CN109368951B - Blanket printing and dyeing wastewater treatment device and method - Google Patents
Blanket printing and dyeing wastewater treatment device and method Download PDFInfo
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- CN109368951B CN109368951B CN201811605821.2A CN201811605821A CN109368951B CN 109368951 B CN109368951 B CN 109368951B CN 201811605821 A CN201811605821 A CN 201811605821A CN 109368951 B CN109368951 B CN 109368951B
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- 238000000034 method Methods 0.000 title claims abstract description 73
- 238000004043 dyeing Methods 0.000 title claims abstract description 35
- 238000007639 printing Methods 0.000 title claims abstract description 32
- 238000004065 wastewater treatment Methods 0.000 title description 7
- 239000002351 wastewater Substances 0.000 claims abstract description 125
- 239000010802 sludge Substances 0.000 claims abstract description 56
- 238000004062 sedimentation Methods 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 238000009826 distribution Methods 0.000 claims abstract description 11
- 230000008569 process Effects 0.000 claims description 55
- 230000001105 regulatory effect Effects 0.000 claims description 23
- 238000007599 discharging Methods 0.000 claims description 15
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 11
- 238000005086 pumping Methods 0.000 claims description 9
- 230000002159 abnormal effect Effects 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000000701 coagulant Substances 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 4
- 244000144992 flock Species 0.000 claims description 4
- 208000034699 Vitreous floaters Diseases 0.000 claims description 3
- 238000005273 aeration Methods 0.000 claims description 3
- 239000008394 flocculating agent Substances 0.000 claims description 3
- 230000001376 precipitating effect Effects 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 230000001276 controlling effect Effects 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000012545 processing Methods 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims 1
- 238000003672 processing method Methods 0.000 claims 1
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 2
- 241000894006 Bacteria Species 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- 239000010865 sewage Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 239000004753 textile Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000001651 autotrophic effect Effects 0.000 description 2
- 239000012752 auxiliary agent Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000004519 grease Substances 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000003403 water pollutant Substances 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 125000003277 amino group Chemical group 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- -1 fluff Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 210000002268 wool Anatomy 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/30—Nature of the water, waste water, sewage or sludge to be treated from the textile industry
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
Abstract
The invention discloses a device and a method for treating blanket printing and dyeing wastewater, wherein the device comprises an adjusting tank, a reaction tank, a primary sedimentation tank, an anaerobic distribution tank, an anaerobic tower, an A/O reactor, a secondary sedimentation tank and a clean water tank which are sequentially connected through pipelines, the primary sedimentation tank is connected to a sludge concentration tank through a sludge discharge pipeline, the secondary sedimentation tank is respectively connected to the anaerobic tower and the A/O reactor through a sludge return pipeline, and the secondary sedimentation tank is connected to the sludge concentration tank through a sludge discharge pipeline. The device and the method for treating the blanket printing and dyeing wastewater can thoroughly degrade organic pollutants in the blanket printing and dyeing wastewater, completely remove ammonia nitrogen in the wastewater, ensure that the chromaticity of the treated wastewater is lower than 80 times, ensure that suspended matters have low concentration, ensure that effluent is clear, and meet the discharge standard.
Description
Technical field:
the invention relates to the technical field of wastewater treatment, in particular to a device and a method for treating blanket printing and dyeing wastewater.
The background technology is as follows:
the blanket printing and dyeing wastewater is the wastewater generated by dyeing and printing the blanket in the production process of the blanket, and other wastewater generated before and after dyeing and before and after printing. The blanket printing and dyeing wastewater has the characteristics of large wastewater volume, high suspended matter concentration, high chromaticity and the like, and the wastewater contains a large amount of nondegradable dye and various dyeing auxiliary agents, so that the wastewater is difficult to treat. Taking Jiangsu textile mill as an example, the Chemical Oxygen Demand (COD) in the production wastewater is 2000-5000 mg/L (average 3500 mg/L), the pH value is 6.5-7.0, the ammonia nitrogen is 90-110 mg/L (average 100 mg/L), the suspended matters in the wastewater are mostly fluff, fiber impurities and the like, and the chroma is more than 5000 times and the wastewater contains grease.
