CN107986569B - High-nitrogen printing wastewater treatment and recycling system and use method thereof - Google Patents

High-nitrogen printing wastewater treatment and recycling system and use method thereof Download PDF

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CN107986569B
CN107986569B CN201711340738.2A CN201711340738A CN107986569B CN 107986569 B CN107986569 B CN 107986569B CN 201711340738 A CN201711340738 A CN 201711340738A CN 107986569 B CN107986569 B CN 107986569B
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printing
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CN107986569A (en
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李方
季慕尧
田晴
刘艳彪
夏琴
陈洪腾
潘玉婷
芮豪杰
王倩
彭翔
杨波
马春燕
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Mbp Environmental Engineering Co ltd
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Donghua University
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • 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
    • C02F3/28—Anaerobic digestion processes
    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5281—Installations for water purification using chemical agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/30—Nature of the water, waste water, sewage or sludge to be treated from the textile industry
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F3/02—Aerobic processes

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Abstract

The invention relates to a high-nitrogen printing wastewater treatment and recycling system and a using method thereof, wherein the system comprises 4 subsystems: 1# subsystem: high concentration organic waste water processing system of printing pretreatment workshop section, 2# subsystem: high nitrogen effluent disposal system of stamp workshop section, 3# subsystem: advanced treatment of membrane and recycling system, 4# subsystem: sludge reduction processing system. According to different water quality and water quantity of each working section of the printing process, respectively collecting and performing quality-divided treatment and recycling, wherein pretreatment wastewater, printing wastewater and rinsing wastewater respectively enter a 1-3 # subsystem for treatment, and generated sludge enters a 4# subsystem for reduction treatment. The system adopts an anaerobic ammonia oxidation technology, and solves the problem that the carbon-nitrogen ratio of the wastewater is seriously disordered. The method has the advantages of high system integration and accurate control, can effectively solve the problems of difficult denitrification and high cost of the printing wastewater, and simultaneously realizes sludge reduction.

Description

High-nitrogen printing wastewater treatment and recycling system and use method thereof
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a high-nitrogen printing wastewater treatment and recycling system and a using method thereof.
Background
Reactive printing is one of the most common processes in dyeing and finishing processes. The process flow comprises a pretreatment process and a printing process, wherein the pretreatment process generally comprises three steps of desizing, scouring and bleaching; the printing process comprises ground color dyeing, printing, drying, steaming, baking, washing, soaping and washing. The water amount of the desizing wastewater only accounts for about 10% of the total wastewater, but the contribution degree of the total COD (chemical oxygen demand) amount accounts for 60% -70%, the main pollutants in the desizing wastewater are the desizing slurry, the main components are starch and polyethylene glycol PVA (polyvinyl alcohol), the COD value is up to 20000-30000 mg/L, the COD amount accounts for more than half of the total amount of the printing and dyeing wastewater, the BOD/COD value is less than 0.1, the biochemical degradability is poor, and great pressure is brought to the tail end treatment of the printing and dyeing wastewater. The waste water generated in the printing process mainly comes from the washing and soaping processes, and the main pollutants are washed paste and mainly contain sodium alginate, urea and the like. In reactive dye printing, because the dye consumption is large, the bath ratio is small, aggregation is easy to occur among dyes, the solubility of the dyes is poor, and the printing effect is influenced, therefore, urea is generally added during the reactive printing to improve the solubility of the dyes, the permeability during steaming and the fixation rate of fibers, but ammonia nitrogen compounds decomposed from the urea in wastewater can sharply increase the total nitrogen in the wastewater. The total nitrogen of the general comprehensive wastewater of the reactive printing and dyeing mill reaches 300-500 mg/L, the COD concentration is 2000-3000 mg/L, and the wastewater has high total nitrogen concentration, serious imbalance of carbon-nitrogen ratio and high treatment difficulty.
