CN110950460B - Multi-function pretreatment and double-membrane filtration coupling strengthening treatment process and method - Google Patents
Multi-function pretreatment and double-membrane filtration coupling strengthening treatment process and method Download PDFInfo
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- 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
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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Abstract
The invention relates to a multi-functional pretreatment and double-membrane filtration coupling strengthening treatment process and a method, which are an integrated innovative technology aiming at improving the effluent standard of tail water of a sewage plant, and comprise two parts of multi-functional pretreatment and double-membrane treatment, wherein the specific technical route is a double-membrane process of ultramicro vortex flocculation, pulse type suction filtration, magnetic modified zeolite exchange adsorption, a nano-membrane ultrafiltration membrane (n-UF) and a nanofiltration membrane (NF); by controlling the flocculation quality of the ultramicro vortex and the action of an FK composite medicament, a vortex flow mechanism is created, and the flocculation effect and the pollutant degradation capability are promoted to be improved; by adopting a multi-component composite nano material nano ultrafiltration membrane (n-UF) and Nanofiltration (NF) double-membrane process with large flux and low energy consumption, various single technologies or combined technologies are selectively operated according to important degradation pollution indexes and effluent requirements in tail water of a sewage plant. The invention integrates flocculation, sedimentation and filtration, is particularly suitable for the project of full index upgrading and transformation of tail water of a sewage plant, and has the advantages of small occupied area, low investment and operation cost and the like.
Description
Technical Field
The invention belongs to the field of advanced sewage treatment and recycling, and particularly relates to a multi-functional pretreatment and double-membrane filtration coupling strengthening treatment process and a method, which are suitable for upgrading and reconstructing projects of town sewage treatment plants in severe cold regions by taking surface water environment quality standard (GB 3838-.
Background
The current discharge standard of pollutants for municipal wastewater treatment plants GB18918-2002 in China sets a third-level standard for the effluent quality of municipal wastewater treatment plants, wherein the first-level standard is divided into A standard and B standard. Along with the increasingly prominent pollution problem in China, the method also aims to improve the water resource bearing of river basinThe load carrying capacity is widely solicited by the national ministry of environmental protection, and aims to improve the sewage discharge standard, and the IV class requirement in the surface water environmental quality standard (GB3838-2002) is used as the discharge standard of the effluent water quality of the sewage plant to replace the current GB18918-2002 primary A standard in the pollutant discharge standard of urban sewage plant. As can be seen from comparison, the former is more strict in most main pollutant indexes than the latter, wherein the indexes which are very much concerned by the environmental protection field include Chemical Oxygen Demand (COD) and five-day Biochemical Oxygen Demand (BOD)5) Ammonia Nitrogen (NH) 3N), total phosphorus (calculated as P), total nitrogen (calculated as N), volatile phenol, petroleum, anionic surfactant and part of heavy metal indexes, and the specific differences are shown in Table 1.
TABLE 1 class I effluent A and surface water class IV Standard limits
The method provides higher requirements and standards for the process of the existing sewage treatment plant, needs to develop a sewage advanced treatment process based on the higher effluent standard, and improves the main pollutant discharge standard from the primary A (COD is less than or equal to 50mg/L and ammonia nitrogen is less than or equal to 5mg/L) of the original sewage treatment plant to IV-class ground water standards (COD is less than or equal to 30mg/L, ammonia nitrogen is less than or equal to 1.5mg/L and total phosphorus is less than or equal to 0.3 mg/L). At present, the conventional methods for upgrading the tail water of the sewage treatment plant comprise a physical and chemical treatment method, a biological treatment method and the like, and the specific physical and chemical methods comprise coagulating sedimentation, filtration, an adsorption method, a chemical oxidation-reduction method, an advanced oxidation method and the like; the biological treatment method can be divided into artificial wetland deep treatment technology, biological contact oxidation method, Biological Aerated Filter (BAF) and other biological technologies. The conventional technology is frequently selected by sewage treatment plants, is developed under the first-level A standard condition, has own treatment advantages and characteristics, and also shows various defects and shortcomings through running practice for many years, such as poor treatment effect of the coagulating sedimentation process on soluble organic matters and high medicament cost; the advanced oxidation has low utilization rate, can generate harmful byproducts and has high energy consumption; the biological treatment method has poor dephosphorization effect and high SS (suspended solid) of effluent; the artificial wetland has large floor area, poor effluent stability and the like, and at present, no integrated innovative process is available, which can realize trendy interest and avoid harm and completely meet the requirements of 24 indexes in IV class in the quality standard of surface water environment (GB 3838-2002).
