CN112374664B - System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed - Google Patents

System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed Download PDF

Info

Publication number
CN112374664B
CN112374664B CN202011017204.8A CN202011017204A CN112374664B CN 112374664 B CN112374664 B CN 112374664B CN 202011017204 A CN202011017204 A CN 202011017204A CN 112374664 B CN112374664 B CN 112374664B
Authority
CN
China
Prior art keywords
liquid
tank
fluidized bed
electrolytic
water
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202011017204.8A
Other languages
Chinese (zh)
Other versions
CN112374664A (en
Inventor
朱庆山
杨海涛
张英志
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Nantong Jinhong Electrochemical Equipment Co ltd
Institute of Process Engineering of CAS
Original Assignee
Nantong Jinhong Electrochemical Equipment Co ltd
Institute of Process Engineering of CAS
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Nantong Jinhong Electrochemical Equipment Co ltd, Institute of Process Engineering of CAS filed Critical Nantong Jinhong Electrochemical Equipment Co ltd
Priority to CN202011017204.8A priority Critical patent/CN112374664B/en
Publication of CN112374664A publication Critical patent/CN112374664A/en
Application granted granted Critical
Publication of CN112374664B publication Critical patent/CN112374664B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen

Abstract

The invention belongs to the fields of chemical industry and environmental protection. The invention particularly discloses a system and a method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in a liquid-solid fluidized bed. And removing solid suspended matters in the ammonia nitrogen wastewater through gravity settling and filtering to realize wastewater pre-purification. Through spraying treatment, the catalyst and the ammonia nitrogen wastewater are fully mixed, and the catalytic components in the electrolytic gas are effectively utilized. And the efficient cracking of ammonia nitrogen in the wastewater is realized through plate-frame electrolysis coupled with three-dimensional electrolysis of a fluidized bed. The raw water at the outlet of the filter is adopted to adjust the pH value of the electrolyzed solution, so that the wastewater recycling is realized. An integrated bipolar plate structure is adopted in plate-and-frame electrolysis, so that the utilization efficiency of materials is improved, and meanwhile, the modes of current series connection and water flow parallel connection are adopted, so that the water quality circulation is enhanced, the mass transfer efficiency is improved, and the decomposition of ammonia nitrogen is promoted.

