CN113354203A - Biological treatment method for electroplating comprehensive wastewater - Google Patents
Biological treatment method for electroplating comprehensive wastewater Download PDFInfo
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- 238000011282 treatment Methods 0.000 title claims abstract description 67
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
Abstract
The invention provides a biological treatment method of electroplating comprehensive wastewater, which comprises the following steps: introducing the electroplating comprehensive wastewater into a primary aerobic tank, adding microbial sludge, and performing primary nitration reaction to obtain treated water I; introducing the obtained treated water I into a primary anoxic tank, adding a carbon source, and carrying out primary denitrification reaction to obtain treated water II; introducing the obtained treated water II into a secondary aerobic tank, and performing secondary nitration reaction to obtain treated water III; introducing the obtained treated water III into a secondary anoxic tank, adding a carbon source, and carrying out secondary denitrification reaction to obtain treated water IV; introducing the obtained treated water IV into a membrane separation tank, and filtering to obtain treated water V; the concentrated microorganism sludge flows back to the first-stage aerobic tank; the method combines the O/A/O/A process with the membrane separation technology, solves the problem of wastewater treatment with high nitrogen content and low carbon content, ensures that the effluent quality is stable and meets the wastewater discharge standard of the electroplating industry, and has better industrial application prospect.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a biological treatment method for electroplating comprehensive wastewater.
Background
The electroplating comprehensive wastewater is mixed wastewater obtained by performing physical and chemical treatment on wastewater of each process in electroplating production and then treating heavy metals, and contains various organic matters and relatively high total nitrogen (including organic nitrogen, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen). And because some electroplating enterprises often use a large amount of nitric acid for deplating, or use a large amount of nitric acid to clean the anode slag at the bottom of the tank when the tank is inverted, the electroplating comprehensive wastewater has the characteristics of high nitrogen content and low carbon content. At present, the waste water is treated by adopting anoxic and aerobic treatment processes, the traditional anoxic-aerobic treatment process is derived from urban waste water treatment process, a preposed denitrification anoxic tank is adopted, nitrified nitrate nitrogen in a postposed aerobic tank flows back to the preposed anoxic tank for denitrification, a carbon source in the waste water can be fully utilized, and the amount of an additional added carbon source is reduced. However, the denitrification effect of the pre-denitrification is limited by the reflux ratio, the denitrification effect has an upper limit, if the nitrified liquid flows back to the pre-anoxic tank from the membrane tank, the dissolved oxygen of the membrane tank is very high, the dissolved oxygen can seriously affect the anoxic state of the anoxic tank and consume a part of carbon source, if the nitrified liquid flows back to the pre-anoxic tank from the aerobic tank, the reflux from the membrane tank to the aerobic tank needs to be increased, the power consumption and the investment operation cost are increased, and the anoxic-aerobic-membrane separation process is difficult to meet the requirement of the total nitrogen discharge standard which is increased.
The traditional biological denitrification technology is widely adopted in engineering. Firstly, converting organic nitrogen in wastewater into ammonia nitrogen; the ammonia nitrogen is further converted into nitrate nitrogen under the action of nitrobacteria; the generated nitrate nitrogen is reduced into nitrogen under the action of denitrifying bacteria. As the nitrifying bacteria participating in the biological denitrification process are generally autotrophic bacteria, the nitrifying bacteria obtain energy from the process of oxidizing ammonia nitrogen or nitrite nitrogen and grow slowly. In recent years, membrane bioreactors have gained attention in electroplating wastewater treatment as a combination of high efficiency membrane separation technology and traditional microbial sludge process. Because the nitrifying bacteria and the denitrifying bacteria in the membrane bioreactor can not run off and the sludge concentration is extremely high, the enrichment of the bacteria which have the special treatment effect on high-concentration pollutants is facilitated, and the types of the microorganisms in the reactor are ensured to be rich. The combined process for treating electroplating wastewater based on the membrane bioreactor is also further developed, such as a combined process of coagulating sedimentation, sand filtration, a membrane bioreactor, activated carbon and ozone, a hydrolytic acidification, a membrane bioreactor, an upflow type contact oxidation column, a separated membrane bioreactor consisting of a contact oxidation tank and a membrane system, and the like. Although the process has a certain treatment effect on the electroplating comprehensive wastewater, when the concentration of the nitrogen-containing pollutants in the inlet water fluctuates greatly, the total nitrogen content of the outlet water still easily exceeds the discharge limit value.