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a multi-functional pretreatment and double-membrane filtration coupling strengthening treatment process and a method, which are an integrated innovative technology aiming at improving the effluent standard of tail water of a sewage plant.
The process route of the project is as follows:
the double-membrane process comprises ultramicro vortex flocculation, pulse type suction filtration, magnetic modified zeolite exchange adsorption, a nano membrane ultrafiltration membrane (n-UF) and a nanofiltration membrane (NF).
The technical scheme of the invention is as follows:
a multi-function pretreatment and double-membrane filtration coupling strengthening treatment process comprises a multi-function pretreatment part and a double-membrane treatment part, wherein the multi-function pretreatment part comprises ultramicro vortex flocculation, pulse type suction filtration and magnetic modified zeolite exchange adsorption, and the double-membrane treatment part comprises a nano ultrafiltration membrane (n-UF) and a nanofiltration membrane (NF);
the ultramicro vortex flocculation reactor is connected with a pulse type suction filtration reactor; the outlet of the pulse type suction filtration reactor is connected with the inlet of the magnetic modified zeolite exchange adsorption reactor; the outlet of the magnetic modified zeolite exchange adsorption reactor is connected with the inlet of a main part of a nanometer ultrafiltration membrane (n-UF); the outlet of the main membrane part of the nano ultrafiltration membrane (n-UF) is connected with the inlet of a nanofiltration membrane (NF);
the ultramicro vortex flocculation process is characterized in that a large number of micro cyclones are utilized, the ultramicro vortex flocculation quality is controlled, a large number of small-scale micro vortex structural fields are formed by fluid, a vortex flow mechanism is created in a reaction device under the action of an FK composite medicament, and the reasonable and effective collision of micro particles and a flocculating agent is promoted;
The mass intensity of the ultramicro vortex flocculation is controlled by the flow velocity gradient (G value), the reaction time (T) and the GT value. G is 20 to 700s-1, GT is 2.0 x 104～3.2×105，T＝2.4～22min；
The mass fraction ratio of the FK composite medicament added by the ultramicro vortex flocculation is as follows: 5-10% of polysilicic acid, 10-15% of poly aluminum chloride (or 8-12% of poly ferric chloride), 1-5% of polyethyleneimine, 5-8% of chitosan and 25% of hydroxyapatite;
the suction filtration process adopts a multi-medium composite filter layer, the filter layer is sequentially filled with cobblestones, medical stones, refined quartz sand and anthracite, the particle sizes of filter materials are respectively 30-180mm, 3-5mm, 0.5-1.5mm and 0.3-0.8mm, the total height H of the filter layer is 1.5-2.0m, the filling heights of various filter materials are determined by the size distribution of the particle sizes, and the heights of the cobblestones, the medical stones, the refined quartz sand and the anthracite filter materials are sequentially and respectively calculated according to the following formula:
H1＝K1(d1-d1min)/(d1max-d1min)H；
H2＝K2(d2-d2min)/(d2max-d2min)H；
H3＝K3(d3-d3min)/(d3max-d3min)H；
H4＝K4(d4-d4min)/(d4max-d4min)H；
wherein: k is an adjustment coefficient, d is the average particle size of the filter material, the minimum particle size of the dmin filter material and the maximum particle size of the dmax filter material, 1, 2, 3 and 4 are cobblestone, medical stone, refined quartz sand and anthracite respectively, and K is1、K2、K3、K4Respectively taking 5-10%, 20-30%, 30-50% and 20-40%, and
the suction filtration process is characterized in that the tail end of the filtration equipment is provided with a pulse type suction filtration device which consists of a vacuum pump, a water storage tank and a spiral suction filtration head which are connected in series into a whole through a closed pipeline, and the pulse type suction filtration is adopted, so that the vacuum degree is 3-12 multiplied by 10 -2Mpa; the single suction filtration time is 3-15s, the regeneration of the filtration layer is carried out by a gas-water positive flushing mode, and the gas flushing strength is about 13-14L/m2S, washing time 3-5 min; the water-washing (rinsing) strength is 5-6L/m2S, rinsing time is about 4-6 min, and total backflushing time is about 7-11 min;
