CN103755108A - Municipal wastewater purification treatment method - Google Patents
Municipal wastewater purification treatment method Download PDFInfo
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- CN103755108A CN103755108A CN201410058396.5A CN201410058396A CN103755108A CN 103755108 A CN103755108 A CN 103755108A CN 201410058396 A CN201410058396 A CN 201410058396A CN 103755108 A CN103755108 A CN 103755108A
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- 238000000746 purification Methods 0.000 title abstract description 5
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The invention discloses a municipal wastewater purification treatment method which comprises a pretreatment step, a bioreaction step, a filtration step, a sterilization step and an adsorption step which are carried out in sequence, wherein in the pretreatment step, gravel and large-sized floating objects can be removed and a stable water source is provided for subsequent treatment; in the bioreaction step, municipal wastewater is removed in low-carbon and high-efficiency manners, the treatment load is high, the treatment effect is good, organic and inorganic carbon sources do no need to be additionally added, and the oxygen consumption and the reflux quantity are low; in the filtration step, small particles and suspended matters in the wastewater are further removed; in the sterilization step, harmful organisms such as bacteria and viruses in the wastewater are killed; in the adsorption step, calcium magnesium ions, fluorine ions and other heavy metal ions in the wastewater can be efficiently removed. Purified product water from which pollutants are basically removed is stable in water quality, and the water quality is superior to the national standard A.
Description
Technical Field
The invention belongs to the field of urban sewage treatment and environmental protection, and particularly relates to a purification treatment method of urban domestic sewage.
Background
At present, water resources in China are seriously deficient, and the water treatment industry pays more and more attention to sewage generated in human production and life. How to save water and realize the efficient and safe recycling of water resources so as to relieve the increasingly tense water use pressure of cities becomes a serious problem facing the environmental protection world.
The proportion of underground water mined in Beijing and surrounding areas is up to 72 percent, which is far beyond the international warning line of 30 to 40 percent of water resource utilization rate. In order to comprehensively improve the sustainable development capability of cities, the national fifteen environment protection plan is definitely stipulated: by 2005, the centralized treatment rate of urban domestic sewage reached 45%. The government of Beijing City also puts forward the construction goal that the reclaimed water of Beijing City reaches 50% of the total amount of sewage treatment. Therefore, how to improve the utilization rate of the recycled reclaimed water and effectively apply the reclaimed water to landscape, greening, municipal miscellaneous use and industrial and agricultural irrigation water of rivers and lakes in cities is an urgent problem.
The standard-reaching discharge of sewage treatment is an important means for relieving the water environment crisis. The state promulgates the discharge standard GB18918-2002 of pollutants for municipal wastewater treatment plants, and requires that effluent reaches the first-level A standard, wherein COD is less than 50mg/L, BOD is less than 10mg/L, TN is less than 15mg/L, TP is less than 0.5mg/L, and the control on nutrient elements is particularly strict. The prior art adopted by sewage treatment plants in China is mostly based on the traditional nitrogen and phosphorus removal theory, has inherent defects and is difficult to realize the discharge of the first-grade A standard treatment.
In the prior art, some advanced urban sewage treatment processes have complex steps and serious energy consumption, stink is distributed around a sewage plant, and the removal effect of the sewage pollutants can obtain the requirement of national standards, but the requirements of people on sewage treatment by sense organs can not be met. Aiming at solving the technical problem, the invention provides a purification treatment method of urban domestic sewage aiming at the defects in the prior art, the method has high removal efficiency of pollutants, and the removal effect is superior to the requirements of national standards.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention aims to provide the method for purifying and treating the urban domestic sewage, which has the advantages of high pollutant removal efficiency, stable effluent quality and the like, and the removal effect is superior to the requirements of national first-grade A standard.
The technical scheme of the invention is as follows.