CN101549907A discloses a membrane biological reaction device and a treatment method for treating high ammonia nitrogen industrial wastewater, the device is an anaerobic water outlet tank, an anoxic tank, a first-stage aerobic tank, a second-stage aerobic tank and a membrane tank which are connected according to a fluid circulation sequence, wherein an immersed unitized hollow fiber membrane filtration device is arranged in the membrane tank to carry out solid-liquid separation on a treatment liquid. The process flows the sludge from the aerobic tank and the membrane tank to the anoxic tank, the two flows of reflux liquid have high dissolved oxygen, the low oxygen state of the anoxic tank is seriously influenced, the denitrification capability is greatly reduced, and the total nitrogen of the effluent is difficult to stably reach the standard.
CN104944689A discloses a device and a method for treating high ammonia nitrogen wastewater, the method comprises the following steps: inoculating microorganism sludge into an anoxic tank and an aerobic tank, wherein the anoxic tank is filled with the microorganism sludge, starting a stirrer, and repeating the following steps: 1) starting a water inlet pump, adopting sequencing batch water inlet, inputting the high ammonia nitrogen wastewater to be treated into an anoxic tank according to the designed treatment amount, and flowing the high ammonia nitrogen wastewater to an aerobic tank through an overflow weir; 2) in the anoxic tank, nitrate nitrogen in the wastewater is reduced under the action of a carbon source; opening an aeration system, oxidizing ammonia nitrogen and organic matters in the wastewater in the aerobic tank, and closing the aeration system; 3) in the membrane separation tank, the wastewater with the designed treatment capacity and subjected to nitrification is discharged after being filtered by a membrane in the membrane component; in the anoxic tank and the membrane separation tank, wastewater with less than 3 times of designed treatment amount flows back to the anoxic tank; in the anoxic tank, equal amount of the denitrified wastewater flows to the aerobic tank through the overflow weir. The process flows mixed liquor from the membrane separation tank back to the anoxic tank, impact is caused on the low oxygen state of the anoxic tank, and only a single-stage treatment process is adopted, so that when the concentration fluctuation of water inflow pollutants is large or microbial sludge is greatly influenced by environmental factors, the total nitrogen content of effluent easily exceeds a discharge limit value.
In summary, it is an urgent need to solve the problem of providing an effective treatment method for electroplating wastewater with high nitrogen content and low carbon content.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a biological treatment method for electroplating comprehensive wastewater, which removes various nitrogen and organic matters in the electroplating comprehensive wastewater through five-stage treatment, ensures that the effluent quality can continuously and stably meet the requirements of wastewater discharge standards in the electroplating industry, and has better industrial application prospect.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a method for biological treatment of electroplating integrated wastewater, comprising the steps of:
(1) primary aerobic treatment: introducing the electroplating comprehensive wastewater into a primary aerobic tank, adding microbial sludge, and performing primary nitration reaction to obtain treated water I;
(2) first-stage anoxic treatment: introducing the treated water I obtained in the step (1) into a primary anoxic tank, adding a carbon source, and performing primary denitrification reaction to obtain treated water II;
(3) secondary aerobic treatment: introducing the treated water II obtained in the step (2) into a secondary aerobic tank for secondary nitration reaction to obtain treated water III;
(4) secondary anoxic treatment: introducing the treated water III obtained in the step (3) into a secondary anoxic tank, adding a carbon source, and performing secondary denitrification reaction to obtain treated water IV;
(5) membrane separation treatment: introducing the treated water IV obtained in the step (4) into a membrane separation tank, and filtering to obtain treated water V; and (4) returning the concentrated microbial sludge after filtration to the primary aerobic tank.
According to the method, firstly, a nitrification reaction is carried out through primary aerobic treatment, ammonia nitrogen or organic nitrogen in the wastewater is oxidized into nitrate nitrogen or nitrite nitrogen, and then a denitrification reaction is carried out through primary anoxic treatment, so that the nitrate nitrogen or nitrite nitrogen in the wastewater is reduced into nitrogen; and continuously oxidizing the residual ammonia nitrogen or organic nitrogen in the wastewater into nitrate nitrogen or nitrite nitrogen through secondary aerobic treatment, and continuously reducing the residual nitrate nitrogen or nitrite nitrogen in the wastewater into nitrogen through denitrification reaction through secondary anoxic treatment. Meanwhile, the microorganism sludge concentrated in the membrane separation tank flows back to the primary aerobic tank, so that the higher sludge concentration is kept in the reaction tank, the conversion of various pollutants by primary treatment is enhanced, and the problem that the denitrification capacity is reduced due to overhigh dissolved oxygen in the anoxic tank caused by the fact that the sludge flows back to the anoxic tank is solved. The method combines the biological treatment of O/A/O/A and the membrane separation treatment process, and the process can maintain normal operation when the inlet water quality has larger fluctuation or the pollutant concentration is higher, so the operation and management are simple, the method is particularly suitable for electroplating comprehensive wastewater with high nitrogen content and low carbon content, the outlet water quality can continuously and stably meet the requirement of the wastewater discharge standard of the electroplating industry, and the method has better industrial application prospect.
