CN108002654B - Suspension method polyvinyl chloride polymerization section wastewater treatment method - Google Patents
Suspension method polyvinyl chloride polymerization section wastewater treatment method Download PDFInfo
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
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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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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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
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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- C02F3/302—Nitrification and denitrification treatment
Abstract
The invention discloses a suspension method for treating waste water in a polyvinyl chloride polymerization section, which mainly comprises the following steps: (1) the PVC slurry stripping wastewater firstly enters a first regulating tank for homogeneous regulation and then enters a pre-oxidation section for treatment; (2) the PVC centrifugal mother liquor wastewater firstly enters a cooling tower for cooling and then enters a sedimentation tank; (3) and (3) the wastewater treated in the steps (1) and (2) sequentially enters a second regulating tank, a first-stage biochemical tank, a second-stage biochemical section, a coagulating sedimentation tank and an advanced treatment section, and the effluent after advanced treatment can be recycled. The process innovatively adopts a microbubble pre-oxidation-filler biofilm reactor-AFMABR-advanced treatment combined process, the pertinence of each unit treatment is strong, a favorable environment is provided for subsequent unit treatment, various characteristic pollutants can be efficiently removed at the same time, and the system has the advantages of high treatment efficiency, low energy consumption, small occupied area, strong impact resistance and the like.
Description
The application is a divisional application of an invention patent application with the application number of 201710123154.3, the application date of 2017, 3/3 and the name of 'a method and a device for treating wastewater in a polyvinyl chloride polymerization section by using a suspension method'.
Technical Field
The invention relates to the field of industrial wastewater treatment, in particular to a device and a method for treating wastewater in a polyvinyl chloride polymerization section by using a suspension method.
Background
The chlor-alkali industry in China is mainly focused on water-deficient areas in the northwest, the water consumption and the water discharge amount also sharply increase along with the increase of the yield of polyvinyl chloride (PVC), and if a proper water recycling process is not adopted, the water resource shortage form is aggravated, and the water consumption pressure of enterprises is increased.
The waste water produced in the suspension method polyvinyl chloride polymerization section mainly comprises wall-coating flushing water of a polymerization kettle, recovered VCM storage tank drainage and condensed water, compressor sealing water, slurry stripping tower top condensed water and PVC polymer resin slurry, and filtered mother liquor produced by the separation of a centrifugal filter after the stripping. The organic pollutants in the wastewater come from chemicals such as an initiator, a dispersing agent and a small amount of a wall coating agent added in the polymerization reaction, and a small amount of raw material Vinyl Chloride (VCM), polymerized isomer products and oligomers. The inorganic contaminants originate mainly from inorganic substances added in the polymerization reaction. The wastewater has the characteristics of large discharge amount, high content of suspended matters, turbidity and colloid, low COD (chemical oxygen demand) and poor biodegradability. Because pure water is adopted in the polymerization process, the hardness, chloride ions and soluble solids of the filtered mother liquor are low, and the filtered mother liquor is a high-quality recycled water source after treatment.
Disclosure of Invention
Aiming at the defects of substandard wastewater treatment and high energy consumption in the conventional suspension method polyvinyl chloride polymerization section, the invention provides a treatment process (method) and a device which have the advantages of compact structure, good treatment effect and high treatment efficiency and can synchronously remove various organic pollutants.
According to a first aspect of the invention, a method for treating waste water in a suspension polyvinyl chloride polymerization section is provided, which comprises the following steps:
(1) the PVC slurry stripping wastewater firstly enters a first regulating tank for carrying out homogeneous regulation on water quality and water quantity;
(2) the PVC slurry steam stripping waste water after water quality adjustment enters a pre-oxidation section;
(3) the PVC centrifugal mother liquor wastewater firstly enters a cooling tower and is cooled to 25-40 ℃;
(4) the centrifugal mother liquor wastewater cooled by the cooling tower enters a sedimentation tank, and PVC particles are recovered through sedimentation;
(5) the pre-oxidized PVC slurry stripping wastewater and the cooled and precipitated centrifugal mother liquor enter a second regulating tank;
(6) the wastewater is subjected to homogeneous regulation of water quality and quantity in a second regulating tank, the effluent of the second regulating tank enters a first-stage biochemical tank, and a filler biofilm reactor is adopted in first-stage biochemical treatment;
(7) the first-level biochemical effluent enters a second-level biochemical section, and the second-level biochemical section adopts an Annular-flow Membrane oxidation biological Reactor (AF-MABR);
(8) the secondary biochemical effluent enters a coagulating sedimentation tank for coagulating sedimentation;
(9) the effluent of the coagulation sedimentation tank enters an advanced treatment section, and the effluent after advanced treatment can be recycled.