Description

System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed
Technical Field
The invention belongs to the fields of chemical industry and environmental protection, and particularly relates to a system and a method for realizing wastewater recycling by removing ammonia nitrogen through three-dimensional electrolysis of a liquid-solid fluidized bed.
Background
The GDP of China in 2019 reaches 99 trillion Renminbi, which is increased by about 58 times compared with that before 30 years. Behind the rapid economic growth, the product yield in the heavy industrial fields of chemical industry, metallurgy, coal, cement, caustic soda and the like has exceeded more than 50% of the world. And the industries have the characteristics of high energy consumption and heavy pollution. That is, nearly 50% of the worldwide emissions of pollutants remain in china each year. The discharge of a large amount of pollutants far exceeds the self-metabolism capability of the environment, and the ecological imbalance is caused. In order to maintain a benign balance of the ecosystem, the pollutants must be artificially disposed of. The ammonia nitrogen wastewater related to the patent is a very typical pollutant.
The ammonia nitrogen wastewater is widely used in a plurality of industrial fields, including textile, pharmacy, pesticide, tanning, petroleum, chemical industry, coal, metallurgy and other fields. In the past, ammonia nitrogen wastewater is mainly treated by a biochemical process, so that energy in the ammonia nitrogen wastewater can be recovered, and the method has the characteristic of low cost. But the biochemical method has the characteristics of large floor area, long treatment period, large investment and the like, and is more suitable for enterprises with larger water quantity. At present, many small and medium-sized enterprises face the problem of ammonia nitrogen wastewater treatment, and the wastewater amount is small and is not suitable for biochemical process. In this case, the physical and chemical processes are required, which mainly include breakpoint chlorination, ion exchange, precipitation and electrocatalytic oxidation. The electrocatalytic oxidation technology has the advantages of compact device, small occupied area, no secondary pollution, high treatment efficiency and the like, and is rapidly developed in recent decades.
At present, the problems of low mass transfer efficiency and high electrode cost mainly exist in the treatment of ammonia nitrogen wastewater by an electrocatalytic oxidation technology. In order to solve the problem, people propose to add three-dimensional particle electrodes between two-dimensional electrode plates, so that the specific surface area of the electrodes is greatly improved, the cost of the electrodes is reduced, and the mass transfer efficiency is improved. Chinese patent application CN104787937A discloses a method for three-dimensional electrode electrolysis treatment of high-concentration ammonia nitrogen wastewater. Titanium-plated steel plates are used as anodes, and steel plates are used as cathodes. And a particle electrode made of an iron-based catalyst is filled between the cathode plate and the anode plate, and the iron-carbon ratio of the particle electrode is 1-6. The initial concentration of the ammonia nitrogen wastewater is 2000-3000 mg/L, and after electrolytic treatment, the concentration of the ammonia nitrogen is 50-70 mg/L. This patent uses iron carbon particles as particle electrodes, and iron is consumed during use, thereby producing iron-containing sludge, which easily blocks the reactor. Moreover, iron-carbon electrodes need to be continuously replenished, increasing operating costs. Chinese patent CN201620686031.1 discloses a device for treating landfill leachate by using three-dimensional electrodes, wherein aluminum-titanium alloy is used as an anode plate, stainless steel is used as a cathode plate, and coal columnar activated carbon is used as a particle electrode. After the electrolytic treatment by the technology, the ammonia nitrogen removal rate is 75-85%. This patent adopts fixed bed structure, and rivers go into down and go out, and the long-term pile up the in-process of active carbon, can harden into the piece, and then block up the water flow. In addition, the fixed bed has short-circuit current, which causes the reduction of the electric energy utilization rate, the temperature rise of the electrolytic bath and the reduction of the service life of the electrode. The Chinese utility model patent CN202400887U discloses a three-dimensional particle electrocatalytic oxidation sewage treatment device. The anode adopts titanium alloy or graphite plate, the cathode adopts titanium alloy or stainless steel plate, solid catalyst is added in the reactor, and COD can be reduced from 64mg/L to 15mg/L through electrochemical treatment. However, in this patent, the particle electrode can rub against the anode during fluidization, reducing the anode life. Moreover, the titanium alloy is adopted as the anode material, so that the catalytic activity is very low, and the energy utilization efficiency is seriously influenced. Chinese patent application CN108423773A discloses a three-dimensional fluidized bed electrolysis apparatus and method suitable for circulating cooling water treatment. This patent adopts the column positive pole, and the external insulating annular perforated plate of positive pole. A fluidization chamber is arranged between the exterior of the insulating plate and the reactor shell, and a large number of conductive particle electrodes are arranged in the fluidization chamber. The particle electrode can inhibit the scaling of the cathode and maintain the good reaction state of the cathode in the fluidizing process. The plastic porous separator in this patent protects the anode from wear. However, the existence of the insulating porous plate can seriously affect the mass transfer of the electrolyte, and the performance of the unipolar particle electrode is generally lower than that of the bipolar particle electrode.
In summary, the electrocatalytic oxidation process has significant advantages in treating ammonia nitrogen wastewater, but the prior art still has the problems of low mass transfer efficiency and high electrode cost. The existing three-dimensional electrolysis technology presents remarkable technical advantages, but has some outstanding problems: (1) the three-dimensional electrolysis of the fixed bed has the problems of caking and hardening of particle electrodes, influence on the flow of electrolyte, short circuit of current, heating of a tank body and the like. (2) Fluidized three-dimensional electrolysis has good mass transfer, but particle electrodes are prone to wear of the anode catalytic coating. The anode can be protected by adding a porous clapboard or a cloth bag, and the new problem of limited anolyte flow also occurs. Moreover, unipolar particle electrodes are generally less effective than bipolar three-dimensional particle electrodes. (3) At present, the field of treating ammonia nitrogen wastewater by electrocatalytic oxidation mainly focuses on the development of an electrolytic cell, and a systematic technology is lacked.
Therefore, the novel technology for realizing wastewater recycling by systematically and efficiently removing ammonia nitrogen through three-dimensional electrolysis is of great significance through technological innovation.
Disclosure of Invention
Aiming at the problems, the invention provides a system and a method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in a liquid-solid fluidized bed so as to realize efficient treatment of ammonia nitrogen wastewater.
In order to achieve the purpose, the invention adopts the following technical scheme:
a system for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in a liquid-solid fluidized bed comprises a filtering working section 1, a spraying working section 2, an electrolysis working section 3 and a water quality adjusting working section 4;
the filtering section 1 comprises a gravity settling tank 1-1, a settling tank blow-down valve 1-2, a filter water inlet pump 1-3, a filter 1-4 and a filter blow-down valve 1-5;
the spraying working section 2 comprises a spraying tower 2-1, a spraying tower drain valve 2-2, a spraying pump 2-3, a catalyst tank 2-4, a catalyst feeding valve 2-5, a catalyst feeding pump 2-6, an induced draft fan 2-7 and a spraying tower feeding pump 2-8;
the electrolysis section 3 comprises a direct current power supply 3-1, an electrolytic bath water feeding pump 3-2, a plate frame electrolytic bath 3-3, a fluidized bed electrolysis liquid inlet valve 3-4, a fluidized bed electrolytic bath 3-5, a fluidized bed electrolysis liquid outlet valve 3-6, a gas-liquid separation tank 3-7 and a separation tank liquid outlet valve 3-8;
the water quality adjusting section 4 comprises an adjusting tank liquid feeding pump 4-1, an adjusting tank 4-2, an adjusting tank liquid discharging valve 4-3, an adjusting tank raw water pump 4-4 and a purifying liquid conveying pump 4-5;