In the invention, the obtained treated water V can be directly discharged, can also be recycled after reverse osmosis desalination, and can also be used as water for on-line cleaning of the hollow fiber component.
The following technical solutions are preferred technical solutions of the present invention, but not limited to the technical solutions provided by the present invention, and technical objects and advantageous effects of the present invention can be better achieved and achieved by the following technical solutions.
As a preferable technical scheme of the invention, the COD content in the electroplating comprehensive wastewater is less than or equal to 250mg/L, such as 150mg/L, 200mg/L, 250mg/L and the like; the ammonia nitrogen content is less than or equal to 150mg/L, such as 60mg/L, 100mg/L or 150mg/L and the like; the total nitrogen content is less than or equal to 200mg/L, for example 80mg/L, 150mg/L or 200mg/L, etc., and the selection of the above-mentioned values is not limited to the recited values, but other values not recited within the respective numerical ranges are equally applicable.
As the preferable technical scheme of the invention, a microporous aeration head is arranged in the primary aerobic tank.
In the invention, the microporous aeration head can uniformly distribute the air conveyed by the aerobic blower in the aerobic tank to provide the required dissolved oxygen for the microorganisms.
Preferably, the time of the primary aerobic treatment is 8 to 12 hours, such as 8 hours, 9 hours, 10 hours, 11 hours or 12 hours, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the concentration of dissolved oxygen in the primary aerobic treatment process is controlled to be 2-5 mg/L, such as 2mg/L, 3mg/L, 4mg/L or 5mg/L, but not limited to the recited values, and other values not recited in the range of the recited values are also applicable.
As the preferable technical scheme of the invention, a submersible stirrer is arranged in the primary anoxic pond.
In the invention, the submersible stirrer is arranged to fully mix the wastewater and the microbial sludge under the anoxic condition to complete denitrification.
Preferably, the time of the first-stage anoxic treatment is 4-8 h, such as 4h, 5h, 6h, 7h or 8h, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the carbon source is used in an amount of COD/TN of 4 to 6, for example, 4, 5 or 6, based on the total nitrogen content in the treated water i, but the amount is not limited to the recited values, and other values not recited in the above range are also applicable.
In the invention, TN represents the total nitrogen amount, and the carbon source amount can be calculated according to the above rule.
Carbon source dosage (total nitrogen concentration of sewage-total nitrogen emission limit) x treated water amount x (COD/TN)/carbon source preparation concentration
Wherein the unit of the carbon source dosage is L/h;
the total nitrogen concentration of the sewage is mg/L;
total nitrogen emission limit in mg/L;
amount of treated water in unit of m3/h；
COD/TN, an empirical calculation constant, and the value of the constant is 4-6 according to the concentration of organic matters in the wastewater;
the carbon source preparation concentration is in mg/L.
In the invention, the anoxic tank can denitrify nitrate nitrogen and nitrite nitrogen in the wastewater into nitrogen gas under an anoxic condition.
As the preferable technical scheme of the invention, a microporous aeration head is arranged in the secondary aerobic tank.
Preferably, the time of the secondary aerobic treatment is 6 to 10 hours, such as 6 hours, 7 hours, 8 hours, 9 hours or 10 hours, but not limited to the recited values, and other values in the range are also applicable.
Preferably, the concentration of dissolved oxygen in the secondary aerobic treatment process is controlled to be 2-5 mg/L, such as 2mg/L, 3mg/L, 4mg/L or 5mg/L, but not limited to the recited values, and other values not recited in the range of the recited values are also applicable.
As the preferable technical scheme of the invention, a submersible stirrer is arranged in the secondary anoxic pond.
Preferably, the time of the secondary anoxic treatment is 2-6h, such as 2h, 3h, 4h, 5h or 6h, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the carbon source is used in an amount of COD/TN of 4 to 6, for example, 4, 5 or 6, based on the total nitrogen content in the treated water iii, but the amount is not limited to the recited values, and other values not recited in the above range are also applicable.
In the present invention, the residence time of the wastewater in each tank has a significant effect on effluent contaminant content. If the retention time is too short, the nitrification reaction of the aerobic tank and the denitrification reaction of the anoxic tank are influenced, so that the removal rate of pollutants such as nitrogen, carbon and the like is reduced; if the residence time is too long, the required structure of the reaction tank is large in size, so that the investment cost is increased, and meanwhile, if the residence time is too long, more energy consumption is consumed, so that the operation cost is increased.
As a preferred technical scheme of the invention, the carbon source is glucose.
As a preferred embodiment of the present invention, the filtration is performed using a hollow fiber membrane module.
In the present invention, the membrane separation treatment is performed in a membrane separation tank.