A method for purifying and treating urban domestic sewage is characterized by comprising a pretreatment step, a biological reaction step, a filtering step, a sterilization step and an adsorption step which are sequentially carried out; wherein,
the pretreatment step comprises: the sewage treatment system comprises a sewage reservoir, a sewage reservoir outlet pipeline, a sewage treatment system and a control system, wherein the sewage reservoir is connected with a water inlet of the sewage reservoir and a municipal sewage source pipeline, the sewage is temporarily stored in the sewage reservoir, the sewage reservoir outlet pipeline is connected with the pretreatment system, the pretreatment system comprises a grit chamber and a rough filtering tank, the sewage firstly enters the grit chamber to precipitate silt, the silt is discharged into a collection pit, the sewage passing through the grit chamber enters the rough filtering tank, and the rough filtering tank is provided with a rotary grid to collect suspended; sewage at a water outlet of the pretreatment system enters a biological reaction step through a lift pump;
the biological reaction step comprises: sequentially carrying out (A) an anaerobic-aerobic dephosphorization and decarbonization process, (B) a multi-stage complete mixed nitrosation process, (C) an upflow anaerobic ammonium oxidation biological filter denitrification process; in particular to a method for preparing a high-performance nano-silver alloy,
(A) anaerobic-aerobic dephosphorization and decarbonization process, controlling the organic load of inlet water to be 0.9-1kgCOD/m3D, the sludge concentration is 2.8-3g/L, the sludge age is 5d, the hydraulic retention time is 5-6h, the retention time ratio of the anaerobic zone to the aerobic zone is 1:3.5-3.8, the aerobic zone is divided into four dissolved oxygen gradients according to the volume ratio of 1:1:1:1, the four dissolved oxygen gradients are respectively 1.55-1.65, 0.75-0.85, 0.45-0.55 and 0.35-0.40mg/L, the sludge in the sedimentation tank flows back to the anaerobic zone, and the sludge reflux ratio is 25-55 percent; implementation ofThe total phosphorus removal rate is more than 93 percent, the COD removal rate is more than 88 percent, the total nitrogen removal rate is 20-22 percent, the ammonia nitrogen removal rate is 15-15.5 percent, the effluent of nitrite nitrogen and nitrate nitrogen is less than 0.45mg/L, and the concentration of suspended matters in the effluent is 15-18 mg/L;
(B) the effluent of anaerobic-aerobic phosphorus and carbon removal process enters the multi-stage fully mixed nitrosation process, and the total nitrogen load of the inlet water is controlled to be 0.4-0.5kgN/m3D, the sludge concentration is 2.5-2.6mg/L, the sludge age is 28-29d, the hydraulic retention time is 2.8-3.0h, the reactor is divided into five dissolved oxygen gradients of 0.55-0.75, 0.15-0.25, 0.45-0.55, 0.16-0.20 and 0.1-0.15mg/L according to the volume ratio of 1:1:1:1, the sludge in the sedimentation tank flows back to the first dissolved oxygen gradient area, and the sludge reflux ratio is 25-30%; the ammonia nitrogen oxidation rate is 59-60%, the ratio of nitrite nitrogen to ammonia nitrogen in the effluent is 1.28-1.32, the nitrate nitrogen in the effluent is less than 3mg/L, the total nitrogen loss is 4-4.55mg/L, and the concentration of suspended matters in the effluent is 10-12 mg/L;
(C) the denitrification process of the upward flow anaerobic ammonium oxidation biological filter comprises the steps of feeding effluent of a multi-stage complete mixed nitrosation process into the upward flow anaerobic ammonium oxidation biological filter, adopting Raschig ring packing, controlling the grain diameter to be 9 mm, 7 mm and 5mm respectively according to the volume ratio of 1:1:1 from bottom to top, controlling the filling ratio to be 50 percent, and controlling the total nitrogen load of inlet water to be 0.9-1.8kgN/m3D, the hydraulic retention time is 0.3-0.5h, the cross-section filtration speed is 0.6-1.2m/h, and the height of the upward flow anaerobic ammonia oxidation biological filter is 0.8-4.8 m; the removal rate of total nitrogen is more than 90 percent, the total nitrogen of effluent is less than 8mg/L, ammonia nitrogen is less than 0.8mg/L, nitrite nitrogen is less than 1mg/L, nitrate nitrogen is less than 6mg/L, COD is less than 40mg/L, BOD is less than 9mg/L, TP is less than 0.3mg/L, and the concentration of effluent suspended matters is less than 5 mg/L;
the filtering step comprises the steps of introducing the sewage flowing out of the biological reaction step into a buffer tank, pressurizing the sewage by a booster pump, and entering a filtering treatment system, wherein a membrane used by the filtering treatment system is a polytetrafluoroethylene microporous filtering membrane, the pore size distribution of the membrane is 30-70 mu m, the porosity is 80-96%, the membrane thickness is 120-180 mu m, and the tensile strength is 300-330 MPa; the working pressure of the polytetrafluoroethylene microporous filtering membrane during filtration is 0.06-0.18MPa, and the water production flux is 100-m2·h）；
The sterilization step comprises the steps of introducing water produced in the filtration step into a sterilization pipeline through a pump, injecting sterilization liquid into the sterilization pipeline in a pulse mode, wherein the pulse frequency is 1-3 times/min, the sterilization liquid is a mixed aqueous solution of potassium hydroxide and hydrogen peroxide, the mass ratio of the potassium hydroxide to the hydrogen peroxide is 1:3, and the concentration of the hydrogen peroxide in the sterilization liquid is 0.8-0.9 g/L;
the adsorption step comprises the steps of conveying the water produced in the sterilization step to an adsorption tower water inlet positioned at the bottom of the adsorption tower, and sequentially filling a non-woven fabric layer, a quartz sand layer and a modified zeolite layer from bottom to top in the adsorption tower, wherein the thickness of the non-woven fabric layer is between 2 and 20mm, and the thickness ratio of the quartz sand layer to the modified zeolite layer is 1: 0.5-0.8, the water flows out from the water outlet of the adsorption tower positioned at the top of the adsorption tower and is conveyed to the water storage tank by a pump, thus obtaining purified product water.