The standard discharge of the blanket printing and dyeing wastewater is one of the important factors puzzling most enterprises, and whether the wastewater can be stably treated and discharged after reaching the standard becomes a big bottleneck restricting the continuous and vigorous development of the enterprises. The water quality discharged after the treatment of the traditional printing and dyeing wastewater treatment process can not reach the standard stably, and is very easy to have great influence on the environment.
The invention comprises the following steps:
aiming at the defects of the prior art, the invention provides a device and a method for treating blanket printing and dyeing wastewater, which effectively solve the problem that the blanket printing and dyeing wastewater is difficult to treat, can thoroughly degrade organic pollutants in the blanket printing and dyeing wastewater, completely remove ammonia nitrogen in the wastewater, ensure that the chromaticity of the treated wastewater is lower than 80 times, the concentration of suspended matters is low, and the effluent is clear and reaches the emission standard. And the sludge yield of the whole process is small, the investment and the operation cost of sludge treatment of enterprises are effectively reduced, and the system has the advantages of low power consumption, low operation cost, simple operation management, stable operation and the like.
Based on the above problems, one of the technical schemes provided by the invention is as follows:
the utility model provides a woollen blanket printing and dyeing wastewater treatment device, includes equalizing basin, reaction tank, primary sedimentation tank, anaerobism distribution tank, anaerobic tower, A/O reactor, secondary sedimentation tank and clean water basin that the pipeline connects gradually, primary sedimentation tank is connected to the mud concentration tank through the mud exhaust pipeline, secondary sedimentation tank is connected to respectively through mud return line anaerobic tower, A/O reactor, secondary sedimentation tank is connected to through the mud exhaust pipeline the mud concentration tank.
In some embodiments, the system further comprises an accident pool for receiving abnormal wastewater, wherein a fine grid is arranged upstream of the water inlet end of the regulating pool, and the accident pool is connected to the regulating pool through a pipeline.
Based on the above problems, another technical solution provided by the present invention is:
a method for treating printing and dyeing wastewater of a blanket comprises the following steps:
(1) Collecting the blanket waste water, automatically flowing through a fine grid to remove flocks and floaters, judging the blanket waste water, automatically flowing into an adjusting tank if the process waste water is normal waste water, automatically flowing into an accident tank if the process waste water is abnormal waste water, temporarily storing in the accident tank, and then pumping into the adjusting tank;
(2) Pumping the process wastewater treated by the regulating tank into a reaction tank, and adding a flocculating agent and a coagulant;
(3) Discharging the process wastewater treated by the reaction tank into a primary sedimentation tank for mud-water separation, precipitating effluent, and discharging the generated materialized sludge into a sludge concentration tank;
(4) Discharging the process wastewater treated by the primary sedimentation tank into an anaerobic distribution tank, and adding a heat source;
(5) Pumping the process wastewater treated by the anaerobic distribution tank into an anaerobic tower, and opening internal circulation in the anaerobic tower;
(6) Overflowing the process wastewater treated by the anaerobic tower to an A/O reactor, wherein the A/O reactor is filled with alkali, and opening reflux;
(7) Automatically flowing the effluent of the A/O reactor to a secondary sedimentation tank for mud-water separation, wherein one part of sludge in the secondary sedimentation tank flows back to the A/O reactor, the other part flows back to the anaerobic tower, and the residual sludge is discharged into the sludge concentration tank;
(8) And discharging the effluent of the secondary sedimentation tank into a clean water tank, and discharging the effluent through a discharge port of the clean water tank.
In some embodiments, the chemical oxygen demand of the process wastewater before entering the regulating tank in the step (1) is 2000-5000 mg/L, and the ammonia nitrogen concentration is 90-110 mg/L; if the chemical oxygen demand of the process wastewater is not more than 5000mg/L and the ammonia nitrogen concentration is not more than 110mg/L, the process wastewater automatically flows into the regulating tank; if the chemical oxygen demand of the process wastewater is more than 5000mg/L or the ammonia nitrogen concentration is more than 110mg/L, the process wastewater automatically flows into an accident pool.
In some embodiments, aeration and agitation are performed in the conditioning tank in step (2).
In some embodiments, the flocculant in step (3) is PAC and the coagulant is PAM.