the liquid inlet of the gravity settling tank 1-1 is connected with an ammonia nitrogen wastewater main pipe; a sewage outlet at the bottom of the gravity settling tank 1-1 is connected with a feed inlet of the settling tank sewage valve 1-2 through a pipeline; the discharge hole of the sedimentation tank blow-down valve 1-2 is connected with a sludge treatment main pipe; a vertical liquid baffle plate is arranged in the gravity settling tank 1-1; the water outlet of the gravity settling tank 1-1 is connected with the water inlet of the filter water inlet pump 1-3 through a pipeline; the water outlet of the filter water inlet pump 1-3 is connected with the water inlet of the filter 1-4 through a pipeline; a filter screen or filled with quartz sand is arranged in the filter 1-4; the sewage outlet at the bottom of the filter 1-4 is connected with the feed inlet of the filter sewage valve 1-5 through a pipeline; the discharge ports of the filter blow-down valves 1-5 are connected with a sludge treatment main pipe; the water outlets of the filters 1 to 4 are respectively connected with the feed inlets of the spray tower feed pumps 2 to 8 and the water inlets of the regulating tank raw water pumps 4 to 4 through pipelines;
the gas outlet of the spray tower 2-1 is connected with the gas inlet of the induced draft fan 2-7 through a pipeline; the air outlets of the induced draft fans 2 to 7 are connected with a harmless gas evacuation header pipe; the gas inlet of the spray tower 2-1 is connected with the gas outlet of the gas-liquid separation tank 3-7 through a pipeline; a water outlet at the bottom of the spray tower 2-1 is connected with a water inlet of the spray tower drain valve 2-2 through a pipeline; the water outlet of the water discharge valve 2-2 of the spray tower is connected with the water inlet of the water feed pump 3-2 of the electrolytic bath through a pipeline; the water inlet of the spray pump 2-3 is connected with the water outlet at the side part of the spray tower 2-1 through a pipeline; the water outlet of the spray pump 2-3 is connected with the water inlet at the top of the spray tower 2-1 through a pipeline; a spraying atomization device is arranged at the top of the spraying tower 2-1; the discharge port of the catalyst tank 2-4 is connected with the feed port of the catalyst feed valve 2-5 through a pipeline; the discharge port of the catalyst feeding valve 2-5 is connected with the feed port of the catalyst feeding pump 2-6 through a pipeline; the discharge hole of the catalyst feeding pump 2-6 is connected with the water inlet at the top of the spray tower 2-1 through a pipeline; the water outlet of the spray tower feed pump 2-8 is connected with the water inlet at the top of the spray tower 2-1 through a pipeline;
the water outlet of the water feeding pump 3-2 of the electrolytic tank is connected with the water inlet of the plate frame electrolytic tank 3-3 through a pipeline; the water flow of the plate frame electrolytic cell 3-3 is in a parallel structure; the plate frame electrolytic cell 3-3 is in a series structure; bipolar plates are arranged in the plate frame electrolytic tank 3-3; the anode of the plate frame electrolytic cell 3-3 is connected with the anode of the direct current power supply 3-1 through a conductive copper beam; the cathode of the plate frame electrolytic cell 3-3 is connected with the cathode of the direct current power supply 3-1 through a conductive copper beam; the water outlet of the plate frame electrolytic tank 3-3 is connected with the liquid inlet of the fluidized bed electrolytic liquid inlet valve 3-4 through a pipeline; the liquid outlet of the fluidized bed electrolytic liquid inlet valve 3-4 is connected with the liquid inlet of the fluidized bed electrolytic tank 3-5 through a pipeline; a granular phase catalyst is arranged in the fluidized bed electrolytic tank 3-5; the anode of the fluidized bed electrolytic bath 3-5 is connected with the anode of the direct current power supply 3-1 through a conductive copper beam; the cathode of the fluidized bed electrolytic bath 3-5 is connected with the cathode of the direct current power supply 3-1 through a conductive copper beam; the liquid outlet of the fluidized bed electrolytic bath 3-5 is connected with the liquid inlet of the fluidized bed electrolytic liquid outlet valve 3-6 through a pipeline; the liquid outlet of the fluidized bed electrolysis liquid outlet valve 3-6 is connected with the liquid inlet of the gas-liquid separation tank 3-7 through a pipeline; the liquid outlet of the gas-liquid separation tank 3-7 is connected with the liquid inlet of the liquid discharge valve 3-8 of the separation tank through a pipeline; the liquid outlet of the separation tank liquid discharge valve 3-8 is connected with the liquid inlet of the adjusting tank liquid feeding pump 4-1 through a pipeline;
the liquid outlet of the adjusting tank liquid feeding pump 4-1 is connected with the liquid inlet of the adjusting tank 4-2 through a pipeline; the raw water inlet of the regulating tank 4-2 is connected with the water outlet of the regulating tank raw water pump 4-4 through a pipeline; a stirring paddle is arranged in the adjusting tank 4-2; the water outlet of the adjusting tank 4-2 is connected with the water inlet of the adjusting tank drain valve 4-3 through a pipeline; the water outlet of the regulating tank drain valve 4-3 is connected with the water outlet of the purified liquid delivery pump 4-5 through a pipeline; the liquid outlet of the purified liquid delivery pump 4-5 is connected with a purified liquid recycling header pipe;
the plate frame electrolytic tank 3-3 is provided with a heat exchange jacket, and a heat exchange medium is water or air; the fluidized bed electrolytic tank 3-5 is provided with a heat exchange jacket, and a heat exchange medium is water or air; a liquid outlet at the top of the fluidized bed electrolytic bath 3-5 is provided with a porous filtering membrane; the pore size is less than 100 microns. Heat is generated during the electrolysis process, which causes the electrolyte to heat up and be removed in the form of a heat exchange jacket. The porous filtering membrane is arranged, so that the catalyst can be prevented from being flushed out of the reactor.
The invention relates to a method for realizing wastewater recycling by removing ammonia nitrogen through three-dimensional electrolysis of a liquid-solid fluidized bed based on the system, which specifically comprises the following steps:
feeding the ammonia nitrogen wastewater into the gravity settling tank 1-1, and performing gravity settling to obtain supernatant and sludge; the sludge is discharged through a blow-down valve 1-2 of the settling tank and is sent for treatment; the supernatant is sent into the filter 1-4 through the filter water inlet pump 1-3 to obtain filtered supernatant and filtered sludge; the filtered sludge is discharged through the filter blow-down valve 1-5 and is sent for treatment; one part of the filtered clear liquid is sent into the spray tower 2-1 through the spray tower feeding pump 2-8; the other part of the filtered clear liquid is sent into the adjusting tank 4-2 through the adjusting tank raw water pump 4-4; the catalyst in the catalyst tank 2-4 is sent into the spray tower 2-1 through the catalyst feeding valve 2-5 and the catalyst feeding pump 2-6 in sequence; electrolytic gas generated by the electrolysis section 3 enters the spray tower 2-1 under the action of negative pressure; under the action of the circulating spraying of the spraying pump 2-3, filtering clear liquid and a catalyst are fully and uniformly mixed, and simultaneously, catalytic components in electrolytic gas are fully absorbed to obtain pretreated ammonia nitrogen wastewater and harmless gas; the residual harmless gas is evacuated through the induced draft fan 2-7;
the pretreated ammonia nitrogen wastewater in the spray tower 2-1 enters the plate frame electrolytic tank 3-3 through the electrolytic tank water feed pump 3-2, and ammonia nitrogen in the wastewater starts to decompose under the action of electrolysis; the energy for electrocatalytic oxidation in the plate-frame electrolytic cell 3-3 is provided by the direct-current power supply 3-1; the ammonia nitrogen wastewater after pre-decomposition enters the fluidized bed electrolytic bath 3-5 through the fluidized bed electrolytic liquid inlet valve 3-4, and the ammonia nitrogen wastewater is subjected to deep decomposition under the action of a particle catalyst; the energy for electrolysis in the fluidized bed electrolytic bath 3-5 is provided by the direct current power supply 3-1; gas generated by the advanced treatment of the ammonia nitrogen wastewater along with electrolysis enters the gas-liquid separation tank 3-7 through the fluidized bed electrolysis liquid outlet valve 3-6 to obtain purified liquid and electrolysis gas; electrolytic gas is sent into the spray tower 2-1; purified liquid sequentially passes through the separation tank liquid discharge valve 3-8 and the adjusting tank liquid feeding pump 4-1 and enters the adjusting tank 4-2; the raw water is uniformly mixed with the raw water from the regulating tank raw water pump 4-4, is regulated to a proper PH range, and is sent for reuse through a regulating tank drain valve 4-3 and a purifying liquid delivery pump 4-5 in sequence after meeting the water quality reuse standard;
the direct current power supply 3-1 has the function of cutting off the power supply when the instantaneous current is too high; the plate frame electrolytic tank 3-3 and the fluidized bed electrolytic tank 3-5 adopt a pulse electrolysis mode, the signal period is 3 seconds, and the duty ratio is 0.25.
One of the features of the present invention is: the catalyst in the spraying section 2 is soluble chloride solution, and the adding amount of the catalyst is 0.1-2% of the mass of the ammonia nitrogen wastewater.
The invention is characterized in that: the water flow in the plate frame electrolytic cell 3-3 is in a parallel structure, and the current is in a series structure.