Preferably, the flux of the hollow fiber membrane module is 12-18L/(m)2H), for example 12L/(m)2·h)、13L/(m2·h)、14L/(m2·h)、15L/(m2·h)、16L/(m2·h)、17L/(m2H) or 18L/(m)2H), but not limited to the recited values, and other values not recited within the range of values are also applicable.
Preferably, the hollow fiber membrane module has a filtration resistance of less than 50kPa, such as 10kPa, 20kPa, 30kPa, 40kPa, 45kPa, or 49kPa, but not limited to the recited values, and other values not recited in the range of values are also applicable.
Preferably, the hollow fiber membrane module is provided with an aeration device and an online membrane cleaning system.
According to the invention, the aeration device can disturb the hollow fiber membrane filaments, so that mud is prevented from being deposited on the membrane filaments, meanwhile, dissolved oxygen in the membrane separation tank can be increased, and the dissolved oxygen is utilized to remove excessive carbon sources flowing from the secondary anoxic tank, so that the COD (chemical oxygen demand) of effluent is prevented from exceeding the standard.
Preferably, the cleaning step of the membrane online cleaning system comprises the steps of carrying out online alternate cleaning of sodium chlorate and hydrochloric acid every 17-23 days, and carrying out offline sodium hypochlorite and hydrochloric acid chemical cleaning every half year.
According to the on-line membrane cleaning system, the pollution of organic matters and microorganisms to the membrane holes of the hollow fiber membranes is removed through sodium hypochlorite cleaning, and the pollution of the inorganic matters to the membrane holes of the hollow fiber membranes is removed through hydrochloric acid cleaning.
In a preferred embodiment of the present invention, the concentration of the microbial sludge in the primary aerobic tank, the primary anoxic tank, the secondary aerobic tank, and the secondary anoxic tank is independently 6 to 10g/L, for example, 6g/L, 7g/L, 8g/L, 9g/L, or 10g/L, but is not limited to the above-mentioned values, and other values not listed in the above-mentioned range are also applicable.
In the present invention, the concentration of the microbial sludge in each tank needs to be controlled. If the concentration of the microorganism sludge is too low, the removal efficiency of each pollutant is low, and the effluent quality easily exceeds the discharge limit value; if the concentration of the microorganisms is too high, the dissolved oxygen content cannot be matched with the concentration of the microorganisms, anaerobic reaction may occur, and even the microorganism sludge is aged.
As the preferable technical scheme of the invention, the microbial sludge is intercepted by the hollow fiber membrane component and flows back to the primary aerobic tank.
Preferably, the reflux ratio of the microbial sludge is 100 to 300%, for example, 100%, 150%, 200%, 250%, or 300%, but is not limited to the recited values, and other values not recited in the range of the values are also applicable.
In the invention, the reflux ratio of the microbial sludge has important influence on the effluent quality. If the reflux ratio is too low, the microbial sludge load in the reaction tank cannot meet the requirement of removing pollutants with high nitrogen content; if the reflux ratio is too high, not only is more energy consumption consumed, but also if the microbial sludge concentration in the reaction tank is too high, the dissolved oxygen concentration in the reaction tank cannot meet the design requirement, and the nitration reaction of the aerobic tank is influenced.
Compared with the prior art, the invention has the following beneficial effects:
1. the method adopts an O/A/O/A + membrane separation five-stage treatment process, and for the electroplating comprehensive wastewater with high nitrogen content and low carbon content, the denitrification effect is not limited by the reflux ratio of the microbial sludge any more, and the method has the characteristics of good denitrification effect and strong impact load resistance, and ensures that the effluent quality can continuously and stably meet the requirements of the wastewater discharge standard of the electroplating industry;
2. in the method, the carbon source consumption, the aerobic aeration intensity and the microbial sludge concentration in the reaction tank can be adjusted according to the removal effect of the previous stage process, and the carbon source consumption and the blower power consumption can be saved under the condition of ensuring the standard treatment of the residual microbial pollutants, so that the operation cost is effectively reduced;
3. in the method, the mixed liquid in the membrane separation tank directly flows back to the primary aerobic tank, so that the influence of the back-flowing dissolved oxygen on the denitrification reaction is eliminated, and meanwhile, the high dissolved oxygen in the back-flowing liquid can be utilized in the aerobic treatment process, so that the aeration intensity is reduced, and the power consumption of a blower is reduced.
4. In the method, the microorganism sludge reflux effect is only to supplement the sludge concentration of the aerobic tank, and the denitrification effect is not limited by the microorganism sludge reflux ratio any more, so the sludge microorganism sludge reflux ratio can be lower than that of the traditional anoxic-aerobic-membrane separation treatment process, thereby reducing the investment of a reflux pump and the energy consumption of microorganism sludge reflux.