The traditional denitrogenation technology is an A/O technology, namely a nitrification/denitrification technology, and the basic principle of biological denitrification is as follows:
(1) and (4) performing ammoniation reaction. Under the action of ammoniating bacteria, organic nitrogen is decomposed and converted into ammoniacal nitrogen, and the process is called ammoniation process, and the ammoniation process is easy to carry out.
(2) And (4) carrying out nitration reaction. The nitration reaction is completed by aerobic autotrophic microorganisms, and NH is added by using inorganic carbon as a carbon source in an aerobic state4 +To NO2 -Then reoxidized to NO3 -The process of (1). The nitration process can be divided into two stages. The first stage is to convert ammonia nitrogen into NO by nitrosobacteria2 -In the second stage, nitrifying bacteria convert nitrite to Nitrate (NO)3 -). The necessary conditions for this reaction are a high dissolved oxygen, DO>2mg/L, which requires the concentration of organic matter in the mixed liquor to be at a low level.
(3) And (4) carrying out denitrification reaction. The denitrification reaction is that nitrite nitrogen and nitrate nitrogen are reduced into gaseous nitrogen (N) by denitrifying bacteria under the anoxic state2) The process of (1). Denitrifying bacteria are heterotrophic microorganisms, and are mostly facultative bacteria, and in an anoxic state, oxygen in nitrate is used as an electron acceptor, and organic matter (BOD component in sewage) is used as an electron donor, so that energy is supplied and the denitrifying bacteria are stably oxidized. The necessary condition for this reaction is that the concentration of biodegradable organic matter in the mixed liquor is at a high level.
For the reactive printing wastewater, most of organic matters are difficult to biodegrade, and the traditional A/O method cannot realize effective denitrification. The anaerobic ammonia oxidation process has been developed rapidly since the 90 s of the 20 th century, wherein the anaerobic ammonia oxidation means that microorganisms directly react with NH under anaerobic conditions, i.e. under anaerobic or anoxic conditions4 +As electron donors, with NO2 -As an electron acceptor, reacting NH4 +And NO2 -Is converted into N2The biological oxidation process of (1). In this process, NH4 +Without the participation of molecular oxygen, and NO2 -The reduction of (2) does not need organic matters to participate. The process has good effect on removing nitrogen from anaerobic nitrification wastewaterThe application prospect can be well applied to printing wastewater high ammonia nitrogen wastewater, the problem that the traditional A/O process cannot effectively denitrify is avoided, backflow and aeration are not needed, and a good economic effect is achieved.
The membrane separation technology is one of the most widely applied processes in the field of water treatment at present. Due to the characteristics of high efficiency and easy operation, the membrane separation technology becomes one of the direct and effective measures for relieving the water resource crisis, especially the water quality pollution. The engineering application of membrane separation in the field of water treatment, along with the increase of international water resource treatment demand and the deep research of related scientific research personnel, the membrane technologies have the advantages of compact structure, convenience in installation, high separation efficiency and the like. A large amount of waste water with high COD concentration and poor biodegradability in printing waste water is difficult to completely treat by a traditional biological method. Effluent of printing pretreatment wastewater and effluent of printing wastewater treatment are concentrated and enter a membrane treatment recycling system for recycling.
Disclosure of Invention
The invention aims to solve the technical problem of providing a high-nitrogen printing wastewater treatment and recycling system and a using method thereof, wherein pretreatment wastewater, printing wastewater and rinsing wastewater are respectively collected according to different wastewater components and concentrations and respectively enter a 1-3 subsystem for treatment, and generated sludge enters a 4# subsystem for reduction treatment. The method has the advantages of high system integration and accurate control, and can effectively solve the problem of difficult denitrification of the printing wastewater.
