CN111977862A - Equipment and method for preparing industrial bactericide by utilizing tail-end wastewater of thermal power plant - Google Patents
Equipment and method for preparing industrial bactericide by utilizing tail-end wastewater of thermal power plant Download PDFInfo
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- CN111977862A CN111977862A CN202010809865.8A CN202010809865A CN111977862A CN 111977862 A CN111977862 A CN 111977862A CN 202010809865 A CN202010809865 A CN 202010809865A CN 111977862 A CN111977862 A CN 111977862A
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Images
Classifications
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- 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
-
- 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
- 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
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F2001/46133—Electrodes characterised by the material
-
- 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
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
- C02F2001/46133—Electrodes characterised by the material
- C02F2001/46138—Electrodes comprising a substrate and a coating
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- 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
- C02F2101/12—Halogens or halogen-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/04—Oxidation reduction potential [ORP]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
Abstract
The invention discloses equipment for preparing an industrial bactericide by utilizing tail-end wastewater of a thermal power plant, which comprises a wastewater regulating tank, an electrolysis device and a bactericide buffer tank which are sequentially communicated through a pipeline; one end of the wastewater regulating tank is provided with an industrial hydrochloric acid and industrial alkali liquor inlet pipe and a tail end wastewater inlet pipe, and a steady flow delivery pump and a self-cleaning filter are arranged between the other end of the wastewater regulating tank and the electrolysis device; the electrolysis device is communicated with two ends of the electrode pickling pipeline to form a pickling loop; the top of the bactericide buffer tank is provided with an exhaust hole, and a bactericide delivery pump for delivering bactericide into a circulating water or wastewater system is arranged at the outlet of the bactericide buffer tank; the invention also provides a preparation method of the bactericide, which can completely remove ammonia nitrogen and COD in the tail end wastewater of the thermal power plant with less equipment investment and low operation cost; the invention has the advantages of less occupied area, simple process, low preparation cost, high efficiency and low energy consumption, and can greatly reduce the treatment cost of the tail-end wastewater.
Description
Technical Field
The invention relates to the field of methods and equipment for treating waste water of a thermal power plant and preparing an industrial bactericide, in particular to equipment and a method for preparing the industrial bactericide by utilizing tail-end waste water of the thermal power plant.
Background
At present, in the power production process of thermal power plants, various waste waters are produced, and the waste waters mainly comprise: slag overflow, coal-containing water, muddy water, chemical flushing water, fine treatment regeneration wastewater, desulfurization wastewater and the like.
Under the guidance of national guidelines of 'classified collection and step recycling', the thermal power industry has formed various mature technical routes for treating conventional wastewater, but still has tail end wastewater represented by desulfurization wastewater and fine treatment regeneration wastewater, which has high ammonia nitrogen and salt content and complex water quality components and is difficult to treat and recycle by a conventional treatment process. In recent years, various end treatment processes such as bypass flue gas evaporation and membrane method salt separation are developed in the thermal power generation industry successively, but the treatment cost is always high. Therefore, there is still a need to develop a new terminal wastewater treatment device with high efficiency and low energy consumption, which can be recycled or discharged at a lower cost.
Meanwhile, in order to prevent the waste water system and the circulating water system from being damaged by breeding and propagation of microorganisms and algae, a large amount of oxidation-type bactericides are used every year in the thermal power plant, and high medicament purchasing cost is generated. In addition, the oxidation-type bactericide belongs to the category of dangerous chemicals, and has certain public safety risks in the processes of transportation, connection and disconnection. Therefore, if a technical route for self-producing industrial bactericide at low cost in a thermal power plant can be found, the production economy of the thermal power plant can be greatly improved, and the road transportation, receiving and unloading risks of dangerous chemicals in the thermal power plant can be reduced.
Based on the situation, the invention provides the method and the equipment for preparing the industrial bactericide by utilizing the tail end wastewater of the thermal power plant, which can treat part of the tail end wastewater of the thermal power plant at lower cost, change waste into valuable, prepare the bactericide by taking chlorine roots in the tail end wastewater as raw materials, and realize the self-sufficiency of the bactericide in a wastewater system and a circulating water system.
Disclosure of Invention
The invention aims to provide equipment and a method for preparing an industrial bactericide by utilizing tail-end wastewater of a thermal power plant aiming at the defects in the prior art, so that the problems of high economic cost and high energy consumption of a wastewater treatment process in the thermal power generation industry are solved.
In order to achieve the purpose, the invention adopts the following technical scheme:
an apparatus for preparing industrial bactericide by using tail-end wastewater of a thermal power plant comprises a wastewater regulating tank, an electrolysis device and a bactericide buffer tank which are sequentially communicated through a pipeline; an industrial hydrochloric acid inlet pipe, an industrial alkali liquor inlet pipe and a tail end wastewater inlet pipe are arranged at one end of the wastewater adjusting tank, a steady flow delivery pump is arranged between the other end of the wastewater adjusting tank and the electrolysis device, and a chlorine root tester and a calculation type pH meter are arranged in the wastewater adjusting tank; a self-cleaning filter is arranged between the steady flow delivery pump and the electrolysis device; the top of the bactericide buffer tank is provided with an exhaust hole; and a bactericide conveying pump for conveying bactericide to a circulating water or waste water system is arranged on a pipeline at an outlet on the right side surface of the bactericide buffer tank.