the magnetically modified zeolite exchange adsorption process adopts magnetically modified zeolite adsorbent comprising high density magnetic molecular layer loaded on the surface of natural zeolite and FeCl3·6H2O is the only iron source, the synthesis temperature is controlled to be 450-500 ℃, and NH is used3·H2O as an etchant, 55-65% H2O2As a scavenging agent, hydrated aluminum-silicon gel is used as a stabilizing agent, calcium-aluminum-melilite-based blast furnace slag is used as an adhesive, 3-aminopropyltriethoxysilane is used for amination on the surface of magnetic particles to synthesize amino-functionalized Fe3O4Modified zeolite adsorbent (Fe)3O4@AmBpO2p·nH2O)。
The double-membrane process of the nano ultrafiltration membrane (n-UF) and the nanofiltration membrane (NF) adopts nano SiO2The membrane comprises a modified blending membrane, wherein the inner diameter of membrane filaments is 0.9mm, the outer diameter of the membrane filaments is 1.5mm, the air inlet pressure is 15-45 psi, the water inlet temperature is 0-40 ℃, the membrane permeation differential pressure (TMP) is 30psi, the maximum backwashing pressure is 130psi, the pH value tolerance range is 1.5-13, the flux range GFD is 30-60, and the backwashing flux range GFD is 170-250;
According to the nano ultrafiltration membrane (n-UF) and nanofiltration membrane (NF) double-membrane process, a nanofiltration membrane component adopts a 2+1 design form, concentrated water circulates to an ultramicro vortex flocculation/suction filtration unit, the nanofiltration membrane adopts a 4021-SR100 polyamide nanofiltration membrane, the pressure is 140psi, the water inlet temperature is 0-40 ℃, the operating transmembrane pressure difference (TMP) is 170psi, the pH value tolerance range is 1.5-13, and the flux range is 3-35 m3D, the salt rejection rate is 98%.
The process method for the multi-functional pretreatment and the double-membrane filtration coupling strengthening treatment can selectively operate each single technology or combined technology according to the key degradation pollution indexes and the effluent requirements in the tail water of the sewage plant, and the selection is according to the following table 2;
TABLE 2 key contaminants and matched process units and operating conditions
The invention has the beneficial effects that:
1. the uniformity of the field intensity in the small-scale vortex is good, and the average intensity is higher when the number of the small-scale vortices of the small-scale vortex internal field is larger;
2. the higher the field strength of the micro-vortex structure is, the higher the flocculation efficiency is, the higher the strength is, the floc can be sheared to reduce the flocculation effect, and particularly, the components of polysilicic acid and hydroxyapatite are added into the FK composite medicament, so that the main effect is to maintain the elastic strength of the micro-vortex floc and effectively resist the centrifugal inertia force and the shearing force generated by vortex.
3. The flocculation effect is strengthened by utilizing the complex flow state and the filter material particles in the filter layer in the micro-flocculation filtration flocculation process, so that the dirt intercepting capability of the filter material in the depth of the filter bed is exerted to a certain extent, the dosage is saved, and the sludge amount is reduced.
4. A small amount of flocculating agent is utilized to be rapidly mixed with pollutant particles in water to form tiny destabilizing particle flocculating constituents which directly enter a filter tank, the flocculating constituents are integrated with flocculation, sedimentation and filtration, the pollutant carrying capacity of the quartz sand filter material is fully exerted, the process is particularly suitable for removing phosphorus and reducing turbidity on occasions with small and compact tail water flocculating constituents of sewage plants, and the process has the advantages of small occupied area, low investment and operation cost and the like.
4. The medical stone filter material has strong capability of adsorbing heavy metal ions in water and has a certain inhibition effect on bacteria.
