air, a dissolved oxygen meter for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value, and a temperature detector for detecting the temperature are further disposed in the aeration tank 41, so as to monitor and adjust the reaction state in the aeration tank 41.

Optionally, the bottom of the sedimentation tank 42 is provided with a conical structure, so as to facilitate the sedimentation and collection of sludge and ensure the stable sludge concentration of the returned sludge, and the pretreatment return line 43 is communicated with the bottom of the sedimentation tank 42, so that the sludge at the bottom can return to the aeration tank 41 through the pretreatment return line 43.

In this embodiment, be provided with elevator pump and defoaming pump in the sedimentation tank 42, the elevator pump provides power for the backward flow of mud, and its drive mud gets into preliminary treatment return line 43 and flows back to aeration tank 41 in, and the defoaming pump can spray the defoaming, plays the defoaming effect.

In this embodiment, the primary a-O biochemical treatment system 50 includes a primary facultative tank 51, a primary aerobic tank 52, a primary nitrifying liquid return line 53, a primary settling tank 54, a primary sludge return line 55, and an intermediate water tank 56. The primary facultative tank 51 is communicated with the sedimentation tank 42 of the activated sludge pretreatment biochemical system 40 and carries out denitrification treatment on the pretreated wastewater; the primary aerobic tank 52 is communicated with the primary facultative tank 51, and a primary aerator is arranged in the primary aerobic tank 52; the primary nitrification liquid return pipeline 53 is communicated with the primary facultative tank 51 and the primary aerobic tank 52, and the nitrification liquid in the primary aerobic tank 52 flows back to the primary facultative tank 51 through the primary nitrification liquid return pipeline 53; the primary sedimentation tank 54 is communicated with the primary aerobic tank 52 and is used for carrying out sedimentation separation on the wastewater from the primary aerobic tank 52; the primary sludge return line 55 is communicated with the primary sedimentation tank 54 and the primary facultative tank 51, and the sludge in the primary sedimentation tank 54 flows back to the primary facultative tank 51 through the primary sludge return line 55; the intermediate water tank 56 is communicated with the primary sedimentation tank 54, and supernatant separated from the primary sedimentation tank 54 enters the intermediate water tank 56.

Preferably, the primary nitrifying liquid return line 53 has a nitrifying liquid reflux ratio of 300%, and the primary sludge return line 55 has a sludge reflux ratio of 100%.

Optionally, similar to the activated sludge pretreatment biochemical system 40, a blower for supplying air, a dissolved oxygen meter for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value, and a temperature detector for detecting the temperature are further disposed in the primary aerobic tank 52, so as to monitor and adjust the state in the primary aerobic tank 52. In the first-stage aerobic tank 52 of the embodiment, the pH value is 7.5-8.5, the dissolved oxygen is below 0.5mg/L, and the temperature is 30-40 ℃.

In this embodiment, similar to the sedimentation tank 42, a sludge scraper and a lift pump are also arranged in the primary sedimentation tank 54, the bottom of the primary sedimentation tank 54 is also provided with a conical structure, the sludge scraper concentrates sludge in the conical structure, the primary sludge return line 55 is communicated with the bottom of the primary sedimentation tank 54, and the lift pump drives sludge to enter the primary sludge return line 55 and return to the primary facultative tank 51. A defoaming pump for spraying defoaming is arranged in the middle water tank 56.

In this embodiment, the secondary a-O biochemical treatment system 60 is substantially similar to the primary a-O biochemical treatment system 50, the secondary a-O biochemical treatment system 60 includes a secondary facultative tank 61, a secondary aerobic tank 62, a secondary sedimentation tank 63, and a secondary sludge return line 64, the secondary facultative tank 61 is communicated with the intermediate tank 56 of the primary a-O biochemical treatment system 50, and performs denitrification treatment on the wastewater after the primary a-O biochemical treatment; the secondary aerobic tank 62 is communicated with the secondary facultative tank 61, and a secondary aerator is arranged in the secondary aerobic tank 62; the secondary sedimentation tank 63 is communicated with the secondary aerobic tank 62, and carries out sedimentation separation on the wastewater from the secondary aerobic tank 62; the secondary sludge return line 64 communicates the secondary sedimentation tank 63 and the secondary facultative tank 61, and the sludge in the secondary sedimentation tank 63 returns to the secondary facultative tank 61 through the secondary sludge return line 64.

Preferably, the sludge recirculation ratio of the secondary sludge recirculation line 64 is 100%.

Similar to the first-stage A-O biochemical treatment system 50, a fan for supplying air, a dissolved oxygen detecting instrument for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value and a temperature detector for detecting the temperature are also arranged in the second-stage aerobic tank 62, the PH value in the second-stage aerobic tank 62 is 7.5-8.5, the dissolved oxygen is below 0.5mg/L, and the temperature is 30-40 ℃. The secondary sedimentation tank 63 is internally provided with a lift pump, the bottom of the secondary sedimentation tank 63 is provided with a conical structure, a secondary sludge return pipeline 64 is communicated with the bottom of the secondary sedimentation tank 63, and the lift pump drives sludge to enter the secondary sludge return pipeline 64 and return to the secondary facultative tank 61.