Preferably, the steady flow delivery pump is electrically connected with the frequency converter; the inlet or the outlet of the self-cleaning filter is connected with a differential pressure gauge, and the self-cleaning filter is communicated with the wastewater regulating tank through a sewage discharge pipeline.
In the invention, a steady flow delivery pump electrically connected with a frequency converter is arranged between a wastewater regulating tank and an electrolysis device, and the frequency converter can regulate the working frequency of the steady flow delivery pump and deliver wastewater to the electrolysis device at a stable flow; the waste water is filtered by a self-cleaning filter, and the remained dirt can be discharged into a waste water adjusting tank through a sewage discharge pipeline; when the impurities attached to the filter are increased, the pressure loss of the filter screen is increased, and when the pressure difference reaches a certain degree, the filter screen needs to be replaced.
Preferably, the electrolytic device comprises at least 3 electrolytic cells which are all cylindrical and are connected in series.
In the invention, the electrolytic tanks are connected in series, and the circuit is simple and easy to control.
Preferably, the electrolysis device is electrically connected with the rectifier cabinet; the shell of the electrolytic cell body is made of transparent tempered glass.
In the invention, the electrolysis device is electrically connected with the rectifier cabinet, the rectifier cabinet is used for converting alternating current into direct current to pass through the electrodes and adjusting the current passing through the electrodes and the voltage between the electrodes, and the material of the electrolysis bath body forming the electrolysis device adopts transparent strengthened glass, so that whether the surface of the internal electrode is scaled or not can be clearly observed.
Preferably, a flow meter is arranged on the pipeline close to the inlet of the electrolysis device; and an ammonia nitrogen tester, a COD tester and an ORP tester are arranged on the pipeline close to the outlet of the electrolysis device.
Preferably, the inlet end and the outlet end of the electrolysis device are communicated with an electrode pickling loop pipeline; and the electrode pickling loop pipeline is sequentially communicated with a pickling tank and a circulating pump.
In the invention, the inlet and the outlet of the electrolysis device are respectively communicated with two ends of the pipeline of the electrode pickling loop, so that the pickling loop can be formed; the electrode pickling loop pipeline of the invention is sequentially communicated with a pickling tank and a circulating pump, and the pickling tank is used for preparing and storing acid solution so as to carry out circulating pickling.
Preferably, one end of the wastewater adjusting tank is also communicated with a Roots blower.
In the invention, one end of the wastewater adjusting tank is communicated with the Roots blower, so that the Roots blower is started in the pH adjusting process of the wastewater adjusting tank, and the wastewater is uniformly mixed with acid or alkali through airflow stirring.
The invention also provides a method for preparing the industrial bactericide by utilizing the tail end wastewater of the thermal power plant, which comprises the following steps:
s1, feeding the tail end wastewater containing ammonia nitrogen, organic matters and dissolved salts into a wastewater adjusting tank, and mixing through an air flow mixing device arranged in the wastewater adjusting tank;
s2, observing a calculation type pH meter in the wastewater adjusting tank, and adjusting the pH to 6-7.5 by adding a proper amount of industrial hydrochloric acid or industrial alkali liquor; and starting the Roots blower in the adjusting process.
S3, starting a steady flow delivery pump to enable tail end waste water to be 20-25 m3The flow of the flow/h enters the electrolysis device after being filtered by the self-cleaning filter;
s4, starting the electrolysis device, selecting a constant current mode or a constant voltage mode, and controlling the retention time of the wastewater in the electrolysis device to be 1.8-2 min under the common catalysis of current and chlorine;
s5, allowing the tail end wastewater to flow out of the outlet of the electrolysis device, discharging hydrogen, and observing an online ammonia nitrogen tester, a COD tester and an ORP tester on an outlet pipeline of the electrolysis device; if the ammonia nitrogen and the COD are close to 0 and the ORP is more than 200mV, the reductive dissolved matters such as the ammonia nitrogen and the COD in the tail end wastewater are qualified after being treated, and the industrial bactericide is synchronously prepared; at the moment, the industrial bactericide is conveyed to the bactericide buffer tank, otherwise, the industrial bactericide is refluxed to the wastewater adjusting tank;
s6, starting a bactericide delivery pump, and delivering the industrial bactericide to a circulating water or wastewater system for use;
s7, cleaning the electrodes of the electrolysis device: communicating an electrolysis device with two ends of an electrode pickling loop pipeline to form a pickling loop; the electrode pickling loop pipeline is sequentially communicated with a pickling tank and a circulating pump; preparing a hydrochloric acid solution with the mass percent of 4-5% in the pickling tank, starting a circulating pump to carry out circulating pickling, and powering off an electrolysis device in the pickling process.
