CN114162968A - Micro-aerobic fluidized bed biofilm device and method for hydrolytic acidification of printing and dyeing wastewater - Google Patents
Micro-aerobic fluidized bed biofilm device and method for hydrolytic acidification of printing and dyeing wastewater Download PDFInfo
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- CN114162968A CN114162968A CN202111375048.7A CN202111375048A CN114162968A CN 114162968 A CN114162968 A CN 114162968A CN 202111375048 A CN202111375048 A CN 202111375048A CN 114162968 A CN114162968 A CN 114162968A
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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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
- 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
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/308—Dyes; Colorants; Fluorescent agents
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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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
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- 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
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- 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
Abstract
The invention discloses a micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater, which comprises a reactor shell, wherein a stirrer is arranged at the top wall of the reactor shell, a gas disperser and a gas chamber are arranged on a bottom plate of the reactor shell, and the gas disperser is arranged in the gas chamber; the top wall of the air chamber is provided with an aeration disc, the top wall of the air chamber is provided with a plurality of through holes, and the through holes are communicated with the through holes on the aeration disc; the edge of the top wall of the air chamber is connected with the inner wall of the reactor shell through an interception plate with a through hole, and a space between the interception plate and the top wall of the reactor shell is filled with printing and dyeing wastewater and a plurality of modified polyurethane sponge suspension carriers attached with growing biological membranes; a water inlet pipe and a water outlet pipe are arranged on the side wall of the reactor shell; the bottom plate of the reactor shell is also connected with an air inlet system. The device solves the problems of low hydrolytic acidification efficiency and incomplete degradation of organic dye. Also discloses an operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater.
Description
Technical Field
The invention belongs to the technical field of industrial wastewater treatment, and particularly relates to a micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater and an operation method of the device.
Background
The printing and dyeing wastewater as an important component of industrial wastewater has the characteristics of large water quantity, high organic concentration, complex components, high chromaticity, three-induced toxicity and the like, and has important value for protecting the environmental pollution and safety of surface water by effective treatment. The existing treatment technology of the printing and dyeing wastewater is mainly based on a chemical method, and degradation of organic dye difficult to degrade is realized mainly by virtue of chemical agents or other oxidation groups generated by external induction, so that the aim of organic matter treatment is fulfilled. With the continuous improvement of environmental protection policies, higher requirements are put forward on the treatment of printing and dyeing wastewater, such as the discharge standard of pollutants for textile dyeing and finishing industry water GB4287-2012, the guidance on promoting the resource utilization of sewage, and the like. However, the chemical method has incomplete degradation of organic matters, often has some degradation byproducts, generates secondary pollution (toxicity), and has obviously higher wastewater treatment cost. Therefore, an economic, environment-friendly and efficient printing and dyeing wastewater treatment technology is urgently needed, so that the printing and dyeing wastewater can be efficiently treated and recycled.
The fluidized bed biofilm reactor is a novel biofilm process, has good application prospect in the aspect of printing and dyeing wastewater treatment due to the characteristics of high biomass, simple structure, strong impact load resistance, high organic matter degradation rate, economy, environmental protection and the like, and still has some problems: 1. the reactor design is simple. The existing hydrolysis acidification reactor only adopts mechanical stirring to realize the flow of the biological membrane carrier, and does not optimize the contact condition of the wastewater and the biological membrane carrier from the multi-phase flow angle, so that the mass transfer efficiency of the system is lower. 2. The hydrolytic acidification efficiency is low. The existing hydrolysis acidification process realizes the decolorization of organic dyes through a microbial anaerobic process and limits the decolorization and hydrolysis of organic dyes difficult to degrade. 3. The abundance of decolorizing functional microorganisms is low. The existing biological membrane or activated sludge culture uses a method for reference in the sewage treatment process, so that the decolorized microorganisms are not enriched and strengthened.
Disclosure of Invention
The invention aims to provide a micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater, which solves the problems of low hydrolytic acidification efficiency and incomplete degradation of organic dye.
The invention also aims to provide an operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater, which solves the problems of low abundance of specific functional microorganisms and poor decoloration effect in the prior art.
The invention adopts a first technical scheme that the micro-aerobic fluidized bed biofilm device for printing and dyeing wastewater hydrolytic acidification comprises a reactor shell, wherein a stirrer is arranged on the top wall of the reactor shell, and a gas disperser and a gas chamber are arranged on the bottom plate of the reactor shell; the top wall of the air chamber is provided with an aeration disc, the top wall of the air chamber is provided with a plurality of through holes, and the through holes are communicated with the through holes on the aeration disc; the edge of the top wall of the air chamber is connected with the inner wall of the reactor shell through an interception plate with a through hole, and a space between the interception plate and the top wall of the reactor shell is filled with printing and dyeing wastewater and a plurality of modified polyurethane sponge suspension carriers attached with growing biological membranes; a water inlet pipe is arranged above the side wall of the reactor shell, and a water outlet pipe is arranged below the side wall of the reactor shell; the bottom plate of the reactor shell is also connected with an air inlet system.
The present invention is also characterized in that,
the stirrer is connected with a controller.