Thus, the primary A-O biochemical treatment system 50 and the secondary A-O biochemical treatment system 60 form a two-stage series A-O biochemical treatment system, so that the biochemical treatment of the wastewater is more effectively carried out, and the treatment effect is ensured.

In this embodiment, the chemical coagulation sedimentation system 70 includes a coagulation sedimentation device 71, a mixing reaction tank 72, a coagulation sedimentation tank 73, and an air flotation coagulation sedimentation device 74. The coagulating sedimentation equipment 71 is communicated with a secondary sedimentation tank 63 of the secondary A-O biochemical treatment system 60, and the wastewater after the secondary A-O biochemical treatment is communicated with FeSO in the coagulating sedimentation equipment 71₄、H₂O₂CaO mixing and reacting, wherein a mechanical stirring device, an aeration stirring device and a PH detection instrument are arranged in the coagulating sedimentation equipment 71; the mixed reaction tank 72 is communicated with the coagulating sedimentation device 71, the wastewater treated by the coagulating sedimentation device 71 enters the mixed reaction tank 72, and a stirring device and an aeration stirring device are arranged in the mixed reaction tank 72; the coagulating sedimentation tank 73 is communicated with the mixing reaction tank 72 and is used for precipitating and separating the wastewater from the mixing reaction tank 72, a mud scraper and a lift pump are also arranged in the coagulating sedimentation tank 73, and the sludge at the bottom enters a sludge concentration tank through the lift pump; the air floatation coagulating sedimentation equipment 74 is communicated with the coagulating sedimentation tank 73, the supernatant separated by the coagulating sedimentation tank 73 enters the air floatation coagulating sedimentation equipment 74, a circulating water pump and a slag scraping machine are arranged in the air floatation coagulating sedimentation equipment 74, and oil substances in the wastewaterAnd the suspended matters are scraped into a scum trough through a scum scraper and enter a crude benzene recovery system, and the supernatant enters an electromagnetic strong oxidation advanced treatment system 80.

In the embodiment, the electromagnetic strong oxidation advanced treatment system 80 comprises an acid regulation dosing tank 81, an electromagnetic strong oxidation system 82, an advanced reaction system 83, a neutralization flocculation device 84, a final sedimentation tank 85 and a sand filter 86 which are communicated in sequence.

The embodiment also provides a standard-reaching direct-discharging process method for industrial wastewater treatment, and the standard-reaching direct-discharging system for industrial wastewater treatment is adopted. The following detailed description is made on the standard-reaching direct-discharging process method for industrial wastewater treatment by combining the standard-reaching direct-discharging system for industrial wastewater treatment:

a gravity oil removal stage: the waste water is high in temperature after quenching, is subjected to heat collection and cooling pretreatment by the heat exchanger 90 and then enters the gravity oil remover 10, the retention time of the waste water in the gravity oil remover 10 is more than or equal to 5 hours, oil condensate with high density and most of floating oil are removed by gravity oil removal, and supernatant flows into the regulating tank 20.

And (3) adjusting: the adjusting tank 20 fully adjusts and mixes the wastewater through a submersible stirrer in the adjusting tank, and the retention time of the wastewater in the adjusting tank 20 is more than or equal to 24 hours.

Air floatation oil removal stage: the wastewater from the adjusting tank 20 is transferred to the air-flotation oil remover 30 under the action of the lift pump, the retention time of the wastewater in the air-flotation oil remover 30 is more than or equal to 1.5 hours, an aluminum sulfate coagulant and a polyacrylamide coagulant aid are added into the air-flotation oil remover 30, more than 95% of oil of floating oil, emulsified oil, dissolved oil and dispersed oil in the wastewater floats upwards and is condensed, solid-liquid separation is carried out through a slag scraper arranged on the air-flotation oil remover 30, and scum is collected and recycled.

Activated sludge pretreatment biochemical stage: the wastewater treated by the air floatation oil remover 30 automatically flows into an activated sludge pretreatment biochemical system 40, aeration and sedimentation are carried out in the activated sludge pretreatment biochemical system 40, and the treated supernatant flows into a primary A-O biochemical treatment system 50;

specifically, in the activated sludge pretreatment biochemical system 40, the wastewater treated by the air floatation oil remover 30 flows automatically and is mixed with the return sludge of the sedimentation tank 42 and then flows into the foremost end of the aeration tank 41, and the retention time of the mixed liquid in the aeration tank 41 is more than or equal to 13 hours; a pretreatment aerator is arranged in the aeration tank 41, and air is supplied by a fan to meet the requirement of dissolved oxygen; the concentration of dissolved oxygen in the aeration tank 41 is 0.5mg/L, and online monitoring is carried out through a dissolved oxygen detection instrument, the PH in the aeration tank 41 is 7.5, the temperature is 30 ℃, and the indexes are monitored in a proper range on line through an instrument arranged in the aeration tank 41. The mixed liquid in the aeration tank 41 automatically flows to the sedimentation tank 42 for sludge-water separation, the retention time of the wastewater in the sedimentation tank 42 is more than or equal to 6.5 hours, the activated sludge in the conical structure at the bottom of the sedimentation tank 42 returns to the foremost end of the aeration tank 41 through the lifting pump, the sludge return ratio is 100 percent, the supernatant in the sedimentation tank 42 is sprayed and defoamed on the foam generated in the aeration tank 41 through the defoaming pump, and the supernatant of the sedimentation tank 42 automatically flows into the primary A-O biochemical treatment system 50. The activated sludge pretreatment biochemical system 40 can regulate and control the incoming water of the biochemical treatment section through activated sludge and maintain an aerobic environment, so that the system can be ensured to be well decarburized, and simultaneously, a great amount of pollutants with an inhibiting effect on organisms can be removed, and the operation of a subsequent system can be ensured.