5. The modified zeolite is endowed with good capability of removing pollutants (such as ammonia nitrogen and phosphate) through modification, mainly depends on ion exchange and adsorption effects, but also has partial biodegradation effect.
6. A nano ultrafiltration membrane (n-UF) system with high flux and low energy consumption, and a nanofiltration membrane (NF) technology with a desalting function. A multi-element composite nano material is adopted to optimize and modify the traditional membrane material, the main function of ultrafiltration is to intercept macromolecular organic matters, colloid, protein, partial fungi and the like, a subsequent nanofiltration device is protected, substances intercepted by the ultrafiltration membrane are attached to the surface of the membrane, the flux of the membrane is reduced, and the attached dirt on the surface of the membrane can be effectively removed by adopting a backwashing measure and matching with a subsequent quick stroke sequence;
7. The membrane treatment system comprises two subsystems of UF and NF, and the UF system is mainly used for removing high-molecular organic matters, bacteria, particles and colloid of a flocculating agent in a water body. Meanwhile, high-quality water is provided for NF in the project, the flux of an NF membrane element is increased, the operation pressure is reduced, the possibility of dirt blockage of the NF membrane is reduced, the chemical cleaning interval is prolonged, the service life of the NF membrane is prolonged, and the operation cost is reduced.
Drawings
Fig. 1 is a schematic view of a multi-functional pretreatment and dual-membrane filtration coupling strengthening treatment process of the present invention, wherein 1: a tail water outlet of the sewage plant; 2: an ultramicro vortex flocculation reactor; 3: a pulse type suction filtration reactor; 4: a magnetically modified zeolite exchange adsorption reactor; 5: a nano ultrafiltration membrane (n-UF) reactor; 6: a nanofiltration membrane (NF) reactor; 7: a water outlet; 8: preprocessing combination with multiple functions; 9: a two-film treatment combination.
Fig. 2 is a schematic diagram of a design form of a nanofiltration membrane component 2+1 of the present invention, wherein 1: a water inlet valve; 2: a nanofiltration membrane module; 3: a water production valve; 4: a water producing port; 5: a nanofiltration concentrated water regulating valve; 6: discharging the nanofiltration concentrated water out of a water barrel; -a filtered water line; -a concentrate line.
Detailed Description
The invention will be described in further detail with reference to the following figures and specific examples, which are given by way of illustration and not by way of limitation.
FIG. 1 provides a coupling strengthening treatment process of multi-functional pretreatment and double-membrane filtration, which comprises two parts of multi-functional pretreatment 8 and double-membrane treatment 9, wherein the multi-functional pretreatment comprises ultramicro vortex flocculation 2, pulsed suction filtration 3 and magnetic modified zeolite exchange adsorption 4, and the double-membrane treatment comprises a nano ultrafiltration membrane (n-UF)5 and a nanofiltration membrane (NF) 6;
the ultramicro vortex flocculation reactor 2 is connected with a pulse type suction filtration reactor 3; the outlet of the pulse type suction filtration reactor 3 is connected with the inlet of the magnetic modified zeolite exchange adsorption reactor 4; the outlet of the magnetic modified zeolite exchange adsorption reactor 4 is connected with the inlet of a main membrane part of a nano ultrafiltration membrane (n-UF) 5; the outlet of the main membrane part of the nano ultrafiltration membrane (n-UF)5 is connected with the inlet of a nanofiltration membrane (NF) 6;
the ultramicro vortex flocculation process is characterized in that a large number of micro cyclones are utilized, the ultramicro vortex flocculation quality is controlled, a large number of small-scale micro vortex structural fields are formed by fluid, a vortex flow mechanism is created in a reaction device under the action of an FK composite medicament, and the reasonable and effective collision of micro particles and a flocculating agent is promoted;
The quality intensity of the ultramicro vortex flocculation is controlled by the flow rate gradient (G value), the reaction time (T) and the GT value. G is 20 to 700s-1, GT is 2.0 x 104～3.2×105，T＝2.4～22min；
The mass fraction ratio of the FK composite medicament added by the ultramicro vortex flocculation is as follows: 5-10% of polysilicic acid, 10-15% of poly aluminum chloride (or 8-12% of poly ferric chloride), 1-5% of polyethyleneimine, 5-8% of chitosan and 25% of hydroxyapatite, and the organic combination of the above agents can exceed the conventional flocculation effect, and also has the effects of heavy metal adsorption, crystal nucleus attachment, cross-linking polymerization and the like, so that the collision holding of small-scale micro-vortex particle flocs can be enhanced, the floc alum breakage can be avoided, and the floc form required by the suction filtration process can be maintained.