Preferably, the anode of the electrolysis device is made of a titanium-based multi-element precious metal coating, the cathode is made of industrial pure titanium, the voltage is less than or equal to 160V, the current is less than or equal to 2500A, and the effective volume of the series connection is 400L.
Preferably, in step S4: observing the chlorine root measuring instrument of the wastewater adjusting tank, selecting a constant current mode when the chlorine root concentration of the tail-end wastewater is lower than 4500mg/L, and selecting a constant voltage mode or a constant current mode when the chlorine root concentration of the tail-end wastewater is higher than 4500mg/L, wherein the voltage of the electrolysis device is less than or equal to 154V, and the current is less than or equal to 2200A; in the step S5: and controlling the ORP at the outlet of the electrolysis device to be 1450-1960 mV.
In the preparation method of the invention, the inventor finds out through a large number of experiments that:
1) when tail-end wastewater containing chlorine radicals with certain concentration passes through the electrolysis device under the action of constant current, when the pH is lower than 5, the corrosion rate of the anode noble metal coating by hydrogen ions is increased to some extent, and when the pH is higher than 8.5, the scaling rate on the surface of the electrode is remarkably accelerated, so that the electrolysis pH of the tail-end wastewater is controlled to be 6-7.5, the service life of the electrode can be prolonged, and the scaling of the electrode can be delayed;
2) when the concentration of chlorine radicals in the tail end wastewater is lower (lower than 4500mg/L), the degradation efficiency of ammonia nitrogen and COD in the constant current mode is higher, and the conversion rate of the chlorine radicals is more stable; when the concentration of the chlorine radicals in the tail end wastewater is higher (higher than 4500mg/L), the electrolysis effect and the conversion rate of the chlorine radicals in the two modes are similar; therefore, when the concentration of the chlorine radicals of the waste water at the tail end is lower than 4500mg/L, a constant current mode is selected, and when the concentration of the chlorine radicals of the waste water at the tail end is higher than 4500mg/L, either a constant voltage mode or a constant current mode can be selected;
3) the tail end wastewater with the same ammonia nitrogen concentration passes through the electrolysis device under the same current action, and the ammonia nitrogen removal effect is obviously influenced by the retention time; the longer the retention time of the wastewater in the electrolysis device is, the better the ammonia nitrogen and COD removal effect is, but the longer the retention time is, the higher the energy consumption and the higher the cost are caused; in addition, after the removal of reducing substances such as ammonia nitrogen, COD and the like is finished (1.5-1.7 min), the generated hypochlorite can approach the peak value only by staying for about 0.2 min; therefore, the residence time of the tail-end wastewater in the electrolysis device is controlled to be 1.8-2 min, so that good effects of removing ammonia nitrogen and COD and preparing a bactericide can be ensured, and energy consumption can be saved;
4) when the tail end wastewater with certain ammonia nitrogen concentration passes through the electrolysis device at a constant flow, the higher the voltage is, the higher the electrolysis scaling risk is, the higher the current is, and the better the ammonia nitrogen removal effect is; however, the current is too large, which causes too high energy consumption and cost increase; therefore, the invention can ensure good ammonia nitrogen removal effect and reduce energy consumption by controlling the voltage of the electrolysis device below 154V and the current below 2200A.
In addition, in step S5, the ORP at the outlet of the electrolysis device is controlled to be 1450-1960 mV, and the content of available chlorine of the prepared industrial bactericide is 80-140 mg/L, so that microorganisms and algae in a wastewater system and a circulating water system can be effectively killed; step S7, preparing a hydrochloric acid solution with the mass percentage of 4-5% in an acid washing box, and carrying out circulating acid washing on the electrode through 1 circulating pump, so that the activity of the electrode can be quickly recovered; the electrolysis device is powered off in the acid washing process, so that the electrolytic coating can be prevented from being corroded by high-concentration hydrogen ions.
Compared with the prior art, the invention has the beneficial effects that:
1. the equipment for preparing the industrial bactericide by utilizing the tail end wastewater of the thermal power plant occupies less area, and can simultaneously achieve the purposes of treating the tail end wastewater of the thermal power plant and preparing the industrial bactericide by using one set of device; the process for preparing the industrial bactericide is simple, the preparation cost is low, the efficiency is high, the energy consumption is low, and the treatment cost of the tail-end wastewater can be greatly reduced.
2. The method completely removes ammonia nitrogen and COD in the tail end wastewater of the thermal power plant with less equipment investment and low operation cost, can treat tail end wastewater with the ammonia nitrogen concentration below 500mg/L, ensures that the concentration of the final effluent is less than 1mg/L, further converts a large amount of chlorine radicals in the treated tail end wastewater of the thermal power plant into hypochlorite radicals by setting the operation working condition, changes the tail end wastewater into an industrial bactericide, can effectively kill microorganisms and algae in a wastewater system and a circulating water system, and realizes the purpose of self-production and self-sufficiency.
3. In the preparation process, the electrolytic pH of the tail end wastewater is controlled to be 6-7.5, so that the service life of the electrode can be prolonged, the scaling of the electrode can be delayed, and the stability of equipment is improved.