Primary A-O biochemical treatment stage: the wastewater treated by the activated sludge pretreatment biochemical system 40 automatically flows into the primary A-O biochemical treatment system 50, anaerobic and aerobic treatment is carried out in the primary A-O biochemical treatment system 50, and the treated supernatant flows into the secondary A-O biochemical treatment system 60;

specifically, in the primary A-O biochemical processing system 50,

effluent of the activated sludge pretreatment biochemical system 40 flows automatically, return sludge of the primary sedimentation tank 54 and return nitrifying liquid of the primary aerobic tank 52 flow into the foremost end of the primary facultative tank 51 after being mixed, the retention time of the mixed liquid in the primary facultative tank 51 is more than or equal to 36 hours, meanwhile, in order to ensure that sewage in the primary facultative tank 51 is uniformly mixed, the mixed liquid is fully stirred by a submersible stirrer in the primary facultative tank, nitrifying bacteria carried by the nitrifying liquid ammonify ammonia nitrogen and organic nitrogen in the wastewater into ammonia nitrogen, the ammonia nitrogen is converted into nitrate through biological nitrification, and in an anoxic section, the nitrate brought by the returned nitrifying liquid is converted into nitrogen through biological denitrification and escapes into the atmosphere, so that the aim of denitrification is fulfilled;

effluent of the primary facultative tank 51 automatically flows into the primary aerobic tank 52, the retention time of wastewater in the primary aerobic tank 52 is more than or equal to 100 hours, nitrifying liquid at the tail end of the primary aerobic tank 52 flows back to the foremost end of the primary facultative tank 51, and the reflux ratio of the nitrifying liquid is 300%;

the mixed liquid in the first-stage aerobic tank 52 automatically flows to a first-stage sedimentation tank 54 for sludge-water separation, the retention time of the wastewater in the first-stage sedimentation tank 54 is more than or equal to 7.6 hours, a sludge scraper in the first-stage sedimentation tank 54 collects activated sludge and concentrates the activated sludge in a conical structure at the bottom of the first-stage sedimentation tank 54, the activated sludge in the conical structure flows back to the foremost end of the first-stage facultative tank 51 through a lift pump, the sludge reflux ratio is 100%, a first-stage aerator is arranged in the first-stage aerobic tank 52, air is supplied by a fan to meet the requirement of dissolved oxygen, and real-time monitoring is carried out through a dissolved oxygen detection instrument, a pH detector and a temperature detector, wherein the optimal pH value is 7.5-8.5, preferably 7.5, and the adding amount; the dissolved oxygen of the nitration reaction is kept below 0.5mg/L, and the aeration rate or the aeration time of a fan is controlled by a dissolved oxygen detection instrument; monitoring the temperature by a temperature detector to ensure that the temperature is about 30-34 ℃, preferably 30 ℃; monitoring the indexes in a proper range on line; the supernatant of the primary sedimentation tank 54 automatically flows into an intermediate water tank 56; the primary aerobic tank 52 is mainly used for removing a large amount of SCN for inhibiting the growth of denitrogenation bacteria in the wastewater^-、CN^-And phenols, and simultaneously completing nitrification;

the supernatant of the first-stage sedimentation tank 54 automatically flows into the intermediate water tank 56, the retention time of the wastewater in the intermediate water tank 56 is more than or equal to 2 hours, the foam generated by aeration in the first-stage aerobic tank 52 is sprayed and digested by the supernatant in the intermediate water tank 56 through a defoaming pump, and the water in the intermediate water tank 56 enters the second-stage A-O biochemical treatment system 60 through a lifting pump.

The first A-O biochemical treatment stage aims at the problems of high toxicity of the wastewater, high concentration of organic matters in the wastewater and NH₃high-N content, according to the operation result of similar wastewater treatment, activated sludge is added into the primary facultative tank 51 and the primary aerobic tank 52, and the living environment of microorganisms is adjusted to play the role of the microorganismsThe properties of different characteristics are shown under the same environment, so that nitration and denitrification reactions are generated to ensure NH₃And finally converting N into nitrogen to enter the atmosphere to finish the denitrification and decarburization processes of nitrification and denitrification, wherein the total nitrogen removal rate of the process can reach 70-80%.

