CN216918935U - Membrane concentrate processing system - Google Patents
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- CN216918935U CN216918935U CN202123432784.XU CN202123432784U CN216918935U CN 216918935 U CN216918935 U CN 216918935U CN 202123432784 U CN202123432784 U CN 202123432784U CN 216918935 U CN216918935 U CN 216918935U
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Abstract
The utility model belongs to the technical field of sewage treatment, and particularly relates to a membrane concentrated solution treatment system. The processing system provided by the utility model comprises: a pH adjusting device; the micro-electrolysis turntable reaction bed is connected with the water outlet of the pH adjusting device, and iron carbon filler is filled in a micro-electrolysis turntable of the micro-electrolysis turntable reaction bed; the anaerobic biological expansion bed is connected with the water outlet of the micro-electrolysis turntable reaction bed; the ozone-hydrogen peroxide catalytic oxidation reactor is connected with a water outlet of the anaerobic biological expansion bed; and the ozone destructor is connected with a tail gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor. The treatment system provided by the utility model has the advantages of short process flow, difficult hardening and blocking of the micro-electrolysis filler, high oxidation efficiency and low operation cost, the membrane concentrated solution treated by the system basically does not contain long-chain organic matters difficult to degrade, the subsequent biochemical treatment can be directly carried out to realize reduction, and the treatment system has good environmental benefit and economic benefit.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, and particularly relates to a membrane concentrated solution treatment system.
Background
The domestic main process for treating the landfill leachate generally adopts pretreatment, UASB, two-stage A/O-MBR and membrane advanced treatment, the membrane advanced treatment generally adopts NF/RO treatment process, and certain amount of concentrated solution is inevitably generated by adopting the membrane treatment process, wherein the concentrated solution of the nanofiltration membrane accounts for 20-25% of the total treatment scale, the concentrated solution of the reverse osmosis accounts for 25-30% of the total treatment scale, the yield of the concentrated solution is large, the pollutant components are complex, the method is waste water with high salinity and high organic matter, and the method realizes effective treatment reduction of the waste water, and is a difficult problem in the landfill leachate treatment process.
At present, the advanced oxidation technology applied to concentrated solution treatment mainly comprises a micro-electrolysis coupling catalytic ozone technology and a micro-electrolysis coupling Fenton technology. In the traditional microelectrolysis coupling catalytic ozone process, iron-carbon fillers in the microelectrolysis process are easy to harden and block, the fillers are complex to replace, the effluent contains ferrous ions after the microelectrolysis oxidation, and the solution is acidic; the catalytic ozone process mostly adopts jet flow/aeration disc aeration, the catalyst is fixed in a reaction tower, the gas-solid-liquid three-phase mixing effect is not ideal in the treatment process, the diameter of the generated ozone bubbles is large, the ozone utilization rate is low, and the operation cost is high. In the traditional micro-electrolysis coupling Fenton technology, the problems that the iron-carbon filler is easy to harden and block, the filler replacement is complex and the like also exist, and the Fenton oxidation process is long in process flow, and simultaneously generates a large amount of chemical sludge, so that the operation cost of the whole process is greatly increased.
SUMMERY OF THE UTILITY MODEL
In view of this, the present invention aims to provide a membrane concentrated solution treatment system, which has a short process flow, is not easy to harden and block micro-electrolysis filler, and has high oxidation efficiency and low operation cost.
The utility model provides a membrane concentrate treatment system, comprising:
a pH adjusting device;
the micro-electrolysis turntable reaction bed is connected with the water outlet of the pH adjusting device, and iron carbon filler is filled in a micro-electrolysis turntable of the micro-electrolysis turntable reaction bed;
the anaerobic biological expansion bed is connected with the water outlet of the micro-electrolysis turntable reaction bed;
the ozone-hydrogen peroxide catalytic oxidation reactor is connected with a water outlet of the anaerobic biological expansion bed, and a main device of the ozone-hydrogen peroxide catalytic oxidation reactor is a three-phase fluidized bed;
and the gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor is connected to the micro-electrolysis turntable reaction bed.
Preferably, the pH adjusting device is a pipeline mixer, and a pH adjusting agent adding port is arranged on the pH adjusting device.
Preferably, the micro-electrolysis rotating disc reaction bed comprises: the device comprises a reaction bed body, a plurality of micro-electrolysis rotating discs, a reaction bed water inlet and a reaction bed water outlet;
the interior of the reaction bed body is divided into an inner circulation area and an outer circulation area which are communicated by a vertically arranged partition plate; the water inlet of the reaction bed is positioned at the bottom of the internal circulation area, and the water outlet of the reaction bed is positioned at the top of the reaction bed body; the micro-electrolysis rotating discs are positioned above the water inlet of the reaction bed and are longitudinally arranged in the internal circulation area.
Preferably, baffles are arranged on two axial sides of each micro-electrolysis turntable, and the distance between each baffle on the two sides and the corresponding micro-electrolysis turntable is different.
Preferably, the micro-electrolysis turntable and the reaction bed body are detachably fixed.
Preferably, the anaerobic organism expanded bed comprises: the system comprises an expansion zone, a three-phase separator, a sludge hopper, an expansion bed water inlet and an expansion bed water outlet;
the expansion zone is positioned in the middle section of the expansion bed, the water inlet of the expansion bed is positioned below the expansion zone, the three-phase separator is positioned above the expansion zone, and the water outlet of the expansion bed is connected with the liquid phase outlet of the three-phase separator; the sludge hopper is positioned at the bottom of the expansion bed.
Preferably, the water outlet end of the water inlet of the expansion bed is provided with a pluggable water distribution device.
Preferably, the ozone-hydrogen peroxide solution catalytic oxidation reactor comprises: a dissolved air tank and a three-phase fluidized bed;
the dissolved air tank is provided with an ozone inlet, a hydrogen peroxide inlet, a backflow water inlet and a dissolved air liquid outlet, and filling materials are filled in the tank;
the three-phase fluidized bed comprises: the fluidized bed comprises a fluidized bed body, a three-phase separator, a fluidized bed water inlet, a dissolved gas-liquid inlet, a backflow water outlet, a fluidized bed water outlet and a fluidized bed tail gas outlet, wherein a solid catalyst is filled in the bed body; the interior of the reaction bed body is divided into an inner circulation area and an outer circulation area which are communicated by a vertically arranged partition plate; the fluidized bed is characterized in that a water inlet of the fluidized bed is positioned at the bottom of the internal circulation zone, a dissolved gas-liquid inlet is positioned at the bottom of the fluidized bed body, the three-phase separator is positioned above the internal and external circulation zones, a backflow water outlet is positioned on the side wall of the fluidized bed body between the internal and external circulation zones and the three-phase separator, a water outlet of the fluidized bed is connected with a liquid phase outlet of the three-phase separator, and a tail gas outlet of the fluidized bed is connected with a gas phase outlet of the three-phase separator;
and a dissolved gas-liquid outlet of the dissolved gas tank is connected with a dissolved gas-liquid inlet of the three-phase fluidized bed, and a backflow water inlet of the dissolved gas tank is connected with a backflow water outlet of the three-phase fluidized bed.
