CN115159776A - Printing and dyeing wastewater treatment process - Google Patents

Printing and dyeing wastewater treatment process Download PDF

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Publication number
CN115159776A
CN115159776A CN202210783379.2A CN202210783379A CN115159776A CN 115159776 A CN115159776 A CN 115159776A CN 202210783379 A CN202210783379 A CN 202210783379A CN 115159776 A CN115159776 A CN 115159776A
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reaction system
wastewater treatment
printing
treatment process
removal rate
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岳秀
赵振宇
肖吉
陈晓霖
吴宏莹
徐紫楠
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Guangdong Industry Technical College
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Guangdong Industry Technical College
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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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • 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
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Activated Sludge Processes (AREA)

Abstract

The invention provides a printing and dyeing wastewater treatment process. The wastewater treatment process provided by the invention selects a hydrogen peroxide + biochemical treatment process, improves the formula of active substances for starting a biological reaction system, adds glucose, soluble starch, monopotassium phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate and ferric sulfate as the active substances, and can promote the absorption of microorganisms in seed mud on the nutrient components under the synergistic effect of magnesium ions, manganese ions and iron ions, reduce the activation time of the microorganisms, improve the starting and operating efficiency of the biological reaction system, reduce the time cost and reduce the addition amount of hydrogen peroxide. Wherein, the starting time of the biological reaction system can be reduced to below 10h and 8h, the running time before wastewater treatment can be reduced to below 10h and 8h, and a good wastewater treatment effect can be achieved in a shorter time.

Description

Printing and dyeing wastewater treatment process
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a printing and dyeing wastewater treatment process.
Background
The printing and dyeing wastewater is wastewater discharged from printing and dyeing factories which mainly process cotton, hemp, chemical fibers and blended products thereof. Has the characteristics of large water discharge, large chromaticity, high content and variety of organic pollutants, large alkalinity, large water quality change and the like, and belongs to one of industrial wastewater difficult to treat.
PVA, i.e. polyvinyl alcohol, is the main raw material for sizing fabrics, except that most of PVA will be recovered and reused in the production process, and a small amount of PVA will be discharged into a wastewater pipeline to enter a sewage treatment section for treatment. PVA has the characteristics of large COD value, poor biodegradability, large viscosity, easy generation of bubbles and the like, which can increase the treatment difficulty of raw water of printing and dyeing wastewater.
At present, the PVA-containing printing and dyeing wastewater treatment process in China mainly adopts pretreatment (chemical coagulation), hydrolytic acidification, aerobe, advanced treatment (chemical coagulation/strong oxidizer/sand filtration and the like). The PVA-containing printing and dyeing wastewater raw water has complex water quality components and high toxicity, and cannot be directly utilized by microorganisms (can not be directly treated by a biochemical method), so that the raw water must be subjected to coagulation pretreatment to remove part of pollutants in the PVA-containing printing and dyeing wastewater, reduce the toxicity of the wastewater (to meet the microbial tolerance requirement of a subsequent aerobic biochemical section), optimize and adjust the pH value of the water quality, then enter the biochemical section for effective treatment, and then pass through an advanced treatment link, so that the treated water quality reaches the standard and is discharged. The chemical coagulation pretreatment needs to add a large amount of coagulation chemical agents, so that the problems of prolonged overall process flow, large chemical agent amount, high cost and large chemical sludge yield are caused, and the problems of limited treatment capacity of subsequent biochemical sections (hydrolysis acidification and aerobic biochemical sections), increase of toxic gas products in a hydrolysis acidification tank, floating of a large amount of dead mud in the aerobic tank and the like are caused due to the fact that the salt content in water is increased and the pH value is obviously changed due to the addition of the agents to the water; and the chemical coagulation pretreatment only transfers PVA from the wastewater into the chemical sludge without being effectively degraded, and the generated chemical sludge becomes a new secondary pollutant, thereby increasing the difficulty and pressure of subsequent sludge treatment.