The invention is characterized in that: the anode in the plate-frame electrolytic cell 3-3 adopts one of a platinum ruthenium iridium tantalum tin antimony manganese coating titanium electrode, a boron-doped diamond coating titanium electrode, a titanium suboxide coating titanium electrode, a lead and lead alloy electrode, a graphite electrode and the like; the cathode adopts one of a titanium electrode, a graphite electrode, a lead and lead alloy electrode and the like; the distance between the anode and the cathode is 2 mm-100 mm; the anode current density is 50-800A/m2。
The invention is characterized in that: the built-in electrode in the plate-and-frame electrolytic cell 3-3 adopts an integrated bipolar plate structure, wherein the coated titanium electrode adopts a single-sided active coating; the lead, lead alloy and graphite electrode are designed integrally by cathode and anode.
The fifth characteristic of the invention is: the anode in the fluidized bed electrolytic bath 3-5 adopts one of a platinum ruthenium iridium tantalum tin antimony manganese coating titanium electrode, a boron-doped diamond coating titanium electrode, a titanium suboxide coating titanium electrode, a lead and lead alloy electrode, a graphite electrode and the like; the cathode adopts one of a stainless steel electrode, a titanium electrode, a nickel electrode, a graphite electrode, an aluminum electrode and the like; the distance between the anode and the cathode is 2 mm-100 mm; the particle phase catalyst substrate is active carbon or zeolite molecular sieve, and the loaded catalytic component is one or more of platinum, ruthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and oxides of the substances; the particle size of the catalyst is 0.1 mm-5.0 mm; the current density of the anode is 50-3000A/m2。
The invention is characterized in that: the fluidized bed electrolytic tank 3-5 is provided with a porous liquid distribution plate, and the opening rate is 3% -15%; the operating linear velocity of the fluidized liquid is 0.1-5.0 m/min, and the bed expansion rate is 1.1-5.0.
The invention is characterized in that: in the fluidized bed electrolytic tank 3-5, the surface of the anode is provided with protrusions, the height of the protrusions is 0.2-0.5 mm, and the coverage rate of the protrusions is 20% -60%.
The invention is characterized in that: and a reticular porous plate is arranged in the fluidized bed electrolytic tank 3-5 and is used for covering the particle phase catalyst to prevent the particle phase catalyst from being taken away by fluid and influencing the catalytic effect. The aperture of the reticular porous plate is smaller than the particle size of the particle phase catalyst so as to ensure that the particle phase catalyst can be netted.
The invention is characterized in that: the adding amount of raw water in the water quality adjusting section 4 is 10-500% of the quality of the water body for electrolytic treatment.
The electrodes used in the present invention are all commercially available.
In the present invention, the mass of soluble chloride in the soluble chloride solution is calculated as the amount of catalyst added.
The ammonia nitrogen wastewater can be recycled and can also be directly treated to reach the discharge standard, and when the ammonia nitrogen wastewater is recycled, the ammonia nitrogen wastewater cannot be directly recycled due to overhigh concentration of the ammonia nitrogen, and generally needs to be treated and recycled. In the invention, the ammonia nitrogen wastewater is generally acidic after being electrolyzed, and the original ammonia nitrogen wastewater is generally alkaline, so that the pH value of the wastewater can be adjusted by mixing the ammonia nitrogen wastewater after being pre-purified and the ammonia nitrogen wastewater after being electrolyzed so as to meet the requirement of recycling.
In the present invention, the anode can be subjected to sand blasting treatment to form protrusions on the surface of the anode, and the wear of the particulate phase catalyst on the anode can be effectively suppressed.
Compared with the prior art, the invention has the following outstanding advantages:
(1) removing solid suspended matters in the ammonia nitrogen wastewater through gravity settling and filtering equipment to realize wastewater pre-purification;
(2) the full mixing of the catalyst and the ammonia nitrogen wastewater is realized through spraying treatment, and the catalytic components in the electrolytic gas are effectively utilized;
(3) the efficient cracking of ammonia nitrogen in the wastewater is realized through plate-frame electrolysis coupled with fluidized bed three-dimensional electrolysis;
(4) the raw water at the outlet of the filter is adopted to adjust the pH value of the electrolyzed solution, so that the wastewater recycling is realized at low cost;
(5) the modes of current series connection and water flow parallel connection are adopted in the plate-frame electrolysis, so that the water quality circulation is enhanced, the mass transfer efficiency is improved, and the decomposition of ammonia nitrogen is promoted;
(6) adding a particle phase catalyst in the fluidized bed electrolysis, greatly increasing the reaction area, strengthening mass transfer and further realizing the high-efficiency decomposition and removal of ammonia nitrogen; meanwhile, the surface of the anode is provided with the protrusions, so that the catalytic coating can be protected, and the abrasion of fluidized particles can be inhibited.
The invention efficiently combines plate-frame electrolysis and fluidized bed electrolysis, strengthens mass transfer, improves the electrode area and further realizes the efficient decomposition and removal of ammonia nitrogen. The method is suitable for large-scale and continuous treatment and recycling of ammonia nitrogen wastewater, and has the advantages of high efficiency, low energy consumption, no pollution, good economy and the like.
Drawings
FIG. 1 is a schematic configuration diagram of a system for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in a liquid-solid fluidized bed.
Reference numerals:
1, a filtering section:
1-1 gravity settling tank 1-2 settling tank blow-down valve
1-3 filter water inlet pump 1-4 filter
1-5 filter blow-down valves;
2, spraying section:
2-1 spray tower 2-2 spray tower drain valve
2-3 spray pump 2-4 catalyst tank
2-5 catalyst feed valve 2-6 catalyst feed pump
2-7 induced draft fans and 2-8 spray tower feed pumps;
3, electrolysis section:
3-1 DC power supply 3-2 electrolytic tank water-feeding pump
3-3 plate frame electrolytic bath 3-4 fluidized bed electrolysis liquid inlet valve
3-6 fluidized bed electrolytic liquid outlet valve of 3-5 fluidized bed electrolytic bath
3-7 gas-liquid separation tank 3-8 separation tank drain valve;
4, water quality adjusting section:
4-1 adjusting tank liquid feeding pump 4-2 adjusting tank
4-3 regulating tank drain valve 4-4 regulating tank raw water pump
4-5 purifying liquid delivery pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. It should be noted that the examples are only for illustrating the technical solutions of the present invention, and not for limiting the same. FIG. 1 is a schematic diagram of a system and a method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in a liquid-solid fluidized bed.
Example 1
With reference to fig. 1, the system for three-dimensionally removing ammonia nitrogen through electrolysis in a liquid-solid fluidized bed to recycle wastewater used in this embodiment includes a filtration section 1, a spraying section 2, an electrolysis section 3, and a water quality regulation section 4;
the filtering section 1 comprises a gravity settling tank 1-1, a settling tank blow-down valve 1-2, a filter water inlet pump 1-3, a filter 1-4 and a filter blow-down valve 1-5;
the spraying working section 2 comprises a spraying tower 2-1, a spraying tower drain valve 2-2, a spraying pump 2-3, a catalyst tank 2-4, a catalyst feed valve 2-5, a catalyst feed pump 2-6, an induced draft fan 2-7 and a spraying tower feed pump 2-8;
the electrolysis section 3 comprises a direct current power supply 3-1, an electrolytic bath water feeding pump 3-2, a plate frame electrolytic bath 3-3, a fluidized bed electrolysis liquid inlet valve 3-4, a fluidized bed electrolytic bath 3-5, a fluidized bed electrolysis liquid outlet valve 3-6, a gas-liquid separation tank 3-7 and a separation tank liquid outlet valve 3-8;
the water quality adjusting section 4 comprises an adjusting tank liquid feeding pump 4-1, an adjusting tank 4-2, an adjusting tank liquid discharging valve 4-3, an adjusting tank raw water pump 4-4 and a purified liquid conveying pump 4-5;
the liquid inlet of the gravity settling tank 1-1 is connected with an ammonia nitrogen wastewater main pipe; a sewage outlet at the bottom of the gravity settling tank 1-1 is connected with a feed inlet of a sewage valve 1-2 of the settling tank through a pipeline; the discharge hole of the sedimentation tank blow-down valve 1-2 is connected with a sludge treatment main pipe; a vertical liquid baffle plate is arranged in the gravity settling tank 1-1; the water outlet of the gravity settling tank 1-1 is connected with the water inlet of the filter water inlet pump 1-3 through a pipeline; the water outlet of the filter water inlet pump 1-3 is connected with the water inlet of the filter 1-4 through a pipeline; a filter screen or quartz sand is filled in the filter 1-4; the drain outlet at the bottom of the filter 1-4 is connected with the feed inlet of the filter drain valve 1-5 through a pipeline; the discharge ports of the filter blow-down valves 1-5 are connected with a sludge treatment main pipe; the water outlets of the filters 1 to 4 are respectively connected with the feed inlets of the spray tower feed pumps 2 to 8 and the water inlets of the regulating tank raw water pumps 4 to 4 through pipelines;