In the art, there are two types of methods for modifying zeolites: one is the modification of zeolite framework elements and the other is the modification of non-framework elements. The modification of framework elements includes acid-base treatment modification and the like, and the modification of non-framework elements includes ion exchange modification, in-zeolite coordination chemistry, surfactant modification and the like. In the present invention, the modified zeolite is a zeolite modified by a modification method which is conventional in the art, for example, a zeolite modified by a sodium chloride solution in the prior art, and may be a zeolite modified by a specific modification method. In general, the zeolite modified by the conventional modification method is slightly weaker in adsorption effect than the zeolite modified by the specific modification method, but the technical effect of the present invention can still be achieved.
Preferably, the modified zeolite is modified mordenite, and the modification step is as follows: uniformly mixing mordenite, kaolin, silica-magnesia gel, sesbania powder and phosphoric acid according to the weight ratio of 10:30:30:20:20, and then adding water to prepare slurry with the solid content of 50-55%; spray-drying the slurry to obtain powdery particles, then roasting the powdery particles in a muffle furnace at the temperature of 500-700 ℃ for 3-5h, and then cooling to room temperature to obtain the modified zeolite, wherein the molar concentration of the phosphoric acid is 0.9-1.3mol/L, and preferably 1.0 mol/L.
The mordenite is commercially available mordenite or mordenite available to those skilled in the art, and is preferably prepared by the following method:
mixing 30g of hexadecyl dimethyl ethyl ammonium bromide and 200g of deionized water, and heating in a constant-temperature water bath kettle at the temperature of 58 ℃ for 4 hours in a water bath manner to obtain a template solution; uniformly stirring 50g of diaspore and 1L of sodium hydroxide solution with the concentration of 2mol/L, putting the mixture into a hydrothermal reaction kettle, keeping the temperature of the hydrothermal reaction kettle at 230 ℃ for 1h, taking the hydrothermal reaction kettle out, adding the diaspore subjected to alkali treatment into 1.5L of hydrochloric acid with the concentration of 2mol/L, stirring the mixture for reaction for 4h, and filtering the reaction solution to obtain filtrate to obtain aluminum source liquid; uniformly mixing 60g of quartz with 1L of 5mol/L sodium hydroxide solution, placing the mixture in a hydrothermal kettle, preserving the temperature of the hydrothermal kettle at 260 ℃ for 12 hours, cooling, filtering, and taking filtrate to obtain silicon source liquid; mixing 80ml of aluminum source liquid and 100ml of silicon source liquid to obtain a silicon-aluminum mixed solution, adding a sodium hydroxide solution to adjust the pH value to 11.8, then dropwise adding 10ml of template liquid, stirring for 3 hours, transferring the mixture to a stainless steel static crystallization kettle with a polytetrafluoroethylene lining, placing the stainless steel static crystallization kettle in a 160 ℃ oven for crystallization for 5 days, carrying out suction filtration, washing with deionized water, drying, roasting at 580 ℃ for 6 hours, and naturally cooling to obtain the mordenite.
The invention discovers that the mordenite has a good effect on the aspect of adsorbing metal ions in sewage due to the specific structure of the mordenite, and pollutants in water are further reduced after the adsorption treatment of the modified mordenite.
In the invention, before the anaerobic-aerobic dephosphorization and decarbonization process and before the multi-stage complete mixed nitrosation process, tap water or purified product water is added to respectively regulate and control the organic load and the total nitrogen load of the sewage, but under the general condition, when the sewage source is stable, additional water source regulation is not needed.