4. In the preparation process, the retention time of the tail end wastewater in the electrolysis device is controlled to be 1.8-2 min, so that good effects of removing ammonia nitrogen and COD and preparing a bactericide can be ensured, and energy consumption can be saved.
5. The electrolysis device can provide a constant current mode and a constant voltage mode, and the electrolysis mode is selected according to different chlorine radical concentrations of the tail end wastewater, so that the equipment has more flexibility; the voltage and the current of the electrolysis device are controlled to be always kept in the optimal range, thereby ensuring good ammonia nitrogen removal effect and reducing energy consumption.
6. In the preparation process, the electrolysis device is communicated with the pickling loop pipeline to form a pickling loop, and the electrode is subjected to circulating pickling, so that the activity of the electrode is quickly recovered, and the use efficiency of the invention is further improved.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
In the figure: 1-a wastewater adjusting tank; 11-a first valve; 12-a second valve; 13-a third valve; 111-end wastewater inlet pipe; 121-industrial hydrochloric acid inlet pipe; 131-an industrial alkali liquor inlet pipe; 14-a calculation type pH meter; 15-chlorine tester; 16-a steady flow delivery pump; 17-a frequency converter; 161-a fourth valve; 162-a fifth valve; 163-a sixth valve; 2-Roots blower; 21-a seventh valve; 22-an eighth valve; 3-self-cleaning filter; 31-differential pressure gauge; 32-self cleaning filter blow down valve; 33-a sewage drain; 4-an electrolysis device; 41-a rectifier cabinet; 42-a first flow meter; 43-ORP meter; 44-COD tester; a 45-ammonia nitrogen tester; 46-a ninth valve; 47-tenth valve; 48-eleventh valve; 49-electrode pickling loop pipeline; 5-a pickling tank; 51-a circulation pump; 511-twelfth valve; 512-a thirteenth valve; 513-a fourteenth valve; 6-a bactericide buffer tank; 61-a biocide delivery pump; 611-a fifteenth valve; 612-second flow meter.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings and embodiments, and it is to be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. 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.
The test methods or test methods described in the following examples are conventional methods unless otherwise specified; the reagents and materials, unless otherwise indicated, are conventionally obtained commercially or prepared by conventional methods.
In the present invention, chemical Oxygen demand (cod) (chemical Oxygen demand) is a chemical method for measuring the amount of reducing substances to be oxidized in a water sample. The oxygen equivalent of a substance (typically an organic substance) that can be oxidized by a strong oxidizing agent in wastewater, wastewater treatment plant effluent, and contaminated water. In the research of river pollution and the property of industrial wastewater and the operation management of wastewater treatment plants, it is an important and relatively fast measurable organic pollution parameter, often denoted by the symbol COD.
The specific structure, operation principle and control mode and spatial arrangement mode which may be involved of the electrolysis device are not specifically limited by the conventional selection in the field, belong to the prior art, and are not considered as the innovation point of the invention, and it is understood by those skilled in the art that the invention is not further described.
The technical features (the components/elements of the invention) of the chlorine root measuring instrument, the calculation type pH meter, the ammonia nitrogen measuring instrument, the COD measuring instrument, the ORP measuring instrument, the rectifier cabinet, the flow meter, etc. are all obtained from conventional commercial sources or manufactured by conventional methods, and the specific structure, the working principle, the control mode and the spatial arrangement mode which may be involved are all selected conventionally in the field, which should not be regarded as the innovation point of the invention, and it is understandable for those skilled in the art, and the patent of the invention is not further described.
All electrical equipment and instruments of the invention are explosion-proof.