In some embodiments, the heat source added in the step (4) is steam, and the temperature of the process wastewater is controlled to be 30-37 ℃.
In some embodiments, the a/O reactor in step (6) is added dropwise with an alkaline solution to control the pH to 7 to 7.5.
In some embodiments, 85% of the mixed liquor at the outlet of the a/O reactor in step (6) is returned to the front water inlet of the a/O reactor.
In some embodiments, 85% of the sludge in the secondary sedimentation tank in the step (7) is returned to the A/O reactor, 13% of the sludge is returned to the anaerobic tower, and 2% of the sludge is discharged into the sludge concentration tank.
Compared with the prior art, the invention has the advantages that:
according to the technical scheme, aiming at the characteristics of high Chemical Oxygen Demand (COD) concentration, high suspended matter (SS) concentration and high chromaticity of the blanket printing and dyeing wastewater, the process wastewater firstly passes through a fine grid to remove flocks and floats, then enters a regulating tank, is treated by a reaction tank-primary sedimentation tank, and is discharged by a clean water tank after being treated step by an anaerobic distribution tank-anaerobic tower-A/O reactor-secondary sedimentation tank, the COD in the blanket printing and dyeing wastewater can be reduced from 2000-5000 mg/L to 160mg/L below, the COD removal rate is above 95%, the ammonia nitrogen in the wastewater is reduced from 90-110 mg/L to 1mg/L below, the ammonia nitrogen removal rate is above 99%, and the chromaticity in the wastewater can be reduced to 80 times without secondary pollution, so that the problem that the blanket printing and dyeing wastewater is difficult to treat is effectively solved; the effluent can reach the intermediate discharge standard (COD is less than or equal to 200mg/L and ammonia nitrogen is less than or equal to 15 mg/L) in the Table 2 in the discharge Standard of Water pollutants for textile dyeing and finishing industry (GB 4287-2012); the whole process has small mud yield, effectively reduces the investment and the operation cost of sludge treatment, and has the advantages of low power consumption, low operation cost, simple operation management, stable operation and the like.
Description of the drawings:
in order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the description of the embodiments will be briefly described below, in which the drawings are only some embodiments of the present invention, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a process flow diagram of the method for treating the printing and dyeing wastewater of the blanket of the invention.
The specific embodiment is as follows:
the above-described aspects are further described below in conjunction with specific embodiments. It should be understood that these examples are illustrative of the present invention and are not intended to limit the scope of the present invention. The implementation conditions used in the examples may be further adjusted according to the conditions of the specific manufacturer, and the implementation conditions not specified are generally those in routine experiments.
Referring to fig. 1, for a schematic structural diagram of an embodiment of the present invention, a blanket printing and dyeing wastewater treatment device is provided, which includes an adjusting tank, a reaction tank, a primary sedimentation tank, an anaerobic distribution tank, an anaerobic tower, an a/O reactor, a secondary sedimentation tank and a hydrophilic tank which are sequentially connected through a pipeline for sludge discharge, wherein the primary sedimentation tank is connected to a sludge concentration tank, the secondary sedimentation tank is respectively connected to the anaerobic tower and the a/O reactor through a pipeline for sludge return, and the secondary sedimentation tank is also connected to the sludge concentration tank through a pipeline for sludge discharge.
In order to receive abnormal waste water, an accident pool is further arranged, a fine grid is arranged at the upstream of the water inlet end of the regulating pool, the accident pool is connected to the regulating pool through a pipeline, the wool and floating matters of the blanket printing and dyeing waste water in the workshop are removed through the fine grid, if the process waste water is normal waste water, the waste water flows automatically to the regulating pool to regulate the water quality, if the process waste water is abnormal waste water, the waste water flows automatically to the accident pool, and the waste water is temporarily stored in the accident pool and then pumped into the regulating pool.