Compared with the prior art, the invention has the beneficial effects that: the pretreatment step can remove gravels and large-size floating objects (such as garbage bags, plastic parts and the like), so that a stable water source is provided for subsequent treatment, the pipeline blockage is avoided, and the conveying efficiency of the pump is improved; the biological reaction step realizes the low-carbon and high-efficiency removal of the urban domestic sewage, and has the advantages of high treatment load, good treatment effect, no need of additional organic and inorganic carbon sources, and low oxygen consumption and reflux; fine particles and suspended matters in the sewage are further removed in the filtering step; the sterilization step eliminates the sanitary harmful organisms such as bacteria, viruses (including part of the activated sludge in the previous process) and the like contained in the sewage; the adsorption step, especially the phosphorus modified zeolite, can efficiently remove calcium and magnesium ions, fluorine ions and other heavy metal ions in the sewage. The purified product water has basically removed pollutants, stable water quality and water quality superior to the national first-class A standard.
Drawings
FIG. 1 is a schematic flow chart of the present invention.
Detailed Description
The present invention will be described in further detail with reference to specific examples.
Example 1
A method for purifying and treating urban domestic sewage is characterized by comprising a pretreatment step, a biological reaction step, a filtering step, a sterilization step and an adsorption step which are sequentially carried out; wherein,
the pretreatment step comprises: the sewage treatment system comprises a sewage reservoir, a sewage reservoir outlet pipeline, a sewage treatment system and a control system, wherein the sewage reservoir is connected with a water inlet of the sewage reservoir and a municipal sewage source pipeline, the sewage is temporarily stored in the sewage reservoir, the sewage reservoir outlet pipeline is connected with the pretreatment system, the pretreatment system comprises a grit chamber and a rough filtering tank, the sewage firstly enters the grit chamber to precipitate silt, the silt is discharged into a collection pit, the sewage passing through the grit chamber enters the rough filtering tank, and the rough filtering tank is provided with a rotary grid to collect suspended; sewage at a water outlet of the pretreatment system enters a biological reaction step through a lift pump;
the biological reaction step comprises: sequentially carrying out (A) an anaerobic-aerobic dephosphorization and decarbonization process, (B) a multi-stage complete mixed nitrosation process, (C) an upflow anaerobic ammonium oxidation biological filter denitrification process; in particular to a method for preparing a high-performance nano-silver alloy,
(A) anaerobic-aerobic dephosphorization and decarbonization process, controlling organic load of inlet water to be 1kgCOD/m3D, the sludge concentration is 3g/L, the sludge age is 5d, the hydraulic retention time is 6h, the retention time ratio of the anaerobic zone to the aerobic zone is 1:3.8, the aerobic zone is divided into four dissolved oxygen gradients of 1.65, 0.85, 0.55 and 0.40mg/L according to the volume ratio of 1:1:1:1, the sludge in the sedimentation tank flows back to the anaerobic zone, and the sludge reflux ratio is 55 percent; the total phosphorus removal rate is 94 percent, the COD removal rate is 89 percent, the total nitrogen removal rate is 22 percent, the ammonia nitrogen removal rate is 15.5 percent, the effluent of nitrite nitrogen and nitrate nitrogen is less than 0.44mg/L, and the concentration of suspended matters in the effluent is 18 mg/L; (B) the effluent of anaerobic-aerobic phosphorus and carbon removal process enters the multi-stage fully mixed nitrosation process, and the total nitrogen load of the inlet water is controlled to be 0.5kgN/m3D, the sludge concentration is 2.6mg/L, the sludge age is 29d, the hydraulic retention time is 3.0h, the reactor is divided into five dissolved oxygen gradients of 0.75, 0.25, 0.55, 0.20 and 0.15mg/L according to the volume ratio of 1:1:1:1, the sludge in the sedimentation tank flows back to the first dissolved oxygen gradient area, and the sludge reflux ratio is 30 percent; the ammonia nitrogen oxidation rate is 60%, the ratio of nitrite nitrogen to ammonia nitrogen in the effluent is 1.32, the nitrate nitrogen in the effluent is less than 3mg/L, the total nitrogen loss is 4.55mg/L, and the concentration of suspended matters in the effluent is 12 mg/L; (C) the denitrification process of the upward flow anaerobic ammonium oxidation biological filter comprises the steps of feeding effluent of a multi-stage complete mixed nitrosation process into the upward flow anaerobic ammonium oxidation biological filter, adopting Raschig ring packing, controlling the grain diameter to be 9 mm, 7 mm and 5mm respectively according to the volume ratio of 1:1:1 from bottom to top, controlling the filling ratio to be 50 percent, and controlling the total nitrogen load of inlet water to be 1.8kgN/m3D, the hydraulic retention time is 0.5h, the cross-sectional filtration speed is 1.2m/h, and the height of the upward flow anaerobic ammonium oxidation biological filter is 4.8 m; the total nitrogen removal rate is more than 90 percent, the total nitrogen of effluent is less than 8mg/L, and the ammonia nitrogen is less than 0.8mg/L, nitrite nitrogen is less than 1mg/L, nitrate nitrogen is less than 6mg/L, COD is less than 40mg/L, BOD is less than 9mg/L, TP is less than 0.3mg/L, and the concentration of suspended matters in effluent is less than 5 mg/L;