The invention discloses a high-nitrogen printing wastewater treatment and recycling system, which comprises 4 subsystems:
(1)1# subsystem: the high-concentration organic wastewater treatment system at the pre-printing treatment section comprises an adjusting tank 1, a sedimentation tank, a hydrolysis acidification tank and an SBR reaction tank;
(2)2# subsystem: the high-nitrogen wastewater treatment system for the printing section comprises an adjusting tank 2, a UASB reaction tank, a SHARON reaction tank and an ANAMMOX reaction tank;
(3)3# subsystem: the membrane advanced treatment and recycling system comprises a membrane bioreactor MBR, an ultrafiltration membrane UF system and a reverse osmosis RO system;
(4)4# subsystem: the sludge reduction treatment system comprises an anaerobic sludge digestion tank, a sludge concentration tank, a sludge dewatering tank and a sludge cake outward transport.
The invention discloses a use method of a high-nitrogen printing wastewater treatment and recycling system, which comprises the following steps:
(1) collecting wastewater of a pre-printing treatment section, and feeding the wastewater into an adjusting tank 1 of a No. 1 subsystem; the effluent enters a sedimentation tank and is added with acid and coagulant for physicochemical treatment; the effluent enters a hydrolytic acidification tank for biodegradation treatment; the effluent enters an SBR reaction tank for aerobic biochemical treatment; the COD concentration of the effluent is 10000-20000 mg/L;
(2) collecting waste water of a printing section, and feeding the waste water into a regulating tank 2 of a 2# subsystem; the effluent enters a UASB reaction tank for anaerobic treatment, and organic nitrogen is converted into ammonia nitrogen NH4-N; outlet water NH4The concentration of-N is 300-500 mg/L, the concentration of COD is 200-300 mg/L, and the wastewater enters a SHARON reaction tank for biological denitrification treatment to enable NH4Nitration of the-N moiety to NO2-N; outlet water NH4The concentration of-N is 150-250 mg/L, NO2The N concentration is 150-250 mg/L, the COD concentration is 50-100 mg/L, and the sewage enters an ANAMMOX reaction tank for anaerobic ammonia oxidation denitrification treatment; the TN concentration of the effluent is less than 20 mg/L;
(3) collecting waste water of a printing and rinsing section, and allowing the waste water to enter a UF system of a 3# subsystem; collecting the effluent of the SBR reaction tank in the step (1) and the effluent of the ANAMMOX reaction tank in the step (2) which enter the MBR of a 3# subsystem together for concentration, wherein the COD concentration of the effluent is 500-800 mg/L, and entering a UF system; further concentrating the wastewater and the wastewater at the printing and rinsing section, wherein the water yield is 95-98%, the COD concentration of the discharged water is 90-110 mg/L, further treating the wastewater in an RO system, the water yield is 70-80%, obtaining concentrated water and purified water, discharging the concentrated water or treating the concentrated water in a No. 1 subsystem, and recycling the purified water for production;
(4) and (2) a sedimentation tank, a hydrolysis acidification tank and an SBR reaction tank of the subsystem 1 in the step (1), a UASB reaction tank, a SHARON reaction tank and an ANAMMOX reaction tank of the subsystem 2 in the step (2), and sludge generated in the MBR of the subsystem 3 in the step (3) all enter an anaerobic sludge digestion tank of the subsystem 4 to be subjected to sludge reduction treatment, and sludge is concentrated and dehydrated to obtain sludge cakes for outward transportation.
And (2) the hydraulic retention time of the regulating reservoir 1 of the subsystem 1 in the step (1) is 7-9 h.
And (2) the hydrolysis acidification pool of the subsystem 1 in the step (1) is in a mechanical stirring type or hydraulic pulse type, and the hydraulic retention time is 36-48 h, so that biodegradable macromolecular organic matters are converted into micromolecular organic matters.
And (2) the hydraulic retention time of the SBR reaction tank of the subsystem 1 in the step (1) is 18-24 h.
The treatment process of the subsystem 1 in the step (1) mainly adopts a biological treatment process of materialization, hydrolytic acidification and aerobic treatment, so that organic matters which are difficult to degrade PVA slurry and easy to biodegrade are removed by a biological method, and the organic load in the subsequent advanced treatment process and the recycling process is reduced.
And (3) the hydraulic retention time of the regulating reservoir 2 of the subsystem 2 in the step (2) is 7-9 h.