In a specific case, in the step (1), the retention time of the wastewater is preferably 6-8 h.
In a specific case, in the step (2), the pre-oxidation section (unit) may adopt a microbubble ozone oxidation process or an ultraviolet/ozone oxidation process. Through the treatment of the pre-oxidation section, macromolecular organic matters and biological toxic substances are degraded, and the B/C ratio is improved. In a preferred embodiment, a microbubble ozone oxidation process is adopted, the diameter of the generated ozone bubbles is 5-50 μm, the retention time is 20-40 min, the gas-water ratio is 0.06-0.2, and the concentration of ozone in water is 10-30 mg/L. Because the ozone microbubbles have larger specific surface area and longer retention time, compared with the conventional technology, the ozone utilization rate is high, the residual ozone amount is less, pollutants can be efficiently removed, and the residual ozone amount is reduced. In the process section, the primary degradation of the refractory macromolecular organic matters can be realized, and the subsequent biochemical process is easy to carry out.
In the step (6), the hydraulic retention time of the primary biochemical pool is 8-24h, the water temperature is 10-25 ℃, and the dissolved oxygen is 0-0.5 mg/L.
In the step (8), a coagulant and a coagulant aid are added into the coagulating sedimentation tank, wherein the coagulant is an inorganic salt coagulant (such as aluminum sulfate, ferric chloride, ferrous sulfate, aluminum potassium sulfate, sodium aluminate, ferric sulfate and the like) or a polymer coagulant (such as polyaluminium chloride or polyferric sulfate), the adding amount is 20-60 mg/L, the coagulant aid is polyacrylamide, and the adding amount is 0.6-1.5 mg/L.
In a specific case, in the step (9), the advanced treatment includes sand filtration, advanced oxidation and carbon filtration, wherein the advanced oxidation employs fenton oxidation, fenton-like oxidation, ozone catalytic oxidation, microbubble ozone oxidation, photocatalysis or electrocatalytic oxidation.
According to a second aspect of the invention, a wastewater treatment device for a suspension polyvinyl chloride polymerization section is provided, which comprises a first regulating tank, a pre-oxidation unit, a cooling tower, a sedimentation tank, a second regulating tank, a primary biochemical tank, a secondary biochemical tank, a coagulating sedimentation tank and a deep treatment unit;
the system comprises a first adjusting tank, a cooling tower, a sedimentation tank, a pre-oxidation unit, a first-stage biochemical tank, a second-stage biochemical tank, a coagulating sedimentation tank and a deep treatment unit, wherein the first adjusting tank is connected with the pre-oxidation unit;
wherein, the first-stage biochemical tank adopts a filler biofilm reactor, and the second-stage biochemical tank adopts AF-MABR.
In certain embodiments, the pre-oxidation unit comprises an ozone generator, a microbubble generator, and an ozone off-gas destruction device. The microbubble generator can be a gas-liquid rotational flow type microbubble generator, a Venturi type microbubble generator, a jet type microbubble generator or a mechanical cutting type microbubble generator.
In other embodiments, the pre-oxidation unit comprises an ozone generator, an ultraviolet light generator, and an ozone off-gas destruction device.
In certain embodiments, one or more combinations of particulate, honeycomb, rope, and soft fillers may be used as fillers in the packed biofilm reactor. Preferably, in the filler biofilm reactor, a stirrer is arranged at each of the water inlet end and the water outlet end and is arranged diagonally, and the stirring direction is adjustable in the operation process.
In some embodiments, the AF-MABR is divided into a water inlet gallery, a plurality of intermediate circulation galleries and a water outlet gallery, wherein each gallery is internally provided with a bubble-free oxygen supply membrane box, and the galleries are separated by a diversion folded plate, so that the wastewater flows in a circulation state in the reactor integrally and is in full contact with efficient microorganisms attached to an oxygen supply membrane component in the bubble-free oxygen supply membrane box.