the filtering step comprises the steps of introducing the sewage flowing out of the biological reaction step into a buffer tank, pressurizing the sewage by a booster pump, and introducing the sewage into a filtering treatment system, wherein a membrane used by the filtering treatment system is a polytetrafluoroethylene microporous filtering membrane, the pore size of the membrane is distributed at 70 mu m, the porosity is 96%, the membrane thickness is 180 mu m, and the tensile strength is 330 MPa; the working pressure of the polytetrafluoroethylene micro-porous filtering membrane is 0.18MPa during filtering, and the produced water flux is 120L/(m)2·h）；
The sterilization step comprises the steps of introducing water produced in the filtering step into a sterilization pipeline through a pump, injecting sterilization liquid into the sterilization pipeline in a pulse mode, wherein the pulse frequency is 3 times/min, the sterilization liquid is a mixed aqueous solution of potassium hydroxide and hydrogen peroxide, the mass ratio of the potassium hydroxide to the hydrogen peroxide is 1:3, and the concentration of the hydrogen peroxide in the sterilization liquid is 0.9 g/L;
the adsorption step includes, carries the water of the output of the sterilization step to the adsorption tower water inlet that is located the bottom of the adsorption tower, and the adsorption tower is from up filled in proper order down has non-woven fabrics layer, quartz sand layer and modified zeolite layer, and wherein, the thickness on non-woven fabrics layer is 20mm, and the thickness ratio on quartz sand layer and modified zeolite layer is 1: 0.8, water flows out from a water outlet of the adsorption tower positioned at the top of the adsorption tower and is conveyed to a water storage tank through a pump, so that purified product water is obtained.
The modified zeolite in the embodiment is sodium chloride modified zeolite, and the preparation method comprises the steps of filling zeolite with the particle size of 0.5-1.0 mm into an organic glass column with the inner diameter of 14mm, and enabling a modifier NaCl solution to pass through a zeolite layer at the flow speed of 0.5m/h until ion exchange is complete.
Example 2
Preparation of phosphorus modified mordenite
(1) Preparation of mordenite:
mixing 30g of hexadecyl dimethyl ethyl ammonium bromide and 200g of deionized water, and heating in a constant-temperature water bath kettle at the temperature of 58 ℃ for 4 hours in a water bath manner to obtain a template solution;
uniformly stirring 50g of diaspore and 1L of sodium hydroxide solution with the concentration of 2mol/L, putting the mixture into a hydrothermal reaction kettle, keeping the temperature of the hydrothermal reaction kettle at 230 ℃ for 1h, taking the hydrothermal reaction kettle out, adding the diaspore subjected to alkali treatment into 1.5L of hydrochloric acid with the concentration of 2mol/L, stirring the mixture for reaction for 4h, and filtering the reaction solution to obtain filtrate to obtain aluminum source liquid;
uniformly mixing 60g of quartz with 1L of 5mol/L sodium hydroxide solution, placing the mixture in a hydrothermal kettle, preserving the temperature of the hydrothermal kettle at 260 ℃ for 12 hours, cooling, filtering, and taking filtrate to obtain silicon source liquid;
mixing 80ml of aluminum source liquid and 100ml of silicon source liquid to obtain a silicon-aluminum mixed solution, adding a sodium hydroxide solution to adjust the pH value to 11.8, then dropwise adding 10ml of template liquid, stirring for 3 hours, transferring the mixture to a stainless steel static crystallization kettle with a polytetrafluoroethylene lining, placing the stainless steel static crystallization kettle in a 160 ℃ oven for crystallization for 5 days, carrying out suction filtration, washing with deionized water, drying, roasting at 580 ℃ for 6 hours, and naturally cooling to obtain mordenite;
(2) modification of mordenite:
uniformly mixing mordenite, kaolin, silica-magnesia gel, sesbania powder and phosphoric acid according to the weight ratio of 10g to 30g to 20g, and then adding water to prepare slurry with the solid content of 55 percent; spray drying the slurry to obtain powdery particles, roasting the powdery particles in a muffle furnace at 700 ℃ for 5h, and cooling to room temperature to obtain the modified zeolite, wherein the molar concentration of phosphoric acid is 1.0 mol/L.
