CN116768360B - Pig farm wastewater treatment method - Google Patents
Pig farm wastewater treatment method Download PDFInfo
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- CN116768360B CN116768360B CN202311016819.2A CN202311016819A CN116768360B CN 116768360 B CN116768360 B CN 116768360B CN 202311016819 A CN202311016819 A CN 202311016819A CN 116768360 B CN116768360 B CN 116768360B
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- 238000011282 treatment Methods 0.000 claims abstract description 50
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- 238000011221 initial treatment Methods 0.000 claims abstract description 10
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Abstract
The invention provides a pig farm wastewater treatment method. The processing method comprises the following steps: introducing wastewater to be treated into a complete mixing reactor; under anaerobic conditions, stirring conditions and a preset first preset pH value, biologically treating the wastewater to be treated, and performing solid-liquid-gas separation by utilizing a three-phase separation assembly to obtain wastewater after primary treatment; under anaerobic conditions and a preset second preset pH value, in an anaerobic ceramic membrane bioreactor, performing biological treatment on the wastewater after primary treatment and performing solid-liquid separation by using a ceramic flat membrane to obtain wastewater after secondary treatment; under the condition of introducing air or oxygen and at a preset third preset pH value, in the inner and outer zone reactors, biological treatment is carried out on the secondary treated wastewater by two modes of short-cut nitrification-anaerobic ammonia oxidation and short-cut nitrification-denitrification to remove nitrogen, so as to obtain treated water. The treatment method provided by the invention has the advantages of high treatment efficiency and good treatment efficiency.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a pig farm wastewater treatment method.
Background
Pig farm wastewater mainly originates from pig manure, pig urine and farm flushing water. The wastewater is rich in nitrogen and phosphorus, organic matters and high suspended matters, is high-concentration organic wastewater, and can cause pollution to water body when being directly discharged.
At present, the treatment process which is more effective for pig farm wastewater comprises a direct SBR process and a Anarwia process, and the Anarwia process is superior to the direct SBR process in operation cost and water outlet effect. The COD value and the ammonia nitrogen concentration value in the treated water quality of the two processes reach the emission standard of pollutants in livestock and poultry farming (GB 18596-2001), but the increasingly improved environmental protection requirements at present cannot be met, and the problems of complex facilities, high energy consumption, large sludge production amount, high subsequent sludge treatment cost and need of professional personnel management still exist.
Disclosure of Invention
The invention aims to provide a pig farm wastewater treatment method with high treatment efficiency and good treatment efficiency.
In order to achieve the above purpose, the invention provides a pig farm wastewater treatment method, which comprises the following steps:
Introducing wastewater to be treated into a complete mixing reactor inoculated with anaerobic digested sludge, wherein the complete mixing reactor comprises a reaction tank, a stirrer accommodated in the reaction tank and a three-phase separation assembly accommodated in the reaction tank and positioned above stirring paddles of the stirrer;
Under anaerobic conditions, stirring conditions and a preset first preset pH value, performing anaerobic digestion biological treatment on the wastewater to be treated and performing solid-liquid-gas separation by utilizing the three-phase separation assembly to obtain wastewater after primary treatment, wherein the first preset pH value is 4-5;
Under anaerobic conditions and a preset second preset pH value, performing anaerobic digestion biological treatment on the wastewater after primary treatment in an anaerobic ceramic membrane bioreactor, and performing solid-liquid separation by utilizing a ceramic flat membrane of the anaerobic ceramic membrane bioreactor to obtain wastewater after secondary treatment, wherein the second preset pH value is 6.8-7.5, and a liquid inlet of the anaerobic ceramic membrane bioreactor is communicated with a water outlet of the completely mixed reactor;
Under the condition of introducing air or oxygen and at a preset third preset pH value, in an inner and outer partition reactor inoculated with biological sludge, performing biological treatment on the wastewater after secondary treatment by two modes of short-cut nitrification-anaerobic ammonia oxidation and short-cut nitrification-denitrification to remove nitrogen and obtain treated water, wherein the biological sludge comprises nitrified sludge and anaerobic ammonia oxidation sludge, the second preset pH value is 7.5-8.0, and an air inlet pipe of the inner and outer partition reactor is communicated with a liquid outlet of the anaerobic ceramic membrane biological reaction.
In a specific embodiment, the starting process of the device used in the processing method is as follows: the method comprises the steps of starting the complete mixing type reactor and the internal and external partition type reactor respectively, and after the complete mixing type reactor and the internal and external partition type reactor are started successfully, communicating the complete mixing type reactor with the anaerobic ceramic membrane type bioreactor, and communicating the internal and external partition type reactor with the anaerobic ceramic membrane type bioreactor so as to enable the complete mixing type reactor, the anaerobic ceramic membrane type bioreactor and the internal and external partition type reactor to be communicated sequentially.
In a specific embodiment, the communicating of the perfect hybrid reactor with the anaerobic ceramic membrane bioreactor comprises: the water outlet of the complete mixing reactor is communicated with the liquid inlet of the anaerobic ceramic membrane bioreactor, the sludge outlet of the complete mixing reactor is communicated with the sludge inlet of the anaerobic ceramic membrane bioreactor, and the anaerobic digested sludge of the complete mixing reactor flows into the anaerobic ceramic membrane bioreactor at a first speed.
In a specific embodiment, when the concentration of the anaerobic digested sludge in the completely mixed reactor is less than 12g/L, the anaerobic digested sludge in the anaerobic ceramic membrane bioreactor is refluxed into the completely mixed reactor at a second speed, and the ratio of the second speed to the first speed is less than or equal to 0.3.
In a specific embodiment, the step of determining that the complete hybrid reactor is successfully started comprises:
Preparing four experimental wastewater with TCOD concentration of 500mg/L, 1000mg/L, 2500mg/L and 5000mg/L by using actual pig farm wastewater;
based on TCOD concentration values, sequentially introducing four kinds of experimental wastewater into the fully mixed reactor according to the sequence of small first and large second for biological treatment, wherein the premise of increasing the TCOD concentration of the experimental wastewater next time is that the COD removal rate corresponding to the current experimental wastewater reaches more than 85 percent;
And when the COD removal rate corresponding to the experimental wastewater with the TCOD concentration of 5000mg/L is stabilized to be more than 85%, the complete mixing reactor is started successfully.