Drawings
FIG. 1 is a process flow diagram of biological treatment of electroplating integrated wastewater provided in example 1 of the present invention.
FIG. 2 is a drawing of an apparatus for biological treatment of electroplating integrated wastewater according to example 1 of the present invention;
the system comprises a first-stage aerobic tank, a second-stage anoxic tank, a 3-stage aerobic tank, a 4-stage anoxic tank, a 5-membrane separation tank, a 6-clean water tank, a 7-aerobic blower, an 8-submersible mixer, a 9-hollow fiber membrane component, a 10-water outlet pump, an 11-hollow fiber membrane blower and a 12-microbial sludge reflux pump.
Detailed Description
In order to better illustrate the present invention and facilitate the understanding of the technical solutions of the present invention, the present invention is further described in detail below. However, the following examples are only simple examples of the present invention and do not represent or limit the scope of the present invention, which is defined by the claims.
The following are typical but non-limiting examples of the invention:
example 1:
the embodiment provides a method for biologically treating electroplating integrated wastewater and a device used by the method, wherein the process flow chart of the method is shown in figure 1, and the device adopted by the method is shown in figure 2.
The method comprises the following steps:
(1) mixing 3000m3Introducing electroplating comprehensive wastewater with the COD content of 245mg/L, the ammonia nitrogen content of 130mg/L and the total nitrogen content of 180mg/L into a primary aerobic tank 1, adding microbial sludge to enable the concentration of the microbial sludge to be 10g/L, staying for 8 hours, enabling dissolved oxygen to be 2.0mg/L, the COD removal rate to be 55% and the ammonia nitrogen removal rate to be 75% to obtain treated water I;
(2) introducing the treated water I obtained in the step (1) into a primary anoxic tank 2, adding a glucose solution with the prepared concentration of 300000mg/L, keeping the treated water for 6 hours, wherein the dosage of the glucose is 275L/h, the dosage of the glucose is calculated according to the total nitrogen content in the treated water I, the COD/TN is 4, the concentration of the microbial sludge in the primary anoxic tank 2 is 10g/L, and the total nitrogen removal rate is 70%, so that treated water II is obtained;
(3) introducing the treated water II obtained in the step (2) into a secondary aerobic tank 3, staying for 6 hours, wherein the dissolved oxygen is 2.0mg/L, the microbial sludge concentration is 10g/L, the COD removal rate is 60%, the ammonia nitrogen removal rate is 90%, and thus treated water III is obtained;
(4) introducing the treated water III obtained in the step (3) into a secondary anoxic tank 4, adding a glucose solution with the prepared concentration of 300000mg/L, keeping the treated water for 6 hours, wherein the dosage of glucose is 65L/h, the dosage of glucose is calculated according to the total nitrogen content in the treated water I, the COD/TN is 4, the concentration of microbial sludge in the secondary anoxic tank 4 is 10g/L, and the total nitrogen removal rate is 75%, so that treated water IV is obtained;
(5) introducing the treated water IV obtained in the step (4) into a membrane separation tank 5, and staying for 2 hours, wherein the area of a hollow fiber membrane component 9 is 8400m2Flux is 12L/(m)2H) stabilizationTransmembrane pressure difference is 18kPa, and treated water V is obtained after filtration; in addition, the microorganism sludge intercepted by the hollow fiber membrane component 9 flows back to the first-stage aerobic tank 1, and the reflux ratio is 100 percent;
(6) the hollow fiber membrane module 9 is cleaned alternately with sodium chlorate and hydrochloric acid on line every 23 days and is cleaned chemically with sodium hypochlorite and hydrochloric acid off line every 6 months.
The device adopted by the method comprises a primary aerobic tank 1, a primary anoxic tank 2, a secondary aerobic tank 3, a secondary anoxic tank 4, a membrane separation tank 5 and a clean water tank 6 which are sequentially connected from left to right;
the bottoms of the primary aerobic tank 1 and the secondary aerobic tank 3 are connected with an aerobic blower 7; a submersible stirrer 9 is respectively arranged in the primary anoxic tank 2 and the secondary anoxic tank 4; 3 groups of hollow fiber membrane assemblies 9 are arranged in the membrane separation tank 5; the bottom of each hollow fiber membrane component 9 is connected with a hollow fiber membrane blower 11;
the membrane separation tank 5 is connected with the clean water tank 6 through a water outlet pump 10; the membrane separation tank 5 is connected with the primary aerobic tank 1 through a microorganism sludge reflux pump 12.