And (3) the hydraulic retention time of the UASB reaction tank of the subsystem 2 in the step (2) is 12-24 h.
And (3) intermittently aerating the SHARON reaction tank of the subsystem 2 in the step (2), wherein the dissolved oxygen is 1.0-1.5 mg/L, the temperature is 28-32 ℃, the pH value is 7.5-8.3, and the hydraulic retention time is 16-24 h.
And (3) adopting a nitrogen collection circulating system in the ANAMMOX reaction tank of the subsystem 2 in the step (2), stirring nitrogen airflow inside the ANAMMOX reaction tank, removing oxygen to enable dissolved oxygen to be 0, and enabling hydraulic retention time to be 3-6 h.
And (3) adopting a hollow fiber microfiltration membrane as the MBR of the subsystem 3 in the step (3), wherein the hydraulic retention time is 12-24 h, and macromolecular organic matters and residual colloid particles such as PVA can be intercepted, so that the effluent quality of the MBR meets the influent quality requirement of an ultrafiltration membrane, and the membrane pollution of the ultrafiltration membrane and the RO membrane is reduced.
The UF system of the subsystem 3# in the step (3) adopts a hollow fiber ultrafiltration membrane or a tubular ultrafiltration membrane.
And (4) discharging the concentrated water in the step (3) to a downstream centralized sewage treatment plant.
And (4) the hydraulic retention time of the anaerobic sludge digestion tank of the subsystem 4 in the step (4) is 36-72 h.
The invention combines different water quality and water quantity of each working section of the printing process to carry out quality-based treatment and reuse: the COD concentration of the wastewater in the pretreatment section is high, the biodegradability is poor, and the water quantity is small; the total nitrogen concentration of the waste water in the printing stage is high, the chroma is high, and the carbon-nitrogen ratio is low; the concentration of the rinsing wastewater is low, the water quantity is large, and the problems of difficult denitrification, high cost and the like in the printing wastewater treatment process are solved.
Advantageous effects
(1) The 4 subsystems of the wastewater treatment and recycling system are ingenious in design, simple to operate and precise in control, and wastewater before printing and printing wastewater are subjected to shunting treatment; meanwhile, the membrane advanced treatment is utilized to realize the reuse of reclaimed water and reduce the operating cost; the finally obtained purified water can meet the water quality requirement of any process water in production.
(2) The printing wastewater treatment system adopts completely autotrophic anammox denitrification, the process does not need a large amount of aeration, the oxygen supply energy consumption is greatly reduced, the energy is saved, the denitrification is not needed to be solved by an external carbon source, the operation cost is reduced, and the system is suitable for the industrial sewage treatment of enterprises mainly based on active printing.
(3) The short-cut nitrification-anaerobic ammonia oxidation technology used by the invention can save about 40% of gas supply amount by controlling nitrification in a nitrosation stage, save power consumption, shorten hydraulic retention time, and reduce the volume of a reactor and the floor area of a traditional denitrification reactor. Meanwhile, the problem that an additional carbon source is needed in the denitrification process of the traditional denitrification process is solved, the sedimentation performance is good, the biological concentration is high, and the sludge bulking is avoided.
(4) The printing treatment wastewater basically has no sludge output, the sludge output of the whole system is less, and the sludge treatment cost is low.
Drawings
FIG. 1 shows a process of the high-nitrogen printing wastewater treatment and recycling system of the invention.
Detailed Description
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
Example 1
The natural yield of cotton yarn produced annually by a certain textile Limited liability company is 6500 tons, the annual knitted grey fabric is 1000 tons, and the annual knitted fabric is 450 thousands, so that the method is a textile enterprise integrating cotton spinning, knitting, printing and dyeing and clothing making. The dyeing and finishing wastewater of the enterprise is divided into desizing wastewater and wastewater generated in the printing process, and the amount of the desizing wastewater is 1600-2000 m3D, the amount of printing waste water is 800-1000 m3D, desizing wastewater CODCrThe concentration is 20000-30000 mg/L, and the COD isCr/BOD<0.3, belong to difficult biodegradable waste water, the printing waste water nitrogen content reaches 300 ~ 500mg/L, and COD concentration is also 2000 ~ 3000mg/L, and not only total nitrogen concentration is high, and carbon-nitrogen ratio imbalance is more serious moreover, and the processing degree of difficulty is big. In order to achieve the standard emission and reduce the operation cost, the company determines to adopt the high-nitrogen printing wastewater treatment and recycling system integrated process to treat and recycle the high-nitrogen printing wastewater which is difficult to treat.