Preferably, a water distribution device is installed at the liquid outlet end of the dissolved gas-liquid inlet, and a dissolved gas releaser is installed on a water outlet hole of the water distribution device.
Compared with the prior art, the utility model provides a membrane concentrate treatment system. The processing system provided by the utility model comprises: a pH adjusting device; the micro-electrolysis turntable reaction bed is connected with the water outlet of the pH adjusting device, and iron carbon filler is filled in a micro-electrolysis turntable of the micro-electrolysis turntable reaction bed; the anaerobic biological expansion bed is connected with the water outlet of the micro-electrolysis turntable reaction bed; the ozone-hydrogen peroxide catalytic oxidation reactor is connected with a water outlet of the anaerobic biological expansion bed, and a main device of the ozone-hydrogen peroxide catalytic oxidation reactor is a three-phase fluidized bed; and the gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor is connected to the micro-electrolysis turntable reaction bed. The working process of the processing system is as follows: conveying the membrane concentrated solution to pH adjusting equipment, adjusting the pH value of the membrane concentrated solution to 5.0-6.0, then feeding the membrane concentrated solution into a micro-electrolysis turntable reaction bed, carrying out electrolysis treatment on wastewater by using iron-carbon fillers in the reaction bed, decomposing long-chain organic matters which are difficult to degrade into short-chain organic matters, and simultaneously generating iron ions and ferrous ions; conveying the effluent of the micro-electrolysis rotary table reaction bed to an anaerobic biological expansion bed by a pump, using iron ions and ferrous ions carried in the effluent of the micro-electrolysis rotary table reaction bed as trace elements for culturing microorganisms in the anaerobic biological expansion bed to stimulate the microorganisms to secrete extracellular polymers, promoting the formation of anaerobic granular sludge, fully mixing the microorganisms attached to the anaerobic granular sludge with organic matters in wastewater in an expansion flow state, and further decomposing long-chain organic matters which cannot be degraded by the micro-electrolysis rotary table reaction bed in the wastewater into short-chain organic matters by using hydrolytic acidification bacteria; the effluent treated by the anaerobic biological expansion bed flows into an ozone-hydrogen peroxide catalytic oxidation three-phase fluidized bed, and the residual long-chain organic matters are further oxidized and decomposed into short-chain organic matters through catalytic oxidation reaction; ozone tail gas generated by the ozone-hydrogen peroxide catalytic oxidation three-phase fluidized bed enters an ozone destructor for treatment, and generated oxygen returns to the micro-electrolysis turntable reaction bed. In the utility model, through a three-stage oxidative degradation process, long-chain organic matters which are difficult to degrade in the membrane concentrated solution are basically converted into short-chain organic matters which are easy to degrade, and the effluent of the three-phase fluidized bed can subsequently flow back to a biochemical system of a percolate treatment station for biochemical treatment again, so that the decrement of the membrane concentrated solution is realized. The treatment system provided by the utility model has the advantages of short process flow, difficult hardening and blocking of the micro-electrolysis filler, high oxidation efficiency and low operation cost, the membrane concentrated solution treated by the system basically does not contain long-chain organic matters difficult to degrade, the subsequent biochemical treatment can be directly carried out to realize reduction, and the treatment system has good environmental benefit and economic benefit.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a process flow diagram of a membrane concentrate treatment system provided by an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a micro-electrolysis rotating disc reaction bed provided by an embodiment of the utility model;
FIG. 3 is a schematic structural diagram of an anaerobic biological expanded bed provided by an embodiment of the utility model;
fig. 4 is a schematic structural diagram of an ozone-hydrogen peroxide solution catalytic oxidation reactor provided in the embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The utility model provides a membrane concentrate treatment system, comprising:
a pH adjusting device;
the micro-electrolysis turntable reaction bed is connected with the water outlet of the pH adjusting device, and iron carbon filler is filled in a micro-electrolysis turntable of the micro-electrolysis turntable reaction bed;
the anaerobic biological expansion bed is connected with a water outlet of the micro-electrolysis turntable reaction bed;
the ozone-hydrogen peroxide catalytic oxidation reactor is connected with a water outlet of the anaerobic biological expansion bed, and a main device of the ozone-hydrogen peroxide catalytic oxidation reactor is a three-phase fluidized bed;
and the gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor is connected to the micro-electrolysis turntable reaction bed.
Referring to fig. 1 to 4, fig. 1 is a process flow diagram of a membrane concentrate treatment system provided in an embodiment of the present invention, fig. 2 is a schematic structural diagram of a micro-electrolysis rotating disc reaction bed provided in an embodiment of the present invention, fig. 3 is a schematic structural diagram of an anaerobic biological expansion bed provided in an embodiment of the present invention, and fig. 4 is a schematic structural diagram of an ozone-hydrogen peroxide catalytic oxidation reactor provided in an embodiment of the present invention; the device comprises a reaction bed water distribution device 1, a micro-electrolysis turntable baffle 2, a micro-electrolysis turntable 3, a reaction bed internal circulation zone 4, a reaction bed external circulation zone 5, a reaction bed water outlet zone 6, an expansion bed water distribution device 7, a sludge hopper 8, a sludge discharge pipe 9, an expansion zone 10, an expansion bed three-phase separator 11, a water inlet spray head 12, a fluidized bed water distribution device 13, a dissolved gas releaser 14, a fluidized bed internal circulation zone 15, a fluidized bed external circulation zone 16, a fluidized bed three-phase separator 17 and a pressure dissolved gas tank 18.
In the treatment system provided by the utility model, the pH adjusting device is used for adjusting the pH of the membrane concentrated solution to be fed into the micro-electrolysis turntable reaction bed, so that the pH value of the membrane concentrated solution meets the water feeding requirement of the micro-electrolysis turntable reaction bed, and the pH value is preferably 5-6. In the utility model, the pH adjusting device is preferably a pipeline mixer, and a pH regulator adding port is arranged on the pH adjusting device; the pH regulator is preferably sulfuric acid.