The suction filtration process adopts a multi-medium composite filter layer, the filter layer is sequentially filled with cobblestones, medical stones, refined quartz sand and anthracite, the particle sizes of filter materials are respectively 30-180mm, 3-5mm, 0.5-1.5mm and 0.3-0.8mm, the total height H of the filter layer is 1.5-2.0m, the filling heights of various filter materials are determined by the size distribution of the particle sizes, and the heights of the cobblestones, the medical stones, the refined quartz sand and the anthracite filter materials are sequentially and respectively calculated according to the following formula:
H1＝K1(d1-d1min)/(d1max-d1min)H；
H2＝K2(d2-d2min)/(d2max-d2min)H；
H3＝K3(d3-d3min)/(d3max-d3min)H；
H4＝K4(d4-d4min)/(d4max-d4min)H；
wherein: k is an adjustment coefficient, d is the average particle size of the filter material, the minimum particle size of the dmin filter material and the maximum particle size of the dmax filter material, 1, 2, 3 and 4 are cobblestone, medical stone, refined quartz sand and anthracite respectively, and K is 1、K2、K3、K4Respectively taking 5-10%, 20-30%, 30-50%, 20-40%, and K1+K2+K3+K4＝100％
The suction filtration process is characterized in that the tail end of the filtration equipment is provided with a pulse type suction filtration device which consists of a vacuum pump, a water storage tank and a spiral suction filtration head which are connected in series into a whole through a closed pipeline, and the pulse type suction filtration is adopted, so that the vacuum degree is 3-12 multiplied by 10-2Mpa; the single suction filtration time is 3-15s, the regeneration of the filtration layer is carried out by a gas-water positive flushing mode, and the gas flushing strength is about 13-14L/m2S, washing time 3-5 min; the water-washing (rinsing) strength is 5-6L/m2S, rinsing time is about 4-6 min, and total backflushing time is about 7-11 min;
the magnetically modified zeolite exchange adsorption process adopts magnetically modified zeolite adsorbent comprising high density magnetic molecular layer loaded on the surface of natural zeolite and FeCl3·6H2O is the only iron source, the synthesis temperature is controlled to be 450-500 ℃, and NH is used3·H2O as an etchant, 55-65% H2O2AsA scavenging agent, aqueous aluminum-silicon gel is used as a stabilizing agent, calcium-aluminum-melilite-based blast furnace slag is used as an adhesive, 3-aminopropyltriethoxysilane is used for amination on the surface of magnetic particles to synthesize amino-functionalized Fe3O4Modified zeolite adsorbent (Fe)3O4@AmBpO2p·nH2O)。
The double-membrane process of the nano ultrafiltration membrane (n-UF) and the nanofiltration membrane (NF) adopts nano SiO 2The membrane comprises a modified blending membrane, wherein the inner diameter of membrane filaments is 0.9mm, the outer diameter of the membrane filaments is 1.5mm, the air inlet pressure is 15-45 psi, the water inlet temperature is 0-40 ℃, the membrane permeation differential pressure (TMP) is 30psi, the maximum backwashing pressure is 30psi, the pH value tolerance range is 1.5-13, the flux range GFD is 30-60, and the backwashing flux range GFD is 170-250;
according to the nano ultrafiltration membrane (n-UF) and nanofiltration membrane (NF) double-membrane process, a nanofiltration membrane component adopts a 2+1 design form, concentrated water circulates to an ultramicro vortex flocculation/suction filtration unit, a nanofiltration membrane adopts a 4021-SR100 polyamide nanofiltration membrane, the pressure is 140psi, the water inlet temperature is 0-40 ℃, the operating transmembrane pressure difference (TMP) is 170psi, the pH value tolerance range is 1.5-13, and the flux range is 3-35 m3D, the salt rejection rate is 98%.