Secondary A-O biochemical treatment stage: the wastewater treated by the primary A-O biochemical treatment system 50 automatically flows into the secondary A-O biochemical treatment system 60, anaerobic and aerobic treatment is carried out in the secondary A-O biochemical treatment system 60, and the treated supernatant flows into the chemical coagulating sedimentation system 70;

specifically, in the secondary A-O biochemical treatment system 60,

the effluent of the first-stage A-O biochemical treatment system 50 is mixed with the return sludge of the second-stage sedimentation tank 63 and then automatically flows into the second-stage facultative tank 61, the retention time of the mixed liquid in the second-stage facultative tank 61 is more than or equal to 36 hours, and the mixed liquid is stirred by a submersible stirrer to ensure uniform mixing;

the effluent of the secondary facultative tank 61 automatically flows into a secondary aerobic tank 62, and the retention time of the wastewater in the secondary aerobic tank 62 is more than or equal to 18 hours;

the mixed liquid in the secondary aerobic tank 62 automatically flows to the secondary sedimentation tank 63 for mud-water separation, the retention time of the mixed liquid in the secondary sedimentation tank 63 is more than or equal to 9 hours, sludge is deposited in a conical structure at the bottom of the secondary sedimentation tank 63 and flows back to the front end of the secondary facultative tank 61 through a lifting pump, the reflux ratio of the sludge is 100 percent, and the components in the secondary aerobic tank 62 and the state parameters thereof are set to be the same as or similar to those of the primary aerobic tank 52; meanwhile, the supernatant in the secondary sedimentation tank 63 is sprayed and digested by a defoaming pump to the foam generated in the secondary aerobic tank 62, and the supernatant in the secondary sedimentation tank 63 automatically flows into the chemical coagulation sedimentation system 70.

The secondary A-O biochemical treatment system 60 performs the tasks of total nitrogen removal and decarburization by adjusting the living environment of the microorganisms to exert the attributes of different characteristics under different environments.

And (3) chemical coagulating sedimentation stage: the wastewater treated by the second-level A-O biochemical treatment system 60 automatically flows into the chemical coagulation sedimentation system 70, and is subjected to chemical coagulation sedimentation treatment in the chemical coagulation sedimentation system 70, and the treated supernatant flows into the electromagnetic strong oxidation advanced treatment system 80;

specifically, in the chemical coagulation sedimentation system 70,

the effluent of the second-stage A-O biochemical treatment system 60 automatically flows into the coagulating sedimentation equipment 71, and simultaneously FeSO is added₄、H₂O₂CaO, the retention time of the wastewater in the coagulating sedimentation equipment 71 is more than or equal to 0.5 hour, and a mechanical stirring device, an aeration stirring device and a PH detection instrument are arranged in the coagulating sedimentation equipment 71 to ensure that the added FeSO₄、H₂O₂CaO is reasonably and fully mixed, and the mixed liquid enters a mixing reaction tank 72;

the effluent of the coagulating sedimentation device 71 automatically flows into a mixing reaction tank 72, the retention time of the mixed liquid in the mixing reaction tank 72 is more than or equal to 0.5 hour, polyacrylamide is added into the mixing reaction tank 72, a stirring device and an aeration stirring device in the mixing reaction tank 72 perform stirring actions, and the treated mixed liquid automatically flows into a coagulating sedimentation tank 73;

the mixed liquid from the mixing reaction tank 72 is statically precipitated in the coagulating sedimentation tank 73 for more than or equal to 8 hours, the sludge in the coagulating sedimentation tank 73 is concentrated by a set sludge scraper and enters a sludge concentration tank through a lift pump, and the supernatant automatically flows into an air floatation coagulating sedimentation device 74;

the supernatant from the coagulating sedimentation tank 73 stays in the air floatation coagulating sedimentation equipment 74 for more than or equal to 1.5 hours, oil substances and suspended matters in the wastewater float upwards in the equipment, are scraped into a scum trough through a scum scraper and enter a crude benzene recovery system, and the supernatant enters an electromagnetic strong oxidation advanced treatment system 80.

Electromagnetic strong oxidation advanced treatment stage: the wastewater treated by the chemical coagulation sedimentation system 70 automatically flows into an electromagnetic strong oxidation advanced treatment system 80, the electromagnetic strong oxidation advanced treatment is carried out in the electromagnetic strong oxidation advanced treatment system 80, the treated sludge enters a sludge treatment system, and finally the effluent reaches the requirement of direct discharge standard;

specifically, in the embodiment, a vertical wave-intensity type electromagnetic strong oxidation system is adopted, in an electromagnetic strong oxidation advanced treatment system 80, the supernatant of a chemical coagulation sedimentation system 70 passes through an acid regulation dosing tank 81 and then enters an electromagnetic strong oxidation system 82 and an advanced reaction system 83, the supernatant stays for more than or equal to 1.8 hours, sewage enters a neutralization flocculation device 84, a final sedimentation tank 85 and a sand filter 86 after undergoing a complex physicochemical reaction in the electromagnetic strong oxidation system 82 and the advanced reaction system 83 for solid-liquid separation, the produced sludge enters a sludge treatment system, and the produced supernatant stably meets the direct discharge standard requirements of a special discharge limit table 3 of "discharge standard of pollutants for coking chemical industry" (GB16171-2012), so that the supernatant can be directly discharged. Before discharging, the waste water can be conveyed to a filter to remove suspended matters and colloidal substances and then discharged.

It should be noted that, a plurality in the above embodiments means at least two.