In one embodiment, the AF-MABR is a cuboid, the water inlet pipe is arranged in the center of one width side, two inner diversion folded plates parallel to the length side are arranged in the water inlet gallery, circulation folded plates parallel to the width side and intermediate baffle plates are arranged in a plurality of intermediate circulation galleries at intervals, the water outlet gallery is provided with a water collecting well, and the other width side corresponding to the water collecting well is provided with a water outlet weir plate. Preferably, the inner diversion folded plate is 10-15% of the length of the circulation folded plate, the length of the circulation folded plate is 75-85% of the width of the reactor, and the total length of the intermediate baffle plate is 70-80% of the width of the reactor.
Under the specific condition, the bubble-free oxygen supply membrane box consists of a supporting frame, a membrane component, an air inlet collecting pipe, air inlet branch pipes, air outlet branch pipes and an air outlet collecting pipe, wherein the membrane component is installed in the supporting frame, the upper end of the supporting frame is provided with a plurality of paths of air inlet branch pipes, the plurality of paths of air inlet branch pipes are connected with the air inlet collecting pipe, the air inlet collecting pipe is connected with an oxygen supply pipeline, the lower end of the supporting frame is provided with a plurality of paths of air outlet branch pipes, and the plurality of paths of. The support frame is a frame in a cuboid, cylinder or hexagonal prism form and is made of steel bars, angle steel, alloy or ABS. The oxygen supply pipeline is externally connected with a compressor or an oxygen source, air or oxygen enters the membrane cavity, bubble-free oxygen supply is carried out through the membrane hole cutting effect, the gas operation pressure is 0.01-0.06 Mpa, microorganisms attached to the membrane component from inside to outside are aerobic bacteria, facultative bacteria and anaerobic bacteria in sequence, COD is removed, synchronous nitrification and denitrification are realized, and NH is removed3-N and TN; finally, the effluent enters a water collecting well and is finally discharged through an overflow weir plate; residence time: 12-30 h.
Preferably, the membrane filament material of the membrane module is a hollow fiber membrane made of polyethylene, polytetrafluoroethylene, polypropylene, polystyrene, polyvinylidene fluoride and/or silicon rubber dense membrane, the membrane module is made in a curtain type or spiral winding type, and the filling density of the membrane filament is as follows: 50 to 200m2/m3(ii) a Wherein, two ends of the membrane wire are sealed by epoxy sealant and are butted with the sealed cavity; one end of the sealed cavity is in butt joint with the membrane wires, and the other end of the sealed cavity is connected with the air inlet branch pipe or the air outlet branch pipe.
In a preferred embodiment, the bubble-free oxygen supply film box is arranged to be rotatable, and consists of a supporting frame, a film assembly, an inlet gas collecting pipe, an outlet gas collecting pipe, a hollow rotating shaft and a motor. The membrane component is transversely installed in the supporting frame around the hollow rotating shaft, one end of the membrane component is connected with the air inlet and air collecting pipe, and the other end of the membrane component is connected with the air outlet and air collecting pipe. The air inlet collecting pipe is connected with the hollow rotating shaft, a plurality of air outlet holes are formed in the connecting portion of the hollow rotating shaft and the air inlet collecting pipe, an air inlet bearing seat is arranged at the top end of the hollow rotating shaft and connected with an external oxygen supply pipeline, and oxygen is conveyed to the air inlet collecting pipe along a central radial hole of the hollow rotating shaft. The gas outlet and gas collecting pipe is connected with a waste gas pipeline.
Compared with the prior art, the suspension method polyvinyl chloride polymerization workshop section wastewater treatment method and the device have the following advantages:
1. the microbubble integrated reaction greatly improves the utilization rate of ozone and the reaction rate with pollutants for the pretreatment of polyvinyl chloride gas wastewater, most of refractory organic matters in the wastewater are quickly and effectively removed, and meanwhile, the biodegradability of the wastewater is improved. The COD of the effluent after final treatment is stabilized below 30mg/L, and the total nitrogen is less than 10 mg/L.