Example 3
A method for purifying and treating urban domestic sewage is characterized by comprising a pretreatment step, a biological reaction step, a filtering step, a sterilization step and an adsorption step which are sequentially carried out; wherein,
the pretreatment step comprises: the sewage treatment system comprises a sewage reservoir, a sewage reservoir outlet pipeline, a sewage treatment system and a control system, wherein the sewage reservoir is connected with a water inlet of the sewage reservoir and a municipal sewage source pipeline, the sewage is temporarily stored in the sewage reservoir, the sewage reservoir outlet pipeline is connected with the pretreatment system, the pretreatment system comprises a grit chamber and a rough filtering tank, the sewage firstly enters the grit chamber to precipitate silt, the silt is discharged into a collection pit, the sewage passing through the grit chamber enters the rough filtering tank, and the rough filtering tank is provided with a rotary grid to collect suspended; sewage at a water outlet of the pretreatment system enters a biological reaction step through a lift pump;
the biological reaction step comprises: sequentially carrying out (A) an anaerobic-aerobic dephosphorization and decarbonization process, (B) a multi-stage complete mixed nitrosation process, (C) an upflow anaerobic ammonium oxidation biological filter denitrification process; in particular to a method for preparing a high-performance nano-silver alloy,
(A) anaerobic-aerobic dephosphorization and decarbonization process, controlling the organic load of inlet water to be 0.9kgCOD/m3D, the sludge concentration is 2.8g/L, the sludge age is 5d, the hydraulic retention time is 5h, the retention time ratio of the anaerobic zone to the aerobic zone is 1:3.5, the aerobic zone is divided into four dissolved oxygen gradients of 1.55, 0.75, 0.45 and 0.35mg/L according to the volume ratio of 1:1:1, the sludge in the sedimentation tank flows back to the anaerobic zone, and the sludge reflux ratio is 25 percent; the total phosphorus removal rate is more than 93%, the COD removal rate is more than 88%, the total nitrogen removal rate is 20%, the ammonia nitrogen removal rate is 15%, the effluent of nitrite nitrogen and nitrate nitrogen is less than 0.45mg/L, and the concentration of suspended matters in the effluent is 15 mg/L;
(B) the effluent of anaerobic-aerobic phosphorus and carbon removal process enters the multi-stage fully mixed nitrosation process, and the total nitrogen load of the inlet water is controlled to be 0.4kgN/m3D, the sludge concentration is 2.5mg/L, the sludge age is 28d, the hydraulic retention time is 2.8h, the reactor is divided into five dissolved oxygen gradients of 0.55, 0.15, 0.45, 0.16 and 0.1mg/L according to the volume ratio of 1:1:1:1, the sludge in the sedimentation tank flows back to the first dissolved oxygen gradient area, and the sludge reflux ratio is 25 percent; the ammonia nitrogen oxidation rate is 59%, the ratio of nitrite nitrogen to ammonia nitrogen in the effluent is 1.28, the nitrate nitrogen in the effluent is less than 3mg/L, the total nitrogen loss is 4mg/L, and the concentration of suspended matters in the effluent is 10 mg/L;
(C) upward flow anaerobic ammonium oxidation biological filter denitrification process and multi-stage complete mixing type nitrite chemical industryThe effluent of the process enters an upward flow anaerobic ammonia oxidation biological filter, Raschig ring packing is adopted, the grain diameter is respectively 9 mm, 7 mm and 5mm according to the volume ratio of 1:1:1 from bottom to top, the packing ratio is 50 percent, and the total nitrogen load of the inlet water is controlled to be 0.9kgN/m3D, the hydraulic retention time is 0.3h, the cross-sectional filtration speed is 0.6m/h, and the height of the upward flow anaerobic ammonium oxidation biological filter is 0.8 m; the removal rate of total nitrogen is more than 90 percent, the total nitrogen of effluent is less than 8mg/L, ammonia nitrogen is less than 0.8mg/L, nitrite nitrogen is less than 1mg/L, nitrate nitrogen is less than 6mg/L, COD is less than 40mg/L, BOD is less than 9mg/L, TP is less than 0.3mg/L, and the concentration of effluent suspended matters is less than 5 mg/L;
the filtering step comprises the steps of introducing the sewage flowing out of the biological reaction step into a buffer tank, pressurizing the sewage by a booster pump, and introducing the sewage into a filtering treatment system, wherein a membrane used by the filtering treatment system is a polytetrafluoroethylene microporous filtering membrane, the pore size of the membrane is distributed at 30 micrometers, the porosity of the membrane is 80%, the thickness of the membrane is 120 micrometers, and the tensile strength of the membrane is 300 MPa; the working pressure of the polytetrafluoroethylene micro-porous filtering membrane is 0.06MPa during the filtration, and the water production flux is 100L/(m)2·h）；
The sterilization step comprises the steps of introducing water produced in the filtering step into a sterilization pipeline through a pump, injecting sterilization liquid into the sterilization pipeline in a pulse mode, wherein the pulse frequency is 1 time/min, the sterilization liquid is a mixed aqueous solution of potassium hydroxide and hydrogen peroxide, the mass ratio of the potassium hydroxide to the hydrogen peroxide is 1:3, and the concentration of the hydrogen peroxide in the sterilization liquid is 0.8 g/L;
the adsorption step includes that the water produced in the sterilization step is conveyed to the water inlet of the adsorption tower positioned at the bottom of the adsorption tower, the adsorption tower is sequentially filled with a non-woven fabric layer, a quartz sand layer and the modified zeolite layer prepared in the embodiment 2 from bottom to top, wherein the thickness of the non-woven fabric layer is 2mm, and the thickness ratio of the quartz sand layer to the modified zeolite layer is 1: 0.5, water flows out from a water outlet of the adsorption tower positioned at the top of the adsorption tower and is conveyed to a water storage tank through a pump, so that purified product water is obtained.
