CN212632303U - Immersed membrane assembly - Google Patents
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- CN212632303U CN212632303U CN202021500140.2U CN202021500140U CN212632303U CN 212632303 U CN212632303 U CN 212632303U CN 202021500140 U CN202021500140 U CN 202021500140U CN 212632303 U CN212632303 U CN 212632303U
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Abstract
The utility model provides an immersion type membrane module, which belongs to the technical field of water treatment. The outer water collecting tank is annular; the central water collecting pipe is positioned in the middle of the outer water collecting tank; the membrane filaments are multiple in number, one end of each membrane filament is fixed on the central water collecting pipe, the other end of each membrane filament is fixed on the outer side water collecting groove, and a channel in the membrane filament is communicated with the outer side water collecting groove fixed on the outer side water collecting groove; the connecting pipes are multiple in number, one end of each connecting pipe is connected to the outer water collecting tank, the other end of each connecting pipe is connected to the central water collecting pipe, and the grooves of the outer water collecting tanks are communicated with the central water collecting pipe through the connecting pipes; the rotatable water producing pipe is connected to the central water collecting pipe and is used for collecting water produced by the internal channel of the membrane yarn; the driving mechanism is used for driving the whole outer side water collecting tank to rotate through the central water collecting pipe; and the support frames are connected to two ends of the central water collecting pipe and used for supporting the membrane component. Can effectively prevent the sludge from accumulating in a large amount at the root of the lower end.
Description
Technical Field
The utility model relates to an immersion type membrane module belongs to water treatment technical field.
Background
With the sustainable development of economy in China, the oil and the finished products thereof play more and more important roles in various fields of industry and agriculture. A large amount of oily wastewater is generated in the processes of oil exploitation, processing, transportation and utilization, and the oily wastewater has high yield and wide pollution range and causes great harm to the ecological environment. Therefore, the treatment of oily wastewater in an efficient and environment-friendly manner is an urgent technical problem to be solved. In the monitoring and analysis of wastewater quality in China, Chemical Oxygen Demand (COD) is a very important index for evaluating the pollution degree of water. The larger the COD value is, the more reducing substances in the water are, the oxygen content in the water is reduced, and the oxygen-deficient death of aquatic organisms is caused, so that the ecological environment is destroyed. Benzene series has strong toxicity of organic matters and can cause direct or indirect damage to aquatic animals, plants and human beings. China takes COD as an index for controlling the discharge of pollutants by each unit.
In many oil recovery effluents, inorganic salts are present in large quantities, which on the one hand interfere with the proper operation of the treatment process and on the other hand have a severe effect on the effluent discharge.
The biological method for treating the oily wastewater is to remove partial organic matters in the oily wastewater while utilizing the self metabolism of microorganisms, thereby achieving the effect of purifying the wastewater. The aerobic biological treatment technology is to utilize the aerobic characteristic of microbes to oxygenate oily waste water to increase the dissolved oxygen content in the oily waste water, so as to degrade organic oily waste water. Compared with a biological chemical method, the digestion efficiency is very high, but the use cost is relatively low, and secondary pollution to the environment is avoided. In biological treatment, MBR is one of the main treatment means, and generally, treated wastewater is obtained by sucking the treated wastewater in a negative pressure manner in real time through a module composed of hollow fiber membrane filaments while performing aerobic reaction. However, most of the immersed membrane assemblies on the market are vertically suspended and installed in a curtain or column mode, and a large amount of sludge is easily accumulated at the root parts of membrane filaments at the lower ends of the assemblies due to the action of gravity in the long-term use process. On one hand, the phenomenon can cause the weight of the component to be increased, the load of a supporting part to be increased, and the membrane shell to be broken when the component is cleaned and hoisted off line in the filtering process; on the other hand, aeration effect is easily weakened, membrane pollution is aggravated, water yield is reduced, a user needs to clean the membrane component at high frequency, so that the risk of membrane component damage is increased, the operation cost is increased, the economy of the membrane component is seriously affected, and the economy of the technology is reduced to a certain extent. Therefore, the development of a radial immersed membrane module for preventing the large accumulation of sludge at the root and a preparation method thereof have important significance for widening the industrial application range of the organic hollow fiber membrane module.
SUMMERY OF THE UTILITY MODEL
The utility model provides a first technical problem be: in the process of treating high COD wastewater containing oil and inorganic salt, no better integrated treatment means exists in the prior art.