The treatment method of the blanket printing and dyeing wastewater treatment device comprises the following steps:
(1) Collecting the blanket waste water, automatically flowing through a fine grid to remove flocks and floaters, judging the blanket waste water, automatically flowing into a regulating tank if the process waste water is normal waste water (i.e. the chemical oxygen demand of the process waste water is not more than 5000mg/L and the ammonia nitrogen concentration is not more than 110 mg/L), automatically flowing into an accident tank if the process waste water is abnormal waste water (i.e. the chemical oxygen demand of the process waste water is more than 5000mg/L or the ammonia nitrogen concentration is more than 110 mg/L), temporarily storing the process waste water in the accident tank, and then pumping the process waste water into the regulating tank, for example, the chemical oxygen demand of the process waste water is 3500mg/L and the ammonia nitrogen concentration is 100mg/L before the process waste water enters the regulating tank in the embodiment, regulating the water quality and the water quantity of the waste water in the regulating tank are regulated, and the aeration stirring is carried out in the regulating tank, so that the homogenized waste water can be prevented from accumulating and generating a large amount of block-shaped substances due to excessively high oiliness and fine particles such as to be rich in fluff and slurry, so as to reduce the influence on the subsequent steps;
(2) And (3) pumping the process wastewater treated by the regulating tank into a reaction tank, adding a flocculating agent (PAC) and a coagulant (PAM) into the reaction tank to remove fine particles such as fluff, slurry and the like in the wastewater, and reducing the concentration of suspended matters in the wastewater so as to reduce the influence on the subsequent steps.
(3) And (3) automatically flowing the process wastewater treated by the reaction tank into a primary sedimentation tank for mud-water separation, precipitating water, and discharging the generated materialized sludge into a sludge concentration tank. After the process wastewater is treated by a reaction tank and a primary sedimentation tank, organic nitrogen, dye, auxiliary agent, slurry, grease and the like in the wastewater are mainly removed, wherein the COD concentration is reduced from 3500mg/L to 1500mg/L, the removal rate is higher than 57%, the ammonia nitrogen concentration is reduced from 100mg/L to 80mg/L, the removal rate is higher than 20%, and the chromaticity is reduced from about 5000 times to below 100 times; every m 3 The water content of the produced materialized sludge is 70% after the pressure filtration of a plate-and-frame filter press by adding 1.03kg of PAC powder and 0.017kg of PAM powder into a wastewater reaction tank, and the yield of the materialized sludge is 4.4 tons of materialized sludge generated by treating 1000 tons of wastewater; compared with a reaction tank and an air floatation tank, the COD concentration is reduced from 3500mg/L to 2500mg/L, the removal rate is about 30%, the ammonia nitrogen concentration is not removed, the chromaticity is up to more than 5000 times and is reduced to less than 200 times, and the yield of materialized sludge is 6.6 tons of materialized sludge generated by treating 1000 tons of wastewater. The primary sedimentation tank has higher removal rate of COD, ammonia nitrogen and chromaticity than the air floatation tank, lower sludge yield, and the primary sedimentation tank in the process route is easier to reach the standard of COD, ammonia nitrogen and chromaticity than the air floatation tank, and has simpler operation, more stable operation, lower sludge yield and lower operation cost.
(4) Discharging the process wastewater treated by the primary sedimentation tank into an anaerobic distribution tank, adding steam as a heat source for heating, and controlling the temperature of the process wastewater to be 30-37 ℃;
(5) And (3) pumping the process wastewater treated by the anaerobic water distribution tank into an anaerobic tower, opening internal circulation in the anaerobic tower, and performing anaerobic reaction on the process wastewater in the anaerobic tower to change macromolecular pollutants in the wastewater into micromolecular pollutants, change refractory pollutants into easily degradable pollutants, and remove organic matters in the anaerobic hydrolysis tower tank. The COD concentration of the effluent is less than 1000mg/L, and the COD removal rate of the anaerobic tower is more than 33%. The method comprises the steps of carrying out a first treatment on the surface of the