The product water obtained in the examples 1 and 3 is detected according to the pollutant discharge standard GB18918-2002 of urban sewage treatment plants, and the detection results are shown in Table 1, so that the water quality is superior to the national first-class A standard. Table 1 shows the results of the first class A standard and examples 1 and 3.
| Serial number | Item | First class Standard A Standard | Example 1 | Example 3 |
| 1 | Chemical Oxygen Demand (COD) in mg/L | 50 | 38 | 34 |
| 2 | Biochemical Oxygen Demand (BOD)5) Unit mg/L | 10 | 8 | 8 |
| 3 | Suspended Substance (SS) in mg/L | 10 | 4 | 3 |
| 4 | Animal and vegetable oil, unit mg/L | 1 | 0.8 | 0.8 |
| 5 | Petroleum, unit mg/L | 1 | 0.3 | 0.2 |
| 6 | Anionic surfactant in mg/L | 0.5 | 0.3 | 0.2 |
| 7 | Total Nitrogen (in N) in mg/L | 15 | 6.6 | 6.1 |
| 8 | Ammonia nitrogen (in terms of N) in mg/L | 5 | 0.7 | 0.5 |
| 9 | Total phosphorus (in terms of P), in mg/L | 0.5 | 0.26 | 0.18 |
| 10 | Chroma (dilution multiple) | 30 | 30 | 30 |
| 11 | pH | 6-9 | 7.2 | 7.1 |
| 12 | Number of fecal Enterobacter (one/L) | 103 | 10 | 10 |
Although the present invention has been described in detail with reference to the above embodiments, it is only a part of the embodiments of the present invention, not all of the embodiments, and other embodiments can be obtained without inventive step according to the embodiments, and the embodiments are within the scope of the present invention.
Claims (1)
1. A method for purifying and treating urban domestic sewage is characterized by comprising a pretreatment step, a biological reaction step, a filtering step, a sterilization step and an adsorption step which are sequentially carried out; wherein,
the pretreatment step comprises: the sewage treatment system comprises a sewage reservoir, a sewage reservoir outlet pipeline, a sewage treatment system and a control system, wherein the sewage reservoir is connected with a water inlet of the sewage reservoir and a municipal sewage source pipeline, the sewage is temporarily stored in the sewage reservoir, the sewage reservoir outlet pipeline is connected with the pretreatment system, the pretreatment system comprises a grit chamber and a rough filtering tank, the sewage firstly enters the grit chamber to precipitate silt, the silt is discharged into a collection pit, the sewage passing through the grit chamber enters the rough filtering tank, and the rough filtering tank is provided with a rotary grid to collect suspended; and sewage at the water outlet of the pretreatment system enters a biological reaction step through a lift pump.