In a specific embodiment, the step of determining that the internal and external partition reactor is started up successfully includes:
Four simulated wastewater with mass concentrations of 200mg/L, 400mg/L, 800mg/L and 1600mg/L of ammonium bicarbonate are prepared;
based on the ammonium bicarbonate mass concentration value, four kinds of simulated wastewater are sequentially introduced into the internal and external zone reactors according to the sequence of small first and large second for biological treatment, and the premise of increasing the mass concentration of the simulated wastewater next time is that the total nitrogen removal rate corresponding to the current simulated wastewater reaches more than 80%;
And when the total nitrogen removal rate corresponding to the simulated wastewater with the mass concentration of 1600mg/L of ammonium bicarbonate is stabilized to be more than 80%, the internal and external zone reactors are successfully started.
In a specific embodiment, the internal and external partition reactor comprises a shell, a first partition cylinder, a second partition cylinder, an aeration disc and a water inlet pipe, wherein the first partition cylinder is contained in the shell and is arranged at intervals with the shell, the second partition cylinder is contained in the first partition cylinder and is arranged at intervals with the first partition cylinder, the aeration disc is installed in the shell and is positioned right below the second partition cylinder, one end of the aeration disc is communicated with a liquid outlet of the anaerobic ceramic membrane bioreactor, the other end of the aeration disc extends out of the aeration disc to the position below the second partition cylinder, the aeration disc is used for providing oxygen so that a space in the second partition cylinder forms an aerobic zone, a zone between the second partition cylinder and the first partition cylinder is an anoxic zone, under the action of rising force provided by the aeration disc, wastewater flowing in through the water inlet pipe firstly flows into the aerobic zone, then flows into the anoxic zone and the anaerobic zone, and circularly flows, and the dissolved oxygen concentration of the aerobic zone is controlled to be 0.3 mg/L to 0.0 mg.
In a specific embodiment, the anaerobic ceramic membrane bioreactor comprises a reactor shell, a liquid inlet arranged at the lower end of the reactor shell, a liquid outlet arranged at the upper end of the reactor shell, a sludge inlet and a sludge outlet arranged at the lower end of the reactor shell, a ceramic flat membrane contained in the reactor shell, and an aeration component, wherein the sludge inlet is communicated with the sludge outlet of the reaction tank, the sludge outlet is communicated with the sludge return opening of the reaction tank, and the aeration component is used for enabling the anaerobic ceramic membrane bioreactor to be in an anaerobic state.
In a specific embodiment, the operation mode of the ceramic flat membrane comprises suction filtration, back flushing and stopping, wherein the ratio of the operation period of the suction filtration to the operation period of the back flushing to the operation period of the stopping is as follows: 4:1:4.
In a specific implementation mode, the three-phase separation assembly is located the top of the stirring thick liquid of agitator, the three-phase separation assembly include with the inner tube that the retort interval set up, both ends respectively with the inner tube with the connecting plate that the retort is connected, and be located in the inner tube and with the guide cylinder that the connecting plate is connected, the inner tube with the guide cylinder is hollow structure, the (mixing) shaft of agitator passes the guide cylinder stretches into in the retort, the delivery port is slightly less than the top of inner tube, wherein, the guide cylinder includes that the upper end stretches out the first part of inner tube, from the lower extreme of first part is gradually to keeping away from the second part that the axis direction of first part extends, the second part with the connecting plate is connected, a plurality of through-holes have been seted up on the connecting plate.
The beneficial effects of the invention at least comprise:
1. The pig farm wastewater treatment method provided by the invention is characterized in that the pig farm wastewater treatment method is carried out by a wastewater treatment device consisting of a complete mixing reactor, an anaerobic ceramic membrane bioreactor and an internal and external partition reactor which are sequentially communicated, wherein in the complete mixing reactor, hydrolysis fermentation bacteria, hydrogen-producing acetogenic bacteria and homoacetogenic bacteria are beneficial to growth by controlling the reaction conditions to be acidic, so that organic matters in the wastewater mainly undergo hydrolysis fermentation and acidification reactions in the complete mixing reactor, and wastewater containing hydrolysis products and acidification products, hydrogen, methane and the like are generated; in the anaerobic ceramic membrane bioreactor, the reaction conditions are controlled to be neutral, so that the methanogenic archaea can grow, hydrolysis products and acidification products can be converted into methane, and organic matters can be removed; the internal and external zone reactors biologically treat nitrogen in the wastewater in a short-cut nitrification-anaerobic ammonia oxidation mode and a short-cut nitrification-denitrification mode to remove nitrogen and obtain treated water; thus, the treatment method provided by the invention is used for treating the wastewater, has the effective points of high treatment efficiency and good treatment effect, and can be used for treating the actual pig farm wastewater with the treatment concentration (calculated by TCOD) of 7000-8000mg/L, the effluent quality can realize that COD is lower than 200mg/L, ammonia nitrogen is lower than 10mg/L, and the removal rates of COD and ammonia nitrogen are all over 95%.
2. According to the invention, the anaerobic digestion process partition is realized through the complete mixing reactor and the anaerobic ceramic membrane bioreactor, the front-end acidic environment is favorable for the growth of hydrolytic fermentation bacteria, hydrogen-producing acetogenic bacteria and homoacetogenic bacteria, and the middle-end neutral environment is favorable for the growth of methanogenic archaea, so that the organic matter removal performance is improved.
3. The starting process of the equipment used in the processing method provided by the invention is as follows: firstly, independently starting the complete mixing reactor and the internal and external partition reactors, and after the complete mixing reactor and the anaerobic ceramic membrane bioreactor are successfully started, communicating the complete mixing reactor with the anaerobic ceramic membrane bioreactor, and communicating the internal and external partition reactors with the anaerobic ceramic membrane bioreactor so as to ensure that the complete mixing reactor, the anaerobic ceramic membrane bioreactor and the internal and external partition reactors are communicated in sequence; therefore, after the mixed reactor and the internal and external partition reactors have better removal effect, the mixed reactor and the internal and external partition reactors are respectively combined with the anaerobic ceramic membrane bioreactor, so that the COD value and the ammonia nitrogen value of the treated water are ensured to be lower.
4. The invention provides a complete mixing type reactor which comprises a reaction tank, a stirrer accommodated in the reaction tank and a three-phase separation assembly accommodated in the reaction tank and positioned above stirring paddles of the stirrer; through setting up three-phase separation subassembly can realize solid-gas-liquid separation, can significantly reduce the mud that gets into in the rear end anaerobic ceramic membrane bioreactor, slow down the membrane pollution by a wide margin.
5. By arranging the ceramic flat membrane in the anaerobic ceramic membrane bioreactor provided by the invention, digested sludge can be intercepted, so that the sludge enters the rear-end internal-external partition reactor to be filtrate, and the usage amount of chemical agents to be added for sludge precipitation is greatly saved; the ceramic flat membrane has the advantages of good pollution resistance, high permeability, good recoverability, good chemical stability, long service life and the like.
6. The invention provides an internal and external partitioned reactor which comprises a shell, a first partition cylinder, a second partition cylinder, an aeration disc and a water inlet pipe, wherein the first partition cylinder is accommodated in the shell and is arranged at intervals with the shell; thus, the arrangement of the reaction chambers of the internal and external partition reactors provides living space for nitrified sludge, denitrified sludge and anaerobic ammonia oxidation sludge, can realize 2 denitrification processes of short-cut nitrification-anaerobic ammonia oxidation and short-cut nitrification-denitrification, and has the advantages of compact structure, small occupied area and good denitrification effect.
In addition to the objects, features and advantages described above, the present invention has other objects, features and advantages. The present invention will be described in further detail with reference to the drawings.
Drawings
FIG. 1 is a flow chart of steps of a pig farm wastewater treatment method according to an embodiment of the present invention;
FIG. 2 is a schematic process flow diagram of a pig farm wastewater treatment method according to an embodiment of the present invention;
FIG. 3 is a schematic perspective view of a fully hybrid reactor according to an embodiment of the present invention;
FIG. 4 is an exploded perspective view of the complete mixing reactor of FIG. 3;
FIG. 5 is a schematic view of a partial perspective view of the complete mixing reactor shown in FIG. 3;
FIG. 6 is a schematic perspective view of an internal and external zone reactor according to an embodiment of the present invention;
FIG. 7 is a schematic view of a partial perspective view of the internally and externally partitioned reactor shown in FIG. 6;
FIG. 8 is a schematic diagram of the flow of wastewater in the internally and externally zoned reactor of FIG. 6.
Detailed Description
The embodiments of the invention are described in detail below with reference to the attached drawings, but the invention can be defined and covered in a number of different embodiments according to the claims.
Referring to fig. 1 to 5, the present invention provides a pig farm wastewater treatment method, which treats pig farm wastewater by a wastewater treatment apparatus 100 comprising a completely mixed reactor 20, an anaerobic ceramic membrane bioreactor 30 and an inner and outer partition reactor 40 which are sequentially communicated, wherein the completely mixed reactor+the anaerobic ceramic membrane bioreactor performs anaerobic digestion treatment on organic matters in the wastewater to remove the organic matters, and the inner and outer partition reactors 40 perform biological treatment on nitrogen in the wastewater to remove the nitrogen by two modes of short-cut nitrification-anaerobic ammonia oxidation and short-cut nitrification-denitrification.
The pig farm wastewater treatment method comprises the following steps:
step S11, introducing wastewater to be treated into a complete mixing reactor 20 inoculated with anaerobic digestion sludge, wherein the complete mixing reactor 20 comprises a reaction tank 21, a stirrer 22 accommodated in the reaction tank, and a three-phase separation assembly 23 accommodated in the reaction tank 21 and positioned above stirring paddles of the stirrer 22;
The waste water to be treated is waste water obtained by removing excrement and impurities in the waste water in a filtering mode, and particularly can be filtered through an air floatation machine.
Preferably, the concentration of the inoculated anaerobic digestion sludge is 8-10 g/L.
In this embodiment, the inoculated anaerobic digested sludge is obtained from municipal sewage plant secondary sedimentation tank sludge (municipal sludge for short), and the municipal sludge is first subjected to elutriation to remove sediment and then the activated sludge at the upper layer.
The reaction tank 21 comprises a tank body 211 with an accommodating space, a water inlet 212 arranged at the lower end of the tank body 211, a water outlet 213 arranged at the upper end of the tank body 211, a sludge outlet 214 arranged at the lower end of the tank body 211, and a sludge return opening 215 arranged at the lower end of the tank body 211; the wastewater to be treated flows into the tank body 211 through the water inlet 212, the water outlet 213 is communicated with the anaerobic ceramic membrane bioreactor 30, anaerobic digested sludge in the reaction tank 211 flows into the anaerobic ceramic membrane bioreactor 30 through the sludge outlet 214, and anaerobic digested sludge in the anaerobic ceramic membrane bioreactor 30 flows back into the reaction tank 211 through the sludge return opening 215.
In this embodiment, the tank 211 is a cylindrical tank, and the water inlet 212 and the water outlet 213 are provided on the side wall of the tank 211 and are opposite to each other; the sludge outlet 214 is formed on the bottom surface/side wall of the tank 211, and the sludge return opening 215 is formed on the bottom surface/side wall of the tank 211.
The stirrer 22 is installed in the tank 211, and comprises a stirring shaft 221, a stirring paddle 222 installed at the lower end of the stirring shaft 221, and a driving motor for driving the stirring shaft 221.
In this embodiment, the stirring shaft 221 is located at a position where the central axis of the tank 211 is located.
In this embodiment, the stirring paddle 222 includes a plurality of sets of paddles, and the distance between the bottom set of paddles and the bottom surface of the tank 211 is 1/5 of the height of the tank, and the distance between the bottom set of paddles and the bottom surface of the tank 211 is 3/5 of the height of the tank.
The three-phase separation assembly 23 is located above the agitator paddle 222 of the agitator 22.
The three-phase separation assembly 23 comprises an inner cylinder 231 arranged at intervals with the tank body 211, a connecting plate 232 with two ends respectively connected with the inner cylinder 231 and the tank body 211, a guide cylinder 233 positioned in the inner cylinder 231 and connected with the connecting plate 232, and a plurality of upright posts 234 for connecting the connecting plate 232 and the guide cylinder 233.
Preferably, the central axis of the tank 211, the central axis of the inner cylinder 231, and the central axis of the guide cylinder 233 are located on the same straight line.
In this embodiment, the inner cylinder 231 has a hollow cylindrical shape.
In this embodiment, the water outlet 213 is slightly lower than the top end of the inner cylinder 231.
In this embodiment, the connection plate 232 has a circular ring structure, and a plurality of through holes 2321 are formed in the connection plate 232.
Preferably, the through hole 2321 is a circular through hole, and its aperture is less than 3mm.
In other embodiments, the through holes 2321 may be through holes with other shapes, but the equivalent pore diameters are smaller than 3mm.
Preferably, the plurality of through holes 2321 are uniformly distributed according to a certain rule.
In this embodiment, an end of the guide cylinder 233 facing the water inlet 212 is horn-shaped, specifically, the guide cylinder 233 includes a first portion 2331 with an upper end extending out of the inner cylinder 231, and a second portion 2332 extending from a lower end of the first portion 2331 gradually toward a central axis direction away from the first portion 2331, and the second portion 2332 is connected to the connecting plate 232.
In this embodiment, the first portion 2331 is hollow cylindrical, the second portion 2332 is hollow truncated cone, and the caliber of the top end of the second portion 2332 is smaller than that of the bottom end.
The top end of the second portion 2332 is an end connected to the first portion 2331, and the bottom end of the second portion 2332 is an end of the second portion 2332 away from the first portion 2331.
Preferably, the second portion 2332 extends out of the inner barrel 231, and the upright 234 is connected at one end to an end of the second portion 2332 remote from the first portion 2331 and at the other end to the connection plate 232.
Preferably, the guide cylinder 233 is spaced from the stirring paddle 222, and the distance between the guide cylinder 233 and the stirring paddle is 3/20-1/4 of the height of the tank 211.
More preferably, the height of the guide cylinder 233 is equal to or less than 1/4 of the height of the tank 211, and in particular, the height of the guide cylinder 233 may be 1/4 of the height of the tank 211, or may be 1/5 of the height of the tank 211, etc.
Preferably, a plurality of the posts 234 are evenly distributed.
In this embodiment, the number of the columns 234 is 6 to 8.
And step S12, performing anaerobic digestion biological treatment on the wastewater to be treated under anaerobic conditions, stirring conditions and a preset first preset pH value, and performing solid-liquid-gas separation by utilizing the three-phase separation assembly to obtain wastewater after primary treatment, wherein the first preset pH value is 4-5.
In this step, the pH can be controlled by adding hydrochloric acid.
In this step, the reaction system in the reaction tank is controlled to be in an acidic environment, which is favorable for the growth of hydrolytic fermentation bacteria, hydrogen-producing acetogenic bacteria and homoacetogenic bacteria, so that the organic matters in the wastewater mainly undergo hydrolytic fermentation and acidification reactions in the complete mixing reactor 20, and wastewater containing hydrolysis products and acidification products, hydrogen, methane and the like are generated.
That is, in the present embodiment, the corresponding anaerobic digestion biological treatment in step S12 is hydrolytic fermentation and acidification treatment.
It will be appreciated that the tank 211 is further provided with a gas outlet, which is in communication with a water sealed bottle, to ensure that no air is introduced into the fully-mixed reactor 20.
The wastewater to be treated flows into the complete mixing reactor 20 through the water inlet 212, and organic matters in the wastewater react with anaerobic digestion activated sludge in the tank 211 under acidic conditions and stirring conditions to generate wastewater containing water products and acidification products, hydrogen, methane and the like; in the reaction process, the generated gas can drive the sludge and impurities at the lower part of the tank body 211 to float upwards, the guide cylinder 233 can separate the floating impurities, the gas can flow out from the upper surface of the guide cylinder 233, the separation between the guide cylinder 233 and the inner cylinder 231 can realize solid-liquid-gas separation, the through holes 2321 on the connecting plate 232 can ensure that the internal-external air pressure difference is not too large, and meanwhile, overflowed sludge can be settled down to fall to the bottom of the tank body 211 after the gas is discharged.
The complete mixing type reactor 20 provided by the invention improves the reactor by adding the three-phase separation component, can realize mud-water separation, can also intercept food residues which are difficult to hydrolyze in a tank body, greatly reduces sludge and impurities entering the rear anaerobic ceramic membrane bioreactor 30, and greatly slows down membrane pollution. The main components of food residues in the waste water are cellulose and hemicellulose polysaccharide organic matters, the hydrolysis period is long (about 30 d), if the food residues are not trapped, irreversible pollution is caused to the membrane in the anaerobic ceramic membrane bioreactor 30, and the service life of the anaerobic ceramic membrane bioreactor 30 is reduced.
S13, performing anaerobic digestion biological treatment on the wastewater after primary treatment in an anaerobic ceramic membrane bioreactor under anaerobic conditions and a preset second preset pH value, and performing solid-liquid separation by utilizing a ceramic flat membrane of the anaerobic ceramic membrane bioreactor to obtain wastewater after secondary treatment, wherein the second preset pH value is 6.8-7.5, and a liquid inlet of the anaerobic ceramic membrane bioreactor is communicated with a water outlet of the complete mixing type reactor;
In this step, the reaction system in the anaerobic ceramic membrane bioreactor is controlled to be in a neutral environment, so that methanogenic archaea is facilitated to grow, and thus, organic matters in the wastewater mainly undergo methanation reaction in the anaerobic ceramic membrane bioreactor 30, and hydrolysis products and acidification products are converted into methane, so that the organic matters in the wastewater are removed.
The invention realizes the anaerobic digestion process partition through the complete mixing reactor 20 and the anaerobic ceramic membrane bioreactor 30, the front acid environment is favorable for the growth of hydrolytic zymobacteria, hydrogen-producing acetogenic bacteria and homoacetogenic bacteria, and the middle neutral environment is favorable for the growth of methanogenic archaea, thereby improving the organic matter removal performance.
Preferably, the sludge in the anaerobic ceramic membrane bioreactor 30 is derived from the completely mixed reactor 20, and in this embodiment, after the completely mixed reactor 20 is successfully started, the completely mixed reactor 20 is communicated with the anaerobic ceramic membrane bioreactor 30, so that the sludge in the completely mixed reactor 20 flows into the anaerobic ceramic membrane bioreactor as inoculated sludge. And after the concentration of the anaerobic digestion activated sludge reaches 50g/L after long-term continuous operation, directly discharging.
The anaerobic ceramic membrane bioreactor 30 provided by the invention has the following structure:
the anaerobic ceramic membrane bioreactor 30 comprises a reactor shell 31, a liquid inlet 32 arranged at the lower end of the reactor shell 31, a liquid outlet 33 arranged at the upper end of the reactor shell 31, a sludge inlet 34 arranged at the lower end of the reactor shell, a ceramic flat membrane 35 accommodated in the reactor shell 31 and an aeration assembly 36, wherein the aeration assembly 36 is used for enabling the anaerobic ceramic membrane bioreactor 30 to be in an anaerobic state.
In this embodiment, the reactor housing 31 is a cylindrical housing, the liquid inlet 32 is formed on a side wall of the reactor housing 31 and is communicated with the water outlet 213 of the completely mixed reactor 20, and the wastewater treated by the completely mixed reactor flows into the reactor housing 31 through the liquid inlet 32; the liquid outlet 33 is arranged on the upper bottom surface of the reactor shell 31 and is communicated with the filtrate outlet of the ceramic flat membrane 35; the sludge inlet 34 is formed on the lower bottom surface of the reactor housing 31 and is communicated with the sludge outlet of the complete mixing reactor 20.
Preferably, the anaerobic ceramic membrane bioreactor 30 further comprises a sludge outlet 37, and when the sludge concentration in the complete mixing reactor 20 is lower than 12g/L, activated sludge in the anaerobic ceramic membrane bioreactor 30 is automatically started and pumped into the complete mixing reactor 20. I.e. the concentration of anaerobic digested activated sludge in the fully mixed reactor is greater than or equal to 12g/L.
The ceramic flat membrane 35 is immersed in the wastewater, and the water quality of the effluent is greatly enhanced through the filtering effect of the membrane, so that anaerobic digestion activated sludge flowing in from the front end is intercepted, and the anaerobic digestion activated sludge enters the inner and outer partition reactors 40 at the rear end and is filtrate, so that the usage amount of chemical agents to be added for sludge precipitation is greatly saved.
The ceramic flat membrane 35 is applied to pig farm wastewater treatment, and the service life of the membrane is greatly prolonged by virtue of the advantages of good pollution resistance, high permeability, good recoverability, good chemical stability, long service life and the like of the ceramic flat membrane.
The aeration assembly 36 comprises a plurality of strip aeration pipes 361, a biogas inlet 362 arranged on the lower bottom surface of the reactor shell 31, a biogas outlet 363 arranged on the upper bottom surface of the reactor shell 31, and an air pump with an air inlet end communicated with the biogas outlet 363 and an air outlet end communicated with the biogas inlet 362, wherein biogas pumped by the air pump is introduced into the plurality of strip aeration pipes 361.
In this embodiment, a plurality of strip-shaped aeration pipes 361 are located below the ceramic flat plate film 35.
The wastewater and the anaerobic digested activated sludge react anaerobically to generate biogas, the biogas is extracted from the upper part of the reactor housing 31 by an air pump, and is introduced into a plurality of strip-shaped aeration pipes 361 to impact the surface of the ceramic flat membrane 35.
And S14, under the condition of introducing air or oxygen and at a preset third preset pH value, in an inner and outer partition reactor inoculated with biological sludge, performing biological treatment on the secondary treated wastewater by two modes of short-cut nitrification-anaerobic ammonia oxidation and short-cut nitrification-denitrification to remove nitrogen and obtain treated water, wherein the biological sludge comprises nitrified sludge and anaerobic ammonia oxidation sludge, the second preset pH value is 7.5-8.0, and an air inlet pipe of the inner and outer partition reactor is communicated with a liquid outlet of the anaerobic ceramic membrane biological reaction.
Preferably, the total concentration of the inoculated nitrified sludge and anaerobic ammoxidation sludge is 8g/L, and after long-term continuous operation, the calcium magnesium phosphate sediment precipitated at the bottom is discharged through a sludge discharge port.
Preferably, the nitrified sludge and anaerobic ammonium oxidation sludge inoculated by the inner and outer partition reactors 40 are crushed by a wall breaking machine, and then are subjected to washing by clean water to remove calcified substances, and then the upper sludge is taken for inoculation.
Referring to fig. 6 to 8, the structure of the internal and external zone reactor 40 provided by the present invention is as follows:
The inside-outside partition reactor 40 includes a housing 41, a first partition tube 42 accommodated in the housing 41 and spaced apart from the housing 41, a second partition tube 43 accommodated in the first partition tube 42 and spaced apart from the first partition tube 42, a plurality of connection rods 44 having one ends connected to the housing 41 and the other ends connected to the first partition tube 42, a plurality of connection columns 45 having one ends connected to the first partition tube 42 and the other ends connected to the second partition tube 43, and an aeration disc 46 installed in the housing 41 and located directly below the second partition tube 43, the aeration disc 46 being for supplying oxygen so that the space in the second partition tube 43 forms an aerobic zone.
The housing 41 includes a cylindrical housing body 411, a hemispherical housing extension 412 extending from one end of the housing body 411, a water inlet pipe 413 having one end communicating with the liquid outlet 33 of the anaerobic ceramic membrane bioreactor 30 and the other end extending through the bottom end of the housing extension 412 and extending out of the aeration disc 46, a sludge outlet 414 provided at the lower end of the housing extension 412, and a water outlet pipe 415 having one end communicating with the anaerobic zone and the other end extending out of the housing body 411.
The shell main body 411 and the shell extension 412 together enclose the reaction scheme of the inner and outer zone reactor 40; the water inlet pipe 413 extends out of the aeration disc 46 so that the incoming wastewater can first go into the second separation cylinder under the action of the lifting force provided by the aeration disc 46; the sludge discharge port 414 is used for discharging the sediment of the calcium magnesium phosphate deposited at the bottom; the treated water discharged through the water outlet pipe 415 is water meeting the discharge standard, and can be directly discharged or used for other purposes.
The first partition cylinder 42 includes a first cylinder body 421 having a hollow cylindrical shape, and a first cylinder extension 422 extending from a lower end of the first cylinder body 421 gradually toward a central axis direction of the housing 41; the first cylinder extension 422 is hollow and truncated cone-shaped, and the top caliber of the first cylinder extension 422 is larger than the bottom caliber.
The second partition cylinder 43 includes a second cylinder body 431 having a hollow cylindrical shape, and a second cylinder extension 432 extending from a lower end of the second cylinder body 431 gradually in a direction away from the central axis of the housing 41; the second cylinder extension 432 is hollow and truncated cone, and the diameter of the top end of the second cylinder extension 432 is smaller than that of the bottom end.
In this embodiment, an end of the second cylinder extension 432 away from the second cylinder body 431 is on the same plane as an end of the first cylinder body 421 near the first cylinder extension 422, and a gap for flowing waste water is provided between a bottom end of the second cylinder extension 432 and the first cylinder body 421.
In this embodiment, the top end of the first cylinder body 421 is higher than the top end of the second cylinder body 431, and the end of the water outlet pipe 415 extending into the anaerobic zone is slightly lower than the top end of the first cylinder body 421.
The first separation cylinder 42 is sandwiched between the second separation cylinder 43 and the casing 41, and the three separate the space in the casing 41 into an aerobic zone 40A, an anoxic zone 40B and an anaerobic zone 40C, wherein the space enclosed by the second separation cylinder 43 is the aerobic zone 40A, the area between the second separation cylinder 43 and the first separation cylinder 42 is the anoxic zone 40B, the area between the first separation cylinder 42 and the casing 41 is the anaerobic zone 40C, the wastewater flowing in through the water inlet pipe 413 directly enters the aerobic zone 40A under the action of the rising force provided by the air exposed by the aeration disc 46, then flows out from the top end of the second separation cylinder 43 into the anoxic zone 40B or the anaerobic zone 40C, the water in the anoxic zone flows into the aerobic zone or the anaerobic zone 40C again, the water in the anaerobic zone flows into the aerobic zone or directly flows out, and the wastewater undergoes the shortcut nitrification-anaerobic ammonia oxidation-denitrification-2 denitrification processes in the internal and external zone reactors.
Preferably, the dissolved oxygen concentration of the aerobic zone is controlled to be 0.3-1.0 mg/L.
In the present embodiment, the plurality of connection rods 44 include a plurality of first connection rods 441 having one end connected to the lower end of the first cylinder extension 422 and the other end connected to the bottom of the housing extension 412, and a plurality of second connection rods 442 having one end connected to the inner wall of the housing main body 411 and the other end connected to the outer wall of the first cylinder main body 421, and the first partition cylinder 42 is fixed by the plurality of first connection rods 441 and the plurality of second connection rods 442.
In this embodiment, the number of the first connecting rods 441 is 6 to 8, and the first connecting rods 441 are uniformly spaced.
In this embodiment, the number of the second connecting rods 442 is 4, and they are uniformly spaced.
In this embodiment, one end of the plurality of connection posts 45 is connected to the inner wall of the first cylinder body 421, and the other end is connected to the outer wall of the second cylinder body 431, and the number of the connection posts 45 is 6 to 8, and the connection posts are uniformly spaced. The second partition cylinder 43 is fixed by a plurality of the connecting posts 45.
In this embodiment, the aeration disc 46 is mounted to the housing extension 412 by a bracket, and the gas introduced into the aeration disc 46 is air or oxygen.
Preferably, the diameter of the aeration disc 46 is smaller than or equal to the caliber of the lower end of the second partition cylinder 43.
Preferably, the central axis of the water inlet pipe 413, the central axis of the aeration disc 46, the central axis of the second separation cylinder 43, the central axis of the first separation cylinder 42, and the central axis of the housing 41 are all on the same straight line.
In the invention, wastewater to be treated enters the tank 211 from the water inlet 212 of the completely mixed reactor, is fully mixed with anaerobic digestion activated sludge in the tank 211 to generate hydrolysis and acidification reaction, so as to obtain primary treatment wastewater, and solid-liquid-gas full separation is realized through the three-phase separation assembly 23, wherein gas is directly discharged above the tank 211, sludge falls back to the bottom of the tank 211, and liquid flows out through the water outlet 213 and is conveyed to the anaerobic ceramic membrane bioreactor 30; in the anaerobic ceramic membrane bioreactor 30, the primary treatment wastewater undergoes methanation reaction to obtain secondary treatment wastewater by anaerobic digestion technology, and meanwhile, anaerobic digestion activated sludge is trapped in the reactor by ceramic flat membrane 35, only filtrate (wastewater) flows out through the liquid outlet and is conveyed to the inner and outer zone reactor 40, the inner and outer zone reactor 40 divides the reaction chamber into an aerobic zone 40A, an anoxic zone 40B and an anaerobic zone 40C by a first separation cylinder 42 and a second separation cylinder 43, the rising force is increased by an aeration disc, the water flowing in through the water inlet pipe firstly directly enters the aerobic zone 40A, then flows into the anoxic zone 40B and the anaerobic zone 40C, and the wastewater circularly flows in the aerobic zone 40A, the anoxic zone 40B and the anaerobic zone 40C, so that the secondary treatment wastewater generates 2 denitrification processes of short-cut nitrification-anaerobic ammonia oxidation and short-denitrification in the inner and outer zone reactor to remove nitrogen, and the purified water meeting the emission standard is obtained.
Preferably, the starting process of the device used in the processing method is: the method comprises the steps of starting the complete mixing reactor and the internal and external partition reactors respectively, and after the complete mixing reactor and the internal and external partition reactors are started successfully, communicating the complete mixing reactor with the anaerobic ceramic membrane bioreactor, and communicating the internal and external partition reactors with the anaerobic ceramic membrane bioreactor so as to enable the complete mixing reactor, the anaerobic ceramic membrane bioreactor and the internal and external partition reactors to be communicated in sequence.
Preferably, the step of judging that the complete mixing reactor is started up successfully includes:
Preparing four experimental wastewater with TCOD concentration of 500mg/L, 1000mg/L, 2500mg/L and 5000mg/L by using actual pig farm wastewater;
based on TCOD concentration values, sequentially introducing four kinds of experimental wastewater into the fully mixed reactor according to the sequence of small first and large second for biological treatment, wherein the premise of increasing the TCOD concentration of the experimental wastewater next time is that the COD removal rate corresponding to the current experimental wastewater reaches more than 85 percent;
And when the COD removal rate corresponding to the experimental wastewater with the TCOD concentration of 5000mg/L is stabilized to be more than 85%, the complete mixing reactor is started successfully.
Specifically, it can be understood that: firstly, 500mg/L of experimental wastewater is introduced into a complete mixing reactor for biological treatment, when the COD removal rate reaches more than 85%, 1000mg/L of experimental wastewater is introduced into the complete mixing reactor for biological treatment, when the COD removal rate reaches more than 85%, 2500mg/L of experimental wastewater is introduced into the complete mixing reactor for biological treatment, when the COD removal rate reaches more than 85%, 5000mg/L of experimental wastewater is introduced into the complete mixing reactor for biological treatment, and when the COD removal rate reaches more than 85%, the starting of the complete mixing reactor is successful.
Preferably, the step of judging that the internal and external partition reactors are started successfully comprises the following steps:
Four simulated wastewater with mass concentrations of 200mg/L, 400mg/L, 800mg/L and 1600mg/L of ammonium bicarbonate are prepared;
based on the ammonium bicarbonate mass concentration value, four kinds of simulated wastewater are sequentially introduced into the internal and external zone reactors according to the sequence of small first and large second for biological treatment, and the premise of increasing the mass concentration of the simulated wastewater next time is that the total nitrogen removal rate corresponding to the current simulated wastewater reaches more than 80%;
And when the total nitrogen removal rate corresponding to the simulated wastewater with the mass concentration of 1600mg/L of ammonium bicarbonate is stabilized to be more than 80%, the internal and external zone reactors are successfully started.
Specifically, it can be understood that: firstly, 200mg/L of simulated wastewater is introduced into an inner and outer zone reactor for biological treatment, when the total nitrogen removal rate reaches more than 80%, 400mg/L of simulated wastewater is introduced into the inner and outer zone reactor for biological treatment, when the total nitrogen removal rate reaches more than 80%, 1600mg/L of simulated wastewater is introduced into the inner and outer zone reactor for biological treatment, and when the total nitrogen removal rate reaches more than 80%, the starting of the inner and outer zone reactor is successful.
Preferably, the communication of the complete hybrid reactor 20 with the anaerobic ceramic membrane bioreactor 30 comprises: the water outlet of the completely mixed reactor 20 is communicated with the liquid inlet of the anaerobic ceramic membrane bioreactor 30, the sludge outlet of the completely mixed reactor 20 is communicated with the sludge inlet of the anaerobic ceramic membrane bioreactor 30, and the anaerobic digested sludge of the completely mixed reactor 20 flows into the anaerobic ceramic membrane bioreactor 30 at a first speed.
Preferably, when the concentration of the anaerobic digested sludge in the completely mixed reactor 20 is less than a preset concentration, the anaerobic digested sludge in the anaerobic ceramic membrane bioreactor 30 is refluxed into the completely mixed reactor 20 at a second speed, and the ratio of the second speed to the first speed is less than or equal to 0.3.
In this embodiment, the predetermined concentration is 12g/L.
Preferably, the communication between the inner and outer zone reactors 40 and the anaerobic ceramic membrane bioreactor 30 comprises: the liquid outlet of the anaerobic ceramic membrane bioreactor 30 is communicated with the water inlet pipe of the inner and outer partition reactor 40.
Preferably, the operation mode of the ceramic flat membrane comprises suction filtration, back flushing and stopping, wherein the ratio of the operation period of the suction filtration to the operation period of the back flushing to the operation period of stopping is as follows: 4:1:4.
By adopting the treatment method provided by the invention to treat the actual pig farm wastewater with the treatment concentration (calculated by TCOD) of 7000-8000mg/L, the effluent quality can realize that COD is lower than 200mg/L, ammonia nitrogen is lower than 10mg/L, and the removal rate of COD and ammonia nitrogen is over 95 percent.
The foregoing is a further detailed description of the invention in connection with specific preferred embodiments, and is not intended to limit the practice of the invention to such description. It will be apparent to those skilled in the art that several simple deductions and substitutions can be made without departing from the spirit of the invention, and these are considered to be within the scope of the invention.
Claims (10)
1. The pig farm wastewater treatment method is characterized by comprising the following steps of:
Introducing wastewater to be treated into a complete mixing reactor inoculated with anaerobic digested sludge, wherein the complete mixing reactor comprises a reaction tank, a stirrer accommodated in the reaction tank and a three-phase separation assembly accommodated in the reaction tank and positioned above stirring paddles of the stirrer;
Under anaerobic conditions, stirring conditions and a preset first preset pH value, performing anaerobic digestion biological treatment on the wastewater to be treated, and performing solid-liquid-gas separation by utilizing the three-phase separation assembly to obtain wastewater after primary treatment, wherein the first preset pH value is 4-5;
Under anaerobic conditions and a preset second preset pH value, in an anaerobic ceramic membrane bioreactor, performing anaerobic digestion biological treatment on the wastewater after primary treatment, and performing solid-liquid separation by utilizing a ceramic flat membrane of the anaerobic ceramic membrane bioreactor to obtain wastewater after secondary treatment, wherein the second preset pH value is 6.8-7.5, a liquid inlet of the anaerobic ceramic membrane bioreactor is communicated with a water outlet of the complete mixing reactor, and sludge of the anaerobic ceramic membrane bioreactor comes from the complete mixing reactor;
Under the condition of introducing air or oxygen and at a preset third preset pH value, in an inner and outer partition reactor inoculated with biological sludge, performing biological treatment on the wastewater after secondary treatment by using two modes of short-cut nitrification-anaerobic ammonia oxidation and short-cut nitrification-denitrification to remove nitrogen, so as to obtain treated water, wherein the biological sludge comprises nitrified sludge and anaerobic ammonia oxidation sludge, the third preset pH value is 7.5-8.0, a water inlet pipe of the inner and outer partition reactor is communicated with a liquid outlet of the anaerobic ceramic membrane bioreactor, the inner and outer partition reactor comprises a shell, a first partition cylinder accommodated in the shell and arranged at intervals with the shell, a second partition cylinder accommodated in the first partition cylinder and arranged at intervals with the first partition cylinder, an aeration disc arranged in the shell and positioned right below the second partition cylinder, and a partition disc with one end communicated with a liquid outlet of the anaerobic ceramic membrane bioreactor and the other end extending from the disc to the lower part of the second partition cylinder, wherein the water inlet pipe is provided with an oxygen-poor circulation zone, and the oxygen-poor circulation zone is formed between the first partition cylinder and the second partition cylinder, and the oxygen-poor circulation zone is formed between the oxygen-poor circulation zone and the oxygen-poor circulation zone.
2. The pig farm wastewater treatment method according to claim 1, wherein the starting process of the equipment used in the treatment method is: the method comprises the steps of firstly starting the complete mixing reactor and the internal and external partition reactors respectively, and after the complete mixing reactor and the internal and external partition reactors are started successfully, communicating the complete mixing reactor with the anaerobic ceramic membrane bioreactor, and communicating the internal and external partition reactors with the anaerobic ceramic membrane bioreactor so as to enable the complete mixing reactor, the anaerobic ceramic membrane bioreactor and the internal and external partition reactors to be communicated in sequence.
3. The pig farm wastewater treatment process according to claim 2, wherein the communication of the fully mixed reactor with the anaerobic ceramic membrane bioreactor comprises: the water outlet of the complete mixing reactor is communicated with the liquid inlet of the anaerobic ceramic membrane bioreactor, the sludge outlet of the complete mixing reactor is communicated with the sludge inlet of the anaerobic ceramic membrane bioreactor, and the anaerobic digested sludge of the complete mixing reactor flows into the anaerobic ceramic membrane bioreactor at a first speed.
4. A pig farm wastewater treatment method according to claim 3, wherein when the concentration of anaerobic digested sludge in the fully mixed reactor is less than a preset concentration, anaerobic digested sludge in the anaerobic ceramic membrane bioreactor is returned to the fully mixed reactor at a second speed, the ratio of the second speed to the first speed being less than or equal to 0.3.
5. The method of pig farm wastewater treatment according to any of claims 2 to 4, wherein the step of determining the success of the start-up of the fully mixed reactor comprises:
Preparing four experimental wastewater with TCOD concentration of 500 mg/L, 1000 mg/L, 2500 mg/L and 5000 mg/L respectively by using actual pig farm wastewater;
Based on TCOD concentration values, sequentially introducing four kinds of experimental wastewater into the fully mixed reactor according to the sequence of small first and large second for biological treatment, wherein the premise of increasing the TCOD concentration of the experimental wastewater next time is that the COD removal rate corresponding to the current experimental wastewater reaches more than 85 percent;
And when the COD removal rate corresponding to the experimental wastewater with the TCOD concentration of 5000 mg/L is stabilized to be more than 85%, the complete mixing type reactor is started successfully.
6. The method for pig farm wastewater treatment according to any of claims 2 to 4, wherein the step of determining the success of the start-up of the inner and outer zone reactors comprises:
Four simulated wastewater with mass concentrations of 200 mg/L, 400 mg/L, 800 mg/L and 1600 mg/L of ammonium bicarbonate are prepared;
Based on the ammonium bicarbonate mass concentration value, four kinds of simulated wastewater are sequentially introduced into the internal and external zone reactors according to the sequence of small first and large second for biological treatment, and the premise of increasing the mass concentration of the simulated wastewater next time is that the total nitrogen removal rate corresponding to the current simulated wastewater reaches more than 80%;
and when the total nitrogen removal rate corresponding to the simulated wastewater with the mass concentration of the ammonium bicarbonate of 1600 mg/L is stabilized to be more than 80%, the internal and external zone reactors are successfully started.
7. The method for treating pig farm wastewater according to claim 1, wherein the dissolved oxygen concentration in the aerobic zone is controlled to be 0.3-1.0 mg/L.
8. The method for pig farm wastewater treatment according to claim 1, wherein the anaerobic ceramic membrane bioreactor comprises a reactor shell, a liquid inlet arranged at the lower end of the reactor shell, a liquid outlet arranged at the upper end of the reactor shell, a sludge inlet and a sludge outlet arranged at the lower end of the reactor shell, a ceramic flat membrane contained in the reactor shell, and an aeration assembly, wherein the sludge inlet is communicated with the sludge outlet of the reaction tank, the sludge outlet is communicated with the sludge return opening of the reaction tank, and the aeration assembly is used for enabling the anaerobic ceramic membrane bioreactor to be in an anaerobic state.
9. The method for treating pig farm wastewater according to claim 8, wherein the operation mode of the ceramic flat membrane comprises suction filtration, back flushing and stopping, wherein the ratio of the operation period of the suction filtration to the operation period of the back flushing to the operation period of the stopping is 4:1:4.
10. The method according to any one of claims 1, 7 to 9, wherein the three-phase separation assembly is located above the stirring paddle of the stirrer, the three-phase separation assembly comprises an inner cylinder arranged at intervals with the reaction tank, a connecting plate with two ends respectively connected with the inner cylinder and the reaction tank, and a guide cylinder located in the inner cylinder and connected with the connecting plate, the inner cylinder and the guide cylinder are hollow structures, a stirring shaft of the stirrer penetrates through the guide cylinder and extends into the reaction tank, the water outlet is lower than the top end of the inner cylinder, the guide cylinder comprises a first part with an upper end extending out of the inner cylinder, a second part extending from the lower end of the first part gradually towards a central axis direction far away from the first part, the second part is connected with the connecting plate, and a plurality of through holes are formed in the connecting plate.
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