The air inlet system comprises an air inlet pipe, one end of the air inlet pipe is connected with an aeration pump, and the other end of the air inlet pipe penetrates through the bottom plate of the reactor shell to be communicated with the interior of the gas disperser; the gas disperser is a shell with a through hole on the side wall; the air blown by the aeration pump passes through the gas disperser, the gas chamber and the aeration disc in sequence and then is dispersed in the reactor shell.
The air inlet pipe is also provided with a gas flowmeter and a ball valve.
The second technical scheme adopted by the invention is that the operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater adopts the device, and is implemented according to the following steps:
step 1: pretreating the modified polyurethane sponge by a potassium dichromate solution and a ferric trichloride solution respectively to obtain a modified polyurethane sponge suspension carrier; adding a plurality of blocks of modified polyurethane sponge suspension carriers and activated sludge into a reactor shell, starting an aeration pump and a stirrer, discharging all inoculated sludge after stirring and aeration, adding simulation water distribution with the same volume, adjusting aeration intensity through a gas flowmeter, and continuously culturing for a plurality of days to grow a biofilm on the surface of the modified polyurethane sponge suspension carriers;
step 2: replacing simulated water distribution in the reactor shell with simulated printing and dyeing wastewater, performing microbial acclimation on the printing and dyeing wastewater by adopting a gradient impact culture method, wherein the gradients are 20%, 40%, 60%, 80% and 100% in sequence, and reducing the dissolved oxygen content in the reactor shell through a gas flowmeter, so that the microorganisms on the surface of the modified polyurethane sponge suspension carrier are in a micro-aerobic environment state, and continuously culturing until the system runs stably.
The present invention is also characterized in that,
the step 1 is implemented according to the following specific steps:
step 1.1, respectively soaking modified polyurethane sponge for 6-10 hours by using a potassium dichromate solution with the concentration of 0.05-0.15 mol/L and a ferric trichloride solution with the concentration of 0.05-0.15 mol/L, and washing the treated modified polyurethane sponge with clear water;
step 1.2, adding a plurality of modified polyurethane sponge suspension carriers obtained in the step 1.1 into a reactor shell according to 35-40% of the effective volume of the reactor shell, and adding 3000-4000 mg/L of activated sludge of a sewage treatment plant into the reactor shell to reach a designed volume;
step 1.3, starting aeration pump and stirrer, and utilizing gasThe inlet aeration intensity is controlled to be 9-10 m by the flow meter3/(h m3Wastewater), controlling the rotating speed of a stirrer to rotate at 50-60 revolutions per minute, fully mixing and contacting the sludge and the modified polyurethane sponge suspension carrier, discharging all inoculated sludge after stirring and aerating for 24 hours, adding equivalent-volume simulated water distribution into a reactor shell, wherein a water carbon source is distributed: nitrogen source: phosphorus source 100:5:1, COD: 1300-1500mg/L, total nitrogen: 60-75mg/L, total phosphorus: 12-15 mg/L.
Step 1.4, adjusting the aeration intensity in the step 1.3 to 4-5 m by using a gas flowmeter3/(h m3Waste water), the stirring speed is unchanged, the continuous operation is carried out for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier in the reactor shell, the treatment efficiency of COD is higher than 80%, and the device is successfully started for biofilm formation.
The step 2 is implemented according to the following specific steps:
step 2.1, replacing the simulated water distribution of the reactor shell with successful film formation in the step 1 with simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacement process, firstly, COD with the mass percentage of 20% is replaced with the simulated printing and dyeing wastewater, and the aeration intensity is adjusted to 1.5-2.0 m by using a gas flowmeter3/(h m3Waste water) so that the content of dissolved oxygen in the device system is controlled to be 0.5-1 mg/L, and the device is operated for 3-5 days;
step 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100%, wherein the running time of each condition is 3-5 days;
and 2.3, continuously operating the reaction device for 7-9 days by adopting 100% printing and dyeing wastewater.
The invention has the beneficial effects that:
1. the carrier interception plate in the device can realize interception of the modified polyurethane sponge carrier, so that a biological membrane falling off from the device and treated wastewater are completely discharged.
2. The stirrer in the device ensures that the modified polyurethane sponge carrier is fully contacted with the wastewater, and the low aeration intensity realizes that the biomembrane in the system is in a micro-aerobic state, thereby increasing the hydrolytic acidification efficiency of the refractory organic matters and improving the conversion of organic macromolecules.
3. According to the method, the enrichment, growth and metabolism of decarbonized bacteria in the biological membrane are accelerated and the metabolism function of the device on the printing and dyeing wastewater is improved by a full-sludge-discharge membrane hanging method and an operation method for impact domestication of the biological membrane growth by the gradient printing and dyeing wastewater.
4. The micro-aerobic fluidized bed biomembrane device can realize high-efficiency decoloration of printing and dyeing wastewater and hydrolysis of organic macromolecules.