Example 2:
the embodiment provides a method for biologically treating electroplating integrated wastewater, which comprises the following steps:
(1) mixing 3000m3Introducing electroplating comprehensive wastewater with the COD content of 160mg/L, the ammonia nitrogen content of 75mg/L and the total nitrogen content of 130mg/L into a primary aerobic tank 1, adding microbial sludge to ensure that the concentration of the microbial sludge is 6g/L, staying for 12 hours, the dissolved oxygen content is 5.0mg/L, the COD removal rate is 50 percent and the ammonia nitrogen removal rate is 75 percent, and obtaining treated water I;
(2) introducing the treated water I obtained in the step (1) into a primary anoxic tank 2, adding a glucose solution with the prepared concentration of 300000mg/L, keeping the glucose solution for 8 hours, wherein the dosage of the glucose is 287L/h, the dosage of the glucose is calculated according to the total nitrogen content in the treated water I, the COD/TN is 6, the concentration of the microbial sludge in the primary anoxic tank 2 is 6g/L, and the total nitrogen removal rate is 65%, so that treated water II is obtained;
(3) introducing the treated water II obtained in the step (2) into a secondary aerobic tank 3, staying for 10 hours, wherein the dissolved oxygen is 5.0mg/L, the microbial sludge concentration is 6g/L, the COD removal rate is 55%, and the ammonia nitrogen removal rate is 80%, so as to obtain treated water III;
(4) introducing the treated water III obtained in the step (3) into a secondary anoxic tank 4, adding glucose, adding a glucose solution with the prepared concentration of 300000mg/L, keeping the glucose solution for 6 hours at the dosage of 76L/h, wherein the dosage of the glucose is calculated according to the total nitrogen content in the treated water I, so that the COD/TN is 6, the concentration of the microbial sludge in the secondary anoxic tank 4 is 6g/L, and the total nitrogen removal rate is 70%, thereby obtaining treated water IV;
(5) introducing the treated water IV obtained in the step (4) into a membrane separation tank 5, and staying for 2 hours, wherein the area of the hollow fiber membrane component 9 is 5600m2Flux is 18L/(m)2H), stabilizing the transmembrane pressure difference to be 30kPa, and filtering to obtain treated water V; in addition, the microorganism sludge intercepted by the hollow fiber membrane component 9 flows back to the first-stage aerobic tank 1, and the reflux ratio is 200%;
(6) the hollow fiber membrane module 9 is cleaned alternately with sodium chlorate and hydrochloric acid on line every 17 days and is cleaned chemically with sodium hypochlorite and hydrochloric acid off line every 8 months.
Example 3:
the embodiment provides a method for biologically treating electroplating integrated wastewater, which comprises the following steps:
(1) mixing 3000m3Introducing electroplating comprehensive wastewater with COD (chemical oxygen demand) content of 200mg/L, ammonia nitrogen content of 105mg/L and total nitrogen content of 155mg/L into a primary aerobic tank 1, adding microbial sludge to enable the concentration of the microbial sludge to be 8g/L, staying for 10 hours, enabling dissolved oxygen to be 3.5mg/L, enabling the COD removal rate to be 50% and the ammonia nitrogen removal rate to be 75%, and obtaining treated water I;
(2) introducing the treated water I obtained in the step (1) into a primary anoxic tank 2, adding a glucose solution with the prepared concentration of 300000mg/L, keeping the treated water for 6 hours, wherein the dosage of the glucose is 292L/h, the dosage of the glucose is calculated according to the total nitrogen content in the treated water I, the COD/TN is 5, the concentration of the microbial sludge in the primary anoxic tank 2 is 8g/L, and the total nitrogen removal rate is 68%, so that treated water II is obtained;
(3) introducing the treated water II obtained in the step (2) into a secondary aerobic tank 3, staying for 8 hours, wherein the dissolved oxygen is 3.5mg/L, the microbial sludge concentration is 8g/L, the COD removal rate is 60%, the ammonia nitrogen removal rate is 85%, and thus treated water III is obtained;
(4) introducing the treated water III obtained in the step (3) into a secondary anoxic tank 4, adding a glucose solution with the prepared concentration of 300000mg/L, keeping the treated water for 4 hours, wherein the dosage of glucose is 72L/h, and the dosage of glucose is calculated according to the total nitrogen content in the treated water I, so that the COD/TN is 5, the concentration of microbial sludge in the secondary anoxic tank 4 is 8g/L, and the total nitrogen removal rate is 72%, thereby obtaining treated water IV;
(5) introducing the treated water IV obtained in the step (4) into a membrane separation tank 5, and staying for 2 hours, wherein the area of a hollow fiber membrane component 9 is 6720m2The flux is 15L/(m)2H), stabilizing the transmembrane pressure difference to 24kPa, and filtering to obtain treated water V; in addition, the microorganism sludge intercepted by the hollow fiber membrane component 9 flows back to the first-stage aerobic tank 1, and the reflux ratio is 300 percent;
(6) the hollow fiber membrane module 9 is cleaned alternately with sodium chlorate and hydrochloric acid on line every 20 days and is cleaned chemically with sodium hypochlorite and hydrochloric acid off line every 8 months.