Examples
The method is characterized in that a first-level A of an urban sewage treatment plant is used as a water outlet standard, the current requirement is on upgrading and modification, the water outlet standard is upgraded to IV type in the 'surface water environment quality standard' (GB3838-2002), the water outlet of a sewage plant is subjected to a multi-function pretreatment and double-membrane filtration coupling strengthening treatment process through tail water of the sewage plant, the process comprises a multi-function pretreatment part 8 and a double-membrane treatment part 9, the multi-function pretreatment part comprises an ultramicro vortex flocculation part 2, a pulse type suction filtration part 3 and a magnetic modified zeolite exchange adsorption part 4, and the double-membrane treatment part comprises a nano ultrafiltration membrane (n-UF)5 and a nanofiltration membrane (NF) 6;
The ultramicro vortex flocculation reactor 2 is connected with a pulse type suction filtration reactor 3; the outlet of the pulse type suction filtration reactor 3 is connected with the inlet of the magnetic modified zeolite exchange adsorption reactor 4; the outlet of the magnetic modified zeolite exchange adsorption reactor 4 is connected with the inlet of a main membrane part of a nano ultrafiltration membrane (n-UF) 5; the outlet of the main membrane part of the nano ultrafiltration membrane (n-UF)5 is connected with the inlet of a nanofiltration membrane (NF) 6;
the ultramicro vortex flocculation process is characterized in that a large number of micro cyclones are utilized, the ultramicro vortex flocculation quality is controlled, a large number of small-scale micro vortex structural fields are formed by fluid, a vortex flow mechanism is created in a reaction device under the action of an FK composite medicament, and the reasonable and effective collision of micro particles and a flocculating agent is promoted;
the mass intensity of the ultramicro vortex flocculation is controlled by the flow velocity gradient (G value), the reaction time (T) and the GT value. G is 20-700 s-1, GT is 2.0 x 104～3.2×105，T＝2.4～22min；
The mass fraction ratio of the FK composite medicament added by the ultramicro vortex flocculation is as follows: 8% polysilicic acid, 12% poly phosphorus aluminum chloride (or 10% poly phosphorus ferric chloride), 4% polyethyleneimine, 6% chitosan, 25% hydroxyapatite, the organic combination of the above medicines can exceed the conventional flocculation effect, and the flocculant also has the effects of heavy metal adsorption, crystal nucleus attachment, cross-linking polymerization and the like, can enhance the collision holding type of the small-scale micro-vortex particle floc, avoids the floc alum floc from being broken, and maintains the floc form required by the suction filtration process.
The suction filtration process adopts a multi-medium composite filter layer, the filter layer is sequentially filled with cobblestones, medical stones, refined quartz sand and anthracite, the particle sizes of filter materials are respectively 30-180mm, 3-5mm, 0.5-1.5mm and 0.3-0.8mm, the total height H of the filter layer is 1.5m, the filling heights of various filter materials are determined by the particle size distribution, and the average particle sizes d of the cobblestones, the medical stones, the refined quartz sand and the anthracite filter materials are respectively 100mm, 4mm, 1.0mm and 0.5mm, and the heights of the filter layers are sequentially and respectively calculated according to the following formula:
H1＝K1(d1-d1min)/(d1max-d1min)H＝0.035m；
H2＝K2(d2-d2min)/(d2max-d2min)H＝0.1875m；