The utility model provides a second technical problem be: the existing immersed membrane component accumulates a large amount of sludge at the root in the operation process, and the radial immersed membrane component and the preparation method thereof are provided, so that the consequences of component weight increase, aeration weakening and membrane pollution aggravation caused by the large amount of accumulation of sludge at the root of the lower end can be effectively prevented, and an important method is provided for ensuring the long-term stable operation of products.
A treatment device for high COD wastewater comprises:
the sedimentation tank is used for performing pre-filtration treatment on the high-COD wastewater;
the air flotation tank is connected with the sedimentation tank and used for carrying out air flotation oil removal treatment on the filtrate obtained by the sedimentation tank;
the flocculation tank is connected with the air flotation tank and is used for degrading the wastewater obtained in the air flotation tank;
the solid-liquid separator is connected with the flocculation tank and is used for carrying out solid-liquid separation treatment on the produced water obtained in the flocculation tank;
the anaerobic reaction tank is connected with the solid-liquid separator and is used for carrying out anaerobic degradation treatment on the produced water of the solid-liquid separator;
the anaerobic reaction tank is connected with the anaerobic reaction tank and is used for carrying out anaerobic degradation treatment on the wastewater obtained in the anaerobic reaction tank;
the MBR reaction tank is connected with the anoxic reaction tank and is used for carrying out MBR aerobic degradation and filtration treatment on the wastewater obtained in the anoxic reaction tank;
the electrodialyzer is connected to the permeation side in the MBR reaction tank and is used for performing electrodialysis treatment on the filtrate in the MBR reaction tank;
the evaporator is connected with the concentrated solution obtained in the electrodialyzer to carry out evaporative crystallization so as to obtain recovered salt;
and the dryer is connected to the bottom of the MBR reaction tank and is used for drying the sludge obtained in the MBR reaction tank.
And the dryer is connected to the bottom of the MBR reaction tank and is used for drying the sludge obtained in the MBR reaction tank.
In one embodiment, the solid-liquid separator is a media filter, and may be one of a porous ceramic filter, a quartz sand filter, or a manganese sand filter.
In one embodiment, the hollow fiber membranes are used in the MBR reaction tank.
In one embodiment, the hollow fiber membrane has a pore size in the range of 20 to 500 nm.
In one embodiment, the fresh water side of the electrodialyser is connected to a water producing basin.
Install the submerged membrane module in the MBR reaction tank described above, include:
the outer water collecting tank is annular;
the central water collecting pipe is positioned in the middle of the outer water collecting tank;
the membrane filaments are multiple in number, one end of each membrane filament is fixed on the central water collecting pipe, the other end of each membrane filament is fixed on the outer side water collecting groove, and a channel in the membrane filament is communicated with the outer side water collecting groove fixed on the outer side water collecting groove;
the connecting pipes are multiple in number, one end of each connecting pipe is connected to the outer water collecting tank, the other end of each connecting pipe is connected to the central water collecting pipe, and the grooves of the outer water collecting tanks are communicated with the central water collecting pipe through the connecting pipes;
the rotatable water producing pipe is connected to the central water collecting pipe and is used for collecting water produced by the internal channel of the membrane yarn;
the driving mechanism is used for driving the whole outer side water collecting tank to rotate through the central water collecting pipe;
and the support frames are connected to two ends of the central water collecting pipe and used for supporting the membrane component.
In one embodiment, the drive mechanism rotates the central manifold via a chain.
In one embodiment, a plurality of outboard sump sidewall interfaces are provided on an exterior of the outboard sump, the outboard sump sidewall interfaces communicating with the outboard sump groove.
In one embodiment, the number of outboard sump side wall interfaces is 3-8.
In one embodiment, the connector is connected to the outboard sump sidewall interface.
In one embodiment, the central header is located at the center of the outer header and perpendicular to the plane of the outer header, and the top projection of the outer header is located at the centerline of the central header.
In one embodiment, the membrane filaments are in the outer header groove and secured between the outer portion of the membrane filaments and the outer header groove by a hard potting adhesive.
In one embodiment, the periphery of the central water collecting pipe is provided with a central water collecting pipe groove, the ends of the membrane wires are arranged in the central water collecting pipe groove, and the outer parts of the membrane wires and the central water collecting pipe groove are fixed through hard pouring sealant.