The AF-MABR membrane has various surface microorganisms, bacteria, protozoon and metazoan are distributed in a cross way, and the sludge reduction is realized by the natural food chain principle, so that the resource consumption is reduced. The design of the annular baffling gallery enables the mass transfer efficiency of microorganisms and sewage to be higher, and the annular baffling gallery has the advantages of high treatment load, small occupied area, strong impact resistance and low energy consumption. Meanwhile, the characteristics of synchronous nitrification and denitrification can be realized by combining the bubble-free aeration technology, the effluent does not need to set nitrification liquid reflux, and carbon sources are not needed to be added, so that the ammonia nitrogen and the total nitrogen can be efficiently removed.
3. Each unit is used for treating pollutants in a targeted manner, the pretreatment unit is used for removing biological inhibition for the post-treatment unit and providing a favorable reaction environment, and the problem that the conventional wastewater recycling treatment of the polyvinyl chloride polymerization section does not reach the standard can be solved through advanced oxidation at the tail end of the process.
Drawings
FIG. 1 is a process route for wastewater treatment in a suspension polymerization section of polyvinyl chloride according to the present invention;
FIG. 2 is a schematic view of the AF-MABR reactor of the present invention;
FIG. 3 is a schematic structural view of a bubble-free oxygen supply membrane box according to the present invention; and
FIG. 4 is a schematic structural view of another bubble-free oxygen supply membrane box of the present invention.
The specific implementation mode is as follows:
the invention is described in further detail below with reference to a specific embodiment and with reference to the attached drawing. Like reference numbers in the figures refer to like or similar components.
Referring to FIG. 1, the stripping waste water of PVC slurry is 20m3The flow of the/h firstly enters a first regulating tank to carry out balanced regulation on water quality and water quantity, the residence time is 8h, then the flow enters a microbubble pre-oxidation unit, the residence time is 30-40 min, and the ozone adding concentration is as follows: 20-40 mg/L. Residual O3Catalytic generation of O under the action of high-efficiency catalyst in ozone tail gas destruction device2。
Preoxidized slurry stripping wastewater and cooled, initially precipitated centrifuge mother liquor wastewater (160 m)3And/h) entering a second regulating tank and then entering a first-stage biochemical tank. The first-stage biochemical tank is a filler biofilm reactor, the reaction tank is filled with filler, and microorganisms are attached to the filler for biological interception, so that the reaction efficiency is improved.
The effluent of the primary biochemical pool enters an AF-MABR reactor, which is a cuboid with the specification of 22m long, 20m wide and 5.5m deep, and is divided into an inlet gallery 11, two intermediate circulation galleries 12 and 13 and an outlet gallery 14 along the length direction, wherein the lengths of the galleries are the same, referring to figure 2. Two symmetrical bubble-free oxygen supply film boxes 3 are arranged in each gallery, and each bubble-free oxygen supply film box 3 is respectively connected with an oxygen inlet pipeline 6 and an exhaust pipeline 9 through pipelines. The water inlet pipe 1 is arranged in the center of one width side of the reactor, two inner diversion folded plates 2 parallel to the length side of the reactor are arranged in the water inlet gallery 11, a first circulation folded plate 4, a middle baffle plate 5 and a second circulation folded plate 10 parallel to the width side are sequentially arranged in the two middle circulation galleries 12 and 13, and the inner diversion folded plates 2 are vertically connected with the first circulation folded plates 4. The two ends of the first circulation folded plate 4 and the second circulation folded plate 10 are water flow openings, and the center of the middle baffle plate 5 is a water flow opening. Wherein the length of the inner diversion flap 2 is 1.7m, the length of the first circulation flap 4 and the second circulation flap 10 is 16m, and the length of the intermediate baffle 5 is 15 m. The center of the water outlet gallery 14 is provided with a water collecting well 7, and the other width side of the reactor corresponding to the water collecting well 7 is provided with a water outlet weir plate 8.