the gas outlet of the spray tower 2-1 is connected with the gas inlet of the induced draft fan 2-7 through a pipeline; the air outlets of the induced draft fans 2 to 7 are connected with a harmless gas evacuation header pipe; the gas inlet of the spray tower 2-1 is connected with the gas outlet of the gas-liquid separation tank 3-7 through a pipeline; a water outlet at the bottom of the spray tower 2-1 is connected with a water inlet of a water discharge valve 2-2 of the spray tower through a pipeline; the water outlet of the water discharge valve 2-2 of the spray tower is connected with the water inlet of the water feed pump 3-2 of the electrolytic bath through a pipeline; the water inlet of the spray pump 2-3 is connected with the water outlet at the side part of the spray tower 2-1 through a pipeline; the water outlet of the spray pump 2-3 is connected with the water inlet at the top of the spray tower 2-1 through a pipeline; a spraying atomization device is arranged at the top of the spraying tower 2-1; the discharge port of the catalyst tank 2-4 is connected with the feed port of the catalyst feed valve 2-5 through a pipeline; the discharge port of the catalyst feeding valve 2-5 is connected with the feed port of the catalyst feeding pump 2-6 through a pipeline; a discharge hole of the catalyst feeding pump 2-6 is connected with a water inlet at the top of the spray tower 2-1 through a pipeline; the water outlet of the feeding pump 2-8 of the spray tower is connected with the water inlet at the top of the spray tower 2-1 through a pipeline;
the water outlet of the water feeding pump 3-2 of the electrolytic tank is connected with the water inlet of the plate frame electrolytic tank 3-3 through a pipeline; the water flow of the plate frame electrolytic cell 3-3 is in a parallel structure; the plate frame electrolytic cell 3-3 is in a series structure; a bipolar plate is arranged in the plate frame electrolytic tank 3-3; the anode of the plate frame electrolytic cell 3-3 is connected with the anode of the direct current power supply 3-1 through a conductive copper beam; the cathode of the plate frame electrolytic cell 3-3 is connected with the cathode of the direct current power supply 3-1 through a conductive copper beam; the water outlet of the plate frame electrolytic bath 3-3 is connected with the liquid inlet of the fluidized bed electrolytic liquid inlet valve 3-4 through a pipeline; the liquid outlet of the fluidized bed electrolytic liquid inlet valve 3-4 is connected with the liquid inlet of the fluidized bed electrolytic bath 3-5 through a pipeline; a granular phase catalyst is arranged in the fluidized bed electrolytic tank 3-5; the anode of the fluidized bed electrolytic bath 3-5 is connected with the anode of the direct current power supply 3-1 through a conductive copper beam; the cathode of the fluidized bed electrolytic bath 3-5 is connected with the cathode of the direct current power supply 3-1 through a conductive copper beam; the liquid outlet of the fluidized bed electrolytic bath 3-5 is connected with the liquid inlet of the fluidized bed electrolytic liquid outlet valve 3-6 through a pipeline; the liquid outlet of the fluidized bed electrolysis liquid outlet valve 3-6 is connected with the liquid inlet of the gas-liquid separation tank 3-7 through a pipeline; the liquid outlet of the gas-liquid separation tank 3-7 is connected with the liquid inlet of a liquid discharge valve 3-8 of the separation tank through a pipeline; the liquid outlet of the liquid discharge valve 3-8 of the separation tank is connected with the liquid inlet of the liquid feeding pump 4-1 of the adjusting tank through a pipeline;
the liquid outlet of the adjusting tank liquid feeding pump 4-1 is connected with the liquid inlet of the adjusting tank 4-2 through a pipeline; the raw water inlet of the regulating tank 4-2 is connected with the water outlet of the regulating tank raw water pump 4-4 through a pipeline; a stirring paddle is arranged in the adjusting tank 4-2; the water outlet of the adjusting tank 4-2 is connected with the water inlet of the adjusting tank drain valve 4-3 through a pipeline; the water outlet of the adjusting tank drain valve 4-3 is connected with the water outlet of the purifying liquid delivery pump 4-5 through a pipeline; the liquid outlet of the purified liquid delivery pump 4-5 is connected with the purified liquid recycling header pipe.
The plate frame electrolytic tank 3-3 is provided with a heat exchange jacket; the fluidized bed electrolytic tank 3-5 is provided with a heat exchange jacket; and a liquid outlet at the top of the fluidized bed electrolytic tank 3-5 is provided with a porous filtering membrane.
The plate frame electrolytic tank 3-3 is provided with a heat exchange jacket, and a heat exchange medium is water or air; the fluidized bed electrolytic tank 3-5 is provided with a heat exchange jacket, and a heat exchange medium is water or air; a liquid outlet at the top of the fluidized bed electrolytic bath 3-5 is provided with a porous filtering membrane; the pore size is less than 100 microns.
Example 2
In this embodiment, the method for realizing wastewater recycling by removing ammonia nitrogen through three-dimensional electrolysis in a liquid-solid fluidized bed of the system in embodiment 1 comprises the following steps:
feeding the ammonia nitrogen wastewater into a gravity settling tank 1-1, and performing gravity settling to obtain supernatant and sludge; the sludge is discharged through a blow-down valve 1-2 of a settling tank and is sent for treatment; the supernatant is sent into a filter 1-4 through a filter water inlet pump 1-3 to obtain filtered supernatant and filtered sludge; the filtered sludge is discharged through a filter blow-down valve 1-5 and is sent for treatment; one part of the filtered clear liquid is sent into a spray tower 2-1 through a spray tower feed pump 2-8; the other part of the filtered clear liquid is sent into an adjusting tank 4-2 through an adjusting tank raw water pump 4-4; the catalyst in the catalyst tank 2-4 is sent into the spray tower 2-1 through a catalyst feeding valve 2-5 and a catalyst feeding pump 2-6 in sequence; electrolytic gas generated in the electrolysis section 3 enters the spray tower 2-1 under the action of negative pressure; under the action of circulating spraying of a spraying pump 2-3, filtering clear liquid and a catalyst are fully and uniformly mixed, and meanwhile, catalytic components in electrolytic gas are fully absorbed, so that pretreated wastewater and harmless gas are obtained; the residual harmless gas is evacuated through an induced draft fan 2-7;
the ammonia nitrogen wastewater in the pretreatment in the spray tower 2-1 enters a plate frame electrolytic cell 3-3 through an electrolytic cell feed pump 3-2, and ammonia nitrogen in the wastewater starts to decompose under the action of electrolysis; the energy for electrocatalytic oxidation in the plate-frame electrolytic cell 3-3 is provided by a direct-current power supply 3-1; the ammonia nitrogen wastewater after pre-decomposition enters a fluidized bed electrolytic bath 3-5 through a fluidized bed electrolytic liquid inlet valve 3-4, and the ammonia nitrogen wastewater is subjected to deep decomposition under the action of a particle catalyst; the energy for electrolysis in the fluidized bed electrolytic bath 3-5 is provided by a direct current power supply 3-1; the gas generated by the advanced treatment of the ammonia nitrogen wastewater along with electrolysis enters a gas-liquid separation tank 3-7 through a fluidized bed electrolysis liquid outlet valve 3-6 to obtain purified liquid and electrolysis gas; sending the electrolytic gas into a spray tower 2-1; purified liquid sequentially passes through a separation tank liquid discharge valve 3-8 and a regulating tank liquid feeding pump 4-1 and enters a regulating tank 4-2; uniformly mixing with raw water from a raw water pump 4-4 of an adjusting tank, adjusting the mixture to a proper PH range, and sending the mixture to be recycled through a drain valve 4-3 of the adjusting tank and a purified liquid delivery pump 4-5 in sequence after the mixture meets the water quality recycling standard; the direct current power supply 3-1 has the function of cutting off the power supply when the instantaneous current is too high; the plate frame electrolytic tank 3-3 and the fluidized bed electrolytic tank 3-5 adopt a pulse electrolysis mode, the signal period is 3 seconds, and the duty ratio is 0.25.
Example 3