Drawings
FIG. 1 is a schematic structural diagram of a micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater;
FIG. 2 is a top view of a retention plate in a micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater according to the invention;
FIG. 3 is a schematic structural diagram of an aeration disc of a micro-aerobic fluidized bed biofilm device according to the invention;
in the figure, 1, a reactor shell, 2, a modified polyurethane sponge carrier, 3, an aeration disc, 4, an air chamber, 5, a gas disperser, 6, a ball valve, 7, a gas flowmeter, 8, an air inlet pipe, 9, an aeration pump, 10, a water inlet pipe, 11, a water outlet pipe, 12, a stirrer, 13, a controller, 14 and a retaining plate.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
The invention provides a micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater, which comprises a reactor shell 1, wherein a stirrer 12 is arranged at the top wall of the reactor shell 1, a gas disperser 5 and a gas chamber 4 are arranged on the bottom plate of the reactor shell 1, and the gas disperser 5 is arranged in the gas chamber 4; the top wall of the air chamber 4 is provided with an aeration disc 3, the top wall of the air chamber 4 is provided with a plurality of through holes, and the through holes are communicated with the through holes on the aeration disc 3; the edge of the top wall of the air chamber 4 is connected with the inner wall of the reactor shell 1 through an interception plate 14 with a through hole, and a space between the interception plate 14 and the top wall of the reactor shell 1 is filled with printing and dyeing wastewater and a plurality of modified polyurethane sponge suspension carriers 2 attached with growing biological membranes; a water inlet pipe 10 is arranged above the side wall of the reactor shell 1, and a water outlet pipe 11 is arranged below the side wall of the reactor shell 1; the bottom plate of the reactor shell 1 is also connected with an air inlet system.
The stirrer 12 is connected with a controller 13. The modified polyurethane sponge suspension carrier 2 is closely contacted with the wastewater under the stirring action of the stirrer 12, and the stirrer 12 works under the control of the controller 13.
The air inlet system comprises an air inlet pipe 8, one end of the air inlet pipe 8 is connected with an aeration pump 9, and the other end of the air inlet pipe 8 penetrates through the bottom plate of the reactor shell 1 and is communicated with the interior of the gas disperser 5; the gas disperser 5 is a shell with through holes on the side wall; the air blown by the aeration pump 9 passes through the gas disperser 5, the gas chamber 4 and the aeration disc 3 in sequence and is dispersed in the reactor shell 1.
The air inlet pipe 8 is also provided with a gas flowmeter 7 and a ball valve 6.
The device mainly utilizes the biomembrane attached and grown on the surface of the modified polyurethane sponge suspension carrier 2 to realize the hydrolytic acidification of the organic dye difficult to degrade in the printing and dyeing wastewater, the suspension carrier 2 is in a fluidized state under the stirring action of the stirrer 12, and the stirrer 12 enables the suspension carrier 2 to be fully contacted with the printing and dyeing wastewater under the accurate regulation and control of the controller 13, so that the transfer efficiency of substances is increased, and the hydrolytic acidification efficiency of organic matters is improved. The modified polyurethane sponge suspension carrier 2 is a square carrier with the length multiplied by the width multiplied by the height multiplied by 1cm, and the specific surface area can reach 30000m2/m3The density of the carrier after the biofilm culturing growth is basically the same as that of the wastewater.
The surface of the aeration disc 5 is uniformly distributed with small holes with the aperture of 0.16-0.50 mm, and the small holes are arranged in a circular way, as shown in figure 3. The air that the aeration pump 9 was bloated enters into gas disperser 5 through intake pipe 8 under the control of gas flowmeter 7, gaseous lateral wall aperture all around through gas disperser 5 disperses in air chamber 4, the impact of gas to the middle of air chamber 4 has been reduced, make the pressure of gas be in the constant state in the air chamber 4, guarantee that other pressure of aeration dish 5 all aperture departments are the same, realize gaseous homodisperse in reactor housing 1, provide the supply of micro dissolved oxygen for the biomembrane.
The interception plate 14 is positioned at the bottom of the reactor shell 1 and shows uniformly distributed small holes, as shown in fig. 2, the diameter of the small holes is smaller than the size of each modified polyurethane sponge suspension carrier 2, so that the modified polyurethane sponge suspension carriers 2 are intercepted, and the treated wastewater and the fallen biological membranes are discharged out of the system through the small hole water inlet and outlet pipes 11.
A micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater comprises the following working processes:
printing and dyeing wastewater and a plurality of pieces of modified polyurethane sponge suspension carriers 2 attached with biological membranes are positioned in a device main body 1, a stirrer 12 drives the wastewater and the modified polyurethane sponge suspension carriers 2 to flow by rotating under the control of a controller 13, so that the wastewater is fully and closely contacted with the biological membranes on the surfaces of the modified polyurethane sponge suspension carriers 2, air blown by an aeration pump 9 enters a gas disperser 5 through an air inlet pipe 8 under the control of a gas flowmeter 7, the gas is dispersed in a gas chamber 4 through peripheral orifices of the gas disperser 5, the air in the gas chamber 4 is dispersed in the device main body 1 through an aeration disc 5, the dissolved oxygen content in the wastewater in the device main body 1 is 0.5-1.0 mg/L under the regulation of the gas flowmeter 7, so that the biological membranes are in a micro-oxygen fluidization state, and the metabolic activity and special function microorganisms of anaerobic bacteria and facultative bacteria in the biological membranes are enriched, the high-efficiency decoloration of the organic dye difficult to degrade in the wastewater and the conversion of macromolecular organic matters are realized, the treated wastewater enters the drain pipe 11 through the interception plate 14 and is discharged out of the system through the drain pipe 11 to enter the next stage of treatment.