Example 1
A method for preparing an industrial bactericide by utilizing tail-end wastewater of a thermal power plant comprises the following steps:
s1: opening a first valve 11, and sending the tail end wastewater containing ammonia nitrogen, organic matters and dissolved salts into a wastewater adjusting tank 1;
s2: observing a calculation type pH meter 14 in the wastewater adjusting tank 1, opening a second valve 12 when the reading is 8.5, adding a proper amount of industrial hydrochloric acid, and adjusting the pH to 6; starting the Roots blower 2 in the pH adjusting process, opening the seventh valve 21 and the eighth valve 22, and stirring by airflow to ensure that the wastewater and the acid are uniformly mixed;
s3: opening the fourth valve 161 and startingA steady flow delivery pump 16, the frequency of which is adjusted by a frequency converter 17, so that the tail end wastewater is 20m3The flow of the flow/h is filtered by the self-cleaning filter 3 and then enters the electrolysis device 4; the dirt in the self-cleaning filter 3 can be discharged into the wastewater regulating reservoir 1 through the sewage discharge pipeline 33 for the next cycle by opening the self-cleaning filter sewage discharge valve 32;
s4: the ninth valve 46 and the tenth valve 47 are kept open, the electrolysis device 4 is started, alternating current is converted into direct current through the rectifier cabinet 41, the chlorine root determinator 15 in the wastewater regulating reservoir 1 is observed, when the reading is 5000mg/L, a constant current mode is selected, the current is controlled to be 1500A, and the retention time is about 1.8 min; under the common catalysis of current and chlorine, ammonia nitrogen and COD in the wastewater are converted into harmless substances such as nitrogen, hydrogen and the like, and hypochlorite is continuously generated;
s5: opening an eleventh valve 48, enabling the tail-end wastewater to flow out from the outlet of the electrolytic device 4, and when the readings of an online ammonia nitrogen determinator 45 at the outlet of the electrolytic device 4 are 0, a COD determinator 44 is 0 and an ORP determinator 43 is 1802mV, indicating that the reductive dissolved matters such as ammonia nitrogen, COD and the like in the tail-end wastewater are qualified after treatment and the industrial bactericide is synchronously prepared, at the moment, closing a backflow valve, namely a ninth valve 46, from the electrolytic device 4 to the wastewater regulating tank 1, so that the industrial bactericide is sent to the bactericide buffer tank 6, and discharging hydrogen generated by reaction from the top of the bactericide buffer tank 6;
s6: when a sufficient amount of industrial bactericide is in the bactericide buffer tank 6, the fifteenth valve 611 is opened, the bactericide delivery pump 61 is started, the industrial bactericide is delivered to a circulating water or wastewater system for use, and the second flow meter 612 can measure the flow rate of the prepared industrial bactericide;
s7: the electrolysis device 4 is powered off, and the electrodes of the electrolysis device 4 are cleaned to keep the electrodes clean, and the method comprises the following specific steps: the electrolytic device 4 is communicated with two ends of an electrode pickling loop pipeline 49 to form a pickling loop, and the electrode pickling loop pipeline 49 is sequentially communicated with a pickling tank 5 and a circulating pump 51; preparing a hydrochloric acid solution with the mass percentage of 4-5% in the pickling tank 5, opening a twelfth valve 511, a thirteenth valve 512 and a fourteenth valve 513, and starting a circulating pump 51 for circular pickling.
Typically, the operating costs of the breakpoint chlorination process are focused on the sodium hypochlorite solution consumption. The practical operation experience of treating ammonia nitrogen wastewater by the breakpoint chlorination method in recent years shows that: aiming at the wastewater with the ammonia nitrogen initial concentration of 60-150 mg/L, when the pH is 6-9, Cl-And NH4+The mass concentration ratio is 7: 1, and the removal rate of ammonia nitrogen is about 98% when the reaction time is about 30-60 min. At present, the purchase price of 10 percent sodium hypochlorite solution is calculated according to 800 yuan/t, and then: the operating cost of the breakpoint chlorination process is about 0.12 yuan/g.
The operation cost of the electrolysis process is mainly focused on the electricity consumption of the electrolysis device. The test results of example 1 show that: treating the tail end wastewater with the ammonia nitrogen initial concentration of 150mg/L until the ammonia nitrogen concentration is 0 and the power consumption for generating 125mg/L of available chlorine is about 0.40 kW.h/g, and calculating if the power price of the power plant is calculated according to 0.32 yuan/kW.h as follows: the operating cost of the electrolysis process is about 0.128 yuan/g, which is equivalent to the operating cost of the breakpoint chlorination process, but additionally produces an industrial germicide with 125mg/L of available chlorine equivalent to the end waste water. Therefore, the invention can change the waste water at the tail end into valuable, not only prepares the bactericide, but also has low preparation cost and high economic benefit.
Example 2
A method for removing ammonia nitrogen and COD in thermal power plant wastewater in a synergic manner comprises the following steps:
s1: opening a first valve 11, and sending the tail end wastewater containing ammonia nitrogen, organic matters and dissolved salts into a wastewater adjusting tank 1;
s2: observing a calculation type pH meter 14 in the wastewater adjusting tank 1, opening a second valve 12 when the reading is 5, adding a proper amount of industrial caustic soda, and adjusting the pH to 7; starting the Roots blower 2 in the pH adjusting process, opening the seventh valve 21 and the eighth valve 22, and stirring by airflow to ensure that the wastewater and the acid are uniformly mixed;
s3: opening the fourth valve 161, starting the steady flow delivery pump 16, adjusting the frequency by the frequency converter 17 to make the end waste water 20m3The flow of the flow/h is filtered by the self-cleaning filter 3 and then enters the electrolysis device 4; the self-cleaning filter blow-down valve 32 is opened to discharge the dirt in the self-cleaning filter 3 into the waste through the blow-down pipe 33Performing the next round of circulation in the water regulating tank 1;
s4: the ninth valve 46 and the tenth valve 47 are kept open, the electrolysis device 4 is started, alternating current is converted into direct current through the rectifier cabinet 41, the chlorine root tester 15 in the wastewater regulating tank 1 is observed, when the reading is 5580mg/L, a constant current mode is selected, the current is controlled to be 2050A, and the retention time is about 1.9 min; under the common catalysis of current and chlorine, ammonia nitrogen and COD in the wastewater are converted into harmless substances such as nitrogen, hydrogen and the like, and hypochlorite is continuously generated;