Therefore, the existing wastewater treatment process needs to be improved, for example, in chinese patent CN106542637A, a proper amount of hydrogen peroxide is introduced into an acidification system of the wastewater treatment process, so that a chemical coagulation pretreatment process of wastewater can be omitted, and the pressure of subsequent sludge treatment is reduced. However, before wastewater treatment, inoculation of seed sludge in a biochemical treatment part and activation starting of activity of microorganisms in the seed sludge are required, and the conventional microorganism activation technology has limited activation capability for microorganism activity and consumes long time, which is not beneficial to efficient treatment of wastewater, so that a printing and dyeing wastewater treatment process with high speed and good wastewater treatment effect needs to be provided.
Disclosure of Invention
Based on the above, the invention aims to overcome the defect of long time consumption of the existing wastewater treatment process, and the treatment effect still needs to be improved, and provides the printing and dyeing wastewater treatment process with high speed and good wastewater treatment effect.
In order to achieve the purpose, the invention adopts the following technical scheme:
a printing and dyeing wastewater treatment process comprises the following steps:
s1, inoculating seed mud and hanging a film:
respectively adding the seed sludge sample into a hydrolytic acidification reaction system and an aerobic biological reaction system for inoculation, and completing biofilm formation after aeration;
s2, starting a biological reaction system:
injecting water containing an active substance a into the hydrolysis acidification reaction system after film formation, and then flowing into the aerobic biological reaction system after film formation; wherein the active substance a comprises glucose, soluble starch, monopotassium phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate and ferric sulfate;
s3, operating a biological reaction system:
injecting water containing an active substance b into the started hydrolytic acidification reaction system, and then flowing into the started aerobic biological reaction system; wherein the active substance b comprises glucose, soluble starch, monopotassium phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate, ferric sulfate, PVA and dye reactive black;
s4, wastewater treatment:
and S3, after the operation is successful, the printing and dyeing wastewater passes through a hydrolysis acidification reaction system and an aerobic biological reaction system in sequence, and hydrogen peroxide is added at a water inlet of the hydrolysis acidification reaction system.
The invention can obviously improve the starting efficiency and shorten the starting and running time by improving the formula of the active substance for starting the biological reaction system: in the active substances, glucose, soluble starch, potassium dihydrogen phosphate and ammonium carbonate are used as nutrient components of microorganisms in the seed sludge, and a large number of experimental researches show that if three sulfates, namely magnesium sulfate, manganese sulfate and ferric sulfate, are added, on one hand, sulfur in the added sulfate can be absorbed by the microorganisms as nutrient components, and on the other hand, the synergistic effect among magnesium ions, manganese ions and iron ions can promote the absorption of the microorganisms in the seed sludge to the nutrient components, so that the activation time of the microorganisms is shortened, the starting and operating efficiency of a biological reaction system is improved, and the time cost is reduced.
The seed sludge is selected from secondary sedimentation tank activated sludge (pH is 6.6-7.2) of urban domestic sewage plants, the concentration of the seed sludge is concentrated to 8500-10100 mg/L, then aeration is carried out for 3 days, and finally water is added to dilute the seed sludge until the concentration of the seed sludge is 14500-16800 mg/L, so that a seed sludge sample is obtained.
Preferably, in the biological reaction system, a combined filler is further added, and the function of the combined filler is to enable the seed mud sample to be uniformly attached to the surface of the combined filler. The combined filler is characterized in that a plastic wafer is pressed and buckled into a double-ring plastic ring, fiber bundles are wound on the surface of the double-ring plastic ring, and snowflake-shaped plastic branches are filled in the hollow interior of the double-ring plastic ring. The snowflake-shaped plastic branches filled inside are not only beneficial to film formation, but also can effectively cut bubbles in water flow, improve the transfer rate and the utilization rate of oxygen, fully exchange on the seed sludge biomembrane, and further improve the efficient treatment of pollutants in water.
The conventional seed sludge inoculation process can be used in the invention, and the seed sludge sample is added in a ratio of 1.
After inoculation of the seed sludge, different biological reaction systems can complete biofilm formation only after aeration in different gas environments, and residual seed sludge samples without biofilm formation are discharged from the bottom of a container of the biological reaction system after successful biofilm formation. The seed sludge is washed by water and is not easy to fall off, namely the film formation is successful, and the seed sludge sample which is not subjected to film formation is washed by water after the film formation is successful.