(1) Collecting wastewater of a pre-printing treatment section, and allowing the wastewater to enter an adjusting tank 1 of a No. 1 subsystem, wherein the hydraulic retention time is 8 h; the effluent enters a sedimentation tank and is added with acid and coagulant for physicochemical treatment; the effluent enters a hydrolytic acidification tank for biodegradation treatment, and a mechanical stirring type is adopted, the hydraulic retention time is 40 hours, so that biodegradable macromolecular organic matters are converted into micromolecular organic matters; the effluent enters an SBR reaction tank for aerobic biochemical treatment, and the hydraulic retention time is 20 hours; the COD concentration of the effluent is 10000-20000 mg/L.
(2) Collecting waste water of a printing section, and allowing the waste water to enter an adjusting tank 2 of a 2# subsystem, wherein the hydraulic retention time is 8 h; the effluent enters a UASB reaction tank for anaerobic treatment, the hydraulic retention time is 20h, and organic nitrogen is converted into ammonia nitrogen NH4-N; outlet water NH4The concentration of-N is 300-500 mg/L, the concentration of COD is 200-300 mg/L, the mixture enters a SHARON reaction tank for biological denitrification treatment, intermittent aeration is adopted, the dissolved oxygen is 1.0-1.5 mg/L, the temperature is 30 ℃, the pH is 7.5-8.3, and the hydraulic retention time is 20h to enable NH to be kept4Nitration of the-N moiety to NO2-N; outlet water NH4-N concentration of 150 to 250mg/L，NO2The N concentration is 150-250 mg/L, the COD concentration is 50-100 mg/L, the obtained product enters an ANAMMOX reaction tank for anaerobic ammonia oxidation denitrification treatment, a nitrogen collection circulation system is adopted, nitrogen airflow stirring is carried out inside the ANAMMOX reaction tank, oxygen is removed to enable dissolved oxygen to be 0, and the hydraulic retention time is 5 hours; the TN concentration of the effluent is less than 20 mg/L.
(3) Collecting waste water of a printing and rinsing section, and allowing the waste water to enter a UF system of a 3# subsystem; collecting the effluent of the SBR reaction tank in the step (1) and the effluent of the ANAMMOX reaction tank in the step (2) to enter an MBR of a 3# subsystem together for concentration, adopting a hollow fiber microfiltration membrane, enabling the hydraulic retention time to be 20 hours, enabling the COD concentration of the effluent to be 500-800 mg/L, recycling the non-degradable desizing auxiliary agent PVA from the high-concentration macromolecular PVA after concentration, and then enabling the high-concentration PVA to enter an UF system; and further concentrating the wastewater together with the wastewater at the printing and rinsing section, adopting a hollow fiber ultrafiltration membrane, wherein the water yield is 95-98%, the COD concentration of the effluent is 90-110 mg/L, further treating the effluent in an RO system, the water yield is 70-80%, obtaining concentrated water and purified water, discharging the concentrated water or treating the concentrated water in a subsystem 1, and the purified water meets the requirement of recycled water quality and can be recycled for the production of a printing process.
(4) And (2) completely feeding all sludge generated in the sedimentation tank, the hydrolysis acidification tank and the SBR reaction tank of the subsystem 1 in the step (1), the UASB reaction tank, the SHARON reaction tank and the ANAMMOX reaction tank of the subsystem 2 in the step (2), and sludge generated in the MBR of the subsystem 3 in the step (3) into an anaerobic sludge digestion tank of the subsystem 4, performing sludge reduction treatment, performing hydraulic retention for 72h, and then performing sludge concentration and dehydration to obtain sludge cakes for outward transportation.