In the treatment system provided by the utility model, the micro-electrolysis turntable of the micro-electrolysis turntable reaction bed is filled with iron-carbon filler; and the water inlet of the micro-electrolysis turntable reaction bed is connected with the water outlet of the pH adjusting device. In the utility model, the iron-carbon filler is preferably a microporous framework type alloy structure filler; the specific gravity of the iron-carbon filler is preferably 1～2t/m3Specifically, it may be 1.5t/m3(ii) a The iron content of the iron-carbon filler is preferably 75-82 wt%, and specifically can be 78 wt%; the carbon content of the iron-carbon filler is preferably 8-15 wt%, and specifically can be 12 wt%; the content of the noble metal catalyst in the iron-carbon filler is preferably 8-15 wt%, and specifically 10 wt%; the noble metal catalyst includes, but is not limited to, one or more of Pt, Pd, and Ag; the specific surface area of the iron-carbon filler is preferably 1-1.5 m2A specific value of 1.3 m/g2(ii)/g; the porosity of the iron-carbon filler is preferably 70-75%, and specifically 72%; the physical strength of the iron-carbon filler is preferably more than or equal to 650kg/m2. In the utility model, the micro-electrolysis turntable reaction bed can utilize iron carbon filler to carry out electrolysis treatment on waste liquid, decompose long-chain organic matters which are difficult to degrade into short-chain organic matters, and simultaneously generate ferric ions and ferrous ions.
In the processing system provided by the utility model, as shown in fig. 2, the structure of the micro-electrolysis rotating disc reaction bed preferably comprises: the device comprises a reaction bed body, a plurality of micro-electrolysis rotating discs 3, a reaction bed water inlet and a reaction bed water outlet. Wherein, the interior of the reaction bed body is divided into a reaction bed inner circulation zone 4 and a reaction bed outer circulation zone 5 which are communicated by a vertically arranged partition plate; the water inlet of the reaction bed is positioned at the bottom of the internal circulation zone 4 of the reaction bed, and the water outlet of the reaction bed is positioned in the water outlet zone 6 of the reaction bed at the top of the bed body; the micro-electrolysis rotating discs 3 are positioned above the water inlet of the reaction bed and are longitudinally arranged in the inner circulation zone 4 of the reaction bed. In the utility model, both axial sides of each micro-electrolysis turntable 3 are preferably provided with micro-electrolysis turntable baffles 2, and the distances between the baffles 2 on both sides and the corresponding micro-electrolysis turntable 3 are preferably different. In the utility model, the baffle plates with different distances on the two sides can ensure that the water flow thrusts on the two sides of the micro-electrolysis turntable are different when water enters, so that the turntable rotates, the iron-carbon filler in the turntable is more fully mixed with the organic matters in the waste liquid, and the hardening and blocking are avoided. In the utility model, the micro-electrolysis turntable 3 and the reaction bed body are preferably detachably fixed, so that the cleaning and the replacement of the filler are convenient. In the utility model, the water outlet end of the water inlet of the reaction bed is preferably provided with a reaction bed water distribution device 1 so that waste liquid can enter the internal circulation zone 4 of the reaction bed more uniformly, and the reaction bed water distribution device 1 is preferably a perforated water distribution pipe.
In the treatment system provided by the utility model, anaerobic granular sludge is arranged in the anaerobic biological expansion bed, and a water inlet of the anaerobic biological expansion bed is connected with a water outlet of the micro-electrolysis rotating disc reaction bed. In the utility model, the anaerobic organism expanded bed can utilize iron ions and ferrous ions carried in effluent of the micro-electrolysis rotating disc reaction bed as microelements for microbial culture to stimulate microorganisms to secrete extracellular polymers and promote the formation of anaerobic granular sludge, microorganisms attached to the anaerobic granular sludge are fully mixed with organic matters in waste liquid in an expansion flow state, and long-chain organic matters which cannot be degraded by the micro-electrolysis rotating disc reaction bed in the waste liquid are further decomposed into short-chain organic matters by hydrolytic acidification bacteria.
In the treatment system provided by the present invention, as shown in fig. 3, the structure of the anaerobic organism expanded bed preferably includes: an expansion zone 10, an expansion bed three-phase separator 11, a sludge hopper 8, an expansion bed water inlet and an expansion bed water outlet. The expansion region 10 is positioned in the middle section of the expansion bed, the water inlet of the expansion bed is positioned below the expansion region 10, the three-phase separator 11 of the expansion bed is positioned above the expansion region 10, and the water outlet of the expansion bed is connected with the liquid-phase outlet of the three-phase separator 11 of the expansion bed; a sludge hopper 8 is located at the bottom of the expanded bed. In the utility model, the water outlet end of the water inlet of the expansion bed is preferably provided with an expansion bed water distribution device 7, and the expansion bed water distribution device 7 is preferably a pluggable water distribution device, more preferably a pluggable perforated water distribution pipe, so as to facilitate later maintenance and replacement. In the utility model, the inclination angle of the water distribution device 7 of the expansion bed is preferably freely adjustable, so that the inlet water of the expansion bed forms a rotational flow by adjusting the inclination angle. In the present invention, the sludge hopper 8 is preferably connected to a plurality of sludge discharge pipes 9, and sludge in the hopper can be discharged out of the expanded bed through the sludge discharge pipes 9.
In the treatment system provided by the utility model, a sludge discharge system matched with the anaerobic organism expanded bed is preferably further included, and the sludge discharge system preferably adopts a central barrel sludge discharge mode. In the utility model, a central barrel is connected with a sludge hopper 8 through a plurality of sludge discharge pipes 9, the central barrel can flow in two directions, sludge is discharged from the inside to the outside, and the sludge is washed from the outside to the inside. The sludge discharge mode preferably adopted by the utility model has the advantages of simple pipeline, uniform sludge discharge and no short flow, and the flushing and stirring are started before the sludge discharge, so that the sludge discharge is smooth and no deposition occurs.
In the treatment system provided by the utility model, the main device of the ozone-hydrogen peroxide catalytic oxidation reactor is a three-phase fluidized bed, and a water inlet of the three-phase fluidized bed is connected with a water outlet of the anaerobic biological expansion bed. In the utility model, the three-phase fluidized bed utilizes the thrust of water flow to ensure that the catalyst solid particles, the oxidant (ozone gas/hydrogen peroxide) and the waste liquid are in a fluidized state, and gas-solid-liquid three phases are highly mixed, so that the catalytic oxidation reaction is efficiently carried out, and long-chain organic matters remained in the waste liquid are oxidized and decomposed into short-chain organic matters.