The aeration process in the hydrolysis acidification reaction system in the step S1 comprises the following steps: introducing nitrogen into a hydrolytic acidification reaction system (anaerobic reaction system and H reaction system), wherein the pressure of the nitrogen is 0.2-0.22 MPa, gradually attaching the seed sludge sample in the reaction system to the surface of the combined filler, aerating until the sludge is changed from light yellow brown to black brown (about 48-72H), stopping introducing the nitrogen, standing for 4-6H, and discharging the seed sludge sample without film hanging from a sludge discharge port at the bottom of a container of the reaction system.
The aeration process in the aerobic biological reaction system in the step S1 comprises the following steps: introducing air into an aerobic biological reaction system (O reaction system), wherein the air pressure is 0.023-0.025 MPa, the seed sludge samples in the reaction system are gradually attached to the surface of the combined filler, the seed sludge samples keep light yellow and are kept unchanged, after 48-72 hours of aeration, stopping introducing the air, standing for 4-6 hours, and then discharging the seed sludge samples without film formation from a sludge discharge port at the bottom of a container of the reaction system.
Preferably, the addition amount of the active substance a in the step s2 is as follows: 0.15-0.40 g/L of glucose, 0.10-0.14 g/L of soluble starch, 0.01-0.02 g/L of monopotassium phosphate, 0.01-0.02 g/L of magnesium sulfate, 0.003-0.01 g/L of ammonium carbonate, 0.01-0.02 g/L of manganese sulfate and 0.01-0.02 g/L of ferric sulfate, the proportion of the components is favorable for successfully starting a biological reaction system (comprising a hydrolytic acidification reaction system and an aerobic biological reaction system), the starting time can be reduced to below 10h and can be reduced to 8h, and the wastewater treatment cost is greatly reduced.
When the biological reaction system is started, the conditions of the reaction system are controlled as follows: 1) The content of dissolved oxygen in a hydrolysis acidification reaction system is 0mg/L, the pH is 6.0-6.5, and the water temperature is 30-32 ℃; 2) The content of dissolved oxygen in the aerobic biological reaction system is 4.0-5.9 mg/L, the pH is 6.0-7.2, and the water temperature is 30-32 ℃.
Wherein, the conditions for successfully starting the biological reaction system are as follows: the removal rate of Chemical Oxygen Demand (COD) in a hydrolysis acidification reaction system reaches 40 percent, and ammonia Nitrogen (NH) 4 + -N) removal rate of 57.1%; the removal rate of Chemical Oxygen Demand (COD) in an aerobic biological reaction system reaches 73.5 percent, and ammonia Nitrogen (NH) 4 + The removal rate of-N) reaches 100 percent.
Preferably, the addition amount of the active substance b in the step s3 is as follows: 0.40-0.60 g/L glucose, 0.30-0.40 g/L soluble starch, 0.01-0.02 g/L potassium dihydrogen phosphate, 0.01-0.02 g/L magnesium sulfate, 0.003-0.01 g/L ammonium carbonate, 0.01-0.02 g/L manganese sulfate, 0.01-0.02 g/L ferric sulfate, 0.18-0.30 g/L PVA and 0.1-0.4 g/L dye active black. The component proportion is beneficial to a biological reaction system (comprising a hydrolytic acidification reaction system and an aerobic biological reaction system) to reach a stable running state in a shorter time, the running time for reaching stability can be reduced to below 10h and can be as low as 8h, and the wastewater treatment cost is greatly reduced.
When the biological reaction system is operated, the conditions of the reaction system are controlled as follows: 1) The content of dissolved oxygen in a hydrolysis acidification reaction system is 0mg/L, the pH is 5.3-7.0, and the water temperature is 30-32 ℃; 2) The content of dissolved oxygen in the aerobic biological reaction system is 4.0-5.9 mg/L, the pH is 6.0-7.2, and the water temperature is 30-32 ℃.
Wherein, the condition that the biological reaction system runs stably is as follows: the removal rate of Chemical Oxygen Demand (COD) in the hydrolysis acidification reaction system is 21.1-46.0%, the removal rate of ammonia nitrogen is 0-67.2%, the removal rate of PVA is 0-29.4%, and the removal rate of chroma is 52.9-78.1%; the removal rate of Chemical Oxygen Demand (COD) in the aerobic biological reaction system is 35.2-91.5%, the removal rate of ammonia nitrogen is 27.7-100%, the removal rate of PVA is 24.0-90.8%, and the removal rate of chroma is 45.8-86.1%.