The invention also provides an operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater, which is implemented by adopting the device according to the following steps:
step 1: pretreating the modified polyurethane sponge by a potassium dichromate solution and a ferric trichloride solution respectively to obtain a modified polyurethane sponge suspension carrier 2; adding a plurality of blocks of modified polyurethane sponge suspension carriers 2 and activated sludge into a reactor shell 1, starting an aeration pump 9 and a stirrer 12, discharging all inoculated sludge after stirring and aeration, adding simulation water distribution with the same volume, adjusting aeration intensity through a gas flowmeter 7, and after continuous culture for a plurality of days, growing a biofilm on the surface of the modified polyurethane sponge suspension carriers 2, wherein the device biofilm-formation starting is successful;
the step 1 is implemented according to the following specific steps:
1.1, respectively soaking modified polyurethane sponge for 6-10 hours by using a potassium dichromate solution with the concentration of 0.05-0.15 mol/L and a ferric trichloride solution with the concentration of 0.05-0.15 mol/L, and washing the treated modified polyurethane sponge 2 by using clean water;
step 1.2, adding a plurality of modified polyurethane sponge suspension carriers 2 obtained in the step 1.1 into a reactor shell 1 according to 35-40% of the effective volume of the reactor shell 1, and adding 3000-4000 mg/L of activated sludge of a sewage treatment plant into the reactor shell 1 to reach the designed volume;
step 1.3, starting an aeration pump 9 and a stirrer 12, and controlling the inlet aeration intensity to be 9-10 m by using a gas flowmeter 73/(h m3Waste water), the 12 rotational speed control of agitator is 50 ~ 60 revolutions per minute, makes mud and modified polyurethane sponge suspension carrier 2 intensive mixing contact, and stirring and aeration discharge after 24 hours all inoculation mud, throw equal volumn simulation water distribution to reactor casing 1 in, wherein the water distribution carbon source: nitrogen source: phosphorus source 100:5:1, COD: 1300-1500mg/L, total nitrogen: 60-75mg/L, total phosphorus: 12-15 mg/L.
Step 1.4, adjusting the aeration intensity in the step 1.3 to 4-5 m by using a gas flowmeter 73/(h m3Waste water), the stirring speed is unchanged, the continuous operation is carried out for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier 2 in the reactor shell 1, the treatment efficiency of COD is higher than 80%, and the device biofilm formation is successfully started.
Step 2: the simulated water distribution in the reactor shell 1 is replaced by simulated printing and dyeing wastewater, the printing and dyeing wastewater is subjected to microbial domestication by adopting a gradient impact culture method, the gradients are 20%, 40%, 60%, 80% and 100% in sequence, and the dissolved oxygen content in the reactor shell 1 is reduced through a gas flowmeter 7, so that the microorganisms on the surface of the modified polyurethane sponge suspension carrier 2 are in a micro-aerobic environment state, and the continuous culture is carried out until the system runs stably.
The step 2 is implemented according to the following specific steps:
step (ii) of2.1, replacing the simulated water distribution of the reactor shell 1 with the successful film formation in the step 1 with the simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacing process, firstly, COD with the mass percentage of 20% is replaced with the simulated printing and dyeing wastewater, and the aeration intensity is adjusted to 1.5-2.0 m by using a gas flowmeter 73/(h m3Waste water) so that the content of dissolved oxygen in the device system is controlled to be 0.5-1 mg/L, and the device is operated for 3-5 days;
step 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100%, wherein the running time of each condition is 3-5 days;
and 2.3, continuously operating the reaction device for 7-9 days by adopting 100% of printing and dyeing wastewater, wherein the printing and dyeing wastewater of the device has an obvious decolorizing effect, and 70-80% of refractory organic dye realizes hydrolytic acidification.
Example 1
The operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater comprises the following steps:
step 1: pretreating the modified polyurethane sponge by a potassium dichromate solution and a ferric trichloride solution respectively to obtain a modified polyurethane sponge suspension carrier 2; adding a plurality of blocks of modified polyurethane sponge suspension carriers 2 and activated sludge into a reactor shell 1, starting an aeration pump 9 and a stirrer 12, discharging all inoculated sludge after stirring and aeration, adding simulation water distribution with the same volume, adjusting aeration intensity through a gas flowmeter 7, and after continuous culture for a plurality of days, growing a biofilm on the surface of the modified polyurethane sponge suspension carriers 2, wherein the device biofilm-formation starting is successful;
the step 1 is implemented according to the following specific steps:
1.1, respectively soaking modified polyurethane sponge for 8 hours by using 0.1mol/L potassium dichromate solution and 0.1mol/L ferric trichloride solution, and washing the treated modified polyurethane sponge suspension carrier 2 by using clear water;
step 1.2, adding a plurality of modified polyurethane sponge suspension carriers 2 obtained in the step 1.1 into a reactor shell 1 according to 37.5 percent of the effective volume of the reactor shell 1, and adding 3500mg/L activated sludge of a sewage treatment plant into the reactor shell 1 to reach the designed volume;
step 1.3, starting the aeration pump 9 and the stirrer 12, and controlling the inlet aeration intensity to be 9.5m by using the gas flowmeter 73/(h m3Wastewater), controlling the rotating speed of a stirrer 12 to be 55 revolutions per minute, fully mixing and contacting the sludge and the modified polyurethane sponge suspension carrier 2, discharging all inoculated sludge after stirring and aerating for 24 hours, adding equivalent-volume simulated water to a reactor shell 1, wherein a water carbon source is distributed: nitrogen source: phosphorus source 100:5:1, COD: 1400mg/L, total nitrogen: 70mg/L, total phosphorus: 13.5 mg/L.