s5: opening an eleventh valve 48, enabling the tail-end wastewater to flow out from the outlet of the electrolytic device 4, and when the readings of an online ammonia nitrogen determinator 45 at the outlet of the electrolytic device 4 are 0, a COD determinator 44 is 0, and an ORP determinator 43 is 1780mV, indicating that the reductive dissolved matters such as ammonia nitrogen, COD and the like in the tail-end wastewater are qualified after treatment, and the industrial bactericide is synchronously prepared, at the moment, closing a backflow valve from the electrolytic device 4 to the wastewater regulating tank 1, namely a ninth valve 46, so that the industrial bactericide is sent to the bactericide buffer tank 6, and discharging hydrogen generated by reaction from the top of the bactericide buffer tank 6;
s6: when a sufficient amount of industrial bactericide is in the bactericide buffer tank 6, the fifteenth valve 611 is opened, the bactericide delivery pump 61 is started, the industrial bactericide is delivered to a circulating water or wastewater system for use, and the second flow meter 612 can measure the flow rate of the prepared industrial bactericide;
s7: the electrolysis device 4 is powered off, and the electrodes of the electrolysis device 4 are cleaned to keep the electrodes clean, and the method comprises the following specific steps: the electrolytic device 4 is communicated with two ends of an electrode pickling loop pipeline 49 to form a pickling loop, and the electrode pickling loop pipeline 49 is sequentially communicated with a pickling tank 5 and a circulating pump 51; preparing a hydrochloric acid solution with the mass percentage of 4-5% in the pickling tank 5, opening a twelfth valve 511, a thirteenth valve 512 and a fourteenth valve 513, and starting a circulating pump 51 for circular pickling.
Typically, the operating costs of the breakpoint chlorination process are focused on the sodium hypochlorite solution consumption. The practical operation experience of treating ammonia nitrogen wastewater by the breakpoint chlorination method in recent years shows that: aiming at the wastewater with the ammonia nitrogen initial concentration of 150-500 mg/L, when the pH is 6-9, Cl-And NH4+The mass concentration ratio is 7: 1, and the removal rate of ammonia nitrogen is about 98% when the reaction time is about 30-60 min. At present, the purchase price of 10 percent of sodium hypochlorite solution is calculated according to 800 yuan/t, and then: the operating cost of the breakpoint chlorination process is about 0.12 yuan/g.
The operation cost of the electrolysis process is mainly focused on the electricity consumption of the electrolysis device. The test result of example 2 shows that: treating the tail end wastewater with the ammonia nitrogen initial concentration of 200mg/L until the ammonia nitrogen concentration is 0 and the power consumption for generating 140mg/L of available chlorine is about 0.42 kW.h/g, and calculating if the power price of the power plant is calculated according to 0.32 yuan/kW.h as follows: the operating cost of the electrolysis process is about 0.134 yuan/g, which is equivalent to the operating cost of the breakpoint chlorination process, but additionally produces an industrial bactericide with 140mg/L of available chlorine equivalent to the end waste water. Therefore, the invention can change the waste water at the tail end into valuable, not only prepares the bactericide, but also has low preparation cost and high economic benefit.
Example 3
A method for removing ammonia nitrogen and COD in thermal power plant wastewater in a synergic manner comprises the following steps:
s1: opening a first valve 11, and sending the tail end wastewater containing ammonia nitrogen, organic matters and dissolved salts into a wastewater adjusting tank 1;
s2: observing a calculation type pH meter 14 in the wastewater adjusting tank 1, opening a second valve 12 when the reading is 9, adding a proper amount of industrial hydrochloric acid, and adjusting the pH to 7.5; starting the Roots blower 2 in the pH adjusting process, opening the seventh valve 21 and the eighth valve 22, and stirring by airflow to ensure that the wastewater and the acid are uniformly mixed;
s3: opening the fourth valve 161, starting the steady flow delivery pump 16, adjusting the frequency by the frequency converter 17 to make the end waste water 25m3The flow of the flow/h is filtered by the self-cleaning filter 3 and then enters the electrolysis device 4; the dirt in the self-cleaning filter 3 can be discharged into the wastewater regulating reservoir 1 through the sewage discharge pipeline 33 for the next cycle by opening the self-cleaning filter sewage discharge valve 32;
s4: the ninth valve 46 and the tenth valve 47 are kept open, the electrolysis device 4 is started, alternating current is converted into direct current through the rectifier cabinet 41, the chlorine root tester 15 in the wastewater regulating reservoir 1 is observed, when the reading is 4000mg/L, a constant voltage mode is selected, the voltage is controlled to be 152V, and the retention time is about 2 min; under the common catalysis of current and chlorine, ammonia nitrogen and COD in the wastewater are converted into harmless substances such as nitrogen, hydrogen and the like, and hypochlorite is continuously generated;
s5: opening an eleventh valve 48, enabling the tail-end wastewater to flow out from the outlet of the electrolytic device 4, and when observing that the readings of an online ammonia nitrogen determinator 45 at the outlet of the electrolytic device 4 are 0, a COD determinator 44 is 0, and an ORP determinator 43 is 1685mV, indicating that the reductive dissolved matters such as ammonia nitrogen, COD and the like in the tail-end wastewater are qualified after being processed, and the industrial bactericide is synchronously prepared, at the moment, closing a backflow valve from the electrolytic device 4 to the wastewater regulating tank 1, namely a ninth valve 46, so that the industrial bactericide is sent to the bactericide buffer tank 6, and discharging hydrogen generated by reaction from the top of the bactericide buffer tank 6;
s6: when a sufficient amount of industrial bactericide is in the bactericide buffer tank 6, the fifteenth valve 611 is opened, the bactericide delivery pump 61 is started, the industrial bactericide is delivered to a circulating water or wastewater system for use, and the second flow meter 612 can measure the flow rate of the prepared industrial bactericide;
s7: the electrolysis device 4 is powered off, and the electrodes of the electrolysis device 4 are cleaned to keep the electrodes clean, and the method comprises the following specific steps: the electrolytic device 4 is communicated with two ends of an electrode pickling loop pipeline 49 to form a pickling loop, and the electrode pickling loop pipeline 49 is sequentially communicated with a pickling tank 5 and a circulating pump 51; preparing a hydrochloric acid solution with the mass percentage of 4-5% in the pickling tank 5, opening a twelfth valve 511, a thirteenth valve 512 and a fourteenth valve 513, and starting a circulating pump 51 for circular pickling.