In the embodiment, printing and dyeing wastewater of a certain enterprise is taken as a treatment object, and the treatment capacity is 15m3And h, the initial value of ammonia nitrogen is 10000. In the spraying section 2, the catalyst is sodium chloride solution, and the adding amount of the catalyst is 2% of the mass of the ammonia nitrogen wastewater. The water flow in the plate frame electrolytic cell 3-3 is in a parallel structure, and the current is in a series structure. The anode in the plate-frame electrolytic cell 3-3 adopts a platinum ruthenium iridium tantalum tin antimony manganese coating titanium electrode; the cathode adopts a titanium electrode; the distance between the anode and the cathode is 2 mm; the anode current density is 800A/m2. The built-in electrode in the plate frame electrolytic cell 3-3 adopts an integrated bipolar plate structure, and the coated titanium electrode adopts a single-sided active coating. The anode in the fluidized bed electrolytic tank 3-5 adopts a platinum ruthenium iridium tantalum tin antimony manganese coating titanium electrode; the cathode adopts a stainless steel electrode; the distance between the anode and the cathode is 2 mm; the particle phase catalyst substrate is active carbon, and the loaded catalytic components are platinum, ruthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and one or more of the mixtures; the catalyst particle size was 0.1 mm; the anode current density is 3000A/m2. A porous liquid distribution plate is arranged in the fluidized bed electrolytic tank 3-5, and the opening rate is 3%; the operating linear velocity of the fluidized liquid is 0.1m/min, and the bed expansion rate is 1.1. In the fluidized bed electrolytic tank 3-5, the surface of the anode is designed with protrusions, the height of the protrusions is 0.2mm, and the coverage rate of the protrusions is 60%. The ammonia nitrogen wastewater is treated by the working sections of filtering, spraying and electrolyzing, and the ammonia nitrogen removal rate is 90 percent. The adding amount of raw water in the water quality adjusting section 4 is 10 percent of the quality of the water body for electrolytic treatment. The water is sent for reuse after being regulated.
Example 4
In the embodiment, landfill leachate of a certain enterprise is taken as a treatment object, and the treatment capacity is 1m3The initial value of ammonia nitrogen is 1000. Catalyst in spray section 2Is calcium chloride solution, and the adding amount of the catalyst is 0.1 percent of the mass of the ammonia nitrogen wastewater. The water flow in the plate frame electrolytic cell 3-3 is in a parallel structure, and the current is in a series structure. The anode in the plate-frame electrolytic cell 3-3 adopts a boron-doped diamond coating titanium electrode; the cathode adopts a titanium electrode; the distance between the cathode and the anode is 100 mm; the anode current density is 50A/m2. The built-in electrode in the plate frame electrolytic cell 3-3 adopts an integrated bipolar plate structure, and the coated titanium electrode adopts a single-sided active coating. The anode in the fluidized bed electrolytic bath 3-5 adopts a boron-doped diamond coating titanium electrode; the cathode adopts a titanium electrode; the distance between the cathode and the anode is 100 mm; the particle phase catalyst substrate is a zeolite molecular sieve, and the loaded catalytic components are a mixture of substances such as platinum, ruthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and the like; the catalyst particle size was 5.0 mm; the anode current density is 50A/m2. The fluidized bed electrolytic tank 3-5 is provided with a porous liquid distribution plate, and the opening rate is 15%; the operating linear velocity of the fluidized liquid is 5.0m/min, and the bed expansion rate is 5.0. In the fluidized bed electrolytic tank 3-5, the surface of the anode is designed with protrusions, the height of the protrusions is 0.5mm, and the coverage rate of the protrusions is 20%. The ammonia nitrogen wastewater is treated by the working sections of filtering, spraying and electrolyzing, and the ammonia nitrogen removal rate is 90 percent. The adding amount of raw water in the water quality adjusting section 4 is 500 percent of the quality of the water body for electrolytic treatment. The water is sent for reuse after being regulated.
Example 5
In the embodiment, the activated carbon washing wastewater of a certain enterprise is taken as a treatment object, and the treatment capacity is 10m3The initial value of ammonia nitrogen is 8000. In the spraying section 2, the catalyst is magnesium chloride solution, and the adding amount of the catalyst is 1 percent of the mass of the ammonia nitrogen wastewater. The water flow in the plate frame electrolytic cell 3-3 is in a parallel structure, and the current is in a series structure. The anode in the plate-frame electrolytic cell 3-3 adopts a titanium electrode with a titanium suboxide coating; the cathode adopts a titanium electrode; the distance between the anode and the cathode is 10 mm; the anode current density is 200A/m2. The built-in electrode in the plate frame electrolytic cell 3-3 adopts an integrated bipolar plate structure, and the coated titanium electrode adopts a single-sided active coating. The anode in the fluidized bed electrolytic tank 3-5 adopts a titanium electrode with a titanium suboxide coating; the cathode adopts a nickel electrode; the distance between the anode and the cathode is 10 mm; the granular phase catalyst matrix is active carbon, and the supported catalytic component is platinumRuthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and the like; the catalyst particle size was 0.5 mm; the anode current density is 200A/m2. The fluidized bed electrolytic tank 3-5 is provided with a porous liquid distribution plate, and the opening rate is 5%; the operating linear velocity of the fluidized liquid is 1.0m/min, and the bed expansion rate is 1.3. In the fluidized bed electrolytic tank 3-5, the surface of the anode is designed with protrusions, the height of the protrusions is 0.3mm, and the coverage rate of the protrusions is 50%. The ammonia nitrogen wastewater is treated by the working sections of filtering, spraying and electrolyzing, and the ammonia nitrogen removal rate is 87.5 percent. The adding amount of raw water in the water quality adjusting section 4 is 50 percent of the quality of the water body for electrolytic treatment. The water is sent for reuse after being regulated.
Example 6
The embodiment takes bottle washing wastewater of a certain enterprise as a treatment object, and the treatment capacity is 5m3The initial COD value was 5000. In the spraying section 2, the catalyst is sodium chloride solution, and the adding amount of the catalyst is 1 percent of the mass of the ammonia nitrogen wastewater. The water flow in the plate frame electrolytic cell 3-3 is in a parallel structure, and the current is in a series structure. The anode in the plate-frame electrolytic cell 3-3 adopts a lead alloy electrode; the cathode adopts a lead alloy electrode; the distance between the anode and the cathode is 10 mm; the anode current density is 200A/m2. The built-in electrodes in the plate frame electrolytic cell 3-3 adopt an integrated lead alloy bipolar plate structure. The anode in the fluidized bed electrolytic tank 3-5 adopts a lead alloy electrode; the cathode adopts a graphite electrode; the distance between the anode and the cathode is 10 mm; the particle phase catalyst substrate is active carbon, and the loaded catalytic components are mixtures of substances such as platinum, ruthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and the like; the catalyst particle size was 0.5 mm; the anode current density is 200A/m2. The fluidized bed electrolytic tank 3-5 is provided with a porous liquid distribution plate, and the opening rate is 5%; the operating linear velocity of the fluidized liquid is 1.0m/min, and the bed expansion rate is 1.3. In the fluidized bed electrolytic tank 3-5, the surface of the anode is designed with protrusions, the height of the protrusions is 0.3mm, and the coverage rate of the protrusions is 50%. The ammonia nitrogen wastewater is treated by the working sections of filtering, spraying and electrolyzing, and the ammonia nitrogen removal rate is 95 percent. The adding amount of raw water in the water quality adjusting section 4 is 200 percent of the quality of the water body for electrolytic treatment. The water is sent for reuse after being regulated.
Example 7
This implementationFor example, waste water from a certain refuse transfer station is treated with a treatment capacity of 1m3The initial COD value was 3000/h. In the spraying section 2, the catalyst is sodium chloride solution, and the adding amount of the catalyst is 1 percent of the mass of the ammonia nitrogen wastewater. The current in the plate frame electrolytic cell 3-3 is in a series structure. The anode in the plate frame electrolytic cell 3-3 adopts a graphite electrode; the cathode adopts a graphite electrode; the distance between the anode and the cathode is 10 mm; the anode current density is 200A/m2. The built-in electrodes in the plate frame electrolytic cell 3-3 adopt an integrated lead alloy bipolar plate structure. The anode in the fluidized bed electrolytic tank 3-5 adopts a graphite electrode; the cathode adopts an aluminum electrode; the distance between the anode and the cathode is 10 mm; the particle phase catalyst substrate is active carbon, and the loaded catalytic components are mixtures of substances such as platinum, ruthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and the like; the catalyst particle size was 0.5 mm; the anode current density is 200A/m2. The fluidized bed electrolytic tank 3-5 is provided with a porous liquid distribution plate, and the opening rate is 5%; the operating linear velocity of the fluidized liquid is 1.0m/min, and the bed expansion rate is 1.3. In the fluidized bed electrolytic tank 3-5, the surface of the anode is designed with protrusions, the height of the protrusions is 0.3mm, and the coverage rate of the protrusions is 50%. The ammonia nitrogen wastewater is treated by the working sections of filtering, spraying and electrolyzing, and the ammonia nitrogen removal rate is 97 percent. The adding amount of raw water in the water quality adjusting section 4 is 150 percent of the quality of the water body for electrolytic treatment. The water is sent for reuse after being regulated.
The invention has not been described in detail and is within the skill of the art.
The present invention may be embodied in many different forms and modifications may be effected therein by one skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.