In one embodiment, the membrane filaments are external pressure type hollow fiber membrane filaments, internal pressure type hollow fiber membrane filaments, self-supporting hollow fiber membrane filaments, hollow fiber membrane filaments with an inner liner tube, or hollow fiber membrane filaments with internal reinforcing ribs.
In one embodiment, the membrane filaments are divided into a plurality of bundle-like strands, each strand forming a fan-like shape with respect to each other.
The manufacturing method of the immersed membrane module comprises the following steps:
step one, manufacturing a membrane wire pre-glue casting block, coating hole blocking media on the end parts of 600 membrane wires of 200-; the hole plugging medium is a substance which can be solidified at normal temperature, such as polyvinyl alcohol or paraffin;
placing a film wire with one end provided with a blocked hole in a glue casting mold, and tidying, wherein the glue casting mold is only provided with an opening at the upper end, the bottom of the glue casting mold is provided with a glue filling opening, the cavity structure of the glue casting mold can be a cuboid, a cylinder or a prism, the material of the glue casting mold can be metal or plastic, and before the film wire is placed, the inner wall of the mold is coated with a proper amount of release agent;
pouring the hard pouring sealant from the bottom, wherein the pouring height is 7-10cm away from the bottom end of the membrane wire, and standing until the hard pouring sealant is cured, wherein the hard pouring sealant can be epoxy resin, polyurethane and the like;
slowly pouring the soft pouring sealant from the opening of the mold to a depth of 1-3cm, and standing until the soft pouring sealant is cured, wherein the soft pouring sealant can be epoxy resin, polyurethane and the like;
one end of the cured membrane wire pre-glue casting block is slowly removed from the mold, and hard glue with the thickness of 1-3cm at the end part is cut off to open the inner hole of the membrane wire to form a water flow channel;
step six, reversing the pre-glued casting block, and preparing the other end according to the same steps;
bonding one end of the pre-glue cast block with the outer side water collecting groove and the central water collecting pipe groove one by one, and sequentially rotating the other end by 90 degrees to bond with the opposite central water collecting pipe groove one by one, and bonding all the pre-glue cast blocks with the outer side water collecting groove and the central water collecting pipe groove according to the step;
step eight, connecting one end of the connecting pipe with the side wall interface of the outer side water collecting tank, and connecting the other end of the connecting pipe with the end interface of the corresponding central water collecting pipe.
A high COD wastewater treatment process comprises the following steps:
step 1, performing pre-filtration treatment on high-COD wastewater;
and 8, dehydrating and drying the sludge in the MBR aerobic reaction process in the 7 step to obtain a sludge cake.
In one embodiment, the high COD wastewater is saline water produced water.
In one embodiment, the water quality index of the produced water containing salt and water oil is as follows: the salt content is 500-.
In one embodiment, the pre-filtration in step 1 is performed by sand filtration.
In one embodiment, the concentration of dissolved oxygen in the anaerobic process in the step 4 is below 0.5mg/L, the temperature of wastewater is 30-43 ℃, the pH value is 7-7.5, and the retention time is 25-50 hours; the dissolved oxygen concentration in the anoxic process in the step 4 is below 0.5mg/L, the wastewater temperature is 30-43 ℃, the pH value is 6.5-7.5, and the retention time is 15-25 hours.
In one embodiment, in step 3, the filtration process requires pretreatment of the solid-liquid separator, and comprises the following steps: soaking the medium filter in a sodium carbonate solution, evaporating water, and percolating a calcium chloride solution into the medium filter to generate calcium carbonate precipitates in the internal pores of the medium filter; filtering by adopting the produced water obtained in the step 2 to generate a filter cake on the surface of the medium filter; percolating the acid solution through a medium filter to dissolve calcium carbonate; in one embodiment, the concentration of the sodium carbonate solution is 10-20wt%, the concentration of the calcium chloride solution is 2-5wt%, and the acid solution is 5-10wt% hydrochloric acid.
In one embodiment, in the step 5, dissolved oxygen is 3-5mg/L during the MBR aerobic reaction treatment, and the retention time is 12-20 hours.