After the biological reaction system operates stably, printing and dyeing wastewater treatment can be carried out, and specifically, the printing and dyeing wastewater and a small amount of low-concentration hydrogen peroxide enter from a water inlet of the hydrolysis acidification reaction system and sequentially pass through the hydrolysis acidification reaction system and the aerobic biological reaction system. Wherein the adding conditions of the hydrogen peroxide are as follows: adding 50-75 mL of 0.2-0.3 wt% hydrogen peroxide at a rate of 70-120 mL/h.
Although the addition of hydrogen peroxide can improve the treatment effect of PVA in wastewater, the addition of hydrogen peroxide can generate certain toxicity to microorganisms to a greater or lesser extent, so that the number of active microorganisms is reduced.
Preferably, the addition amount of the hydrogen peroxide is 70mL of 0.3wt% hydrogen peroxide, and the addition speed is 100mL/h.
For the wastewater treatment process, it should be noted that the hydrolysis acidification reaction system and the aerobic biological reaction system are respectively located in different reactors, in the wastewater treatment process, wastewater is firstly injected into the hydrolysis acidification reactor through a water inlet of the hydrolysis acidification reactor, after the hydrolysis acidification reactor is filled, the effluent of the hydrolysis acidification reactor can automatically flow to the water inlet of the aerobic biological reactor and flow into the aerobic biological reactor under the hydrodynamic action due to the communication with the aerobic biological reactor. The water inlet speed and the water outlet speed of the hydrolysis acidification reactor are kept consistent, so that the retention time of flowing wastewater in the hydrolysis acidification reactor can be kept consistent.
Compared with the prior art, the invention has the beneficial effects that:
according to the invention, the formula of the active substance for starting the biological reaction system is improved, glucose, soluble starch, potassium dihydrogen phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate and ferric sulfate are added as the active substance, and under the synergistic effect of magnesium ions, manganese ions and iron ions, the absorption of microorganisms in seed mud to the nutrient components can be promoted, the activation time of the microorganisms is reduced, the starting and operating efficiency of the biological reaction system is improved, and the time cost is reduced; the addition amount of hydrogen peroxide in the wastewater treatment process can be reduced. Wherein, the starting time of the biological reaction system can be reduced to below 10h and 8h, the running time before wastewater treatment can be reduced to below 10h and 8h, good wastewater treatment effect can be achieved in a shorter time, and the time cost of wastewater treatment is greatly reduced.
Detailed Description
The present invention will be further described with reference to specific examples for better illustrating the objects, technical solutions and advantages of the present invention, but the examples are not intended to limit the present invention in any way. Reagents, methods and apparatus used in the present invention are conventional in the art unless otherwise indicated. Unless otherwise indicated, reagents and materials used in the present invention are commercially available.
Example 1
The embodiment provides a printing and dyeing wastewater treatment process, which comprises the following steps:
s1, inoculating seed mud and hanging a film:
s11, taking activated sludge (pH is 6.9) in a secondary sedimentation tank of a municipal domestic sewage plant as seed sludge, concentrating the seed sludge to 9500mg/L by gravity, aerating in air for 3 days, and finally adding water to dilute the seed sludge until the concentration of the seed sludge is 15000mg/L to obtain a seed sludge sample;
s12, respectively filling the obtained seed mud sample in a hydrolysis acidification (anaerobic biological) reactor (H reactor) and an aerobic biological reactor (O reactor) for inoculation, wherein the reactors are filled with combined fillers, the combined fillers are in a structure that a plastic wafer is pressed and buckled into a double-ring plastic ring, fiber bundles are wound on the surface of the double-ring plastic ring, snowflake-shaped plastic branches are filled in the hollow interior of the double-ring plastic ring, and the effective volume of the reactors is 3.2L;
s13, introducing nitrogen into the H reactor inoculated with the seed sludge sample, wherein the pressure of the nitrogen is 0.20MPa, gradually attaching the sludge in the reactor to the surface of the combined filler in the aeration process, after 48 hours of aeration, changing the seed sludge sample attached to the surface of the combined filler from light yellow brown to black brown, stopping introducing the nitrogen, standing for 4 hours, and then washing the residual seed sludge sample without a film by using water flow to discharge the seed sludge sample from a sludge discharge port at the bottom of the reactor;