Step 1.4, adjusting the aeration intensity in the step 1.3 to 4.5m by using a gas flowmeter 73/(h m3Waste water), the stirring speed is unchanged, the continuous operation is carried out for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier 2 in the reactor shell 1, the treatment efficiency of COD is higher than 80%, and the device biofilm formation is successfully started.
Step 2: the simulated water distribution in the reactor shell 1 is replaced by simulated printing and dyeing wastewater, the printing and dyeing wastewater is subjected to microbial domestication by adopting a gradient impact culture method, the gradients are 20%, 40%, 60%, 80% and 100% in sequence, and the dissolved oxygen content in the reactor shell 1 is reduced through a gas flowmeter 7, so that the microorganisms on the surface of the modified polyurethane sponge suspension carrier 2 are in a micro-aerobic environment state, and the continuous culture is carried out until the system runs stably.
The step 2 is implemented according to the following specific steps:
step 2.1, replacing the simulated water distribution of the reactor shell 1 with the successful film formation in the step 1 with the simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacing process, firstly, COD with the mass percentage of 20% is replaced with the simulated printing and dyeing wastewater, and the aeration intensity is adjusted to 1.75m by using a gas flowmeter 73/(h m3Wastewater) so that the content of dissolved oxygen in the device system is controlled to be 0.75mg/L, and the device is operated for 4 days;
step 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100% respectively, wherein the running time of each condition is 4 days;
and 2.3, continuously operating the reaction device for 8 days by adopting 100 percent of printing and dyeing wastewater.
Example 2
The operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater comprises the following steps:
step 1: pretreating the modified polyurethane sponge by a potassium dichromate solution and a ferric trichloride solution respectively to obtain a modified polyurethane sponge suspension carrier 2; adding a plurality of blocks of modified polyurethane sponge suspension carriers 2 and activated sludge into a reactor shell 1, starting an aeration pump 9 and a stirrer 12, discharging all inoculated sludge after stirring and aeration, adding simulation water distribution with the same volume, adjusting aeration intensity through a gas flowmeter 7, and after continuous culture for a plurality of days, growing a biofilm on the surface of the modified polyurethane sponge suspension carriers 2, wherein the device biofilm-formation starting is successful;
the step 1 is implemented according to the following specific steps:
1.1, respectively soaking modified polyurethane sponge for 6 hours by using 0.05mol/L potassium dichromate solution and 0.05mol/L ferric trichloride solution, and washing the treated modified polyurethane sponge suspension carrier 2 by using clear water;
step 1.2, adding a plurality of modified polyurethane sponge suspension carriers 2 obtained in the step 1.1 into a reactor shell 1 according to 35% of the effective volume of the reactor shell 1, and adding 3000mg/L of activated sludge of a sewage treatment plant into the reactor shell 1 to reach the designed volume;
step 1.3, starting the aeration pump 9 and the stirrer 12, and controlling the inlet aeration intensity to be 9m by using the gas flowmeter 73/(h m3Wastewater), controlling the rotating speed of a stirrer 12 to 50 revolutions per minute, fully mixing and contacting sludge and the modified polyurethane sponge suspension carrier 2, discharging all inoculated sludge after stirring and aerating for 24 hours, adding equivalent-volume simulated water to a reactor shell 1, wherein a water carbon source is distributed: nitrogen source: phosphorus source 100:5:1, COD: 1300mg/L, total nitrogen: 60mg/L, total phosphorus: 12 mg/L.
Step 1.4, the aeration intensity in the step 1.3 is improvedAdjusted to 4m by a gas flowmeter 73/(h m3Waste water), the stirring speed is unchanged, the continuous operation is carried out for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier 2 in the reactor shell 1, the treatment efficiency of COD is higher than 80%, and the device biofilm formation is successfully started.
Step 2: the simulated water distribution in the reactor shell 1 is replaced by simulated printing and dyeing wastewater, the printing and dyeing wastewater is subjected to microbial domestication by adopting a gradient impact culture method, the gradients are 20%, 40%, 60%, 80% and 100% in sequence, and the dissolved oxygen content in the reactor shell 1 is reduced through a gas flowmeter 7, so that the microorganisms on the surface of the modified polyurethane sponge suspension carrier 2 are in a micro-aerobic environment state, and the continuous culture is carried out until the system runs stably.
The step 2 is implemented according to the following specific steps:
step 2.1, replacing the simulated water distribution of the reactor shell 1 with the successful film formation in the step 1 with the simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacing process, firstly, COD with the mass percentage of 20% is replaced with the simulated printing and dyeing wastewater, and the aeration intensity is adjusted to 1.5m by using a gas flowmeter 73/(h m3Wastewater) so that the content of dissolved oxygen in the device system is controlled at 0.5mg/L, and the device is operated for 3 days;
step 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100% respectively, wherein the running time of each condition is 3 days;
and 2.3, continuously operating the reaction device for 7 days by adopting 100% printing and dyeing wastewater.