Example 4:
this example provides a method for the biological treatment of electroplating integrated wastewater, which is comparable to the method of example 1, except that: in the step (4), the dosage of the glucose is calculated according to the total nitrogen content in the treated water III, so that COD/TN is 2, the total nitrogen removal rate is 38%, and the total nitrogen content in the effluent water in the final step (4) is 33mg/L and far exceeds the total nitrogen emission limit value.
Example 5:
this example provides a method for the biological treatment of electroplating integrated wastewater, which is comparable to the method of example 2, except that: in the step (4), the dosage of the glucose is calculated according to the total nitrogen content in the treated water III, so that the COD/TN is 8, the total nitrogen removal rate in the step is increased to 85%, the total nitrogen content of the treated water IV in the step (4) is 6.8mg/L and is far lower than the total nitrogen emission limit value, but the dosage of the carbon source is large, the operation cost is increased, and the COD of the treated water V obtained in the step (5) is increased to 47 mg/L. Excessive carbon source enters the membrane separation tank 5, is easy to be pumped away during membrane separation, and has the risk of excessive COD (chemical oxygen demand) of effluent water quality.
Example 6:
this example provides a method for the biological treatment of electroplating integrated wastewater, which is comparable to the method of example 3, except that: the microbial sludge intercepted by the hollow fiber membrane component 9 in the step (5) flows back to the primary aerobic tank 1, the reflux ratio is 500%, the COD removal rate in the step (1) is improved to 57%, the ammonia nitrogen removal rate is 80%, the total nitrogen removal rate in the step (2) is improved to 71%, but the energy consumption of the operation of the microbial sludge reflux pump is increased by 20%.
Example 7:
this example provides a method for the biological treatment of electroplating integrated wastewater, which is comparable to the method of example 1, except that: and (5) refluxing the microbial sludge intercepted by the hollow fiber membrane component 9 to the primary aerobic tank 1, wherein the reflux ratio is 50%. At the moment, the COD removal rate in the step (1) is reduced to 48%, the ammonia nitrogen removal rate is reduced to 67%, the total nitrogen removal rate in the step (2) is reduced to 65%, the COD of the effluent in the step (5) is increased to 53, the ammonia nitrogen is increased to 5.4mg/L, the total nitrogen is increased to 15.4mg/L, and the effluent quality fails to reach the standard.
Comparative example 1:
this comparative example provides a method for biological treatment of electroplating integrated wastewater, which is comparable to the method of example 1, except that: and (4) directly introducing the treated water II into the membrane separation tank 5 without performing the step (3) and the step (4). The COD content in the effluent of the membrane separation tank 5 is 102mg/L, the ammonia nitrogen content is 22.8mg/L, the total nitrogen content is 54mg/L, and the three indexes exceed the emission limit value.
The COD content, ammonia nitrogen content, total nitrogen content, suspended solid concentration and effluent quality of the treated water V obtained in examples 1-7 and comparative example 1 were determined to reach the standard, and the results are shown in Table 1.
TABLE 1
In the embodiment 1-3, the treatment method is adopted, and the amount of the carbon source and the reflux ratio of the microbial sludge in the treatment process are further controlled, so that the COD content in the treated water is less than or equal to 50mg/L, the ammonia nitrogen content is less than or equal to 5.0mg/L, and the total nitrogen content is less than or equal to 15.0 mg/L; example 4 the addition of carbon source was reduced during the secondary anoxic treatment, i.e. COD/TN ═ 2, so that the total nitrogen content in the treated water exceeded the emission limit; in the example 5, the addition of a carbon source is added in the secondary anoxic treatment process, that is, COD/TN is 8, so that the total nitrogen content in the treated water is 6.8mg/L and is far lower than the total nitrogen emission limit value, but the operation cost is too high due to large carbon source consumption, and the effluent COD content is increased to 47mg/L, so that the effluent COD exceeds the standard. Example 6 in the treatment process, the reflux ratio of the microbial sludge is increased to 500%, the effluent pollutant content is reduced, but the energy consumption of a reflux pump is increased, so that the operation cost is overhigh; example 7 the reflux ratio of the microbial sludge was reduced to 50% during the treatment process so that the COD, ammonia nitrogen and total nitrogen content of the treated water all exceeded the emission limits.
Comparative example 1 reduces a group of aerobic-anoxic treatments, so that COD, ammonia nitrogen and total nitrogen in the effluent quality exceed the discharge limit.