similarly, air is introduced into the O reactor inoculated with the seed sludge sample, the air pressure of the air is 0.023MPa, the seed sludge sample is attached to the surface of the combined packing in the reactor in the air introduction process, the color is kept to be light yellow brown, the air introduction is stopped after the air introduction is continuously carried out for 48 hours, the standing is carried out for 4 hours, and then the residual seed sludge sample without film hanging is washed by water flow to be discharged from a sludge discharge port at the bottom of the reactor;
s2, starting a biological reaction system:
s21, preparing artificial inflow water a containing an active substance a: the feed water a contains glucose 0.3g/L, soluble starch 0.12g/L, and potassium dihydrogen phosphate (KH) 2 PO 4 ·3H 2 O) 0.01g/L, magnesium sulfate 0.01g/L, ammonium carbonate 0.006g/L, manganese sulfate 0.01g/L, ferric sulfate 0.01g/L, and measuring COD and NH in the feed water a 4 + -concentration of N (mg/mL);
s22, injecting the water inlet a obtained in the step S21 into an H reactor, controlling the content of Dissolved Oxygen (DO) in the H reactor to be 0mg/L, the pH to be 6.0-6.5, the water temperature to be 30-32 ℃, and testing COD (chemical oxygen demand) and NH (NH) in water at a water outlet after the water inlet a stays in the H reactor for 8 hours 4 + Concentration of-N (mg/mL), and removal rate (%) was calculated (compared with the quality of S21. Prepared inlet water a), and COD removal rate up to 40% and NH were calculated 4 + The N removal rate reaches 57.1%, indicating that the H reactor is successfully started;
then the inlet water a flows into an O reactor from an H reactor, the content of Dissolved Oxygen (DO) in the O reactor is controlled to be 4.0-5.9 mg/L, the pH value is 6.0-7.2, the water temperature is 30-32 ℃, after the inlet water a stays in the O reactor for 8 hours, COD and NH in the water are tested at a water outlet 4 + Concentration of N (mg/mL), calculated removal rate (%) (compared with water quality at the water outlet of the H reactor), calculated COD removal rate of 73.5%, NH 4 + The N removal rate reaches 100%, indicating that the O reactor is successfully started;
s3, operating the biological reaction system
S31, preparing artificial inflow water b containing an active substance b: the feed water b contains glucose 0.5g/L, soluble starch 0.35g/L, and potassium dihydrogen phosphate (KH) 2 PO 4 ·3H 2 O) 0.01g/L, magnesium sulfate 0.01g/L, ammonium carbonate 0.006g/L, manganese sulfate 0.01g/L, ferric sulfate 0.01g/L, PVA 0.2g/L, and dye reactive black 0.3g/L, and COD and NH in the influent water b were measured 4 + N, the concentration of PVA (mg/mL) and the absorbance (measured with a spectrophotometer, reflecting the colorimetric values);
s32, injecting the water inlet b obtained in the step S31 into an H reactor, controlling the content of Dissolved Oxygen (DO) in the H reactor to be 0mg/L, the pH value to be 5.3-7.0, the water temperature to be 30-32 ℃, and testing COD (chemical oxygen demand) and NH (NH) in water at a water outlet after the water inlet b stays in the H reactor for 8 hours 4 + Concentration (mg/mL) and absorbance of N and PVA, and removal rate (%) calculated (as compared with the quality of S31. Prepared feed water b), and COD removal rate up to 36.9% and NH calculated 4 + The N removal rate is 38.8 percent, the PVA removal rate is 19.6, and the chroma reduction rate is 70 percent, which indicates that the H reactor runs stably;
then the water b flows into an O reactor from an H reactor, the content of Dissolved Oxygen (DO) in the O reactor is controlled to be 4.0-5.9 mg/L, the pH value is in the range of 6.0-7.2, the water temperature is 30-32 ℃, after the water b stays in the O reactor for 8 hours, COD and NH in the water are tested at a water outlet 4 + Concentration (mg/mL) and absorbance of N and PVA, calculating removal rate (%) (compared with water quality at the water outlet of the H reactor), calculating to obtain COD removal rate of 70.2%, and NH 4 + The N removal rate is 91.6, the PVA removal rate is 63.3%, and the chroma reduction rate is 70.3%, which indicates that the operation of the O reactor is stable;
s4, wastewater treatment:
s3, after the operation is successful, adding 70mL of 0.3wt% hydrogen peroxide at the water inlet of the H reactor at the speed of 100mL/H, simultaneously injecting the printing and dyeing wastewater into the H reactor at the speed of 400mL/H through the water inlet of the H reactor, then flowing through the O reactor, finally testing COD and NH in the treated wastewater after flowing out of the water outlet of the O reactor 4 + The concentrations (mg/mL) and the absorbances of N and PVA were calculated as the removal (%) in comparison with the water quality at the water inlet of the H reactor, and the test results are detailed in Table 1.