Example 3
The operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater comprises the following steps:
step 1: pretreating the modified polyurethane sponge by a potassium dichromate solution and a ferric trichloride solution respectively to obtain a modified polyurethane sponge suspension carrier 2; adding a plurality of blocks of modified polyurethane sponge suspension carriers 2 and activated sludge into a reactor shell 1, starting an aeration pump 9 and a stirrer 12, discharging all inoculated sludge after stirring and aeration, adding simulation water distribution with the same volume, adjusting aeration intensity through a gas flowmeter 7, and after continuous culture for a plurality of days, growing a biofilm on the surface of the modified polyurethane sponge suspension carriers 2, wherein the device biofilm-formation starting is successful;
the step 1 is implemented according to the following specific steps:
1.1, respectively soaking modified polyurethane sponge for 10 hours by using 0.15mol/L potassium dichromate solution and 0.15mol/L ferric trichloride solution, and washing the treated modified polyurethane sponge suspension carrier 2 by using clear water;
step 1.2, adding a plurality of blocks of the modified polyurethane sponge suspension carriers 2 obtained in the step 1.1 into a reactor shell 1 according to 40% of the effective volume of the reactor shell 1, and adding 4000mg/L of activated sludge of a sewage treatment plant into the reactor shell 1 to reach the designed volume;
step 1.3, starting the aeration pump 9 and the stirrer 12, and controlling the inlet aeration intensity to be 9m by using the gas flowmeter 73/(h m3Wastewater), controlling the rotating speed of a stirrer 12 to be 60 revolutions per minute, fully mixing and contacting the sludge and the modified polyurethane sponge suspension carrier 2, discharging all inoculated sludge after stirring and aerating for 24 hours, adding equivalent-volume simulated water to a reactor shell 1, wherein a water carbon source is distributed: nitrogen source: phosphorus source 100:5:1, COD: 1500mg/L, total nitrogen: 75mg/L, total phosphorus: 15 mg/L.
Step 1.4, adjusting the aeration intensity in the step 1.3 to 5m by using a gas flowmeter 73/(h m3Waste water), the stirring speed is unchanged, the continuous operation is carried out for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier 2 in the reactor shell 1, the treatment efficiency of COD is higher than 80%, and the device biofilm formation is successfully started.
Step 2: the simulated water distribution in the reactor shell 1 is replaced by simulated printing and dyeing wastewater, the printing and dyeing wastewater is subjected to microbial domestication by adopting a gradient impact culture method, the gradients are 20%, 40%, 60%, 80% and 100% in sequence, and the dissolved oxygen content in the reactor shell 1 is reduced through a gas flowmeter 7, so that the microorganisms on the surface of the modified polyurethane sponge suspension carrier 2 are in a micro-aerobic environment state, and the continuous culture is carried out until the system runs stably.
The step 2 is implemented according to the following specific steps:
step 2.1, replacing the simulated water distribution of the reactor shell 1 with the successful film formation in the step 1 with the simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacing process, firstly, COD with the mass percentage of 20% is replaced with the simulated printing and dyeing wastewater, and the aeration intensity is adjusted to 2m by using a gas flowmeter 73/(h m3Wastewater) so that the content of dissolved oxygen in the device system is controlled at 1mg/L, and the device is operated for 5 days;
step 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100% respectively, wherein the running time of each condition is 5 days;
and 2.3, continuously operating the reaction device for 9 days by adopting 100 percent of printing and dyeing wastewater.
Comparative example 1
Step 1: device biofilm start
Step 1.1, polyethylene is selected as a suspension carrier, the suspension carrier is added into a device main body according to 37.5% of the effective volume of the device, and 3500mg/L activated sludge of a sewage treatment plant is added into the device main body, so that the device reaches the designed volume.
Step 1.2, starting the stirrer on the basis of the step 1.1, and controlling the inlet aeration intensity to be 9.5m by using a gas flowmeter3/(h m3Waste water), the agitator speed control is at 55 revolutions per minute, makes mud and suspension carrier intensive mixing contact, and stirring and aeration discharge whole inoculation mud after 24 hours, throw equal volumn simulation water distribution to the device main part, wherein the water distribution carbon source: nitrogen source: phosphorus source 100:5:1, COD: 1400mg/L, total nitrogen: 70mg/L, total phosphorus: 13.5 mg/L.
Step 1.3, adjusting the aeration intensity in the step 1.2 to 4.5m by using a gas flowmeter3/(h m3Waste water), the stirring speed is unchanged, the device continuously runs for 7d, a biological film grows on the surface of the suspension carrier in the main body of the device, the treatment efficiency of COD is higher than 80 percent, and the device is successfully started by film-hanging
Step 2: method for operating a device
Step 2.1, the simulation of the successful film hanging device body in the step 1 is matchedReplacing water with simulated printing and dyeing wastewater, wherein the replacement process adopts an equivalent increase method, firstly replacing 20 percent of COD with the simulated printing and dyeing wastewater, and adjusting the aeration intensity to 1.75m by using a gas flowmeter3/(h m3Wastewater) so that the dissolved oxygen content in the system of the apparatus was controlled to 0.8mg/L, and the apparatus was operated for 4 days.