Example 2
A certain textile company is a large domestic knitting and printing enterprise, integrates knitting, printing and dyeing into a whole, and has the water discharge of 10000-12000 m3The discharged wastewater contains a large amount of residual dye, slurry, surfactant, alkaline agent and other complex components, has the characteristics of large chromaticity, high organic matter concentration, strong alkalinity, large water quality and water quantity change and the like, and is not ideal in removal effect by adopting common physical, chemical and biological methods. The amount of desizing wastewater of the company is 6000 to 8000m3The printing wastewater amount is 2000-4000 m3D, desizing wastewater CODCrThe concentration is 20000-30000 mg/L, and the COD isCr/BOD<0.3 belongs to the waste water difficult to biodegrade, the nitrogen content of the printing waste water reaches 300-500 mg/L, the COD concentration is 2000-3000 mg/L, the total nitrogen concentration is high, the carbon-nitrogen ratio is seriously disordered, and the treatment difficulty is high. In order to achieve the standard emission and reduce the operation cost, the company determines to adopt the high-nitrogen printing wastewater treatment and recycling system integrated process to treat and recycle the high-nitrogen printing wastewater which is difficult to treat.
(1) Collecting wastewater of a pre-printing treatment section, and allowing the wastewater to enter an adjusting tank 1 of a No. 1 subsystem, wherein the hydraulic retention time is 8 h; the effluent enters a sedimentation tank and is added with acid and coagulant for physicochemical treatment; the effluent enters a hydrolytic acidification tank for biodegradation treatment, and a mechanical stirring type is adopted, the hydraulic retention time is 40 hours, so that biodegradable macromolecular organic matters are converted into micromolecular organic matters; the effluent enters an SBR reaction tank for aerobic biochemical treatment, and the hydraulic retention time is 20 hours; the COD concentration of the effluent is 10000-20000 mg/L.
(2) Collecting waste water of a printing section, and allowing the waste water to enter an adjusting tank 2 of a 2# subsystem, wherein the hydraulic retention time is 8 h; the effluent enters a UASB reaction tank for anaerobic treatment, the hydraulic retention time is 20h, and organic nitrogen is converted into ammonia nitrogen NH4-N; outlet water NH4The concentration of-N is 300-500 mg/L, the concentration of COD is 200-300 mg/L, the mixture enters a SHARON reaction tank for biological denitrification treatment, intermittent aeration is adopted, the dissolved oxygen is 1.0-1.5 mg/L, the temperature is 30 ℃, the pH is 7.5-8.3, and the hydraulic retention time is 20h to enable NH to be kept4Nitration of the-N moiety to NO2-N; outlet water NH4The concentration of-N is 150-250 mg/L, NO2The N concentration is 150-250 mg/L, the COD concentration is 50-100 mg/L, the obtained product enters an ANAMMOX reaction tank for anaerobic ammonia oxidation denitrification treatment, a nitrogen collection circulation system is adopted, nitrogen airflow stirring is carried out inside the ANAMMOX reaction tank, oxygen is removed to enable dissolved oxygen to be 0, and the hydraulic retention time is 5 hours; the TN concentration of the effluent is less than 20 mg/L.
(3) Collecting waste water of a printing and rinsing section, and allowing the waste water to enter a UF system of a 3# subsystem; collecting the effluent of the SBR reaction tank in the step (1) and the effluent of the ANAMMOX reaction tank in the step (2) to enter an MBR of a 3# subsystem together for concentration, adopting a hollow fiber microfiltration membrane, enabling the hydraulic retention time to be 20 hours, enabling the COD concentration of the effluent to be 500-800 mg/L, recycling the non-degradable desizing auxiliary agent PVA from the high-concentration macromolecular PVA after concentration, and then enabling the high-concentration PVA to enter an UF system; and further concentrating the wastewater together with the wastewater at the printing and rinsing section, adopting a hollow fiber ultrafiltration membrane, wherein the water yield is 95-98%, the COD concentration of the effluent is 90-110 mg/L, further treating the effluent in an RO system, the water yield is 70-80%, obtaining concentrated water and purified water, discharging the concentrated water or treating the concentrated water in a subsystem 1, and the purified water meets the requirement of recycled water quality and can be recycled for the production of a printing process.