From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:

1. the problem that the industrial wastewater treatment process in the prior art cannot meet the requirement of direct discharge standard is solved;

2. the process composition is reasonable, the route is clear and concise, the biochemical treatment and the physicochemical treatment are orderly and organically combined, and the four main body units are optimally combined and mutually supported;

3. the overall COD removal rate is more than or equal to 98 percent, the removal rate of organic characteristic pollutants is more than or equal to 98 percent, the removal rate of high-difficult-to-degrade components such as benzopyrene, cyanide, polycyclic aromatic hydrocarbon and the like is far greater than the table three emission limit value, and individual indexes cannot be detected, so that the high-efficiency recycling of coking wastewater and other difficult-to-treat industrial wastewater becomes reality, and a technical and technological basis is provided for high-efficiency recycling, energy conservation and emission reduction;

4. the method has the advantages of convenient operation management, stable process and low investment and operation cost, overcomes the problem of high treatment cost of the organic pollutants with high difficulty in degradation, breaks through the technical and process bottlenecks which cannot be solved by the organic pollutants with high difficulty in degradation, and has remarkable social, economic and environmental benefits.

It is to be understood that the above-described embodiments are only a few, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular is intended to include the plural unless the context clearly dictates otherwise, and it should be further understood that the terms "comprises" and/or "comprising," when used in this specification, specify the presence of features, steps, operations, devices, components, and/or combinations thereof.

It should be noted that the terms "first," "second," and the like in the description and claims of this application and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used is interchangeable under appropriate circumstances such that the embodiments of the application described herein are capable of operation in sequences other than those illustrated or described herein.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. The utility model provides an industrial waste water handles system in line up to standard which characterized in that includes:

a gravity oil remover (10), wherein the gravity oil remover (10) can remove part of oil condensate and floating oil in the wastewater;

the adjusting tank (20), the adjusting tank (20) is communicated with the gravity oil remover (10), and can be used for conditioning and mixing the wastewater;

the air flotation oil remover (30), the air flotation oil remover (30) is communicated with the adjusting tank (20), and the air flotation oil remover (30) can remove oil in wastewater;

the activated sludge pretreatment biochemical system (40), the activated sludge pretreatment biochemical system (40) is communicated with the air floatation oil remover (30), and is used for pretreating the wastewater from the air floatation oil remover (30);

the primary A-O biochemical treatment system (50), the primary A-O biochemical treatment system (50) is communicated with the activated sludge pretreatment biochemical system (40), and primary A-O biochemical treatment is carried out on the pretreated wastewater;

the secondary A-O biochemical treatment system (60), the secondary A-O biochemical treatment system (60) is communicated with the primary A-O biochemical treatment system (50), and secondary A-O biochemical treatment is carried out on the wastewater after the primary A-O biochemical treatment;

the chemical coagulation sedimentation system (70), the chemical coagulation sedimentation system (70) is communicated with the secondary A-O biochemical treatment system (60), and the waste water after the secondary A-O biochemical treatment is subjected to chemical coagulation sedimentation treatment;

the electromagnetic strong oxidation advanced treatment system (80), the electromagnetic strong oxidation advanced treatment system (80) is communicated with the chemical coagulating sedimentation system (70), and the wastewater after the chemical coagulating sedimentation treatment is subjected to electromagnetic strong oxidation advanced treatment.

2. The industrial wastewater treatment standard direct discharge system according to claim 1, wherein a regulating submersible stirrer is arranged in the regulating reservoir (20), and the regulating submersible stirrer is used for quenching, tempering and mixing wastewater in the regulating reservoir (20).

3. The industrial wastewater treatment standard direct discharge system according to claim 1, wherein the activated sludge pretreatment biochemical system (40) comprises:

the aeration tank (41), the aeration tank (41) is communicated with the air floatation oil remover (30), and a pretreatment aerator is arranged in the aeration tank (41) to carry out aeration treatment on the wastewater in the aeration tank (41);

the sedimentation tank (42) is communicated with the aeration tank (41), solid-liquid separation is carried out on the wastewater from the aeration tank (41), and the supernatant obtained by separation flows into the primary A-O biochemical treatment system (50);

a pretreatment return line (43), wherein the pretreatment return line (43) is communicated with the sedimentation tank (42) and the aeration tank (41), and at least part of sludge in the sedimentation tank (42) returns to the aeration tank (41) through the pretreatment return line (43).

4. The industrial wastewater treatment standard direct discharge system according to claim 3, wherein the sludge reflux ratio of the pretreatment reflux pipeline (43) is 100%.

5. The standard-reaching direct-discharge system for industrial wastewater treatment according to claim 3, wherein a fan for supplying air, a dissolved oxygen detecting instrument for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value and a temperature detector for detecting the temperature are arranged in the aeration tank (41).

6. The industrial wastewater treatment standard direct discharge system according to claim 3, wherein the bottom of the sedimentation tank (42) is provided with a conical structure, and the pretreatment return line (43) is communicated with the bottom of the sedimentation tank (42).

7. The industrial wastewater treatment standard direct discharge system according to claim 3, wherein a lift pump and a defoaming pump are arranged in the sedimentation tank (42), the lift pump drives sludge into the pretreatment return pipeline (43) and returns the sludge to the aeration tank (41), and the defoaming pump can perform spray defoaming.