(6) Overflowing the process wastewater treated by the anaerobic tower to an A/O reactor, adjusting the pH value of the wastewater, and adding alkali into the water inlet of the A/O reactor every m 3 Adding 0.34kg of flake NaOH into the wastewater under control, adjusting the pH value of the wastewater to 7.0-7.5 so as to meet the requirement of autotrophic bacteria nitrification under oxygen supply conditions on alkalinity, and simultaneously, refluxing the mixed solution at the outlet of the A/O reactor to the water inlet at the front end so as to meet the requirement of denitrification of the iso-oxygen bacteria on NO under anoxic conditions 3 - Is not limited to the above-mentioned requirements. The A/O reactor carries out aerobic biological treatment on the process wastewater, the A/O reactor operates in an A/O mode, the anoxic section at the front section and the aerobic section at the rear section are connected in series, DO at the A section is not more than 0.2mg/L, and DO at the O section is 2-4 mg/L. Starch, fiber, carbohydrate and other suspended pollutants and soluble organic matters in the sewage are hydrolyzed into organic acid in the anoxic section heterotrophic bacteria, so that macromolecular organic matters are decomposed into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, and when the products after anoxic hydrolysis enter an A/O reactor for aerobic treatment, the biodegradability and oxygen efficiency of the sewage can be improved; in the anoxic zone, heterotrophic bacteria ammoniate pollutants such as proteins, fats and the like (N on an organic chain or amino groups in amino acids) to release ammonia (NH) 4 + ) Under the condition of sufficient oxygen supply, the nitrifying action of autotrophic bacteria can make NH 3 -N(NH 4 + ) Oxidation to NO 3 - Denitrification of the heterotrophic bacteria under anoxic conditions results in NO 3 - Reduction to molecular nitrogen (N) 2 ) The ecological cycle of C, N and O is completed, and the sewage is harmless and treated up to the standard. Thus, the organics are mostly degraded after the a/O reactor treatment. Through the A/O reactorThe COD concentration of the treated wastewater is less than 160mg/L, the removal rate is higher than 84%, the ammonia nitrogen concentration is less than 1mg/L, and the removal rate is higher than 98%; if the amount of the flaky NaOH is not added, the pH value of the wastewater is lower than 7.0, and the concentration of ammonia nitrogen is higher than 20mg/L, so that the ammonia nitrogen exceeds the standard;
(7) The effluent of the A/O reactor automatically flows to a secondary sedimentation tank for mud-water separation, 85% of sludge in the secondary sedimentation tank flows back to the A/O reactor, 13% of sludge flows back to the anaerobic tower, 2% of residual sludge is discharged into a sludge concentration tank, wherein the sludge flowing back to the anaerobic tower can be subjected to anaerobic digestion, the residual sludge is greatly reduced, the water content of the produced residual sludge is 70% after the produced residual sludge is subjected to filter pressing by a plate-and-frame filter press, and the yield of the residual sludge is 0.1 ton of residual sludge produced by processing 1000 tons of wastewater;
(8) And (3) discharging the effluent of the secondary sedimentation tank into a clean water tank after the secondary sedimentation tank is clarified, wherein the chromaticity of the effluent is smaller than 80 times, and then discharging the effluent through a discharge port of the clean water tank.
After the raw water is treated by the reaction tank-primary sedimentation tank, the effect of removing suspended matters in the process wastewater is quite obvious, and the load is lightened for subsequent treatment, so that the anaerobic tower and the A/O reactor have higher treatment efficiency, and the blockage of equipment and pipelines is prevented. After pretreatment in the reaction tank-primary sedimentation tank, COD of the process wastewater can be reduced from 3500mg/L to below 1500mg/L, the removal rate can be more than 57%, ammonia nitrogen can be reduced from 100mg/L to below 80mg/L, the removal rate can be more than 20%, and the chromaticity can be reduced from about 5000 times to below 100 times. After the process wastewater passes through the anaerobic tower, the COD of the process wastewater is reduced from 1500mg/L to 1000mg/L, and the COD removal rate reaches 33%. The COD concentration of the process wastewater treated by the A/O reactor and the secondary sedimentation tank is also greatly reduced, wherein the COD concentration is reduced to below 160mg/L from 1000mg/L, the removal efficiency is above 84%, the ammonia nitrogen concentration is reduced to below 1mg/L from 80mg/L, and the removal efficiency is above 98%. The discharge indexes all reach the intermediate discharge standard of the table 2 in the discharge standard of water pollutants in the textile dyeing and finishing industry (GB 4287-2012).
In this example, the residence time of the regulating tank was 48 hours, the residence time of the accident tank was 24 hours, the reaction time of the reaction tank was 20 to 30 minutes, and the surface load of the primary sedimentation tank was 0.49m 3 /(m 2 H), sinkingThe settling time was 5 hours, the anaerobic column residence time was 48 hours, the A/O reactor residence time was 48 hours, the secondary sedimentation tank surface load was 0.37m 3 /(m 2 H), the sedimentation time is 8 hours, and the concentration time of the sludge concentration tank is 12 hours.