It can be seen from the above examples and comparative examples that the method of the present invention can effectively remove various nitrogen and organic matters in the wastewater by five-stage aerobic-anoxic-membrane separation treatment, and aiming at the electroplating comprehensive wastewater with high nitrogen content and low carbon content, and further control the reaction conditions in the treatment process, such that the COD content in the treated water is less than or equal to 50mg/L, the ammonia nitrogen content is less than or equal to 5.0mg/L, and the total nitrogen content is less than or equal to 15.0 mg/L. The method has simple process flow, ensures that the effluent quality can continuously and stably meet the requirement of the wastewater discharge standard of the electroplating industry, and has better industrial application prospect.
The applicant states that the present invention is illustrated in detail by the above examples, but the present invention is not limited to the above detailed methods, i.e. it is not meant that the present invention must rely on the above detailed methods for its implementation. It will be apparent to those skilled in the art that any modifications to the present invention, equivalents thereof, additions of additional operations, selection of specific ways, etc., are within the scope and disclosure of the present invention.
Claims (10)
1. A method for biologically treating electroplating integrated wastewater is characterized by comprising the following steps:
(1) primary aerobic treatment: introducing the electroplating comprehensive wastewater into a primary aerobic tank, adding microbial sludge, and performing primary nitration reaction to obtain treated water I;
(2) first-stage anoxic treatment: introducing the treated water I obtained in the step (1) into a primary anoxic tank, adding a carbon source, and performing primary denitrification reaction to obtain treated water II;
(3) secondary aerobic treatment: introducing the treated water II obtained in the step (2) into a secondary aerobic tank for secondary nitration reaction to obtain treated water III;
(4) secondary anoxic treatment: introducing the treated water III obtained in the step (3) into a secondary anoxic tank, adding a carbon source, and performing secondary denitrification reaction to obtain treated water IV;
(5) membrane separation treatment: introducing the treated water IV obtained in the step (4) into a membrane separation tank, and filtering to obtain treated water V; and (4) returning the concentrated microbial sludge after filtration to the primary aerobic tank.
2. The method according to claim 1, wherein the COD content in the electroplating integrated wastewater is less than or equal to 250mg/L, the ammonia nitrogen content is less than or equal to 150mg/L, and the total nitrogen content is less than or equal to 200 mg/L.
3. The method according to claim 1 or 2, wherein the primary aerobic tank is provided with a microporous aeration head;
preferably, the time of the primary aerobic treatment is 8-12 h;
preferably, the concentration of dissolved oxygen in the primary aerobic treatment process is controlled to be 2-5 mg/L.
4. A method according to any one of claims 1 to 3, wherein a submersible mixer is provided in the primary anoxic tank;
preferably, the time of the first-stage anoxic treatment is 4-8 h;
preferably, the carbon source is used in an amount of 4-6 COD/TN based on the total nitrogen in the treated water I.
5. The preparation method of the method according to any one of claims 1 to 4, wherein a microporous aeration head is arranged in the secondary aerobic tank;
preferably, the secondary aerobic treatment time is 6-10 h;
preferably, the concentration of dissolved oxygen in the secondary aerobic treatment process is controlled to be 2-5 mg/L.
6. The method of any one of claims 1 to 5, wherein a submersible mixer is provided in the secondary anoxic tank;
preferably, the time of the secondary anoxic treatment is 2-6 h;
preferably, the carbon source is used in an amount of 4-6 COD/TN based on the total nitrogen in the treated water III.
7. The method of any one of claims 1 to 6, wherein the carbon source is glucose.
8. The method according to any one of claims 1 to 7, wherein the filtration of step (5) is performed using a hollow fiber membrane module;
preferably, the flux of the hollow fiber membrane module is 12-18L/(m)2·h)；
Preferably, the filtration resistance of the hollow fiber membrane module is less than 50 kPa;
preferably, the hollow fiber membrane component is provided with an aeration device and an online membrane cleaning system;
preferably, the cleaning step of the membrane online cleaning system comprises the steps of carrying out online alternate cleaning of sodium chlorate and hydrochloric acid every 17-23 days, and carrying out offline sodium hypochlorite and hydrochloric acid chemical cleaning every half year.
9. The method according to any one of claims 1 to 8, wherein the concentration of the microbial sludge in the primary aerobic tank, the primary anoxic tank, the secondary aerobic tank and the secondary anoxic tank is independently 6 to 10 g/L.
10. The method according to any one of claims 1 to 9, wherein the reflux ratio of the microbial sludge in the step (5) is 100 to 300%.
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| KR20070014857A (en) * | 2005-07-29 | 2007-02-01 | 주식회사 미래엔지니어링 | System and method for biological treatment of wastewater using mbr and zeolite powder |
| CN110436630A (en) * | 2019-09-02 | 2019-11-12 | 上海水合环境工程有限公司 | Toxic, high nitrogenous chemical engineering sewage coupled film biological treatment reactor |
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