8. The industrial wastewater treatment standard straight-line system according to claim 1, wherein the primary A-O biochemical treatment system (50) comprises:

the primary facultative tank (51), the primary facultative tank (51) is communicated with the activated sludge pretreatment biochemical system (40), and the primary facultative tank carries out denitrification treatment on the pretreated wastewater;

the primary aerobic tank (52), the primary aerobic tank (52) is communicated with the primary facultative tank (51), and a primary aerator is arranged in the primary aerobic tank (52);

the primary nitrification liquid return pipeline (53) is communicated with the primary facultative tank (51) and the primary aerobic tank (52), and the nitrification liquid in the primary aerobic tank (52) flows back to the primary facultative tank (51) through the primary nitrification liquid return pipeline (53);

the primary sedimentation tank (54) is communicated with the primary aerobic tank (52), and is used for carrying out sedimentation separation on the wastewater from the primary aerobic tank (52);

the primary sludge return pipeline (55) is communicated with the primary sedimentation tank (54) and the primary facultative tank (51), and the sludge in the primary sedimentation tank (54) flows back to the primary facultative tank (51) through the primary sludge return pipeline (55);

the middle water tank (56), the middle water tank (56) with the primary sedimentation tank (54) intercommunication, the supernatant that the primary sedimentation tank (54) separated gets into in the middle water tank (56).

9. The industrial wastewater treatment standard direct discharge system according to claim 8, wherein the primary nitrifying liquid return line (53) has a nitrifying liquid reflux ratio of 300%, and the primary sludge return line (55) has a sludge reflux ratio of 100%.

10. The industrial wastewater treatment standard direct discharge system according to claim 8, wherein a blower for supplying gas, a dissolved oxygen detecting instrument for detecting the concentration of dissolved oxygen, a PH detector for detecting the PH value, and a temperature detector for detecting the temperature are further arranged in the primary aerobic tank (52), the PH value in the primary aerobic tank (52) is 7.5-8.5, the dissolved oxygen is below 0.5mg/L, and the temperature is 30-40 ℃.

11. The industrial wastewater treatment standard direct discharge system according to claim 8, wherein a mud scraper and a lift pump are arranged in the primary sedimentation tank (54), the bottom of the primary sedimentation tank (54) is provided with a conical structure, the mud scraper concentrates sludge in the conical structure, the primary sludge return line (55) is communicated with the bottom of the primary sedimentation tank (54), and the lift pump drives sludge into the primary sludge return line (55) and returns to the primary facultative tank (51).

12. The industrial wastewater treatment standard direct discharge system according to claim 8, wherein a defoaming pump for spray defoaming is arranged in the intermediate water tank (56).

13. The industrial wastewater treatment standard straight line system of claim 1, wherein the secondary A-O biochemical treatment system (60) comprises:

the secondary facultative tank (61), the said secondary facultative tank (61) communicates with said first class A-O biochemical treatment system (50), and carry on the denitrogenation to the waste water after the biochemical treatment of first class A-O;

the secondary aerobic tank (62), the secondary aerobic tank (62) is communicated with the secondary facultative tank (61), and a secondary aerator is arranged in the secondary aerobic tank (62);

the secondary sedimentation tank (63) is communicated with the secondary aerobic tank (62), and is used for carrying out sedimentation separation on the wastewater from the secondary aerobic tank (62);

a secondary sludge return line (64), the secondary sludge return line (64) communicates the secondary sedimentation tank (63) and the secondary facultative tank (61), and sludge in the secondary sedimentation tank (63) flows back into the secondary facultative tank (61) through the secondary sludge return line (64).

14. The industrial wastewater treatment standard direct discharge system according to claim 13, wherein the secondary sludge return line (64) has a sludge return ratio of 100%.

15. The industrial wastewater treatment standard direct discharge system according to claim 13, wherein a fan for supplying air, a dissolved oxygen detecting instrument for detecting the concentration of dissolved oxygen, a pH detector for detecting the pH value and a temperature detector for detecting the temperature are further arranged in the secondary aerobic tank (62), the pH value in the secondary aerobic tank (62) is 7.5-8.5, the dissolved oxygen is below 0.5mg/L, and the temperature is 30-40 ℃.

16. The industrial wastewater treatment standard direct discharge system according to claim 13, wherein a lift pump is arranged in the secondary sedimentation tank (63), the bottom of the secondary sedimentation tank (63) is provided with a conical structure, the secondary sludge return line (64) is communicated with the bottom of the secondary sedimentation tank (63), and the lift pump drives sludge into the secondary sludge return line (64) and returns to the secondary facultative tank (61).

17. The industrial wastewater treatment standard direct discharge system of claim 1, wherein the chemical coagulation sedimentation system (70) comprises:

the coagulating sedimentation equipment (71), the coagulating sedimentation equipment (71) is communicated with the secondary A-O biochemical treatment system (60), and the wastewater after the secondary A-O biochemical treatment and the FeSO in the coagulating sedimentation equipment (71)₄、H₂O₂The CaO mixing reaction, wherein a mechanical stirring device, an aeration stirring device and a PH detection instrument are arranged in the coagulating sedimentation equipment (71);

the mixing reaction tank (72) is communicated with the coagulating sedimentation equipment (71), the wastewater treated by the coagulating sedimentation equipment (71) enters the mixing reaction tank (72), and a stirring device and an aeration stirring device are arranged in the mixing reaction tank (72);

the coagulating sedimentation tank (73) is communicated with the mixing reaction tank (72) and is used for precipitating and separating the wastewater from the mixing reaction tank (72), a mud scraper and a lifting pump are arranged in the coagulating sedimentation tank (73), and the sludge at the bottom enters a sludge concentration tank through the lifting pump;

the device comprises an air flotation coagulating sedimentation device (74), wherein the air flotation coagulating sedimentation device (74) is communicated with a coagulating sedimentation tank (73), supernatant separated by the coagulating sedimentation tank (73) enters the air flotation coagulating sedimentation device (74), a circulating water pump and a slag scraping machine are arranged in the air flotation coagulating sedimentation device (74), oil substances and suspended matters in wastewater are scraped into a slag floating groove through the slag scraping machine to enter a crude benzene recovery system, and the supernatant enters the electromagnetic strong oxidation advanced treatment system (80).