The above examples are provided for illustrating the technical concept and features of the present invention and are intended to enable those skilled in the art to understand the contents of the present invention and to implement the same, and are not intended to limit the scope of the present invention. All equivalent changes or modifications made according to the spirit of the present invention should be included in the scope of the present invention.
Claims (8)
1. A method for treating blanket printing and dyeing wastewater is characterized by comprising the following steps: the treatment device comprises an adjusting tank, a reaction tank, a primary sedimentation tank, an anaerobic distribution tank, an anaerobic tower, an A/O reactor, a secondary sedimentation tank and a clean water tank which are sequentially connected through pipelines, wherein the primary sedimentation tank is connected to a sludge concentration tank through a sludge discharge pipeline, the secondary sedimentation tank is respectively connected to the anaerobic tower and the A/O reactor through a sludge return pipeline, and the secondary sedimentation tank is connected to the sludge concentration tank through a sludge discharge pipeline; the processing method of the processing device comprises the following steps:
(1) Collecting the blanket waste water, automatically flowing through a fine grid to remove flocks and floaters, judging the blanket waste water, automatically flowing into an adjusting tank if the process waste water is normal waste water, automatically flowing into an accident tank if the process waste water is abnormal waste water, temporarily storing the process waste water in the accident tank, pumping the process waste water into the adjusting tank, wherein the chemical oxygen demand of the process waste water before entering the adjusting tank is 2000-5000 mg/L, and the ammonia nitrogen concentration is 90-110 mg/L;
(2) Pumping the process wastewater treated by the regulating tank into a reaction tank, and adding a flocculating agent and a coagulant;
(3) Discharging the process wastewater treated by the reaction tank into a primary sedimentation tank for mud-water separation, precipitating effluent, and discharging the generated materialized sludge into a sludge concentration tank;
(4) Discharging the process wastewater treated by the primary sedimentation tank into an anaerobic distribution tank, and adding a heat source;
(5) Pumping the process wastewater treated by the anaerobic distribution tank into an anaerobic tower, and opening internal circulation in the anaerobic tower;
(6) Overflowing the process wastewater treated by the anaerobic tower to an A/O reactor, adding alkali into an inlet of the A/O reactor, opening reflux, and refluxing 85% of mixed liquid at an outlet of the A/O reactor to a front water inlet of the A/O reactor;
(7) Automatically flowing the effluent of the A/O reactor to a secondary sedimentation tank for mud-water separation, wherein one part of sludge in the secondary sedimentation tank flows back to the A/O reactor, the other part flows back to the anaerobic tower, and the residual sludge is discharged into the sludge concentration tank;
(8) And discharging the effluent of the secondary sedimentation tank into a clean water tank, and discharging the effluent through a discharge port of the clean water tank.
2. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: the device also comprises an accident pool for receiving abnormal wastewater, wherein a fine grid is arranged at the upstream of the water inlet end of the regulating pool, and the accident pool is connected to the regulating pool through a pipeline.
3. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: and (3) in the step (1), if the chemical oxygen demand of the process wastewater is more than 5000mg/L or the ammonia nitrogen concentration is more than 110mg/L, automatically flowing into an accident pool.
4. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: and (3) performing aeration stirring in the regulating tank in the step (2).
5. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: and (3) the flocculant in the step (3) is PAC, and the coagulant is PAM.
6. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: and (3) heating the wastewater in the step (4) to steam, and controlling the temperature of the process wastewater to be 30-37 ℃.
7. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: and (3) dropwise adding alkali solution into the A/O reactor in the step (6) to control the pH to be 7-7.5.
8. The method for treating waste water from printing and dyeing of carpets according to claim 1, wherein: and (3) refluxing 85% of sludge in the secondary sedimentation tank in the step (7) to the A/O reactor, refluxing 13% of sludge to the anaerobic tower, and discharging 2% of sludge to the sludge concentration tank.
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| CN106007239A (en) * | 2016-07-22 | 2016-10-12 | 苏州苏沃特环境科技有限公司 | Standard meeting treatment system for tannery wastewater |
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