In the treatment system provided by the present invention, as shown in fig. 4, the ozone-hydrogen peroxide solution catalytic oxidation reactor preferably includes: a dissolved air vessel 18 and a three-phase fluidized bed. In the present invention, the dissolved air tank 18 is preferably provided with an ozone inlet, a hydrogen peroxide inlet, a reflux inlet and a dissolved gas-liquid outlet; the tank is preferably filled with a filler; the filler is preferably a porous rotating spherical filler; the diameter of the porous rotary spherical filler is preferably 60-100 mm, and specifically can be 80 mm; the density of the porous rotating spherical filler is preferably 0.8-1.2 g/cm3Specifically, it may be 0.92g/cm3(ii) a The material of the porous rotating spherical filler is preferably polyurethane. In the present invention, the structure of the three-phase fluidized bed preferably includes: a fluidized bed body, a fluidized bed three-phase separator 17, a fluidized bed water inlet, a dissolved gas-liquid inlet, a backflow water outlet, a fluidized bed water outlet and a fluidized bed tail gas outlet, wherein a solid catalyst (namely, catalyst solid particles) is filled in the bed body; wherein, the carrier material of the solid catalyst is preferably a high-strength silicon-aluminum compound; the active components of the solid catalyst are noble metals and transition metals, preferably including 40-50 wt% of MnO, 10-15 wt% of CuO and CeO2 5～10wt％、Al2O3 15～20wt％、SiO2 5～10wt％、TiO23-5 wt%; the bulk density of the solid catalyst is preferably 0.5-1.5 g/mL, and more preferably 0.7-0.9 g/mL; the specific surface area of the solid catalyst is preferably more than or equal to 200m2(ii)/g; the particle size of the solid catalyst is preferably 1-10 mm, and more preferably 3-5 mm; the interior of the reaction bed body is divided into a fluidized bed inner circulation area 15 and a fluidized bed outer circulation area 16 which are communicated by a vertically arranged partition plate; the water inlet of the fluidized bed is positioned at the bottom of the internal circulation area 15 of the fluidized bed, the solution-gas inlet is positioned at the bottom of the fluidized bed body, the three-phase separator 18 of the fluidized bed is positioned above the internal and external circulation areas 15 and 16, the return water outlet is positioned on the side wall of the fluidized bed body between the internal and external circulation areas 15 and 16 and the three-phase separator 18 of the fluidized bed, the water outlet of the fluidized bed is connected with the liquid phase outlet of the three-phase separator 18 of the fluidized bed, and the tail gas outlet of the fluidized bed is connected with the gas phase outlet of the three-phase separator 18 of the fluidized bed; the water outlet end of the water inlet of the fluidized bed is preferably provided with a water inlet spray head 12 so as to improve the inflow velocity and promote the formation of fluidized state in the bed body; the liquid outlet end of the dissolved gas liquid inlet is provided with a fluidized bed water distribution device 13, a dissolved gas releaser 14 is preferably arranged on a water outlet hole of the fluidized bed water distribution device 13, bubbles generated by releasing through the dissolved gas releaser 14 are small in diameter, large in surface contact area and high in strength and are not easy to dissipate, and therefore full contact between ozone and organic pollutants and catalysts is facilitated. In the utility model, a dissolved gas-liquid outlet of a dissolved gas tank 18 is connected with a dissolved gas-liquid inlet of the three-phase fluidized bed, and a reflux water inlet of the dissolved gas tank 18 is connected with a reflux water outlet of the three-phase fluidized bed; when the equipment is operated, the wastewater part treated by catalytic oxidation in the three-phase fluidized bed flows out through the backflow water outlet, enters the pressure gas dissolving tank together with hydrogen peroxide and ozone to form gas solution, and then flows out from the gas solution outlet of the pressure gas dissolving tank and flows back into the three-phase fluidized bed through the backflow water inlet of the three-phase fluidized bed.
In the treatment system provided by the utility model, the gas inlet of the ozone destructor is connected with the tail gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor, more specifically connected with the tail gas outlet of the three-phase fluidized bed; the air outlet of the ozone destructor is connected back to the micro-electrolysis rotating disc reaction bed, more particularly to the reaction bed internal circulation zone 4 of the micro-electrolysis rotating disc reaction bed. In the utility model, the ozone destructor can decompose the ozone tail gas generated by the ozone-hydrogen peroxide catalytic oxidation reactor into oxygen, and the generated oxygen returns to the micro-electrolysis turntable reaction bed, thereby not only playing a role of stirring, but also improving the micro-electrolysis reaction efficiency, promoting the ferrous ions to be converted into the ferric ions and being beneficial to oxidizing organic matters in water.
The utility model also provides a method for processing the membrane concentrated solution in the processing system in the technical scheme, which comprises the following steps:
and conveying the membrane concentrated solution to the membrane concentrated solution treatment system, allowing the membrane concentrated solution to flow through the pH adjustment equipment to complete the pH value adjustment, sequentially entering the micro-electrolysis turntable reaction bed, the anaerobic biological expansion bed and the ozone-hydrogen peroxide catalytic oxidation reactor for treatment, and obtaining the treated membrane concentrated solution at a water outlet of the ozone-hydrogen peroxide catalytic oxidation reactor.
In the treatment method provided by the utility model, in the operation process of the system, the hydraulic effective retention time of the membrane concentrated solution in the micro-electrolysis turntable reaction bed is 20-90 min, and specifically can be 30min, 42min or 60 min.
In the treatment method provided by the utility model, during the operation of the system, the oxygen concentration of the anaerobic organism expanded bed is preferably 0; the concentration of suspended solids (MLSS) of mixed liquid of anaerobic sludge in the anaerobic biological expanded bed is preferably 10000-50000 mg/L, and specifically 30000 mg/L; the ratio (MLVSS/MLSS) of the concentration of the volatile suspended solids of the mixed liquor of the anaerobic sludge in the anaerobic biological expanded bed to the concentration of the suspended solids of the mixed liquor is preferably 0.6-0.9, and specifically can be 0.75.
In the treatment method provided by the utility model, in the operation process of the system, the hydraulic effective retention time of the waste water treated by the micro-electrolysis rotating disc reaction bed in the anaerobic biological expansion bed is preferably 1-5 h, and specifically can be 1.8h, 2h or 3 h.
In the treatment method provided by the utility model, the ozone-dioxygen is generated during the operation of the systemThe concentration of ozone in a dissolved air tank of the water catalytic oxidation reactor is preferably 20-40 wt%, specifically 30 wt%, and H2O2The concentration is preferably 0.5 to 2 wt%, and specifically may be 1 wt%.
In the treatment method provided by the utility model, in the operation process of the system, the return flow of the wastewater of the three-phase fluidized bed of the ozone-hydrogen peroxide catalytic oxidation reactor is preferably 20-40% of the water inflow, and particularly can be 30%.