18. The industrial wastewater treatment standard direct discharge system according to claim 1, wherein the electromagnetic strong oxidation advanced treatment system (80) comprises an acid regulation dosing tank (81), an electromagnetic strong oxidation system (82), an advanced reaction system (83), a neutralization flocculation device (84), a final sedimentation tank (85) and a sand filter (86) which are communicated in sequence.

19. An industrial wastewater treatment standard direct discharge process method, which is characterized in that the industrial wastewater treatment standard direct discharge system of any one of claims 1 to 18 is adopted, and the industrial wastewater treatment standard direct discharge process method comprises the following steps:

the method comprises the following steps that waste water is subjected to heat collection and cooling pretreatment through a heat exchanger (90), and then enters a gravity oil remover (10), the waste water stays in the gravity oil remover (10) for more than or equal to 5 hours, oil condensate and floating oil with high density are removed through gravity oil removal, and supernatant flows into a regulating tank (20);

the adjusting tank (20) fully adjusts and mixes the wastewater, and the retention time of the wastewater in the adjusting tank (20) is more than or equal to 24 hours;

the wastewater flowing out of the regulating tank (20) is conveyed to an air flotation oil remover (30), the retention time of the wastewater in the air flotation oil remover (30) is more than or equal to 1.5 hours, an aluminum sulfate coagulant and a polyacrylamide coagulant aid are added into the air flotation oil remover (30), more than 95% of oil of water floating oil, emulsified oil, dissolved oil and dispersed oil in the wastewater floats upwards and is coagulated, solid-liquid separation is carried out through a slag scraper arranged on the air flotation oil remover (30), and scum is collected and recycled;

the wastewater treated by the air floatation oil remover (30) automatically flows into an activated sludge pretreatment biochemical system (40), aeration and sedimentation are carried out in the activated sludge pretreatment biochemical system (40), and the treated supernatant flows into a primary A-O biochemical treatment system (50);

the wastewater treated by the activated sludge pretreatment biochemical system (40) automatically flows into the primary A-O biochemical treatment system (50), anaerobic and aerobic treatment is carried out in the primary A-O biochemical treatment system (50), and the treated supernatant flows into the secondary A-O biochemical treatment system (60);

the wastewater treated by the primary A-O biochemical treatment system (50) automatically flows into the secondary A-O biochemical treatment system (60), anaerobic and aerobic treatment is carried out in the secondary A-O biochemical treatment system (60), and the treated supernatant flows into a chemical coagulation sedimentation system (70);

the wastewater treated by the secondary A-O biochemical treatment system (60) automatically flows into the chemical coagulation sedimentation system (70), chemical coagulation sedimentation treatment is carried out in the chemical coagulation sedimentation system (70), and the treated supernatant flows into the electromagnetic strong oxidation advanced treatment system (80);

the wastewater treated by the chemical coagulation sedimentation system (70) automatically flows into the electromagnetic strong oxidation advanced treatment system (80), the electromagnetic strong oxidation advanced treatment system (80) carries out electromagnetic strong oxidation advanced treatment, the treated sludge enters the sludge treatment system, and finally the effluent reaches the requirement of direct discharge standard.

20. The industrial wastewater treatment standard direct discharge process method according to claim 19, wherein, in the activated sludge pretreatment biochemical system (40),

the wastewater treated by the air floatation oil remover (30) flows automatically and is mixed with return sludge of the sedimentation tank (42) and then flows into the foremost end of the aeration tank (41), and the retention time of the mixed liquid in the aeration tank (41) is more than or equal to 13 hours;

the mixed liquid in the aeration tank (41) automatically flows to the sedimentation tank (42) for sludge-water separation, the retention time of the wastewater in the sedimentation tank (42) is more than or equal to 6.5 hours, the activated sludge in the conical structure at the bottom of the sedimentation tank (42) flows back to the foremost end of the aeration tank (41) through a lift pump, and the supernatant of the sedimentation tank (42) automatically flows into the primary A-O biochemical treatment system (50).

21. The industrial wastewater treatment standard direct discharge process method according to claim 20, wherein the dissolved oxygen concentration in the aeration tank (41) is 0.5mg/L and is monitored on line by a dissolved oxygen detection instrument, the pH in the aeration tank (41) is 7.5, the temperature is 30 ℃, and the supernatant in the sedimentation tank (42) is subjected to spray defoaming on the foam generated in the aeration tank (41) by a defoaming pump.