(4) And (2) completely feeding all sludge generated in the sedimentation tank, the hydrolysis acidification tank and the SBR reaction tank of the subsystem 1 in the step (1), the UASB reaction tank, the SHARON reaction tank and the ANAMMOX reaction tank of the subsystem 2 in the step (2), and sludge generated in the MBR of the subsystem 3 in the step (3) into an anaerobic sludge digestion tank of the subsystem 4, performing sludge reduction treatment, performing hydraulic retention for 72h, and then performing sludge concentration and dehydration to obtain sludge cakes for outward transportation.

Claims (6)

1. The utility model provides a high nitrogen printing waste water treatment retrieval and utilization device which characterized in that: includes 4 subsystems:
(1)1# subsystem: the high-concentration organic wastewater treatment system at the pre-printing treatment section comprises an adjusting tank 1, a sedimentation tank, a hydrolysis acidification tank and an SBR reaction tank;
(2)2# subsystem: the high-nitrogen wastewater treatment system for the printing section comprises an adjusting tank 2, a UASB reaction tank, a SHARON reaction tank and an ANAMMOX reaction tank;
(3)3# subsystem: the membrane advanced treatment and recycling system comprises a membrane bioreactor MBR, an ultrafiltration membrane UF system and a reverse osmosis RO system;
(4)4# subsystem: the sludge reduction treatment system comprises an anaerobic sludge digestion tank, a sludge concentration tank, a sludge dewatering tank and a sludge cake outward transport;
wherein (1) collecting wastewater of a pre-printing treatment section and feeding the wastewater into a regulating tank 1 of a 1# subsystem; the effluent enters a sedimentation tank and is added with acid and coagulant for physicochemical treatment; the effluent enters a hydrolytic acidification tank for biodegradation treatment; the effluent enters an SBR reaction tank for aerobic biochemical treatment; (2) collecting waste water of a printing section, and feeding the waste water into a regulating tank 2 of a 2# subsystem; the effluent enters a UASB reaction tank for anaerobic treatment to remove organic nitrogenConversion to ammonia nitrogen NH4-N; the effluent enters a SHARON reaction tank for biological denitrification treatment to ensure that NH is generated4Nitration of the-N moiety to NO2-N; the effluent enters an ANAMMOX reaction tank for anaerobic ammonia oxidation denitrification treatment; (3) collecting waste water of a printing and rinsing section, and allowing the waste water to enter a UF system of a 3# subsystem; collecting the effluent of the SBR reaction tank in the step (1) and the effluent of the ANAMMOX reaction tank in the step (2) which enter the MBR of the 3# subsystem together for concentration, and enabling the effluent to enter the UF system; further concentrating the wastewater and wastewater at the printing and rinsing section, further treating the effluent in an RO system to obtain concentrated water and purified water, discharging the concentrated water or treating the concentrated water in a 1# subsystem, and recycling the purified water for production; (4) and (2) a sedimentation tank, a hydrolysis acidification tank and an SBR reaction tank of the subsystem 1 in the step (1), a UASB reaction tank, a SHARON reaction tank and an ANAMMOX reaction tank of the subsystem 2 in the step (2), and sludge generated in the MBR of the subsystem 3 in the step (3) all enter an anaerobic sludge digestion tank of the subsystem 4 to be subjected to sludge reduction treatment, and sludge is concentrated and dehydrated to obtain sludge cakes for outward transportation.