Typically, the operating costs of the breakpoint chlorination process are focused on the sodium hypochlorite solution consumption. The practical operation experience of treating ammonia nitrogen wastewater by the breakpoint chlorination method in recent years shows that: aiming at the wastewater with the ammonia nitrogen initial concentration of 60-150 mg/L, when the pH is 6-9, Cl-And NH4+The mass concentration ratio is 7: 1, and the removal rate of ammonia nitrogen is about 98% when the reaction time is about 30-60 min. At present, the purchase price of 10 percent of sodium hypochlorite solution is calculated according to 812 yuan/t, and then: the operating cost of the breakpoint chlorination process is about 0.12 yuan/g.
The operation cost of the electrolysis process is mainly focused on the electricity consumption of the electrolysis device. The test result of example 3 shows that: treating the tail end wastewater with the ammonia nitrogen initial concentration of 150mg/L until the ammonia nitrogen concentration is 0 and the power consumption for generating 120mg/L of available chlorine is about 0.43 kW.h/g, and calculating if the power price of the power plant is calculated according to 0.32 yuan/kW.h as follows: the operating cost of the electrolysis process is about 0.138 yuan/g, which is equivalent to the operating cost of the breakpoint chlorination process, but additionally produces an industrial bactericide with 120mg/L of available chlorine equivalent to the end waste water. Therefore, the invention can change the waste water at the tail end into valuable, not only prepares the bactericide, but also has low preparation cost and high economic benefit.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. The invention discloses equipment for preparing an industrial bactericide by utilizing tail-end wastewater of a thermal power plant, which comprises a wastewater regulating tank, an electrolysis device and a bactericide buffer tank which are sequentially communicated through a pipeline; one end of the wastewater regulating tank is provided with an industrial hydrochloric acid and industrial alkali liquor inlet pipe and a tail end wastewater inlet pipe, and a steady flow delivery pump and a self-cleaning filter are arranged between the other end of the wastewater regulating tank and the electrolysis device; the electrolysis device is communicated with two ends of the electrode pickling pipeline to form a pickling loop; the top of the bactericide buffer tank is provided with an exhaust hole, and a bactericide delivery pump for delivering bactericide into a circulating water or wastewater system is arranged at the outlet of the bactericide buffer tank; the invention also provides a preparation method of the bactericide, which can completely remove ammonia nitrogen and COD in the tail end wastewater of the thermal power plant with less equipment investment and low operation cost; the equipment for preparing the industrial bactericide by utilizing the tail-end wastewater of the thermal power plant is characterized by comprising a wastewater adjusting tank (1), an electrolysis device (4) and a bactericide buffer tank (6) which are sequentially communicated through pipelines; an industrial hydrochloric acid inlet pipe (121), an industrial alkali liquor inlet pipe (131) and a tail end wastewater inlet pipe (111) are arranged at one end of the wastewater adjusting tank (1), and a steady flow delivery pump (16) is arranged between the other end of the wastewater adjusting tank and the electrolysis device (4); a chlorine root determinator (15) and a calculation type pH meter (14) are arranged in the wastewater adjusting tank (1); a self-cleaning filter (3) is arranged between the steady flow delivery pump (16) and the electrolysis device (4); the top of the bactericide buffer tank (6) is provided with an exhaust hole; and a bactericide delivery pump (61) for delivering the bactericide to a circulating water or waste water system is arranged on a pipeline at the outlet of the right side surface of the bactericide buffer tank (6).
2. The apparatus for preparing industrial bactericide by utilizing tail end wastewater of thermal power plant as claimed in claim 1, characterized in that said steady flow delivery pump (16) is electrically connected with a frequency converter (17); a differential pressure gauge (31) is connected at the inlet or the outlet of the self-cleaning filter (3), and the self-cleaning filter (3) is communicated with the wastewater regulating pool (1) through a sewage discharge pipeline (33).