22. The industrial wastewater treatment standard straight-line process according to claim 19, wherein, in the primary A-O biochemical treatment system (50),

effluent of the activated sludge pretreatment biochemical system (40) flows automatically, return sludge of the primary sedimentation tank (54) and return nitrifying liquid of the primary aerobic tank (52) are mixed and then flow into the foremost end of the primary facultative tank (51), the mixed liquid stays in the primary facultative tank (51) for more than or equal to 36 hours, nitrifying bacteria carried by the nitrifying liquid ammonify ammonia nitrogen and organic nitrogen in wastewater into ammonia nitrogen, and the ammonia nitrogen is converted into nitrate through biological nitrification, and in an anoxic section, the nitrate carried by the return nitrifying liquid is converted into nitrogen through biological denitrification by the denitrifying bacteria;

effluent of the primary facultative tank (51) automatically flows into the primary aerobic tank (52), the retention time of wastewater in the primary aerobic tank (52) is more than or equal to 100 hours, and nitrified liquid at the tail end of the primary aerobic tank (52) flows back to the foremost end of the primary facultative tank (51);

the mixed liquid of the primary aerobic tank (52) automatically flows to the primary sedimentation tank (54) for mud-water separation, the retention time of wastewater in the primary sedimentation tank (54) is more than or equal to 7.6 hours, a mud scraper in the primary sedimentation tank (54) collects activated sludge and concentrates the activated sludge in a conical structure at the bottom of the primary sedimentation tank (54), the activated sludge in the conical structure flows back to the foremost end of the primary facultative tank (51) through a lift pump, and the supernatant of the primary sedimentation tank (54) automatically flows into an intermediate water tank (56);

supernatant of the primary sedimentation tank (54) automatically flows into the intermediate water tank (56), the retention time of wastewater in the intermediate water tank (56) is more than or equal to 2 hours, the supernatant in the intermediate water tank (56) sprays and digests foam generated by aeration in the primary aerobic tank (52) through a defoaming pump, and water in the intermediate water tank (56) enters the secondary A-O biochemical treatment system (60) through a lifting pump.

23. The industrial wastewater treatment standard straight-line process according to claim 19, wherein, in the secondary A-O biochemical treatment system (60),

the effluent of the primary A-O biochemical treatment system (50) is mixed with the return sludge of the secondary sedimentation tank (63) and then automatically flows into the secondary facultative tank (61), the retention time of the mixed liquid in the secondary facultative tank (61) is not less than 36 hours, and the mixed liquid is stirred by a submersible stirrer;

the effluent of the secondary facultative tank (61) automatically flows into a secondary aerobic tank (62), and the retention time of the wastewater in the secondary aerobic tank (62) is more than or equal to 18 hours;

the mixed liquid in the secondary aerobic tank (62) automatically flows to the secondary sedimentation tank (63) for mud-water separation, the retention time of the mixed liquid in the secondary sedimentation tank (63) is not less than 9 hours, sludge is deposited in a conical structure at the bottom of the secondary sedimentation tank (63) and flows back to the front end of the secondary facultative tank (61) through a lifting pump, meanwhile, the supernatant in the secondary sedimentation tank (63) is sprayed and digested on the foam generated in the secondary aerobic tank (62) through a defoaming pump, and the supernatant in the secondary sedimentation tank (63) automatically flows into the chemical coagulation sedimentation system (70).

24. The industrial wastewater treatment standard straight-line process according to claim 19, characterized in that, in the chemical coagulation sedimentation system (70),

effluent of the secondary A-O biochemical treatment system (60) automatically flows into a coagulating sedimentation device (71), and FeSO is added at the same time₄、H₂O₂CaO, the retention time of the wastewater in the coagulating sedimentation equipment (71) is more than or equal to 0.5 hour;

effluent of the coagulating sedimentation equipment (71) automatically flows into a mixing reaction tank (72), the retention time of mixed liquid in the mixing reaction tank (72) is more than or equal to 0.5 hour, polyacrylamide is added into the mixing reaction tank (72), a stirring device and an aeration stirring device are stirred, and the treated mixed liquid automatically flows into a coagulating sedimentation tank (73);

the mixed liquid from the mixed reaction tank (72) is statically precipitated in the coagulating sedimentation tank (73) for more than or equal to 8 hours, sludge in the coagulating sedimentation tank (73) is concentrated by a set sludge scraper and enters a sludge concentration tank by a lift pump, and supernatant automatically flows into an air floatation coagulating sedimentation device (74);

the supernatant from the coagulating sedimentation tank (73) stays in the air floatation coagulating sedimentation equipment (74) for more than or equal to 1.5 hours, oil substances and suspended matters in the wastewater float in the equipment, are scraped into a scum trough through a scum scraper and enter a crude benzene recovery system, and the supernatant enters the electromagnetic strong oxidation advanced treatment system (80).

25. The industrial wastewater treatment standard direct discharge process method according to claim 19, characterized in that in the electromagnetic strong oxidation advanced treatment system (80),

the supernatant of the chemical coagulation sedimentation system (70) enters an electromagnetic strong oxidation system (82) and a deep reaction system (83) after passing through an adjusting tank (20), stays for more than or equal to 1.8 hours, then enters a neutralization flocculation device (84), a final sedimentation tank (85) and a sand filter (86) for solid-liquid separation, the produced sludge enters a sludge treatment system, and the produced supernatant can be directly discharged.