The biological reaction step comprises: sequentially carrying out (A) an anaerobic-aerobic dephosphorization and decarbonization process, (B) a multi-stage complete mixed nitrosation process, (C) an upflow anaerobic ammonium oxidation biological filter denitrification process; in particular to a method for preparing a high-performance nano-silver alloy,
(A) anaerobic-aerobic dephosphorization and decarbonization process, controlling the organic load of inlet water to be 0.9-1kgCOD/m3D, the sludge concentration is 2.8-3g/L, the sludge age is 5d, the hydraulic retention time is 5-6h, the retention time ratio of the anaerobic zone to the aerobic zone is 1:3.5-3.8, the aerobic zone is divided into four dissolved oxygen gradients according to the volume ratio of 1:1:1:1, the four dissolved oxygen gradients are respectively 1.55-1.65, 0.75-0.85, 0.45-0.55 and 0.35-0.40mg/L, the sludge in the sedimentation tank flows back to the anaerobic zone, and the sludge reflux ratio is 25-55 percent; the total phosphorus removal rate is more than 93 percent, the COD removal rate is more than 88 percent, the total nitrogen removal rate is 20-22 percent, the ammonia nitrogen removal rate is 15-15.5 percent, the effluent of nitrite nitrogen and nitrate nitrogen is less than 0.45mg/L, and the concentration of suspended matters in the effluent is 15-18 mg/L;
(B) the effluent of anaerobic-aerobic phosphorus and carbon removal process enters the multi-stage fully mixed nitrosation process, and the total nitrogen load of the inlet water is controlled to be 0.4-0.5kgN/m3D, the sludge concentration is 2.5-2.6mg/L, the sludge age is 28-29d, the hydraulic retention time is 2.8-3.0h, the reactor is divided into five dissolved oxygen gradients of 0.55-0.75, 0.15-0.25, 0.45-0.55, 0.16-0.20 and 0.1-0.15mg/L according to the volume ratio of 1:1:1:1, the sludge in the sedimentation tank flows back to the first dissolved oxygen gradient area, and the sludge reflux ratio is 25-30%; the ammonia nitrogen oxidation rate is 59-60%, the ratio of nitrite nitrogen to ammonia nitrogen in the effluent is 1.28-1.32, the nitrate nitrogen in the effluent is less than 3mg/L, the total nitrogen loss is 4-4.55mg/L, and the concentration of suspended matters in the effluent is 10-12 mg/L;
(C) the denitrification process of the upward flow anaerobic ammonium oxidation biological filter comprises the steps of feeding effluent of a multi-stage complete mixed nitrosation process into the upward flow anaerobic ammonium oxidation biological filter, adopting Raschig ring packing, controlling the grain diameter to be 9 mm, 7 mm and 5mm respectively according to the volume ratio of 1:1:1 from bottom to top, controlling the filling ratio to be 50 percent, and controlling the total nitrogen load of inlet water to be 0.9-1.8kgN/m3D, the hydraulic retention time is 0.3-0.5h, the cross-section filtration speed is 0.6-1.2m/h, and the height of the upward flow anaerobic ammonia oxidation biological filter is 0.8-4.8 m; the removal rate of the total nitrogen is more than 90 percent, the total nitrogen of effluent is less than 8mg/L, the ammonia nitrogen is less than 0.8mg/L, the nitrite nitrogen is less than 1mg/L, the nitrate nitrogen is less than 6mg/L, the COD is less than 40mg/L, the BOD is less than 9mg/L, the TP is less than 0.3mg/L, and the concentration of suspended matters in the effluent is less than 5 mg/L.
The filtering step comprises the steps of introducing the sewage flowing out of the biological reaction step into a buffer tank, pressurizing the sewage by a booster pump, and entering a filtering treatment system, wherein a membrane used by the filtering treatment system is a polytetrafluoroethylene microporous filtering membrane, the pore size distribution of the membrane is 30-70 mu m, the porosity is 80-96%, the membrane thickness is 120-180 mu m, and the tensile strength is 300-330 MPa; the working pressure of the polytetrafluoroethylene microporous filtering membrane is 0.06-0.18MPa during the filtration, and the water production flux is 100-2·h）。
The sterilization step comprises the steps of introducing water produced in the filtering step into a sterilization pipeline through a pump, injecting sterilization liquid into the sterilization pipeline in a pulse mode, wherein the pulse frequency is 1-3 times/min, the sterilization liquid is a mixed aqueous solution of potassium hydroxide and hydrogen peroxide, the mass ratio of the potassium hydroxide to the hydrogen peroxide is 1:3, and the concentration of the hydrogen peroxide in the sterilization liquid is 0.8-0.9 g/L.
The adsorption step comprises the steps of conveying the water produced in the sterilization step to an adsorption tower water inlet positioned at the bottom of the adsorption tower, and sequentially filling a non-woven fabric layer, a quartz sand layer and a modified zeolite layer from bottom to top in the adsorption tower, wherein the thickness of the non-woven fabric layer is between 2 and 20mm, and the thickness ratio of the quartz sand layer to the modified zeolite layer is 1: 0.5-0.8, the water flows out from the water outlet of the adsorption tower positioned at the top of the adsorption tower and is conveyed to the water storage tank by a pump, thus obtaining purified product water.
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