3. The equipment for preparing industrial bactericide by utilizing tail-end wastewater of thermal power plant as claimed in claim 1, characterized in that said electrolysis device (4) comprises at least 3 electrolytic cells which are cylindrical and connected in series.
4. The apparatus for preparing industrial bactericide by using tail end wastewater of thermal power plant according to claim 3, characterized in that the electrolysis device (4) is electrically connected with the rectifier cabinet (41); the shell of the electrolytic cell body is made of transparent tempered glass.
5. The apparatus for preparing industrial bactericide by using tail end wastewater of thermal power plant according to claim 4, characterized in that a flow meter (42) is arranged on the pipeline near the inlet of the electrolyzer (4); and an ammonia nitrogen tester (45), a COD tester (44) and an ORP tester (43) are arranged on the pipeline close to the outlet of the electrolysis device (4).
6. The apparatus for preparing industrial bactericide by using tail end wastewater of thermal power plant as claimed in claim 5, characterized in that the inlet end and outlet end of said electrolyzer (4) are connected with electrode pickling loop pipeline (49); the electrode pickling loop pipeline (49) is sequentially communicated with a pickling tank (5) and a circulating pump (51).
7. The equipment for preparing the industrial bactericide by utilizing the tail end wastewater of the thermal power plant as claimed in claim 1, wherein one end of the wastewater adjusting tank (1) is also communicated with a Roots blower (2).
8. A method for preparing an industrial bactericide by utilizing tail-end wastewater of a thermal power plant is characterized by comprising the following steps:
s1, feeding the tail end wastewater containing ammonia nitrogen, organic matters and dissolved salts into a wastewater adjusting tank (1), and mixing through an airflow mixing device arranged in the wastewater adjusting tank (1);
s2, observing a calculation type pH meter (14) in the wastewater adjusting tank (1), and adjusting the pH to 6-7.5 by adding a proper amount of industrial hydrochloric acid or industrial alkali liquor; and starting the Roots blower (2) in the adjusting process.
S3, starting a steady flow delivery pump (16) to enable tail end wastewater to be 20-25 m3The flow of/h enters the electrolysis device (4) after being filtered by the self-cleaning filter (3);
s4, starting the electrolysis device (4), selecting a constant current mode or a constant voltage mode, and controlling the retention time of the wastewater in the electrolysis device (4) to be 1.8-2 min under the common catalysis of current and chlorine;
s5, discharging the tail end wastewater from the outlet of the electrolysis device (4) and simultaneously discharging hydrogen, and observing an online ammonia nitrogen measuring instrument (45), a COD measuring instrument (44) and an ORP measuring instrument (43) on the outlet pipeline of the electrolysis device (4); if the ammonia nitrogen and the COD are close to 0 and the ORP is more than 200mV, the reductive dissolved matters such as the ammonia nitrogen and the COD in the tail end wastewater are qualified after being treated, and the industrial bactericide is synchronously prepared; at the moment, the industrial bactericide is conveyed to a bactericide buffer tank (6), otherwise, the industrial bactericide is refluxed to a wastewater adjusting tank;
s6, starting a bactericide delivery pump (61), and delivering the industrial bactericide to a circulating water or wastewater system for use;
s7, cleaning the electrodes of the electrolysis device (4): communicating an electrolysis device (4) with two ends of an electrode pickling loop pipeline (49) to form a pickling loop; the electrode pickling loop pipeline (49) is sequentially communicated with a pickling tank (5) and a circulating pump (51); preparing a hydrochloric acid solution with the mass percentage of 4-5% in the pickling tank (5), starting a circulating pump (51) to carry out circulating pickling, and cutting off the power of the electrolysis device (4) in the pickling process.
9. The method for preparing the industrial bactericide by utilizing the tail end wastewater of the thermal power plant as claimed in claim 8, wherein the anode material of the electrolysis device (4) is a titanium-based multi-element precious metal coating, the cathode material is industrial pure titanium, the voltage is less than or equal to 160V, the current is less than or equal to 2500A, and the effective volume in series connection is 400L.
10. The method for preparing industrial bactericide by using tail end wastewater of thermal power plant as claimed in claim 8, wherein in step S4: observing a chlorine root determinator (15) of the wastewater adjusting tank (1), selecting a constant current mode when the concentration of chlorine roots of the tail-end wastewater is lower than 4500mg/L, and selecting a constant voltage mode or a constant current mode when the concentration of chlorine roots of the tail-end wastewater is higher than 4500mg/L, wherein the voltage of the electrolytic device (4) is less than or equal to 154V, and the current is less than or equal to 2200A; in the step S5: controlling the ORP at the outlet of the electrolysis device (4) to be 1450-1960 mV.
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| CN113480059A (en) * | 2021-08-16 | 2021-10-08 | 浙江浙能技术研究院有限公司 | Self-mass-adjusting pretreatment electrochemical oxidation system and treatment process |
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