In the treatment method provided by the utility model, in the operation process of the system, the hydraulic effective retention time of the post-wastewater treated by the anaerobic biological expanded bed in the three-phase fluidized bed of the ozone-hydrogen peroxide catalytic oxidation reactor is preferably 30-120 min, and specifically can be 60min, 80min or 90 min.
According to the technical scheme provided by the utility model, the micro-electrolysis rotating disc reaction bed and the anaerobic biological expansion bed are used as the pretreatment process of the ozone-hydrogen peroxide catalytic oxidation three-phase fluidized bed, so that part of organic matters are degraded in advance, and the organic matters which are most difficult to degrade are left in the pretreatment process by using the ozone degradation, so that the utilization efficiency of ozone is improved, and the ozone consumption is saved; and compared with the single catalytic ozone technology, the energy consumption of the micro-electrolysis rotating disc reaction bed and the anaerobic organism expansion bed is lower than that of an ozone-hydrogen peroxide catalytic oxidation three-phase fluidized bed, so that the whole operation treatment cost is reduced, and the oxidation efficiency of catalytic ozone is improved. The technical scheme provided by the utility model has the advantages of short treatment process flow, difficulty in hardening and blocking of the micro-electrolysis filler, high oxidation efficiency and low operation cost, the treated membrane concentrated solution basically does not contain long-chain organic matters which are difficult to degrade, the subsequent biochemical treatment can be directly carried out to realize reduction, and the membrane concentrated solution has good environmental benefit and economic benefit. More specifically, the technical scheme provided by the utility model has the following advantages:
1) baffles with different intervals are preferably arranged on two sides of a micro-electrolysis turntable in the micro-electrolysis turntable reaction bed, and when water enters, the micro-electrolysis turntable rotates due to different water flow thrust on two sides of the turntable, so that micro-electrolysis filler is mixed with organic matters in wastewater more fully, and the problems of hardening and blocking of the micro-electrolysis filler, low solid-liquid mass transfer efficiency and the like are solved.
2) The micro-electrolysis turntable and the micro-electrolysis turntable reaction bed body are preferably detachably fixed, and the filler is more convenient to replace.
3) The anaerobic biological expansion bed is arranged between the micro-electrolysis turntable reaction bed and the ozone-hydrogen peroxide catalytic oxidation reactor, and ferric ions and ferrous ions generated by effluent of the micro-electrolysis turntable reaction bed are used as trace elements for culturing anaerobic granular sludge, so that a flocculation precipitation device and precipitate treatment are omitted, and the operation cost of the whole process is reduced.
4) The top of the anaerobic biological expansion bed is preferably provided with a three-phase separator, so that the gas-solid-liquid three-phase effective separation is ensured, and the anaerobic granular sludge is prevented from being brought into the ozone-hydrogen peroxide catalytic oxidation reactor.
5) The main device of the ozone-hydrogen peroxide catalytic oxidation reactor is a three-phase fluidized bed, so that solid particles of a catalyst, ozone gas and sewage are in a fluidized state, and gas, solid and liquid phases are highly mixed, so that the catalytic oxidation efficiency is improved; meanwhile, by introducing hydrogen peroxide, the catalytic oxidation efficiency is further improved.
6) The dissolved gas releaser is preferably arranged at the dissolved gas liquid inlet of the three-phase fluidized bed, bubbles generated by the release of the dissolved gas releaser have small diameter, large surface contact area and high strength, are not easy to dissipate, and are more favorable for fully contacting the ozone with organic matters and catalysts in wastewater.
7) The top of the three-phase fluidized bed is preferably provided with a three-phase separator, so that the gas-solid-liquid three-phase is effectively separated, and the loss of solid particles of the catalyst is avoided.
8) Oxygen generated by the ozone destructor is introduced into the micro-electrolysis turntable reaction bed, so that the reaction efficiency of the micro-electrolysis turntable reaction bed is improved, ferrous ions are promoted to be converted into ferric ions and organic matters in water are oxidized, and the stirring effect is achieved.
For the sake of clarity, the following examples are given in detail.
Example 1
In this embodiment, a membrane concentrate processing system is provided, as shown in fig. 1, the system includes: the device comprises a pH adjusting device, a micro-electrolysis turntable reaction bed, an anaerobic organism expansion bed, an ozone-hydrogen peroxide catalytic oxidation reactor and an ozone destructor; wherein the pH adjusting device is a pipeline mixer, the specific structures of the micro-electrolysis turntable reaction bed, the anaerobic organism expansion bed and the ozone-hydrogen peroxide catalytic oxidation reactor are shown in figures 2-4, the water outlet of the pH adjusting device is connected with the water inlet of the micro-electrolysis turntable reaction bed, the water outlet of the micro-electrolysis turntable reaction bed is connected with the water inlet of the anaerobic biological expansion bed, the water outlet of the anaerobic organism expanded bed is connected with the water inlet of the ozone-hydrogen peroxide catalytic oxidation reactor, the air inlet of the ozone destructor is connected with the tail gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor, the gas outlet of the ozone destructor is connected back to the micro-electrolysis turntable reaction bed, and the water outlet of the ozone-hydrogen peroxide catalytic oxidation reactor is connected with a downstream biochemical treatment system.
In this embodiment, as shown in fig. 2, the micro-electrolysis rotating disc reaction bed comprises: a reaction bed water distribution device 1 (specifically a perforated water distribution pipe), a micro-electrolysis turntable baffle 2, a micro-electrolysis turntable 3, a reaction bed internal circulation zone 4, a reaction bed external circulation zone 5 and a reaction bed water outlet zone 6; the micro-electrolysis rotating disc 3 is filled with iron-carbon filler which adopts a micro-pore framework type alloy structure (the specific gravity is 1.5 t/m)378 wt% of iron, 12 wt% of carbon, 10 wt% of Pt as a noble metal catalyst, and 1.3m of specific surface area2G, porosity of 72%, physical strength of 650kg/m or more2) The total amount of the packing in the reaction bed was 1.5 t. When the equipment is operated, the membrane concentrated solution is added with acid through a pipeline mixer to adjust the pH value and then is lifted to a reaction bed water distribution device 1 of the micro-electrolysis turntable reaction bed, when the membrane concentrated solution rises to a micro-electrolysis turntable baffle 2, the micro-electrolysis turntable 3 is pushed to rotate by using water flow thrust on two sides of the baffle, so that the micro-electrolysis filler and the organic wastewater are fully mixed, meanwhile, oxygen is introduced into an inner circulation zone 4 of the reaction bed after the tail gas of the ozone-hydrogen peroxide catalytic oxidation reactor is recovered, and the self inner circulation is realized by using the density difference between the inner circulation zone and an outer circulation zone.