2. The use method of the high-nitrogen printing wastewater treatment and recycling device in claim 1 comprises the following steps:
(1) collecting wastewater of a pre-printing treatment section, and feeding the wastewater into an adjusting tank 1 of a No. 1 subsystem; the effluent enters a sedimentation tank and is added with acid and coagulant for physicochemical treatment; the effluent enters a hydrolytic acidification tank for biodegradation treatment; the effluent enters an SBR reaction tank for aerobic biochemical treatment;
(2) collecting waste water of a printing section, and feeding the waste water into a regulating tank 2 of a 2# subsystem; the effluent enters a UASB reaction tank for anaerobic treatment, and organic nitrogen is converted into ammonia nitrogen NH4-N; the effluent enters a SHARON reaction tank for biological denitrification treatment to ensure that NH is generated4Nitration of the-N moiety to NO2-N; the effluent enters an ANAMMOX reaction tank for anaerobic ammonia oxidation denitrification treatment;
(3) collecting waste water of a printing and rinsing section, and allowing the waste water to enter a UF system of a 3# subsystem; collecting the effluent of the SBR reaction tank in the step (1) and the effluent of the ANAMMOX reaction tank in the step (2) which enter the MBR of the 3# subsystem together for concentration, and enabling the effluent to enter the UF system; further concentrating the wastewater and wastewater at the printing and rinsing section, further treating the effluent in an RO system to obtain concentrated water and purified water, discharging the concentrated water or treating the concentrated water in a 1# subsystem, and recycling the purified water for production;
(4) and (2) a sedimentation tank, a hydrolysis acidification tank and an SBR reaction tank of the subsystem 1 in the step (1), a UASB reaction tank, a SHARON reaction tank and an ANAMMOX reaction tank of the subsystem 2 in the step (2), and sludge generated in the MBR of the subsystem 3 in the step (3) all enter an anaerobic sludge digestion tank of the subsystem 4 to be subjected to sludge reduction treatment, and sludge is concentrated and dehydrated to obtain sludge cakes for outward transportation.
3. The use method of the high-nitrogen printing wastewater treatment and recycling device according to claim 2, characterized in that: the hydraulic retention time of the regulating reservoir 1 of the subsystem 1 in the step (1) is 7-9 h; the hydrolysis acidification tank is in a mechanical stirring type or hydraulic pulse type, and the hydraulic retention time is 36-48 h; the hydraulic retention time of the SBR reaction tank is 18-24 hours; the COD concentration of the effluent of the SBR reaction tank is 10000-20000 mg/L.
4. The use method of the high-nitrogen printing wastewater treatment and recycling device according to claim 2, characterized in that: the hydraulic retention time of the regulating reservoir 2 of the subsystem 2 in the step (2) is 7-9 h; the hydraulic retention time of the UASB reaction tank is 12-24 h; intermittent aeration is adopted in the SHARON reaction tank, the dissolved oxygen is 1.0-1.5 mg/L, the temperature is 28-32 ℃, the pH is = 7.5-8.3, and the hydraulic retention time is 16-24 h; the ANAMMOX reaction tank adopts a nitrogen collection circulating system, nitrogen airflow stirring is carried out inside the ANAMMOX reaction tank, oxygen is removed to enable dissolved oxygen to be 0, and the hydraulic retention time is 3-6 hours; the TN concentration of the effluent of the ANAMMOX reaction tank is less than 20 mg/L.
5. The use method of the high-nitrogen printing wastewater treatment and recycling device according to claim 2, characterized in that: the MBR of the subsystem 3 in the step (3) adopts a hollow fiber microfiltration membrane, and the hydraulic retention time is 12-24 h; the UF system adopts a hollow fiber ultrafiltration membrane or a tubular ultrafiltration membrane; the COD concentration of the effluent of the UF system is 90-110 mg/L, and the water yield is 95-98%; the water yield of the RO system is 70-80%.
6. The use method of the high-nitrogen printing wastewater treatment and recycling device according to claim 2, characterized in that: and (4) the hydraulic retention time of the anaerobic sludge digestion tank of the subsystem 4 in the step (4) is 36-72 h.
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