Example 2
The embodiment provides a printing and dyeing wastewater treatment process, which is different from the process of embodiment 1 in that:
1) Step S2. In the following steps: activity in influent aThe formula of the substance a comprises glucose 0.15g/L, soluble starch 0.1g/L, and potassium dihydrogen phosphate (KH) 2 PO 4 ·3H 2 O) 0.02g/L, magnesium sulfate 0.02g/L, ammonium carbonate 0.003g/L, manganese sulfate 0.02g/L, ferric sulfate 0.02g/L; s22, allowing the medium inlet water a to stay in the H reactor and the O reactor for 10 hours;
2) Step S3. In the following steps: the formulation of active substance b in the inlet water b is 0.6g/L glucose, 0.3g/L soluble starch, and potassium dihydrogen phosphate (KH) 2 PO 4 ·3H 2 O) 0.02g/L, magnesium sulfate 0.02g/L, ammonium carbonate 0.003g/L, manganese sulfate 0.02g/L, ferric sulfate 0.02g/L, PVA 0.3g/L, and dye reactive black 0.1g/L; s32, allowing the medium inlet water b to stay in the H reactor and the O reactor for 10 hours;
and S4, the effect of the removal rate of each index in the wastewater is detailed in Table 1.
Example 3
The embodiment provides a printing and dyeing wastewater treatment process, which is different from the process of embodiment 1 in that:
1) Step S2. In the following steps: the formula of active substance a in the inlet water a is 0.4g/L of glucose, 0.14g/L of soluble starch and potassium dihydrogen phosphate (KH) 2 PO 4 ·3H 2 O) 0.01g/L, magnesium sulfate 0.01g/L, ammonium carbonate 0.01g/L, manganese sulfate 0.01g/L, ferric sulfate 0.01g/L; s22, allowing the medium inlet water a to stay in the H reactor and the O reactor for 10 hours;
2) Step S3, the following steps: the formulation of active substance b in the inlet water b is 0.4g/L glucose, 0.4g/L soluble starch, and potassium dihydrogen phosphate (KH) 2 PO 4 ·3H 2 O) 0.01g/L, magnesium sulfate 0.01g/L, ammonium carbonate 0.01g/L, manganese sulfate 0.01g/L, ferric sulfate 0.01g/L, PVA 0.18g/L, and dye reactive black 0.4g/L; s32, allowing the medium inlet water b to stay in the H reactor and the O reactor for 10 hours;
and S4, the effect of the removal rate of each index in the wastewater is detailed in Table 1.
Example 4
The embodiment provides a printing and dyeing wastewater treatment process, which is different from the process of embodiment 1 in that: and S4, adding 50mL of 0.2wt% hydrogen peroxide at the speed of 70 mL/h.
Example 5
The embodiment provides a printing and dyeing wastewater treatment process, which is different from the process of embodiment 1 in that: and S4, adding 75mL of hydrogen peroxide with the concentration of 0.3wt% into the hydrogen peroxide at the speed of 120mL/h.
Comparative example 1
The comparative example provides a printing and dyeing wastewater treatment process, which is different from the process of example 1 in that:
magnesium sulfate, manganese sulfate and ferric sulfate are not added in the formulas of the active substance a and the active substance b, and the retention time of the inlet water a and the inlet water b in the H reactor and the O reactor is as long as 12 hours;
and S4, the effect of the removal rate of each index in the wastewater is detailed in Table 1.