In this embodiment, as shown in fig. 3, the expanded bed water distributor 7 (specifically, a perforated water distributor), a sludge hopper 8 and a sludge discharge pipe 9 are disposed at the bottom of the expanded bed of anaerobic organism, the middle is an expansion zone 10, and the top is an expanded bed three-phase separator 11. When the equipment is operated, ferric ions and ferrous ions generated by the micro-electrolysis turntable reaction bed are used as trace elements for culturing anaerobic granular sludge, organic matters which are difficult to degrade in water are further decomposed into short-chain organic matters which are easy to degrade through hydrolytic acidification bacteria in the anaerobic granular sludge, and the gas-solid-liquid three-phase effective separation is realized through a top three-phase separator.
In this embodiment, as shown in fig. 4, the ozone-hydrogen peroxide catalytic oxidation reactor includes a three-phase fluidized bed and a dissolved air tank 18; wherein, the dissolved air tank 18 is filled with filler which adopts porous rotary spherical filler (diameter phi 80, material is polyurethane, density is 0.92 g/cm)3) The loading amount is 0.4 t; a water inlet spray head 12, a fluidized bed water distribution device 13, a dissolved gas releaser 14, a fluidized bed internal circulation zone 15, a fluidized bed external circulation zone 16 and a fluidized bed three-phase separator 17 are arranged in the three-phase fluidized bed, and a reflux water outlet is arranged at the lower part of the fluidized bed three-phase separator 18; the three-phase fluidized bed is filled with catalyst solid particles, the catalyst solid particles adopt a high-strength silicon-aluminum compound as a carrier, and various precious metals and transition metals (specifically including 40-50 wt% of MnO, 10-15 wt% of CuO and CeO) are loaded on the carrier 2 5～10wt％、Al2O3 15～20wt％、SiO 2 5～10wt％、TiO23-5 wt%), and the loading is 3.5 t. When the equipment is operated, part of the treated wastewater in the fluidized bed flows out through the return water outlet, enters the pressure dissolved gas tank 18 together with hydrogen peroxide and ozone to form dissolved gas liquid, and then flows out from the dissolved gas liquid outlet of the pressure dissolved gas tank and is released into the three-phase fluidized bed through the dissolved gas releaser 14.
Example 2
Nanofiltration membrane concentrated solution 120m produced in the treatment process of waste penetrating fluid of certain waste incineration plant3D: COD is 2050mg/L, BOD5420mg/L, 6mg/L ammonia nitrogen, 155mg/L total nitrogen and 10000mg/L TDS.
The processing system provided by the embodiment 1 of the utility model is adopted for processing, and the specific process comprises the following steps: the nanofiltration membrane concentrated solution is lifted to a pipeline mixer by a pump and is passed through sulfuric acidPumping sulfuric acid into a pipeline mixer by a metering pump, adjusting the pH to 5.0-6.0, and then introducing the sulfuric acid into a micro-electrolysis turntable reaction bed for oxidation treatment, wherein the hydraulic effective retention time of wastewater in the micro-electrolysis turntable reaction bed is 60 min; during treatment, uniform water distribution is realized through the reaction bed water distribution device 1; the interior of the micro-electrolysis turntable reaction bed is provided with a plurality of layers of micro-electrolysis turntable baffles 2, and the micro-electrolysis turntable 3 is pushed to rotate by water flow thrust, so that the iron-carbon filler is fully mixed with organic matters in the wastewater; the self liquid flow circulation is realized by utilizing the density difference between the inner circulation zone 4 of the reaction bed and the outer circulation zone 5 of the reaction bed. The effluent of the micro-electrolysis reaction bed is lifted to an expansion bed water distribution device 7 in an anaerobic biological expansion bed by a pump through a reaction bed water outlet area 6, microorganisms attached to anaerobic granular sludge in an expansion area 10 are fully mixed with organic matters in wastewater, long-chain organic matters which cannot be degraded by the micro-electrolysis turntable reaction bed in the wastewater are further decomposed into short-chain organic matters, the oxygen concentration of the anaerobic biological expansion bed is 0, the anaerobic sludge MLSS is 30050mg/L, MLVSS/MLSS which is 0.75, the hydraulic effective retention time of the anaerobic biological expansion bed is 3 hours, and after full reaction, the three-phase separator 11 of the expansion bed realizes the effective separation of gas, solid and liquid phases, so that the anaerobic biological expansion bed has certain biomass, and higher volume load is realized. The effluent treated by the anaerobic biological expansion bed flows into a three-phase fluidized bed, high-speed jet flow is realized through a water inlet spray head 12, meanwhile, the effluent subjected to catalytic oxidation in the three-phase fluidized bed flows out from a water return outlet (the return flow of the wastewater is 30 percent of the water inlet), the effluent enters a pressure dissolved air tank 18 together with hydrogen peroxide and ozone (the concentrations of ozone and hydrogen peroxide in the dissolved air are respectively controlled at 30 percent by weight and 1 percent by weight), the effluent in the pressure dissolved air tank 18 is lifted to a fluidized bed water distribution device 13 by a pump, dissolved air releasers 14 are uniformly arranged on the fluidized bed water distribution device 13, and the ozone and H generated by the release of the dissolved air releasers 142O2The catalyst is fully contacted with organic matters and catalysts in the wastewater to generate catalytic oxidation reaction; meanwhile, the liquid flow circulation of the fluidized bed is realized by utilizing the density difference between the internal circulation zone 15 of the fluidized bed and the external circulation zone 16 of the fluidized bed; the top of the three-phase fluidized bed is provided with a fluidized bed three-phase separator 17, which ensures the effective separation of gas, solid and liquid phases and avoids the loss of solid particles of the catalyst; wastewater passes through the three-phase flowAnd carrying out catalytic oxidation reaction in the fluidized bed, further oxidizing and decomposing the residual long-chain organic matters into short-chain organic matters, wherein the hydraulic effective retention time of the wastewater in the three-phase fluidized bed is 90 min. Ozone tail gas generated by the three-phase fluidized bed enters an ozone destructor for treatment, and generated oxygen returns to an internal circulation zone 4 of the micro-electrolysis rotating disc reaction bed.
After the treatment of the system, the long-chain organic matters which are difficult to degrade in the membrane concentrated solution are basically converted into short-chain organic matters which are easy to degrade, and the final effluent quality of the three-phase fluidized bed is as follows: COD is 1230mg/L, BOD is 482mg/L, TDS is 8030mg/L, and treatment cost is 12.8 yuan/m3. The effluent can be subsequently returned to a biochemical system of a percolate treatment station for biochemical treatment again, and finally the decrement of the membrane concentrated solution is realized.