And 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100% respectively, wherein the running time of each condition is 4 days.
And 2.3, continuously operating the reaction device for 8 days by adopting 100% of printing and dyeing wastewater, and monitoring the hydrolysis acidification efficiency of the printing and dyeing wastewater.
Comparative example 2
Step 1: device biofilm start
Step 1.1, selecting modified polyurethane sponge as a suspension carrier, adding the modified polyurethane sponge into a device main body according to 37.5% of the effective volume of the device, and adding 3500mg/L activated sludge of a sewage treatment plant into the device main body 1, so that the device reaches the designed volume.
Step 1.2, starting an aeration pump and a stirrer on the basis of the step 1.1, and controlling the inlet aeration intensity to be 9.5m by using a gas flowmeter 73/(h m3Waste water), the agitator speed control is at 55 revolutions per minute, makes mud and suspension carrier intensive mixing contact, and stirring and aeration discharge whole inoculation mud after 24 hours, throw equal volumn simulation water distribution to the device main part, wherein the water distribution carbon source: nitrogen source: phosphorus source 100:5:1, COD: 1400mg/L, total nitrogen: 70mg/L, total phosphorus: 13.5 mg/L.
Step 1.3, in the step 1.2, the aeration intensity and the stirring speed are unchanged, the device continuously runs for 7 days, a biological membrane grows on the surface of the suspension carrier in the main body of the device, the treatment efficiency of COD is higher than 80 percent, and the device is successfully started by membrane hanging
Step 2: method for operating a device
Step 2.1, replacing the simulated water distribution of the device main body for successfully hanging the membrane in the step 1 with the simulated printing and dyeing wastewater, closing the aeration device, and operating until the growth of the biological membrane is good and the hydrolytic acidification efficiency is stable
Comparative example 3
Step 1: device biofilm start
Step 1.1, selecting modified polyurethane sponge as a suspension carrier, respectively soaking the suspension carrier by using 0.1mol/L potassium dichromate and 0.1mol/L ferric trichloride solution, and washing the treated suspension carrier by using clear water.
Step 1.2, adding the modified polyurethane sponge suspension carrier obtained in the step 1.1 into a device main body according to 37.5% of the effective volume of the device, and adding 3500mg/L activated sludge of a sewage treatment plant into the device main body, so that the device reaches the designed volume.
Step 1.3, on the basis of the steps 1.1 and 1.2, starting an aeration pump and a stirrer, and controlling the inlet aeration intensity to be 9.5m by using a gas flow meter3/(h m3Waste water), the agitator speed control is at 55 revolutions per minute, makes mud and suspension carrier intensive mixing contact, and stirring and aeration discharge whole inoculation mud after 24 hours, throw equal volumn simulation water distribution to the device main part, wherein the water distribution carbon source: nitrogen source: phosphorus source 100:5:1, COD: 1400mg/L, total nitrogen: 70mg/L, total phosphorus: 13.5 mg/L.
Step 1.4, adjusting the aeration intensity in the step 1.3 to 4.5m by using a gas flowmeter3/(h m3Waste water), the stirring speed is unchanged, the device continuously runs for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier in the main body of the device, the treatment efficiency of COD is higher than 80%, and the device is successfully started by hanging the membrane
Step 2: method for operating a device
And 2.1, replacing the simulated water distribution of the device main body with the successful film hanging in the step 1 by simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacing process, firstly, 20 percent of COD is replaced by the simulated printing and dyeing wastewater, the aeration device is closed, and the device runs for 4 days.
And 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100% respectively, wherein the running time of each condition is 4 days.
And 2.3, continuously operating the reaction device for 8 days by adopting 100% of printing and dyeing wastewater, and monitoring the hydrolysis acidification effect of the printing and dyeing wastewater.
The hydrolytic acidification efficiencies of the different protocols were monitored and analyzed, and the comparative results are shown in table 1.
TABLE 1 analysis results of hydrolytic acidification properties of printing and dyeing wastewater under different case conditions
As is apparent from Table 1, the embodiment of the invention can realize higher biodegradability, decolorization efficiency and biomass, and has higher COD removal efficiency, and the operation method of the invention has obvious improvement effect on improving hydrolytic acidification efficiency.
Claims (7)
1. The micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater is characterized by comprising a reactor shell (1), wherein a stirrer (12) is arranged at the top wall of the reactor shell (1), a gas disperser (5) and a gas chamber (4) are arranged on the bottom plate of the reactor shell (1), and the gas disperser (5) is arranged in the gas chamber (4); the top wall of the air chamber (4) is provided with an aeration disc (3), the top wall of the air chamber (4) is provided with a plurality of through holes, and the through holes are communicated with the through holes on the aeration disc (3); the edge of the top wall of the air chamber (4) is connected with the inner wall of the reactor shell (1) through an interception plate (14) with a through hole, and the space between the interception plate (14) and the top wall of the reactor shell (1) is filled with printing and dyeing wastewater and a plurality of modified polyurethane sponge suspension carriers (2) attached with growing biological membranes; a water inlet pipe (10) is arranged above the side wall of the reactor shell (1), and a water outlet pipe (11) is arranged below the side wall of the reactor shell (1); the bottom plate of the reactor shell (1) is also connected with an air inlet system.