Comparative example 2
The comparative example provides a printing and dyeing wastewater treatment process, which is different from the process of example 1 in that:
magnesium sulfate is not added in the formula of the active substance a and the active substance b, and the retention time of the water inlet a and the water inlet b in the H reactor and the O reactor is 10 hours;
and S4, the effect of removing rate of each index in the wastewater is shown in Table 1.
Comparative example 3
The comparative example provides a printing and dyeing wastewater treatment process, which is different from the process of example 1 in that:
manganese sulfate is not added in the formulas of the active substance a and the active substance b, and the retention time of the inlet water a and the inlet water b in the H reactor and the O reactor is 10 hours;
and S4, the effect of removing rate of each index in the wastewater is shown in Table 1.
Comparative example 4
The comparative example provides a printing and dyeing wastewater treatment process, which is different from the process of example 1 in that:
ferric sulfate is not added in the formulas of the active substance a and the active substance b, and the retention time of the inlet water a and the inlet water b in the H reactor and the O reactor is 10H;
and S4, the effect of the removal rate of each index in the wastewater is detailed in Table 1.
TABLE 1 effects of wastewater treatment of examples and comparative examples
Figure BDA0003730703930000091
From the above results, it can be seen that:
glucose, soluble starch, monopotassium phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate and ferric sulfate are used as active substances for starting a biochemical reaction system, the starting and running time of the biochemical reaction system can be remarkably reduced to be below 10 hours and as low as 8 hours, and the removal effect of all substances in the wastewater is remarkable under the condition that a small amount of hydrogen peroxide is added.
In the comparative example 1, three sulfates of magnesium sulfate, manganese sulfate and ferric sulfate are not added, the starting and running time of a biological reaction system is obviously greater than that of each embodiment of the invention, and the wastewater treatment effect is not obvious; although sulfate is added into the active substances of comparative examples 2 to 4, one of the sulfate and the sulfate is absent, and although the start-up and running time of a biological reaction system can be reduced to a certain extent, the treatment effect of the wastewater is still to be improved under the same wastewater treatment condition, and further, the synergistic effect among three salt solutions of magnesium sulfate, manganese sulfate and ferric sulfate is further shown, and the synergistic effect among the three salt solutions can also obviously improve the wastewater treatment effect.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the protection scope of the present invention, and although the present invention is described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions can be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.

Claims (10)

1. A printing and dyeing wastewater treatment process is characterized by comprising the following steps:
s1, inoculating seed mud and hanging a film:
respectively adding the seed sludge sample into a hydrolytic acidification reaction system and an aerobic biological reaction system for inoculation, and completing biofilm formation after aeration;
s2, starting a biological reaction system:
injecting water containing an active substance a into the hydrolysis acidification reaction system after film formation, and then flowing into the aerobic biological reaction system after film formation; wherein the active substance a comprises glucose, soluble starch, potassium dihydrogen phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate and ferric sulfate;
s3, operating a biological reaction system:
injecting water containing an active substance b into the started hydrolysis acidification reaction system, and then flowing into the started aerobic biological reaction system; wherein the active substance b comprises glucose, soluble starch, monopotassium phosphate, magnesium sulfate, manganese sulfate, ammonium carbonate, ferric sulfate, PVA and dye reactive black;
s4, wastewater treatment:
and S3, after the operation is stable, the printing and dyeing wastewater passes through a hydrolysis acidification reaction system and an aerobic biological reaction system in sequence, and hydrogen peroxide is added at a water inlet of the hydrolysis acidification reaction system.
2. The printing and dyeing wastewater treatment process according to claim 1, wherein in step s2, the addition amount of the active substance a is as follows: 0.15-0.40 g/L glucose, 0.10-0.14 g/L soluble starch, 0.01-0.02 g/L monopotassium phosphate, 0.01-0.02 g/L magnesium sulfate, 0.003-0.01 g/L ammonium carbonate, 0.01-0.02 g/L manganese sulfate and 0.01-0.02 g/L ferric sulfate.