Fig. 3 shows a static bubble-free oxygen supply membrane box 3, and the bubble-free oxygen supply membrane box 3 is composed of a support frame 31, a membrane assembly 32, an air inlet collecting pipe 33, an air inlet branch pipe 34, an air outlet branch pipe 35 and an air outlet collecting pipe 36. The membrane module 32 is vertically installed in the supporting frame 31, the upper end of the supporting frame 31 is provided with a plurality of air inlet branch pipes 34, the plurality of air inlet branch pipes 34 are connected with the air inlet collecting pipe 33, and the air inlet collecting pipe 33 is connected with the oxygen supply pipeline 6. The lower end of the supporting frame 31 is provided with a plurality of outlet branch pipes 35, and the plurality of outlet branch pipes 35 are connected with an outlet gas collecting pipe 36. Wherein the gas inlet collecting pipe 33 is connected with the oxygen supply pipeline 6, and the gas outlet collecting pipe 36 is connected with the waste gas pipeline 9. The oxygen supply pipeline 6 is externally connected with a compressor or an oxygen source, air or oxygen enters the film cavity, bubble-free oxygen supply is carried out under the film hole cutting action, and the operation pressure is 0.01-0.06 Mpa. In this embodiment, the membrane module 32 is a polyvinylidene fluoride (PVDF) hollow fiber spiral winding type module, which is provided with 8 groups, the length of the membrane filament is 0.8m, the outer diameter is 900 μm, about 25 ten thousand membrane filaments are placed, and the packing density is 70m2/m3。
The first-stage biochemical effluent firstly enters the AF-MABR reactor along with the water inlet pipe 1, and then the water flows in the reactor integrally in a circulating flow state. Passes through the water inlet gallery 11, the middle galleries 12 and 13 and the water outlet gallery 14 in sequence and is fully contacted with the membrane modules 32 in each bubble-free oxygen supply membrane box 3. The microorganisms attached to the surface of the membrane filaments of the membrane component 32 from inside to outside are aerobic bacteria, facultative bacteria and anaerobic bacteria in sequence, COD is removed, synchronous nitrification and denitrification are realized, and NH is removed3-N and TN. Finally, the effluent enters a water collecting well 7 and is finally discharged through an overflow weir plate 8; the residence time was about 12 h.
After the biochemical reaction of AF-MABR is finished, the mixed liquor enters a coagulation unit, a coagulant is selected from high-molecular polyaluminium chloride, the adding concentration is 40mg/L, a coagulant aid is selected from polyacrylamide, the adding concentration is 1mg/L, the sludge at the bottom is transported out after being dehydrated, and the supernatant enters an advanced oxidation unit for treatment after being subjected to sand filtration.
Advanced oxidation is used as an advanced treatment process, the selected process is ozone heterogeneous catalytic oxidation, the active component of the catalyst is a composite catalyst which is composed of Fe-Cu-Mn oxide according to the mass ratio of m (Fe), (m), (Cu), (m), (Mn), (1.8-2), (1.5-3) and 2, alumina, silica gel, active carbon, diatomite and the like are used as carriers, the retention time is 10-40 min, and the ozone adding concentration is as follows: 20-60 mg/L. The advanced oxidation effluent is filtered by carbon, the final effluent reaches the national comprehensive sewage discharge first-grade standard, and the pollutant indexes after treatment in each stage are shown in table 1.
Table 1: index of removing pollutant in each stage
In other embodiments of the present invention, an alternative rotary bubble-free oxygen supply membrane cassette 3 to that of FIG. 3 may be employed, as shown in FIG. 4, with the bubble-free oxygen supply membrane cassette 3 being comprised of a support frame 31, a membrane module 32, an inlet header 33, an outlet header 36, a hollow rotating shaft 37, and a motor 38. The membrane module 32 is mounted in the support frame 31 in a transverse manner around a hollow rotating shaft 37, and one end of the membrane module 32 is connected with the inlet gas header 33 and the other end is connected with the outlet gas header 36. The air inlet gas collecting pipe 33 is connected with the hollow rotating shaft 37, a plurality of air outlet holes are formed in the connecting portion of the hollow rotating shaft 37 and the air inlet gas collecting pipe 33, an air inlet bearing seat 40 is arranged at the top end of the hollow rotating shaft 37, the air inlet bearing seat 40 is connected with an external oxygen supply pipeline 6, and oxygen or air is conveyed to the air inlet gas collecting pipe 33 along a central radial hole of the hollow rotating shaft 37. The outlet header 36 is connected to the exhaust gas line 9. The motor 38 rotates the hollow rotating shaft 37 through the belt 39, and drives the whole membrane module 32 to rotate in the AF-MABR reactor, so that the water flow is fully contacted with the membrane module 32. The membrane filament material and fabrication process of the membrane assembly 32 may be the same as the embodiment shown in FIG. 3. Experiments prove that the reaction efficiency can be improved by more than 20% by adopting the rotary bubble-free oxygen supply film box shown in figure 4 to replace the static bubble-free oxygen supply film box shown in figure 3.