Claims (9)

1. A system for realizing wastewater recycling by three-dimensional electrolysis and ammonia nitrogen removal of a liquid-solid fluidized bed is characterized by comprising a filtering working section (1), a spraying working section (2), an electrolysis working section (3) and a water quality adjusting working section (4);
the filtering section (1) comprises a gravity settling tank (1-1), a settling tank blow-down valve (1-2), a filter water inlet pump (1-3), a filter (1-4) and a filter blow-down valve (1-5);
the spraying working section (2) comprises a spraying tower (2-1), a spraying tower drain valve (2-2), a spraying pump (2-3), a catalyst tank (2-4), a catalyst feeding valve (2-5), a catalyst feeding pump (2-6), an induced draft fan (2-7) and a spraying tower feeding pump (2-8);
the electrolysis section (3) comprises a direct-current power supply (3-1), an electrolysis bath water feed pump (3-2), a plate frame electrolysis bath (3-3), a fluidized bed electrolysis liquid inlet valve (3-4), a fluidized bed electrolysis bath (3-5), a fluidized bed electrolysis liquid outlet valve (3-6), a gas-liquid separation tank (3-7) and a separation tank liquid outlet valve (3-8);
the water quality adjusting section (4) comprises an adjusting tank liquid feeding pump (4-1), an adjusting tank (4-2), an adjusting tank liquid discharging valve (4-3), an adjusting tank raw water pump (4-4) and a purified liquid conveying pump (4-5);
the liquid inlet of the gravity settling tank (1-1) is connected with an ammonia nitrogen wastewater main pipe; a sewage outlet at the bottom of the gravity settling tank (1-1) is connected with a feed inlet of the settling tank sewage valve (1-2) through a pipeline; the discharge hole of the sedimentation tank blow-down valve (1-2) is connected with a sludge treatment main pipe; a vertical liquid baffle plate is arranged in the gravity settling tank (1-1); the water outlet of the gravity settling tank (1-1) is connected with the water inlet of the filter water inlet pump (1-3) through a pipeline; the water outlet of the filter water inlet pump (1-3) is connected with the water inlet of the filter (1-4) through a pipeline; a filter screen is arranged in the filter (1-4) or quartz sand is filled in the filter; a sewage discharge port at the bottom of the filter (1-4) is connected with a feed inlet of the filter sewage discharge valve (1-5) through a pipeline; the discharge hole of the filter blow-down valve (1-5) is connected with a sludge treatment main pipe; the water outlets of the filters (1-4) are respectively connected with the feed inlets of the spray tower feed pumps (2-8) and the water inlets of the regulating tank raw water pumps (4-4) through pipelines;
the air outlet of the spray tower (2-1) is connected with the air inlet of the induced draft fan (2-7) through a pipeline; the air outlet of the induced draft fan (2-7) is connected with a harmless gas evacuation header pipe; the gas inlet of the spray tower (2-1) is connected with the gas outlet of the gas-liquid separation tank (3-7) through a pipeline; a water outlet at the bottom of the spray tower (2-1) is connected with a water inlet of a drain valve (2-2) of the spray tower through a pipeline; the water outlet of the spray tower drain valve (2-2) is connected with the water inlet of the electrolytic bath water supply pump (3-2) through a pipeline; a water inlet of the spray pump (2-3) is connected with a water outlet at the side part of the spray tower (2-1) through a pipeline; the water outlet of the spray pump (2-3) is connected with the water inlet at the top of the spray tower (2-1) through a pipeline; the top of the spray tower (2-1) is provided with a spray atomization device; the discharge hole of the catalyst tank (2-4) is connected with the feed hole of the catalyst feed valve (2-5) through a pipeline; the discharge port of the catalyst feeding valve (2-5) is connected with the feed port of the catalyst feeding pump (2-6) through a pipeline; the discharge hole of the catalyst feeding pump (2-6) is connected with the water inlet at the top of the spray tower (2-1) through a pipeline; the water outlet of the spray tower feed pump (2-8) is connected with the water inlet at the top of the spray tower (2-1) through a pipeline;
the water outlet of the electrolytic bath water feed pump (3-2) is connected with the water inlet of the plate frame electrolytic bath (3-3) through a pipeline; the water flow of the plate frame electrolytic cell (3-3) is in a parallel structure; the current of the plate frame electrolytic cell (3-3) is in a series structure; bipolar plates are arranged in the plate frame electrolytic tank (3-3); the anode of the plate frame electrolytic cell (3-3) is connected with the anode of the direct current power supply (3-1) through a conductive copper beam; the cathode of the plate frame electrolytic cell (3-3) is connected with the cathode of the direct current power supply (3-1) through a conductive copper beam; the water outlet of the plate frame electrolytic tank (3-3) is connected with the liquid inlet of the fluidized bed electrolytic liquid inlet valve (3-4) through a pipeline; the liquid outlet of the fluidized bed electrolytic liquid inlet valve (3-4) is connected with the liquid inlet of the fluidized bed electrolytic tank (3-5) through a pipeline; a granular phase catalyst is arranged in the fluidized bed electrolytic tank (3-5); the anode of the fluidized bed electrolytic tank (3-5) is connected with the anode of the direct current power supply (3-1) through a conductive copper beam; the cathode of the fluidized bed electrolytic tank (3-5) is connected with the cathode of the direct current power supply (3-1) through a conductive copper beam; the liquid outlet of the fluidized bed electrolytic bath (3-5) is connected with the liquid inlet of the fluidized bed electrolytic liquid outlet valve (3-6) through a pipeline; the liquid outlet of the fluidized bed electrolysis liquid outlet valve (3-6) is connected with the liquid inlet of the gas-liquid separation tank (3-7) through a pipeline; the liquid outlet of the gas-liquid separation tank (3-7) is connected with the liquid inlet of the liquid discharge valve (3-8) of the separation tank through a pipeline; the liquid outlet of the separation tank liquid discharge valve (3-8) is connected with the liquid inlet of the adjusting tank liquid feeding pump (4-1) through a pipeline;
the liquid outlet of the adjusting tank liquid feeding pump (4-1) is connected with the liquid inlet of the adjusting tank (4-2) through a pipeline; the raw water inlet of the regulating tank (4-2) is connected with the water outlet of the raw water pump (4-4) of the regulating tank through a pipeline; a stirring paddle is arranged in the adjusting tank (4-2); the water outlet of the adjusting tank (4-2) is connected with the water inlet of the adjusting tank drain valve (4-3) through a pipeline; the water outlet of the regulating tank drain valve (4-3) is connected with the water outlet of the purified liquid delivery pump (4-5) through a pipeline; the liquid outlet of the purified liquid delivery pump (4-5) is connected with a purified liquid recycling header pipe;
a porous liquid distribution plate is arranged in the fluidized bed electrolytic tank (3-5), and the aperture ratio is 3% -15%; the operating linear velocity of the fluidized liquid is 0.1-5.0 m/min, and the bed expansion rate is 1.1-5.0; in the fluidized bed electrolytic tank (3-5), the surface of the anode is provided with protrusions, the height of the protrusions is 0.2-0.5 mm, and the protrusion coverage rate is 20% -60%.
2. A method for realizing wastewater recycling by removing ammonia nitrogen through three-dimensional electrolysis of a liquid-solid fluidized bed based on the system of claim 1 comprises the following steps:
feeding the ammonia nitrogen wastewater into the gravity settling tank (1-1), and performing gravity settling to obtain supernatant and sludge; the sludge is discharged through a blow-down valve (1-2) of the settling tank and is sent for treatment; the supernatant is sent into the filter (1-4) through the filter water inlet pump (1-3) to obtain filtered supernatant and filtered sludge; the filtered sludge is discharged through the filter blow-down valve (1-5) and is sent for treatment; one part of the filtered clear liquid is sent into the spray tower (2-1) through the spray tower feeding pump (2-8); the other part of the filtered clear liquid is sent into the adjusting tank (4-2) through the adjusting tank raw water pump (4-4); the catalyst in the catalyst tank (2-4) is sent into the spray tower (2-1) through the catalyst feeding valve (2-5) and the catalyst feeding pump (2-6) in sequence; electrolytic gas generated by the electrolysis section (3) enters the spray tower (2-1) under the action of negative pressure; under the action of the circulating spraying of the spraying pump (2-3), filtering clear liquid and a catalyst are fully and uniformly mixed, and simultaneously, catalytic components in electrolytic gas are fully absorbed to obtain pretreated ammonia nitrogen wastewater and harmless gas; harmless gas is evacuated through the induced draft fan (2-7);
the pretreated ammonia nitrogen wastewater in the spray tower (2-1) enters the plate frame electrolytic tank (3-3) through the electrolytic tank water feed pump (3-2), and ammonia nitrogen in the wastewater starts to decompose under the action of electrolysis; the energy for electrocatalytic oxidation in the plate-frame electrolytic cell (3-3) is provided by the direct current power supply (3-1); the ammonia nitrogen wastewater after pre-decomposition enters the fluidized bed electrolytic bath (3-5) through the fluidized bed electrolytic liquid inlet valve (3-4), and the ammonia nitrogen wastewater is subjected to deep decomposition under the action of a particle catalyst; the energy for electrolysis in the fluidized bed electrolytic bath (3-5) is provided by the direct current power supply (3-1); gas generated by the advanced treatment of the ammonia nitrogen wastewater along with electrolysis enters the gas-liquid separation tank (3-7) through the fluidized bed electrolysis liquid outlet valve (3-6) to obtain purified liquid and electrolysis gas; the electrolytic gas is sent into the spray tower (2-1); purified liquid sequentially passes through the separation tank liquid discharge valve (3-8) and the adjusting tank liquid feeding pump (4-1) and enters the adjusting tank (4-2); the water is uniformly mixed with raw water from the regulating tank raw water pump (4-4), the mixture is regulated to a proper PH range, and after the water quality recycling standard is met, the mixture is sent for recycling through the regulating tank drain valve (4-3) and the purified liquid delivery pump (4-5) in sequence.
3. The method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen through a liquid-solid fluidized bed according to claim 2, wherein the catalyst in the spraying section (2) is a soluble chloride solution, and the addition amount of the catalyst is 0.1-2% of the mass of the ammonia nitrogen wastewater.
4. The method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen through a liquid-solid fluidized bed according to claim 2, characterized in that water flows in the plate frame electrolytic cell (3-3) are in a parallel structure and current is in a series structure.
5. The method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen through a liquid-solid fluidized bed according to claim 2, characterized in that the plate-frame electrolytic tank (3-3) is provided with a heat exchange jacket, and a heat exchange medium is water or air; the fluidized bed electrolytic tank (3-5) is provided with a heat exchange jacket, and a heat exchange medium is water or air; a liquid outlet at the top of the fluidized bed electrolytic tank (3-5) is provided with a porous filtering membrane; the pore size is less than 100 microns.
6. The method for realizing wastewater reuse by three-dimensional electrolytic removal of ammonia nitrogen through a liquid-solid fluidized bed according to claim 2, wherein the anode in the plate-and-frame electrolytic cell (3-3) is one of a platinum ruthenium iridium tantalum tin antimony manganese coating titanium electrode, a boron-doped diamond coating titanium electrode, a titanium suboxide coating titanium electrode, a lead and lead alloy electrode and a graphite electrode; the cathode adopts one of a titanium electrode, a graphite electrode, lead and a lead alloy electrode; the distance between the anode and the cathode is 2 mm-100 mm; the anode current density is 50-800A/m2。
7. The method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen through a liquid-solid fluidized bed according to claim 2, characterized in that an integrated bipolar plate structure is adopted as a built-in electrode in the plate frame electrolytic cell (3-3), wherein a single-sided active coating is adopted as a coating titanium electrode; the lead, lead alloy and graphite electrode are designed integrally by cathode and anode.
8. The method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen through liquid-solid fluidized bed according to claim 2The method is characterized in that the anode in the fluidized bed electrolytic bath (3-5) adopts one of a platinum ruthenium iridium tantalum tin antimony manganese coating titanium electrode, a boron-doped diamond coating titanium electrode, a titanium suboxide coating titanium electrode, a lead and lead alloy electrode and a graphite electrode; the cathode adopts one of a stainless steel electrode, a titanium electrode, a nickel electrode, a graphite electrode and an aluminum electrode; the distance between the anode and the cathode is 2 mm-100 mm; the particle phase catalyst substrate is active carbon or zeolite molecular sieve, and the loaded catalytic component is one or more of platinum, ruthenium, iridium, tantalum, tin, antimony, lead, manganese, cobalt, lanthanum, cerium, titanium and oxides thereof; the particle size of the catalyst is 0.1 mm-5.0 mm; the current density of the anode is 50-3000A/m2。
9. The method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen through a liquid-solid fluidized bed according to claim 2, wherein the addition amount of raw water in the water quality adjusting section (4) is 10-500% of the quality of an electrolytic treatment water body.
CN202011017204.8A 2020-09-24 2020-09-24 System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed Active CN112374664B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202011017204.8A CN112374664B (en) 2020-09-24 2020-09-24 System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202011017204.8A CN112374664B (en) 2020-09-24 2020-09-24 System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed

Publications (2)

Publication Number Publication Date
CN112374664A CN112374664A (en) 2021-02-19
CN112374664B true CN112374664B (en) 2022-03-08

Family

ID=74586572

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202011017204.8A Active CN112374664B (en) 2020-09-24 2020-09-24 System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed

Country Status (1)

Country Link
CN (1) CN112374664B (en)

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH08187419A (en) * 1995-01-06 1996-07-23 Toshiba Corp Waste gas treatment and device therefor
CN102417260B (en) * 2011-10-14 2013-04-10 朗照技术(北京)有限公司 Treating method for landfill leachate
CN103539316B (en) * 2013-10-14 2014-12-10 褚衍洋 Process for simultaneously processing high-concentration waste emulsion, pickling waste liquid, and waste lye
CN105540952B (en) * 2015-12-31 2018-04-13 中新环科（天津）科技有限公司 Murexide waste water treatment process
CN107098513B (en) * 2017-04-28 2021-01-01 浙江奇彩环境科技股份有限公司 Method for treating high-concentration morpholine wastewater
CN207645869U (en) * 2017-11-30 2018-07-24 江苏云瑞环境科技股份有限公司 A kind of pharmaceutical wastewater apparatus for electrochemical treatment
CN108101163B (en) * 2017-12-21 2020-11-03 衢州华友钴新材料有限公司 Method for recovering valuable metals and reducing ammonia nitrogen and COD (chemical oxygen demand) from industrial wastewater
CN210001729U (en) * 2019-04-17 2020-01-31 山东碧宇环保工程有限公司 purifying tanks suitable for decentralized sewage treatment
CN111410345A (en) * 2020-04-20 2020-07-14 深圳市世清环保科技有限公司 Method and system for treating comprehensive wastewater generated by anodic oxidation process

Also Published As

Publication number Publication date
CN112374664A (en) 2021-02-19

Similar Documents

Publication Publication Date Title
Li et al. Three-dimensional particle electrode system treatment of organic wastewater: A general review based on patents
CN112374663B (en) System and method for treating organic wastewater by three-dimensional electrocatalytic oxidation of liquid-solid fluidized bed
CN101691251A (en) Electric catalysis reactor capable of reducing side reaction for wastewater treatment
CN101077801A (en) Fluid bed three-dimensional electrode reactor for treating organic waste water
CN102992523A (en) Reverse osmosis concentrated wastewater treatment method
CN105906116A (en) Fluidized bed photocatalytic three-dimensional electrolytic reactor and application thereof
CN113105028B (en) System and method for realizing organic wastewater recycling by three-dimensional electrolytic removal of organic matters through liquid-solid fluidized bed
CN202400887U (en) Three-dimensional particle electrolytic catalytic oxidation sewage treating device
CN113735227A (en) Aeration type three-dimensional electro-Fenton fluidized bed
Xiong et al. Removal of formic acid from wastewater using three-phase three-dimensional electrode reactor
CN112374664B (en) System and method for realizing wastewater recycling by three-dimensional electrolytic removal of ammonia nitrogen in liquid-solid fluidized bed
CN113105029B (en) System and method for treating ammonia nitrogen wastewater by three-dimensional electrocatalytic oxidation of liquid-solid fluidized bed
CN111333235A (en) Landfill leachate treatment system and process
CN107162119B (en) Method and device for three-dimensional electrolysis of fully-mixed flow wastewater
CN203625090U (en) Electrocatalytic wastewater treatment system
CN202400888U (en) Device for treating sewage through advanced oxidation
CN107986519A (en) A kind of electro-catalysis and photocatalysis sewage processing method
CN212504150U (en) Electrocatalytic oxidation device and wastewater treatment system
CN212102375U (en) Gas field high concentration organic waste water electrochemical coupling treatment recycling device
CN203699987U (en) Wastewater treatment system
CN107935126B (en) Up-flow three-dimensional electro-catalytic device
CN202170260U (en) Iron-carbon micro-electrolysis device
CN202519116U (en) Mobile water treatment system
CN107758805B (en) Electrocatalytic particles for treating cyanide-containing wastewater and electrocatalytic oxidation method
CN204752289U (en) Little electrolysis reaction unit of continuous flow based on indisputable carbon filler of module formula improvement

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant