CN209872704U - Device for low-energy-consumption high-efficiency enhanced treatment of printing and dyeing wastewater - Google Patents
Device for low-energy-consumption high-efficiency enhanced treatment of printing and dyeing wastewater Download PDFInfo
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- CN209872704U CN209872704U CN201920625935.7U CN201920625935U CN209872704U CN 209872704 U CN209872704 U CN 209872704U CN 201920625935 U CN201920625935 U CN 201920625935U CN 209872704 U CN209872704 U CN 209872704U
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Abstract
The utility model provides a device for low energy consumption and high efficiency reinforced treatment of printing and dyeing wastewater, which comprises a regulating tank, an acidification tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank and a sedimentation tank which are communicated in sequence, wherein the secondary sedimentation tank is communicated with the anoxic tank through a pipeline; the middle part in the acidification tank is provided with a fixed filler, and the acidification tank is communicated with a biochar dosing tank; the outer wall of the acidification tank is provided with a permanent magnet. The acidification tank is a reinforced anaerobic digestion tank, and the magnetic field intensity of a permanent magnet on the outer wall is 80-120 mT. The bottom of the acidification tank is provided with an uniform water distributor, and the biochar dosing tank is communicated with the uniform water distributor.
Description
Technical Field
The utility model relates to a waste water treatment field, especially a device of printing and dyeing wastewater is reinforceed to low energy consumption high efficiency.
Background
China is a large country in the textile industry, and the textile printing and dyeing industry is a typical industry with high water consumption and high energy consumption. And the urban development and the improvement of the living standard of people promote the increasing discharge of the printing and dyeing wastewater. The printing and dyeing wastewater is a general term of wastewater discharged from each working section in the printing and dyeing process, and chemical agents and dyes used in the wastewater are main pollutants of the printing and dyeing wastewater. The printing and dyeing wastewater contains various refractory organic matters and heavy metals, and has the characteristics of large chromaticity, poor biodegradability, large change of water quality and water quantity and biotoxicity. The traditional single method is used for treatment, and the printing and dyeing wastewater cannot reach the standard and is discharged. When the wastewater which does not reach the standard is directly discharged into rivers and lakes, the toxic and harmful substances in the water body can be accumulated, the ecological balance of the water body is damaged, and the safety problem of drinking water is caused.
The printing and dyeing wastewater contains complex organic matters which are difficult to degrade, macromolecular organic matters are difficult to degrade and utilize by microorganisms, and denitrification can be performed only in a mode of adding a carbon source, so that the wastewater treatment cost is increased. By using a combined process of hydrolytic acidification pretreatment and aerobic treatment, the biodegradability of the printing and dyeing wastewater can be increased through an anaerobic hydrolysis process, and high-concentration macromolecular organic matters are degraded into micromolecular organic matters. Through a subsequent aerobic combined process, micromolecular organic matters generated in the acidification and hydrolysis process are further mineralized as a denitrification carbon source, so that the aim of removing organic matters in the printing and dyeing wastewater is fulfilled. The removal of azo dyes in the printing and dyeing wastewater can be realized by using an adsorbent or a high-grade oxidant. However, desorption of azo dyes is difficult to achieve, and regeneration of the adsorbent requires additional investment, and the regenerated adsorbent has a shortened service life. This makes the use of the adsorbents difficult on a large scale in printing and dyeing wastewater treatment processes. The use of the high-grade oxidizing agent requires strictly controlled reaction conditions, and for printing and dyeing wastewater with large variation in water quality and water quantity, the high-grade oxidizing agent is difficult to apply in the actual printing and dyeing wastewater treatment process. The printing and dyeing wastewater is treated by using an anaerobic-aerobic combined biological method, macromolecular organic matters can be degraded into micromolecular substances by using a strong reducing environment in an anaerobic process, and organic carbon is provided for an aerobic process to carry out denitrification treatment. Compared with other treatment methods, the biological method is easier to operate and maintain, has lower operation cost, and can solve the problems of large energy consumption and high cost of the printing and dyeing wastewater treatment process.
In order to ensure the treatment effect of the printing and dyeing wastewater and save the treatment cost, more ideas are used for treating the wastewater by using an anaerobic-aerobic activated sludge method. For example, a utility model patent with application No. 200810242897.3, published as 2009, 06, 17 discloses a method for efficient biological enhanced treatment of printing and dyeing wastewater. The utility model adopts the activated carbon combined anoxic-aerobic activated sludge method to perform strengthening treatment on the printing and dyeing wastewater with high chroma and complex composition. The process comprises the steps of introducing printing and dyeing wastewater subjected to hydrolytic acidification into an anoxic-aerobic tank, adding methanol into an anoxic zone in two sections to realize efficient denitrification, and adding powdered activated carbon with the concentration of 200mg/L into an aerobic zone to improve the decolorization effect. However, the activated sludge process suffers from a small organic load and generates a large amount of excess sludge, and the addition of methanol and the addition of activated carbon increases the cost input for water treatment, while the thermal regeneration of activated carbon generates a large amount of energy consumption. Chinese patent application No. 201310732911.9, published as 2014, 09/04, discloses a method for advanced treatment of printing and dyeing wastewater, which comprises the following steps: adjusting the pH value of the azo dye wastewater, introducing the wastewater into a reduction tank, and reducing azo bonds by activated aluminum powder; introducing the reduced wastewater supernatant into an oxidation tank, and carrying out oxidation reaction by using a Fenton reagent; introducing the wastewater after the reaction into a neutralization sedimentation tank for solid-liquid separation; the supernatant is introduced into an adsorption tank and decolorized by adopting activated carbon, so that the treatment process is relatively simple, and the removal effect of chromaticity and organic matters can be ensured. The treatment technologies usually improve the decolorization degree of the printing and dyeing wastewater by adding reagents and simplify the treatment process, but have the problems of harsh reaction conditions, complex operation management and high operation cost, and have poor practical engineering applicability.
SUMMERY OF THE UTILITY MODEL
Utility model purpose: the utility model aims to solve the technical problem that to the not enough of prior art, a device of printing and dyeing waste water is reinforceed to low energy consumption high efficiency is provided.
In order to solve the technical problem, the utility model provides a device for low-energy consumption and high-efficiency reinforced treatment of printing and dyeing wastewater, which comprises a regulating tank, an acidification tank, an anoxic tank, an aerobic tank, a secondary sedimentation tank and a sedimentation tank which are sequentially communicated, wherein the secondary sedimentation tank is communicated with the anoxic tank through a pipeline;
the middle part in the acidification tank is provided with a fixed filler, and the acidification tank is communicated with a biochar dosing tank for adding biochar to the acidification tank; the utility model discloses an it has the biological charcoal granule to add in the intensive hydrolytic acidification pond, and the biological charcoal provides the habitat for hydrolytic acidification bacterium, forms the biomembrane, and the partial biological charcoal that dissolves can provide necessary microelement for the microorganism, guarantees the activity of microorganism.
The outer wall of the acidification tank is provided with a permanent magnet. The permanent magnet outside the tank body can effectively improve the activity of microbial hydrolase, enhance the hydrolytic acidification capability of microbes on granular organic matters and simultaneously improve the shock resistance of the reinforced hydrolytic acidification tank; in addition, the biochar has porosity, so that adsorption and removal of chromaticity can be further enhanced.
In the utility model, the acidification tank is a reinforced anaerobic digestion tank, and the magnetic field intensity of the permanent magnet on the outer wall is 80-120 mT.
The utility model discloses in, the bottom is equipped with uniform water distributor in the acidizing pond, and equalizing basin and biological charcoal add the medicinal cupping and communicate uniform water distributor respectively.
In the utility model, the fixed filler is polypropylene, the diameter of the filler ring-shaped support is 80-120mm, the height is 5mm, the fiber bundle filler is fixed on the ring-shaped support, the length of the fiber bundle is 40-80mm, and the bundle interval is 5-8 mm.
In the utility model, the oxygen-deficient tank is filled with polypropylene filler.
In the utility model, a polyethylene hollow cylindrical filler is arranged in the aerobic tank.
The utility model discloses in, the sedimentation tank communicates the coagulant jar.
The utility model also discloses an operation method of the device of high-efficient intensive processing printing and dyeing waste water of low energy consumption, the step is as follows:
step 1: introducing the printing and dyeing wastewater into an adjusting tank, and adjusting the pH of the printing and dyeing wastewater to 6.5-8;
step 2: introducing the product of the regulating tank into an acidification tank, and adding biochar into the acidification tank to ensure that the mass ratio of the biochar to the volatile fatty acid is 0.2-0.26; and (4) detecting the content of the volatile fatty acid by adopting a titration method.
And step 3: introducing the product of the acidification tank into an anoxic tank, and removing pollutants in the wastewater by using a filler; the time is 10-12 hours, and the sludge retention time is 3-4 days.
And 4, step 4: introducing the product of the anoxic tank into an aerobic tank, and removing pollutants in the wastewater by using a filler; the time is 6-8 hours.
And 5: introducing the product of the aerobic tank into a secondary sedimentation tank to complete sludge-water separation; the retention time is 10-14 days.
Step 6: and (4) introducing the product of the secondary sedimentation tank into a sedimentation tank, fully contacting with a coagulant to remove the chroma, and performing coagulating sedimentation to finally obtain water.
In the utility model, in step 6, the coagulant is polymerized ferrous sulfate, the pH value is 8.5-9, the coagulant adding amount is 100-160mg/L, namely, each liter of wastewater is added with 100-160mg of polymerized ferrous sulfate, and the reaction time in the sedimentation tank is 20-30 min.
Has the advantages that: the utility model discloses use oxygen deficiency moving bed biomembrane reaction tank-mud membrane to mix good oxygen pond combined process and carry out the follow-up biochemical treatment of waste water, its structures area is little, and moves the problem that the biomass loss of moving bed biomembrane method effectively solving traditional activated sludge method is high, the excess sludge volume is many, head loss is big, and the biological height in the reactor can effectively improve treatment effeciency, operation stability.
The utility model discloses at first adopt and strengthen the hydrolytic acidification pond to handle printing and dyeing wastewater, the required carbon source of denitrification can be regarded as to the volatile fatty acid of play aquatic, reduces extra carbon source volume, throws in the processing biological treatment unit and adds the filler and assist with magnetic field and strengthen, and the microbial activity is high, and the biomass is big, and the shock load capacity is strong. The device is convenient to operate and manage, simple in structure, low in energy consumption and capable of effectively improving the stability and the treatment efficiency of the printing and dyeing wastewater treatment process and achieving the excellent effects of low energy consumption, high efficiency and stability in the printing and dyeing wastewater treatment process.
The method is characterized in that biochar, an external magnetic field and biological filler are added for interception, so that the activity and biomass of microorganisms with hydrolysis and acidification functions in a hydrolysis and acidification tank are improved, the generation of easily degradable carbon sources of the microorganisms is improved, the biodegradability of subsequent secondary biological treatment of wastewater is improved, the biological filler is also added in a secondary biochemical section, denitrifying and nitrifying microorganisms can be enriched, the effect of removing pollutants can be greatly reduced even without adding a carbon source, namely, the treatment effect of the printing and dyeing wastewater can be enhanced with low energy consumption and high efficiency, and the good treatment effect can be still kept under the real condition of large water quality and water quantity change of industrial wastewater.
Drawings
These and other advantages of the invention will become apparent from the following more detailed description of the invention, when taken in conjunction with the accompanying drawings and detailed description.
Fig. 1 is a schematic view of the device connection.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
Referring to the figure 1, 1-regulating tank, 2-pH dosing tank, 3-charcoal dosing tank, 4-intensified hydrolytic acidification tank, 5-combined filler, 6-permanent magnet, 7-uniform water distributor, 8-anoxic moving bed biomembrane reaction tank, 9-sludge membrane mixed aerobic tank, 10-secondary sedimentation tank, 11-coagulating sedimentation tank and 12-polymerized ferrous sulfate dosing tank.
A device for low-energy-consumption and high-efficiency reinforced treatment of printing and dyeing wastewater comprises an adjusting tank 1, a reinforced hydrolysis acidification tank 4, an anoxic moving bed biomembrane reaction tank 8, a sludge-membrane mixed aerobic tank 9, a secondary sedimentation tank 10 and a coagulating sedimentation tank 11 which are sequentially connected, and is also provided with a pH dosing tank and a biochar dosing tank; the pH dosing tank is connected with the regulating tank, an electromagnetic valve is arranged at the joint, and a first pH meter is arranged inside the regulating tank 1; the top of the intensified hydrolytic acidification tank 4 is provided with a flow guide pipe which is connected with an anoxic moving bed biomembrane reaction tank 8, the upper part of the intensified hydrolytic acidification tank 4 is provided with a fixed filler, the bottom of the intensified hydrolytic acidification tank is provided with a biochar dosing pipe and a uniform water distributor, and the outside of the tank body is provided with a permanent magnet; the biochar dosing tank is connected with the uniform water distributor through a conduit; a suspended moving bed filler is arranged in the anoxic moving bed biomembrane reaction tank 8; moving bed filler is added into the sludge-film mixing aerobic tank; the secondary sedimentation tank 10 is connected with the anoxic tank through a conduit to complete backflow; the coagulating sedimentation tank 11 is connected with the polymeric ferrous sulfate dosing tank and is provided with a second pH meter.
Furthermore, a filler is arranged in the intensified hydrolytic acidification tank 4, a uniform water distributor is arranged at the bottom, a water outlet is arranged at the top, and printing and dyeing wastewater enters the reactor from the bottom and flows out from the top; the filler is corrosion-resistant elastic polypropylene combined filler and is arranged at the middle upper part of the reinforced anaerobic digestion tank, the filling ratio of the filler is 15-25%, the diameter of the filler is 80-120mm, and the density is 1.4-1.6g/cm 3; the particle size of the biochar added in the biochar medicine adding tank is 200-400 mu m, and the biochar is obtained by thermal cracking of fruit trees; the reinforced anaerobic digestion tank is externally wrapped with a permanent magnet, and the magnetic field intensity is 80-120 mT.
Furthermore, a guide plate, a grid plate, a suspended filler and a stirring device are arranged in the anoxic moving bed biomembrane reaction tank 8, wastewater enters the reaction tank from the bottom and is drained to the mud membrane mixed aerobic tank from a water outlet, the suspended filler has the diameter of 25mm, the height of 10mm, the density of 0.95g/cm3, the specific surface area of 460m2/m3 and the filling ratio of 35-45%;
furthermore, a mud-film mixed aerobic tank 9 is provided with a guide plate, a grid plate and moving bed filler, wastewater enters the aerobic tank from the bottom and is guided to a secondary sedimentation tank from a water outlet, the moving bed filler is a polyethylene hollow cylinder with the height of 5-11mm, the wall thickness of 0.2-0.4mm and the outer diameter of 4-6mm, and the filling ratio of the moving bed filler is 30-40%;
further, the coagulant is polymeric ferrous sulfate, the pH value is adjusted to 8.5-9, the adding amount of the coagulant is 100-160mg/L, and the contact time with the wastewater is 20-30 min.
An operation method of a device for low-energy-consumption and high-efficiency reinforced treatment of printing and dyeing wastewater mainly comprises the following steps:
step 1: firstly pumping the printing and dyeing wastewater into an adjusting tank by a pump, measuring the pH of inlet water by a pH meter, then controlling a pH medicine adding tank, and adjusting the pH of the inlet water to 6.5-8;
step 2: pumping the sewage with the adjusted pH value into a hydrolysis acidification tank through a uniform water distributor, adding biochar at the position, wherein the adding amount of the biochar is 0.2-0.26 according to the content of volatile fatty acid in the effluent of the enhanced hydrolysis acidification tank, detecting the content of the volatile fatty acid by adopting a titration method, after adding the biochar, providing a habitat for hydrolysis acidification bacteria, forming a biological membrane on the surface of the biochar, providing necessary trace elements for microorganisms by partially dissolved biochar, ensuring the activity of the microorganisms, effectively improving the activity of microbial hydrolase by using a permanent magnet outside a tank body, enhancing the hydrolysis acidification capability of the microorganisms on granular organic matters, and simultaneously improving the impact resistance of the enhanced hydrolysis acidification tank; in addition, the biochar has porosity, so that the adsorption and removal of chromaticity can be further enhanced; the combined filler at the middle upper part of the tank body can intercept suspended matters in water flow, and the magnetic field outside the tank body can also strengthen the activity of hydrolytic acidification bacteria, so that the efficient and stable hydrolytic acidification function is ensured, and the biodegradability of the subsequent treatment of wastewater is improved;
and step 3: the wastewater treated by the enhanced hydrolysis acidification tank enters an anoxic moving bed biomembrane reaction tank through a guide pipe, the suspended filler in the anoxic moving bed biomembrane reaction tank can quickly enrich denitrifying bacteria, the denitrifying bacteria flow back to nitrate nitrogen at the position from a secondary sedimentation tank, and the enriched denitrifying bacteria are reduced into nitrogen by taking an easily degradable carbon source in the effluent of the enhanced anaerobic digestion tank as a substrate;
and 4, step 4: then the wastewater enters a sludge-film mixed aerobic tank, and microorganisms with a longer epoch period are stored in an environment with active sludge and a biological film coexisting, so that the microbial diversity is improved, the removal rate of COD and ammonia nitrogen can be remarkably improved, and the operation stability is also improved; and the treated mud-water mixture enters a secondary sedimentation tank to complete mud-water separation, enters a coagulating sedimentation tank, is fully contacted with a coagulant to achieve the aim of further removing the chroma, and is subjected to coagulating sedimentation to obtain final effluent.
Example 1:
in this embodiment, a set of lab scale experimental apparatus is adopted, the treated printing and dyeing wastewater originates from a cotton linen printing and dyeing mill, and the effluent quality of the batch of printing and dyeing wastewater is as follows: the pH value is 12-13, the chroma is 900-1500 times, the COD is 1800-2500mg/L, the BOD is 650-820mg/L, the ammonia nitrogen is 59-74mg/L, and the total phosphorus is 6.3-10.5 mg/L. Waste water is first of allThe wastewater enters an adjusting tank, sodium hydroxide alkali liquor is added into the adjusting tank to increase the pH value to 7, then the wastewater is pumped into a reinforced hydrolysis acidification tank through an uniform water distributor, 100mg/L of biochar is added in the first day, biochar particles are added according to the mass of volatile fatty acid in the effluent, the mass ratio of the biochar to the volatile fatty acid is 0.26, the particle size of the added biochar is 400 mu m, the hydraulic retention time of the wastewater in the reinforced hydrolysis acidification tank is 12h, a fixed combined filler is added at the middle upper part of the reinforced hydrolysis acidification tank, the filler filling ratio is 25%, an annular filler support is 80mm in diameter and 5mm in height, a fiber bundle filler is fixed on the annular support, the fiber bundle length is 80mm, the bundle interval is 5mm, and the density is 1.4g/cm3The permanent magnetic field intensity outside the pool body is 80mT, the organic load is gradually improved to the operation stability when the reinforced hydrolysis acidification pool operates, because the biochar can provide a habitat for the growth of microorganisms, a biological film is convenient to form, and the fixed combined filler is arranged on the middle upper part of the pool body, in addition, the activity of the microorganisms can be effectively improved by the permanent magnetic field outside the pool body, the starting time of the reinforced hydrolysis acidification pool is greatly reduced, the water flow retention time is 12 hours, the sludge retention time is 4d, after the pool operates for 12 days, the concentration of volatile fatty acid in the outlet water of the reinforced hydrolysis acidification pool can reach 1310 +/-36 mg COD/L, the content of easily degradable dissolved organic matters in the waste water is greatly increased, and a good foundation is provided for subsequent biochemical treatment. Then the wastewater enters an anoxic moving bed biofilm reactor to be mixed with the sewage flowing back from a secondary sedimentation tank, and moving bed filler with the diameter of 25mm, the height of 10mm and the density of 0.95g/cm is added into the anoxic tank3Specific surface area of 460m2/m3The filling ratio is 45 percent, the retention time of the wastewater is 8 hours, denitrifying bacteria enriched on the filler of the moving bed reduce nitrate nitrogen into nitrogen by taking biodegradable volatile organic acid generated by the reinforced hydrolytic acidification tank as a carbon source, and no additional carbon source is needed in the treatment process. Then the sewage enters a sludge-film mixed aerobic tank to further remove COD (chemical oxygen demand) and ammonia nitrogen, a polyethylene hollow cylinder with the height of 11mm, the wall thickness of 0.4mm and the outer diameter of 6mm is added into the tank, the filling ratio of the filler is 40 percent, the retention time of the wastewater is 14 hours, the ammonia oxidizing bacteria with longer generation period in the tank can be enriched on the filler, and the sludge-film mixed aerobic tank is improvedAnd (3) completing sludge-water separation in a secondary sedimentation tank by virtue of the ammonia nitrogen oxidation capacity of the tank, then entering a coagulating sedimentation tank, adjusting the pH to 8.5, adding 160mg/L of polymeric ferrous sulfate to enable the polymeric ferrous sulfate to be in contact with the wastewater for 20min, and performing solid-liquid separation on the wastewater, wherein the COD (chemical oxygen demand) of the effluent of the process is 85-126mg/L, the TN (total nitrogen) concentration is 17-26mg/L, and the chroma is 9-22.
Example 2:
the difference from example 1 is that the printing and dyeing wastewater used in this example originates from a cotton knitting and dyeing mill in a certain market, and the effluent quality of the printing and dyeing wastewater of this batch is as follows: 1300mg/L of COD 900-. The wastewater firstly enters an adjusting tank, sodium hydroxide alkali liquor is added into the adjusting tank to increase the pH value to 6.5, then the wastewater is pumped into a reinforced hydrolysis acidification tank through an uniform water distributor, 80mg/L of biochar is added in the first day, biochar particles are added according to the mass of volatile fatty acid in the effluent, the mass ratio of the biochar to the volatile fatty acid is 0.2, the particle size of the added biochar is 300 mu m, the hydraulic retention time of the wastewater in the reinforced hydrolysis acidification tank is 11h, a fixed combined filler is added at the middle upper part of the reinforced hydrolysis acidification tank, the filler filling ratio is 20%, the diameter of a filler annular support is 100mm, the height of the filler annular support is 5mm, a fiber bundle filler is fixed on the annular support, the length of the fiber bundle is 60mm, the bundle spacing is 6mm, and the density is 1.5g/cm3The permanent magnetic field intensity outside the pool body is 100mT, the organic load is gradually improved when the reinforced hydrolysis acidification pool runs until the operation is stable, the retention time of the waste water is 11h, the retention time of the sludge is 4d, after the reinforced hydrolysis acidification pool runs for 11 days, the concentration of the volatile fatty acid in the outlet water of the reinforced hydrolysis acidification pool can reach 510 +/-21 mg COD/L, the content of easily degradable soluble organic matters in the waste water is greatly increased, and a good foundation is provided for the subsequent biochemical treatment. Then the wastewater enters an anoxic moving bed biofilm reactor to be mixed with the sewage flowing back from a secondary sedimentation tank, and moving bed filler with the diameter of 25mm, the height of 10mm and the density of 0.95g/cm is added into the anoxic tank3Specific surface area of 460m2/m3The filling ratio is 35 percent, the waste water stays for 7 hours, the denitrifying bacteria enriched on the filling material of the moving bed reduces the nitrate nitrogen into nitrogen by taking the volatile organic acid which is easy to biodegrade and generated in the reinforced hydrolytic acidification tank as a carbon source,no additional carbon source is required in the treatment process. Then the sludge enters a sludge membrane mixing aerobic tank to further remove COD and ammonia nitrogen, a polyethylene hollow cylinder with the height of 9mm, the wall thickness of 0.3mm and the outer diameter of 5mm is added into the tank, the filling ratio of the filler is 30%, the waste water stays for 10 hours, ammonia oxidizing bacteria with a longer generation period in the tank can be enriched on the filler, the ammonia nitrogen oxidizing capability of the sludge membrane mixing aerobic tank is improved, sludge-water separation is completed in a secondary sedimentation tank, then the sludge-water separation enters a coagulating sedimentation tank, the pH is adjusted to 9, 100mg/L of polymeric ferrous sulfate is added to enable the sludge to be in contact with the waste water for 25 minutes, the waste water is subjected to solid-liquid separation, and the COD of the effluent of the process is 76-114mg/L, the TN concentration is 14-22mg/L, the chroma is 8-17, and the SS is 16-28.
Example 3:
the example adopts a pilot test device, the treated printing and dyeing wastewater originates from a printing and dyeing enterprise engaged in garment dyeing, and the total discharge of the wastewater can reach 3000 t.d-1The COD of the wastewater is 1000-1600mg/L, the BOD is 255-365mg/L, the chroma is 500-600 times, the pH is 8-12, and the ammonia nitrogen is 50-70 mg/L. Wastewater firstly enters an adjusting tank, sodium hydroxide alkali liquor is added into the adjusting tank to increase the pH value to 8, then the wastewater is pumped into a reinforced hydrolysis acidification tank through an uniform water distributor, 100mg/L of biochar is added in the first day, biochar particles are added according to the mass of volatile fatty acid in effluent, the mass ratio of the biochar to the volatile fatty acid is 0.23, the particle size of the added biochar is 200 mu m, the hydraulic retention time of the wastewater in the reinforced hydrolysis acidification tank is 12h, the sludge retention time is 3d, a fixed combined filler at the middle upper part of the reinforced hydrolysis acidification tank is 15%, the diameter and the height of a filler ring-shaped support are 120mm and 5mm, a fiber bundle filler is fixed on the ring-shaped support, the length of a fiber bundle is 40mm, the bundle spacing is 8mm, and the density is 1.6g/cm3The permanent magnetic field intensity outside the pool body is 120mT, the organic load is gradually improved to the stable operation when the reinforced hydrolysis acidification pool operates, after 14 days of operation, the concentration of the volatile fatty acid in the effluent of the reinforced hydrolysis acidification pool can reach 476 +/-25 mgCOD/L, the content of the easily degradable soluble organic matters in the wastewater is greatly increased, and a good foundation is provided for the subsequent biochemical treatment. Then the wastewater enters an anoxic moving bed biofilm reactor to be mixed with the sewage which flows back from the secondary sedimentation tank,the moving bed filler added in the anoxic tank has the diameter of 25mm, the height of 10mm and the density of 0.95g/cm3Specific surface area of 460m2/m3The filling ratio is 45 percent, the waste water stays for 6 hours, denitrifying bacteria enriched on the filler of the moving bed reduce nitrate nitrogen into nitrogen by taking easily biodegradable volatile organic acid generated by the reinforced hydrolytic acidification tank as a carbon source, and no additional carbon source is needed in the treatment process. Then the sludge enters a sludge membrane mixing aerobic tank to further remove COD and ammonia nitrogen, a polyethylene hollow cylinder with the height of 7mm, the wall thickness of 0.2mm and the outer diameter of 4mm is added into the tank, the filling ratio of the filler is 40%, the waste water stays for 11 hours, ammonia oxidizing bacteria with a longer generation period in the tank can be enriched on the filler, the ammonia nitrogen oxidizing capability of the sludge membrane mixing aerobic tank is improved, sludge-water separation is completed in a secondary sedimentation tank, then the sludge-water separation enters a coagulating sedimentation tank, the pH is adjusted to 9, 120mg/L of polymeric ferrous sulfate is added to enable the sludge-water separation to be in contact with the waste water for 30 minutes, the waste water is subjected to solid-liquid separation, the COD of the effluent of the process is 82-123mg/L, the TN concentration is 17-26mg/L, and the chroma is.
The utility model provides a device of high-efficient intensive processing printing and dyeing waste water of low energy consumption, the method and the way that specifically realize this technical scheme are many, above only the utility model discloses a preferred embodiment should point out, to the ordinary skilled person in this technical field, is not deviating from the utility model discloses under the prerequisite of principle, can also make a plurality of improvements and moist decorations, these improvements should also regard as with moist decorations the utility model discloses a protection scope. All the components not specified in the present embodiment can be realized by the prior art.
Claims (8)
1. A device for low-energy-consumption and high-efficiency enhanced treatment of printing and dyeing wastewater is characterized by comprising a regulating tank (1), an acidification tank (4), an anoxic tank (8), an aerobic tank (9), a secondary sedimentation tank (10) and a sedimentation tank (11) which are sequentially communicated;
a fixed filler (5) is arranged in the acidification tank (4), and the acidification tank (4) is communicated with the biochar dosing tank (3) and is used for adding biochar into the acidification tank (4);
the outer wall of the acidification tank (4) is provided with a permanent magnet (6).
2. An apparatus for low energy consumption and high efficiency treatment of printing and dyeing wastewater according to claim 1, characterized in that the acidification tank (4) is an enhanced anaerobic digestion tank.
3. A low energy consumption and high efficiency enhanced treatment apparatus for printing and dyeing wastewater according to claim 1, characterized in that the magnetic field strength of the permanent magnet (6) of the outer wall is 80-120 mT.
4. The device for low-energy-consumption and high-efficiency enhanced treatment of the printing and dyeing wastewater according to claim 1, characterized in that an uniform water distributor (7) is arranged at the bottom in the acidification tank (4), and the regulating tank (1) and the biochar dosing tank (3) are respectively communicated with the uniform water distributor (7).
5. The device for low-energy-consumption and high-efficiency reinforced treatment of printing and dyeing wastewater according to claim 1, characterized in that the fixed filler (5) is polypropylene.
6. A low energy consumption and high efficiency enhanced treatment device for printing and dyeing wastewater according to claim 1, characterized in that the anoxic tank (8) is filled with polypropylene filler.
7. The device for low-energy-consumption and high-efficiency enhanced treatment of the printing and dyeing wastewater according to claim 1, characterized in that a polyethylene hollow cylindrical filler is arranged in the aerobic tank (9).
8. The device for low-energy-consumption and high-efficiency enhanced treatment of printing and dyeing wastewater according to claim 1, characterized in that the sedimentation tank (11) is communicated with a coagulant tank (12).
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| CN109987800A (en) * | 2019-04-30 | 2019-07-09 | 江苏环保产业技术研究院股份公司 | A kind of device and its operation method of low energy consumption high-efficiency intensive treatment dyeing waste water |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109987800A (en) * | 2019-04-30 | 2019-07-09 | 江苏环保产业技术研究院股份公司 | A kind of device and its operation method of low energy consumption high-efficiency intensive treatment dyeing waste water |
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