The invention organically combines the micro-bubble preoxidation-filler biofilm reactor-AFMABR-advanced treatment, each unit has high pollutant treatment efficiency and strong pertinence, the pretreatment unit provides good reaction environment for the subsequent unit, the pollutant removal efficiency is high, the impact resistance is strong, and the process as an organic whole can be efficiently and stably discharged and operated up to the standard
The present invention has been described in detail with reference to the above embodiments, but the above description is only a preferred embodiment of the present invention and should not be construed as limiting the scope of the present invention. All equivalent changes and modifications made within the scope of the present invention shall fall within the scope of the present invention.
Claims (4)
1. A suspension method for treating waste water in a polyvinyl chloride polymerization section is characterized by comprising the following steps:
(1) the PVC slurry stripping wastewater firstly enters a first regulating tank for carrying out homogeneous regulation on water quality and water quantity;
(2) the PVC slurry steam stripping waste water after water quality adjustment enters a pre-oxidation section;
(3) the PVC centrifugal mother liquor wastewater firstly enters a cooling tower and is cooled to 25-40 ℃;
(4) the centrifugal mother liquor wastewater cooled by the cooling tower enters a sedimentation tank, and PVC particles are recovered through sedimentation;
(5) the pre-oxidized PVC slurry stripping wastewater and the cooled and precipitated centrifugal mother liquor enter a second regulating tank;
(6) the wastewater is subjected to homogeneous regulation of water quality and quantity in a second regulating tank, the effluent of the second regulating tank enters a first-stage biochemical tank, and a filler biofilm reactor is adopted in first-stage biochemical treatment;
(7) the first-stage biochemical effluent enters a second-stage biochemical section, and the second-stage biochemical section adopts an annular flow oxidation membrane bioreactor;
the annular flow oxidation membrane bioreactor is divided into a water inlet gallery, a plurality of middle circulation galleries and a water outlet gallery, wherein each gallery is internally provided with a bubble-free oxygen supply membrane box, and the galleries are separated by a diversion folded plate, so that the wastewater flows in the reactor integrally in a circulation state and is in full contact with efficient microorganisms attached to an oxygen supply membrane component in the bubble-free oxygen supply membrane box; the membrane filament material of the membrane component is a hollow fiber membrane made of polyethylene, polytetrafluoroethylene, polypropylene, polystyrene, polyvinylidene fluoride and/or silicon rubber dense membrane;
(8) the secondary biochemical effluent enters a coagulating sedimentation tank for coagulating sedimentation;
(9) the effluent of the coagulation sedimentation tank enters an advanced treatment section, and the effluent after advanced treatment can be recycled.
2. The method for treating wastewater in a polyvinyl chloride polymerization workshop section by using a suspension method as claimed in claim 1, wherein in the step (2), a micro-bubble ozone oxidation process or an ultraviolet/ozone oxidation process is adopted in the pre-oxidation section.
3. The method for treating wastewater in a polyvinyl chloride polymerization workshop section by using a suspension method according to claim 1, wherein the hydraulic retention time of the primary biochemical pool is 8-24 hours, the water temperature is 10-25 ℃, and the dissolved oxygen is 0-0.5 mg/L.
4. The method for treating wastewater in a polyvinyl chloride polymerization workshop section by using a suspension method according to claim 1, wherein a coagulant and a coagulant aid are added into the coagulation sedimentation tank in the step (8), the coagulant is an inorganic salt coagulant or a polymer coagulant, the adding amount is 20-60 mg/L, the coagulant aid is polyacrylamide, and the adding amount is 0.6-1.5 mg/L.
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| CN110482710A (en) * | 2019-05-30 | 2019-11-22 | 江苏滤盾膜科技有限公司 | A kind of sewage treatment microbial film coupling carrier |
| CN112047562B (en) * | 2019-06-06 | 2021-11-16 | 中国科学院过程工程研究所 | Ozone catalytic oxidation system, wastewater advanced treatment system comprising ozone catalytic oxidation system and treatment method |
| CN115650513B (en) * | 2022-10-31 | 2024-04-19 | 广东工业大学 | Rare earth mine tail water treatment method based on MABR |
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