Example 3
170m reverse osmosis membrane concentrated solution produced in garbage penetrating fluid treatment process of certain garbage incineration plant3D: COD 806mg/L, BOD5153mg/L, 12mg/L ammonia nitrogen, 210mg/L total nitrogen and 20060mg/L TDS.
The processing system provided by the embodiment 1 of the utility model is adopted for processing, and the specific process comprises the following steps: the nanofiltration membrane concentrated solution is lifted to a pipeline mixer by a pump, sulfuric acid is pumped into the pipeline mixer by a sulfuric acid metering pump, the pH is adjusted to 5.0-6.0, then the obtained product enters a micro-electrolysis turntable reaction bed for oxidation treatment, and the hydraulic effective retention time of the wastewater in the micro-electrolysis turntable reaction bed is 30 min; during treatment, uniform water distribution is realized through the reaction bed water distribution device 1; the interior of the micro-electrolysis turntable reaction bed is provided with a plurality of layers of micro-electrolysis turntable baffles 2, and the micro-electrolysis turntable 3 is pushed to rotate by water flow thrust, so that the iron-carbon filler is fully mixed with organic matters in the wastewater; the self liquid flow circulation is realized by utilizing the density difference between the inner circulation zone 4 of the reaction bed and the outer circulation zone 5 of the reaction bed. The effluent of the micro-electrolysis reaction bed is pumped to an expansion bed water distribution device 7 in an anaerobic biological expansion bed through a reaction bed effluent area 6, microorganisms attached to anaerobic granular sludge in an expansion area 10 are fully mixed with organic matters in the wastewater, long-chain organic matters which are not degraded by the micro-electrolysis turntable reaction bed in the wastewater are further decomposed into short-chain organic matters, and the anaerobic biological expansion bedThe oxygen concentration of the anaerobic sludge is 0, the anaerobic sludge MLSS is 30040mg/L, MLVSS/MLSS which is 0.75, the hydraulic effective retention time of the anaerobic biological expanded bed is 2 hours, the gas, solid and liquid three-phase effective separation is realized through the expanded bed three-phase separator 11 after the full reaction, a certain biomass of the anaerobic biological expanded bed is ensured, and a higher volume load is realized. The effluent treated by the anaerobic biological expansion bed flows into a three-phase fluidized bed, high-speed jet flow is realized through a water inlet spray head 12, meanwhile, the effluent subjected to catalytic oxidation in the three-phase fluidized bed flows out from a water return outlet (the return flow of the wastewater is 30 percent of the water inlet), the effluent enters a pressure dissolved air tank 18 together with hydrogen peroxide and ozone (the concentrations of ozone and hydrogen peroxide in the dissolved air are respectively controlled at 30 percent by weight and 1 percent by weight), the effluent in the pressure dissolved air tank 18 is lifted to a fluidized bed water distribution device 13 by a pump, dissolved air releasers 14 are uniformly arranged on the fluidized bed water distribution device 13, and the ozone and H generated by the release of the dissolved air releasers 142O2The catalyst is fully contacted with organic matters and catalysts in the wastewater to generate catalytic oxidation reaction; meanwhile, the liquid flow circulation of the fluidized bed is realized by utilizing the density difference between the fluidized bed internal circulation zone 15 and the fluidized bed external circulation zone 16; the top of the three-phase fluidized bed is provided with a fluidized bed three-phase separator 17, which ensures the effective separation of gas, solid and liquid phases and avoids the loss of solid particles of the catalyst; the waste water is subjected to catalytic oxidation reaction in the three-phase fluidized bed, the residual long-chain organic matters are further oxidized and decomposed into short-chain organic matters, and the hydraulic effective retention time of the waste water in the three-phase fluidized bed is 60 min. Ozone tail gas generated by the three-phase fluidized bed enters an ozone destructor for treatment, and generated oxygen returns to an internal circulation zone 4 of the micro-electrolysis rotating disc reaction bed.
After the treatment of the system, the long-chain organic matters which are difficult to degrade in the membrane concentrated solution are basically converted into short-chain organic matters which are easy to degrade, and the final effluent quality of the three-phase fluidized bed is as follows: COD 508mg/L, BOD 210mg/L, TDS 15030mg/L, and treatment cost 7.51 yuan/m3. The effluent can be subsequently returned to a biochemical system of a percolate treatment station for biochemical treatment again, and finally the decrement of the membrane concentrated solution is realized.
Example 4
Nanofiltration and nanofiltration produced in the treatment process of refuse leachate of certain refuse incineration plantMixed concentrated solution of reverse osmosis membrane concentrated water of 200m3D: COD is 1310mg/L, BOD5223mg/L of ammonia nitrogen, 12mg/L of total nitrogen, 253mg/L of total nitrogen and 13050mg/L of TDS.
The processing system provided by the embodiment 1 of the utility model is adopted for processing, and the specific process comprises the following steps: the concentrated solution is lifted to a pipeline mixer by a pump, sulfuric acid is pumped into the pipeline mixer through a sulfuric acid metering pump, the pH is adjusted to 5.0-6.0, then the concentrated solution enters a micro-electrolysis turntable reaction bed for oxidation treatment, and the hydraulic effective retention time of the wastewater in the micro-electrolysis turntable reaction bed is 42 min; during treatment, uniform water distribution is realized through the reaction bed water distribution device 1; a plurality of layers of micro-electrolysis turntable baffles 2 are arranged in the micro-electrolysis turntable reaction bed, and the micro-electrolysis turntable 3 is pushed to rotate by water flow thrust, so that the iron-carbon filler is fully mixed with organic matters in the wastewater; the self liquid flow circulation is realized by utilizing the density difference between the inner circulation zone 4 of the reaction bed and the outer circulation zone 5 of the reaction bed. The effluent of the micro-electrolysis reaction bed is lifted to an expansion bed water distribution device 7 in an anaerobic biological expansion bed by a pump through a reaction bed water outlet area 6, microorganisms attached to anaerobic granular sludge in an expansion area 10 are fully mixed with organic matters in wastewater, long-chain organic matters which cannot be degraded by the micro-electrolysis turntable reaction bed in the wastewater are further decomposed into short-chain organic matters, the oxygen concentration of the anaerobic biological expansion bed is 0, the anaerobic sludge MLSS is 30020mg/L, MLVSS/MLSS which is 0.75, the hydraulic effective retention time of the anaerobic biological expansion bed is 1.8h, and after full reaction, the three-phase separator 11 of the expansion bed realizes the effective separation of gas, solid and liquid phases, so that the anaerobic biological expansion bed has certain biomass, and higher volume load is realized. The effluent treated by the anaerobic biological expansion bed flows into a three-phase fluidized bed, high-speed jet flow is realized through a water inlet spray head 12, meanwhile, the effluent subjected to catalytic oxidation in the three-phase fluidized bed flows out from a water return outlet (the return flow of the wastewater is 30 percent of the water inlet), the effluent enters a pressure dissolved air tank 18 together with hydrogen peroxide and ozone (the concentrations of ozone and hydrogen peroxide in the dissolved air are respectively controlled at 30 percent by weight and 1 percent by weight), the effluent in the pressure dissolved air tank 18 is lifted to a fluidized bed water distribution device 13 by a pump, dissolved air releasers 14 are uniformly arranged on the fluidized bed water distribution device 13, and the ozone and H generated by the release of the dissolved air releasers 142O2And is mixed with wasteOrganic matters in water are fully contacted with the catalyst to generate catalytic oxidation reaction; meanwhile, the liquid flow circulation of the fluidized bed is realized by utilizing the density difference between the internal circulation zone 15 of the fluidized bed and the external circulation zone 16 of the fluidized bed; the top of the three-phase fluidized bed is provided with a fluidized bed three-phase separator 17, so that the gas-solid-liquid three-phase is effectively separated, and the loss of solid particles of the catalyst is avoided; the waste water is subjected to catalytic oxidation reaction in the three-phase fluidized bed, the residual long-chain organic matters are further oxidized and decomposed into short-chain organic matters, and the hydraulic effective retention time of the waste water in the three-phase fluidized bed is 80 min. Ozone tail gas generated by the three-phase fluidized bed enters an ozone destructor for treatment, and generated oxygen returns to an internal circulation zone 4 of the micro-electrolysis rotating disc reaction bed.