H3＝K3(d3-d3min)/(d3max-d3min)H＝1.0975m；
H4＝K4(d4-d4min)/(d4max-d4min)H＝0.18m；
wherein: k is an adjustment coefficient, d is the average grain diameter mm of the filter material, the minimum grain diameter mm of the dmin filter material and the maximum grain diameter mm of the dmax filter material, 1, 2, 3 and 4 are cobblestone, medical stone, refined quartz sand and anthracite respectively, and K is1、K2、K3、K4Respectively taking 5%, 25%, 40% and 30%, and
the suction filtration process comprises a pulse suction filtration device arranged at the end of a filtration device, a vacuum pump, a water storage tank and a spiral suction filtration head which are connected in series into a whole through a closed pipeline, and adopts pulse suction filtration with the vacuum degree of 6 multiplied by 10-2Mpa; the single suction filtration time is 3-15s, the regeneration of the filtration layer is carried out in a gas-water positive flushing mode, and the gas flushing strength is about 13L/m2S, wash time 3 min; the water washing (rinsing) strength is 5L/m2S, rinsing time is about 4min, and total backflushing time is about 7 min;
The magnetic modified zeolite exchange adsorption process adopts magnetic modified zeolite adsorbent, which is prepared by loading high-density magnetic molecular layer on the surface of natural zeolite and FeCl3·6H2O is the only iron source, the synthesis temperature is controlled to be 450-500 ℃, and NH is used3·H2O as an etchant, 55-65% H2O2As a scavenging agent, hydrous aluminum-silicon gel is used as a stabilizing agent, calcium-aluminum yellow feldspar based blast furnace slag is used as an adhesive, 3-aminopropyltriethoxysilane is used for amination on the surface of magnetic particles, and Fe with functionalized amino groups is synthesized3O4Modified zeolite adsorbent (Fe)3O4@AmBpO2p·nH2O)。
The nano ultrafiltration membrane (n-UF) and nanofiltration membrane (NF) double-membrane process adopts nano SiO2The modified blended membrane has membrane filament inner diameter of 0.9mm, membrane filament outer diameter of 1.5mm, air inlet pressure of 25psi, water inlet temperature of 22 deg.C, membrane permeation pressure difference (TMP) of 30psi, maximum backwash pressure of 130psi, pH tolerance range of 7, fluxThe range GFD is 40, and the backwashing flux range GFD is 200;
the nano ultrafiltration membrane (n-UF) and nanofiltration membrane (NF) double-membrane process is characterized in that a nanofiltration membrane component adopts a 2+1 design form, concentrated water circulates to an ultramicro vortex flocculation/suction filtration unit, the nanofiltration membrane adopts a 4021-SR100 polyamide nanofiltration membrane, the pressure is 140psi, the water inlet temperature is 22 ℃, the operating transmembrane pressure difference (TMP) is 170psi, the pH value tolerance range is 7, and the flux range is 10m 3And d, the salt rejection rate is 98%.
According to the multi-functional pretreatment and double-membrane filtration coupling strengthening treatment process method, according to the key degradation pollution indexes and effluent requirements in tail water of a sewage plant, a double-membrane process of ultramicro vortex flocculation/suction filtration, magnetic modified zeolite exchange adsorption, a nano-membrane ultrafiltration membrane (n-UF) and a nanofiltration membrane (NF) is selected, and the addition amount of FK agents is 45 ppm; the filtration speed of magnetic modified zeolite exchange adsorption is 10 m/h; n-UF chemical cleaning cycle 10 d; the recovery rate of NF concentrated water is 70 percent.
The detection data of the sewage treatment plant according to actual measurement are shown in the table 3.