3. The printing and dyeing wastewater treatment process according to claim 1, wherein in step s3, the addition amount of the active substance b is as follows: 0.40-0.60 g/L glucose, 0.30-0.40 g/L soluble starch, 0.01-0.02 g/L monopotassium phosphate, 0.01-0.02 g/L magnesium sulfate, 0.003-0.01 g/L ammonium carbonate, 0.01-0.02 g/L manganese sulfate, 0.01-0.02 g/L ferric sulfate, 0.18-0.30 g/L PVA and 0.1-0.4 g/L dye active black.
4. The printing and dyeing wastewater treatment process according to claim 1, wherein the aeration process in the hydrolysis acidification reaction system in step s1 is: and introducing nitrogen into the hydrolysis acidification reaction system, wherein the pressure of the nitrogen is 0.2-0.22 MPa, and aerating until the sludge is changed from light brown to black brown.
5. The printing and dyeing wastewater treatment process according to claim 1, wherein the aeration process in the aerobic biological reaction system in step s1 is: introducing air into the aerobic biological reaction system, wherein the air pressure is 0.023-0.025 MPa, and the aeration time is 48-72 h.
6. The printing and dyeing wastewater treatment process according to claim 1, wherein in step S2. The content of dissolved oxygen in the hydrolysis acidification reaction system is 0mg/L, the pH is 6.0-6.5, and the water temperature is 30-32 ℃; the content of dissolved oxygen in the aerobic biological reaction system is 4.0-5.9 mg/L, the pH is 6.0-7.2, and the water temperature is 30-32 ℃.
7. The printing and dyeing wastewater treatment process according to claim 1, wherein in step S3. The content of dissolved oxygen in the hydrolysis acidification reaction system is 0mg/L, the pH is 5.3-7.0, and the water temperature is 30-32 ℃; the content of dissolved oxygen in the aerobic biological reaction system is 4.0-5.9 mg/L, the pH is 6.0-7.2, and the water temperature is 30-32 ℃.
8. The printing and dyeing wastewater treatment process according to claim 1, wherein in step S4, the addition conditions of the hydrogen peroxide solution are as follows: adding 50-75 mL of 0.2-0.3 wt% hydrogen peroxide at a rate of 70-120 mL/h.
9. The printing and dyeing wastewater treatment process according to claim 1, wherein the conditions for successful start-up in step s2 are as follows: the removal rate of chemical oxygen demand in the hydrolysis acidification reaction system reaches 40%, and the removal rate of ammonia nitrogen reaches 57.1%; the removal rate of chemical oxygen demand in the aerobic biological reaction system reaches 73.5 percent, and the removal rate of ammonia nitrogen reaches 100 percent.
10. The printing and dyeing wastewater treatment process according to claim 1, wherein the conditions for smooth operation in step s3. Are: the removal rate of chemical oxygen demand in the hydrolysis acidification reaction system is 21.1-46.0%, the removal rate of ammonia nitrogen is 0-67.2%, the removal rate of PVA is 0-29.4%, and the removal rate of chroma is 52.9-78.1%; the removal rate of chemical oxygen demand in the aerobic biological reaction system is 35.2-91.5%, the removal rate of ammonia nitrogen is 27.7-100%, the removal rate of PVA is 24.0-90.8%, and the removal rate of chroma is 45.8-86.1%.
CN202210783379.2A 2022-07-05 2022-07-05 Printing and dyeing wastewater treatment process Pending CN115159776A (en)

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Citations (2)

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Publication number Priority date Publication date Assignee Title
CN106542637A (en) * 2016-10-28 2017-03-29 广州中国科学院沈阳自动化研究所分所 A kind of hydrogen peroxide of the simulation containing PVA dyeing waste waters collaboration biochemical processing method
CN107364955A (en) * 2017-07-31 2017-11-21 山东中车华腾环保科技有限公司 A kind of colonization method for being used to handle the filler of sanitary sewage

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106542637A (en) * 2016-10-28 2017-03-29 广州中国科学院沈阳自动化研究所分所 A kind of hydrogen peroxide of the simulation containing PVA dyeing waste waters collaboration biochemical processing method
CN107364955A (en) * 2017-07-31 2017-11-21 山东中车华腾环保科技有限公司 A kind of colonization method for being used to handle the filler of sanitary sewage

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岳秀等: "双氧水协同生化法强化处理印染废水" *

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