After the treatment of the system, the long-chain organic matters which are difficult to degrade in the membrane concentrated solution are basically converted into short-chain organic matters which are easy to degrade, and the final effluent quality of the three-phase fluidized bed is as follows: COD is 1030mg/L, BOD is 420mg/L, TDS is 11060mg/L, and treatment cost is 10.8 yuan/m3. The effluent can be subsequently returned to a biochemical system of a percolate treatment station for biochemical treatment again, and finally the decrement of the membrane concentrated solution is realized.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (9)
1. A membrane concentrate treatment system, comprising:
a pH adjusting device;
the micro-electrolysis turntable reaction bed is connected with the water outlet of the pH adjusting device, and iron carbon filler is filled in a micro-electrolysis turntable of the micro-electrolysis turntable reaction bed;
the anaerobic biological expansion bed is connected with a water outlet of the micro-electrolysis turntable reaction bed;
the ozone-hydrogen peroxide catalytic oxidation reactor is connected with a water outlet of the anaerobic biological expansion bed, and a main device of the ozone-hydrogen peroxide catalytic oxidation reactor is a three-phase fluidized bed;
and the gas outlet of the ozone-hydrogen peroxide catalytic oxidation reactor is connected to the micro-electrolysis turntable reaction bed.
2. The membrane concentrate treatment system of claim 1, wherein the pH adjustment device is a line mixer having a pH adjuster dosing port disposed thereon.
3. The membrane concentrate treatment system of claim 1, wherein the micro-electrolytic rotating disc reaction bed comprises: the device comprises a reaction bed body, a plurality of micro-electrolysis rotating discs, a reaction bed water inlet and a reaction bed water outlet;
the interior of the reaction bed body is divided into an inner circulation area and an outer circulation area which are communicated by a vertically arranged partition plate; the water inlet of the reaction bed is positioned at the bottom of the internal circulation area, and the water outlet of the reaction bed is positioned at the top of the reaction bed body; the micro-electrolysis rotating discs are positioned above the water inlet of the reaction bed and are longitudinally arranged in the internal circulation area.
4. The membrane concentrate treatment system of claim 3, wherein each of the microelectrolytic disks is provided with baffles on both axial sides, and the baffles on both sides are spaced at different intervals from the corresponding microelectrolytic disk.
5. The membrane concentrate treatment system of claim 3, wherein the micro-electrolysis turntable is removably secured to the reaction bed.
6. The membrane concentrate treatment system of claim 1, wherein the anaerobic bio-expanded bed comprises: the system comprises an expansion zone, a three-phase separator, a sludge hopper, an expansion bed water inlet and an expansion bed water outlet;
the expansion zone is positioned in the middle section of the expansion bed, the water inlet of the expansion bed is positioned below the expansion zone, the three-phase separator is positioned above the expansion zone, and the water outlet of the expansion bed is connected with the liquid phase outlet of the three-phase separator; the sludge hopper is positioned at the bottom of the expansion bed.
7. The membrane concentrate treatment system of claim 1, wherein the outlet end of the inlet of the expanded bed is fitted with a pluggable water distribution device.
8. The membrane concentrate treatment system of claim 1, wherein the ozone-hydrogen peroxide catalytic oxidation reactor comprises: a dissolved air tank and a three-phase fluidized bed;
the dissolved air tank is provided with an ozone inlet, a hydrogen peroxide inlet, a backflow water inlet and a dissolved air liquid outlet, and filling materials are filled in the tank;
the three-phase fluidized bed comprises: the fluidized bed comprises a fluidized bed body, a three-phase separator, a fluidized bed water inlet, a dissolved gas-liquid inlet, a backflow water outlet, a fluidized bed water outlet and a fluidized bed tail gas outlet, wherein a solid catalyst is filled in the bed body; the interior of the fluidized bed body is divided into an inner circulation area and an outer circulation area which are communicated by a vertically arranged partition plate; the fluidized bed is characterized in that a water inlet of the fluidized bed is positioned at the bottom of the internal circulation zone, a dissolved gas-liquid inlet is positioned at the bottom of the fluidized bed body, the three-phase separator is positioned above the internal and external circulation zones, a backflow water outlet is positioned on the side wall of the fluidized bed body between the internal and external circulation zones and the three-phase separator, a water outlet of the fluidized bed is connected with a liquid phase outlet of the three-phase separator, and a tail gas outlet of the fluidized bed is connected with a gas phase outlet of the three-phase separator;
and a dissolved gas-liquid outlet of the dissolved gas tank is connected with a dissolved gas-liquid inlet of the three-phase fluidized bed, and a backflow water inlet of the dissolved gas tank is connected with a backflow water outlet of the three-phase fluidized bed.
9. The membrane concentrate treatment system of claim 8, wherein a water distribution device is installed at the liquid outlet end of the dissolved gas liquid inlet, and a dissolved gas releaser is installed on the water outlet hole of the water distribution device.
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| CN114133118B (en) * | 2021-12-31 | 2024-03-08 | 福建龙净环保股份有限公司 | Membrane concentrate treatment system and treatment method |
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