TABLE 3 monitoring data of wastewater treatment plants
Claims (1)
1. A multi-function pretreatment and double-membrane filtration coupling strengthening treatment process is characterized in that the process scheme comprises two parts, namely, multi-function pretreatment and double-membrane treatment, the specific process route is a double-membrane process comprising ultramicro vortex flocculation, pulsed suction filtration, magnetic modified zeolite exchange adsorption, nanometer membrane ultrafiltration membrane n-UF and a nanofiltration membrane NF, the multi-function pretreatment part comprises ultramicro vortex flocculation, pulsed suction filtration and magnetic modified zeolite exchange adsorption, and the double-membrane treatment part comprises nanometer membrane ultrafiltration membrane n-UF and the nanofiltration membrane NF; the outlet of the pulse type suction filtration reactor is connected with the inlet of the magnetic modified zeolite exchange adsorption reactor; the outlet of the magnetic modified zeolite exchange adsorption reactor is connected with the inlet of a nano membrane ultrafiltration membrane n-UF membrane component; the outlet of the nano membrane ultrafiltration membrane n-UF membrane component is connected with the NF inlet of a nanofiltration membrane;
The quality intensity of the ultramicro vortex flocculation is controlled by a flow velocity gradient G value, a reaction time T and a GT value which is the product of the flow velocity gradient G value and the reaction time T, wherein G = 20-700 s-1，GT=2.0×104~3.2×105，T=2.4~22 min；
The pulse type suction filtration process adopts a multi-medium composite filter layer, the filter layer is sequentially filled with cobblestones, medical stones, refined quartz sand and anthracite, the particle sizes of filter materials are respectively 30-180mm, 3-5mm, 0.5-1.5mm and 0.3-0.8mm, the total height H of the filter layer is 1.5-2.0m, the filling heights of various filter materials are determined by the size distribution of the particle sizes, and the heights of the cobblestones, the medical stones, the refined quartz sand and the anthracite filter materials are sequentially and respectively calculated by the following formulas:
H1=K1(d1-d1min)/(d1max-d1min)H;
H2=K2(d2-d2min)/(d2max-d2min)H;
H3=K3(d3-d3min)/(d3max-d3min)H;
H4=K4(d4-d4min)/(d4max-d4min)H;
wherein: k is the adjustment coefficient, d is the average particle size of the filter material, dminMinimum particle size of filter material, dmaxThe maximum grain size of the filter material is 1, 2, 3 and 4, which are cobblestone, medical stone, refined quartz sand and anthracite, K1、K2、K3、K4Respectively taking 5-10%, 20-30%, 30-50% and 20-40%, and
the pulse type suction filtration process is characterized in that a pulse type suction filtration device is arranged at the tail end of the filtration equipment and consists of a vacuum pump, a water storage tank and a spiral type suction filtration headThe components are connected in series into a whole through a closed pipeline, pulse type suction filtration is adopted, and the vacuum degree is 3-12 multiplied by 10-2Mpa; the single suction filtration time is 3-15s, the regeneration of the filtration layer is carried out by a gas-water positive flushing mode, and the gas flushing strength is about 13-14L/m 2S, washing time 3-5 min; rinsing strength of 5-6L/m2S, rinsing time is about 4-6 min, and total backflushing time is about 7-11 min;
the magnetically modified zeolite exchange adsorption process adopts magnetically modified zeolite adsorbent comprising high density magnetic molecular layer loaded on the surface of natural zeolite and FeCl3·6H2O is the only iron source, the synthesis temperature is controlled to be 450-500 ℃, and NH is used3·H2O is used as an etching agent, and the mass concentration of H is 55-65%2O2As a scavenging agent, hydrated aluminum-silicon gel is used as a stabilizing agent, calcium-aluminum-melilite-based blast furnace slag is used as an adhesive, 3-aminopropyltriethoxysilane is used for amination on the surface of magnetic particles to synthesize amino-functionalized Fe3O4Modified zeolite adsorbent Fe3O4@AmBpO2p·nH2O；
The nano-membrane ultrafiltration membrane n-UF and nanofiltration membrane NF double-membrane process adopts nano SiO as ultrafiltration membrane2 The modified blend membrane has the membrane filament inner diameter of 0.9mm, the membrane filament outer diameter of 1.5 mm, the air inlet pressure of 15-45 psi, the water inlet temperature of 0-40 ℃, the membrane permeation differential pressure TMP of 30psi, the maximum backwashing pressure of 130 psi, the tolerance range of pH value of 1.5-13, the flux range GFD = 30-60, and the backwashing flux range GFD = 170-250;
according to the nano-membrane ultrafiltration membrane n-UF and nanofiltration membrane NF double-membrane process, a nanofiltration membrane component adopts a 2+1 design form, concentrated water circulates to an ultramicro vortex flocculation/suction filtration unit, a nanofiltration membrane adopts a 4021-SR100 polyamide nanofiltration membrane, the pressure is 140psi, the water inlet temperature is 0-40 ℃, the operating transmembrane pressure difference TMP is 170 psi, the pH value tolerance range is 1.5-13, and the flux range is 3-35 m 3And d, the salt rejection rate is 98%.
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