2. The micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater as claimed in claim 1, wherein the stirrer (12) is connected with a controller (13).
3. The micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater as per claim 1, wherein the air intake system comprises an air intake pipe (8), one end of the air intake pipe (8) is connected with an aeration pump (9), and the other end of the air intake pipe (8) passes through the bottom plate of the reactor shell (1) and is communicated with the inside of the gas disperser (5); the gas disperser (5) is a shell with a through hole on the side wall; the air blown by the aeration pump (9) passes through the gas disperser (5), the air chamber (4) and the aeration disc (3) in sequence and then is dispersed in the reactor shell (1).
4. The micro-aerobic fluidized bed biofilm device for the hydrolytic acidification of printing and dyeing wastewater as claimed in claim 3, wherein a gas flow meter (7) and a ball valve (6) are further arranged on the gas inlet pipe (8).
5. The operation method of the micro-aerobic fluidized bed biomembrane device for hydrolytic acidification of printing and dyeing wastewater is characterized by adopting the device as claimed in any one of claims 1 to 4, and is implemented by the following steps:
step 1: pretreating the modified polyurethane sponge by a potassium dichromate solution and a ferric trichloride solution respectively to obtain a modified polyurethane sponge suspension carrier (2); adding a plurality of modified polyurethane sponge suspension carriers (2) and activated sludge into a reactor shell (1), starting an aeration pump (9) and a stirrer (12), discharging all inoculated sludge after stirring and aeration, adding simulation water distribution with the same volume, adjusting aeration intensity through a gas flowmeter (7), and growing a biofilm on the surface of the modified polyurethane sponge suspension carriers (2) after continuous culture for several days;
step 2: the simulated water distribution in the reactor shell (1) is replaced by simulated printing and dyeing wastewater, the printing and dyeing wastewater is subjected to microbial domestication by adopting a gradient impact culture method, the gradients are 20%, 40%, 60%, 80% and 100% in sequence, and the dissolved oxygen content in the reactor shell (1) is reduced through a gas flowmeter (7), so that the microorganisms on the surface of the modified polyurethane sponge suspension carrier (2) are in a micro-aerobic environment state, and the system is continuously cultured until the system runs stably.
6. The operation method of the micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater as claimed in claim 5, wherein the step 1 is implemented according to the following specific steps:
1.1, respectively soaking modified polyurethane sponge for 6-10 hours by using a potassium dichromate solution with the concentration of 0.05-0.15 mol/L and a ferric trichloride solution with the concentration of 0.05-0.15 mol/L, and washing the treated modified polyurethane sponge suspension carrier (2) by using clear water;
step 1.2, adding a plurality of modified polyurethane sponge suspension carriers (2) obtained in the step 1.1 into a reactor shell (1) according to 35-40% of the effective volume of the reactor shell (1), and adding 3000-4000 mg/L of activated sludge of a sewage treatment plant into the reactor shell (1) to reach the designed volume;
step 1.3, starting an aeration pump (9) and a stirrer (12), and controlling the inlet aeration intensity to be 9-10 m by using a gas flowmeter (7)3/h m3In the wastewater treatment process, the rotating speed of a stirrer (12) is controlled to be 50-60 revolutions per minute, so that sludge and a modified polyurethane sponge suspension carrier (2) are fully mixed and contacted, all inoculated sludge is discharged after stirring and aeration are carried out for 24 hours, and equal-volume simulated water is added into a reactor shell (1), wherein a carbon source is distributed: nitrogen source: phosphorus source 100:5:1, COD: 1300-1500mg/L, total nitrogen: 60-75mg/L, total phosphorus: 12-15 mg/L.
Step 1.4, adjusting the aeration intensity in the step 1.3 to 4-5 m by using a gas flowmeter (7)3/(h m3Waste water), the stirring speed is unchanged, the continuous operation is carried out for 7d, a biomembrane grows on the surface of the modified polyurethane sponge suspension carrier (2) in the reactor shell (1), the treatment efficiency of COD is higher than 80%, and the device starts up the biofilm formation successfully.
7. The operation method of the micro-aerobic fluidized bed biofilm device for hydrolytic acidification of printing and dyeing wastewater as claimed in claim 5, wherein the step 2 is implemented according to the following specific steps:
step 2.1, replacing simulated water distribution of the reactor shell (1) with successful film formation in the step 1 with simulated printing and dyeing wastewater, wherein an equivalent increasing method is adopted in the replacing process, firstly, COD with the mass percentage of 20% is replaced with the simulated printing and dyeing wastewater, and the aeration intensity is adjusted to 1.5-2.0 m by using a gas flowmeter (7)3/h m3Controlling the content of dissolved oxygen in the device system to be 0.5-1 mg/L by using the wastewater, and running for 3-5 days;
step 2.2, gradually increasing the proportion of COD (chemical oxygen demand) in the printing and dyeing wastewater to 40%, 60%, 80% and 100%, wherein the running time of each condition is 3-5 days;
and 2.3, continuously operating the reaction device for 7-9 days by adopting 100% printing and dyeing wastewater.
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