In one embodiment, in step 7, the current intensity of the electrodialysis process is 50-300mA/cm2。
Advantageous effects
The utility model provides an integrated processing technique can handle high COD waste water better, can eliminate the less oil drop in the waste water effectively through the method of air supporting at first, loops through anaerobism again, oxygen deficiency, the treatment of good oxygen and eliminates the COD in the waste water, utilizes the processing of MBR membrane simultaneously, filters the waste water of good oxygen processing simultaneously, obtains the waste water after handling, and filters mud; desalting the wastewater through subsequent electrodialysis treatment, crystallizing the concentrated water to obtain waste salt, and drying the sludge to obtain a mud cake, so that zero discharge of the wastewater is realized.
The radial immersed membrane module can filter under the condition of continuous dynamic rotation due to the special structure of the module. The dynamic rotation makes the upper and lower end positions of the membrane component continuously reverse, the sludge deposition process is destroyed by using the relative direction change of the root of the membrane component and the gravity, and the problem caused by the large amount of accumulated sludge at the root of the membrane component is eliminated or greatly reduced, thereby prolonging the cleaning period of the membrane component and prolonging the service life of the membrane component.
Drawings
FIG. 1 is a flow diagram of a high COD wastewater treatment process;
FIG. 2 is a flow diagram of a high COD wastewater treatment plant;
FIG. 3 is a schematic view of a radial submerged membrane module;
FIG. 4 is a schematic cross-sectional view of a rotatable water production pipe;
FIG. 5 is a schematic cross-sectional view of a plug;
FIG. 6 is a schematic view of a radial submerged membrane module system;
FIG. 7 is a schematic view of a casting mold;
FIG. 8 is a schematic view of a pre-glued ingot;
figure 9 is a comparison of the filter run flow after flocculation.
1-outer water collecting tank, 2-membrane wire pre-glue cast block, 3-central water collecting pipe, 4-connecting pipe, 5-outer water collecting tank side wall interface, 6-central water collecting pipe end interface, 7-central water collecting pipe connecting port, 8-outer water collecting tank groove, 9-central water collecting pipe groove, 10-total water producing port, 11-fixed bent pipe, 12-rotary joint, 13-shaft seal, 14-transmission mechanism, 15-plug threaded end, 16-plug end cap, 17-support frame, 18-radial immersed membrane component, 19-plug, 20-rotatable water producing pipe, 21-chain, 22-driving mechanism, 23-sewage tank, 24-glue casting mold, 25-glue inlet, 26-membrane wire, 27-hard pouring sealant, 28-soft pouring sealant, 29-cylindrical membrane wire pre-glue casting block, 30-square column membrane wire pre-glue casting block, 31-rhombic column membrane wire pre-glue casting block, 32-sedimentation tank, 33-air flotation tank, 34-flocculation tank, 35-flocculant adding tank, 36-solid-liquid separator, 37-anaerobic reaction tank, 38-anoxic reaction tank, 39-MBR reaction tank, 40-electrodialyzer, 41-water production tank, 42-evaporator and 43-dryer.
Detailed Description
The utility model discloses the characteristics of the waste water that will handle are high COD and oiliness to still contain more salinity in the waste water. For example, oil field produced water contains residual oil, and wastewater produced in some reservoirs is characterized by high salinity. In a specific example, the water quality index of the produced water containing salt water: the salt content is 500-.
In the treatment step, larger suspended matters can be eliminated by a pretreatment method, and larger residues and larger particles in water are removed by a pretreatment tank. The sedimentation tank used here can be an inclined plate sedimentation tank, and larger particles are removed by sedimentation.
After the primary treatment, the wastewater is treated by an air floatation method, so that oil drops in the wastewater can float upwards under the action of bubbles, and most of oil content can be eliminated.
In order to reduce the load of the subsequent treatment steps, the water produced after air floatation is treated in a coagulation mode, and the used coagulant can adopt inorganic flocculants such as polyaluminium chloride, aluminium sulfate, ferrous sulfate, polyferric sulfate, basic aluminium chloride and the like, and also can adopt organic flocculants such as anionic polyacrylamide, cationic polyacrylamide, nonionic polyacrylamide, zwitterionic polyacrylamide and the like; the addition amount and pH can be adjusted according to the type of the flocculant. After flocculation is finished, formed floccules can be filtered out in a settling and filtering mode. The filtration used herein may be a medium filtration or the like, for example, a filter medium such as porous ceramics, quartz sand, manganese sand or the like. During the filtering process of the medium, oil drops, colloids and the like in the oily wastewater can block an internal channel of the medium filtering material, so that the flux in the filtering process is obviously attenuated, and the blockage in the material is difficult to remove in a flushing mode, and the flow is more difficult to recover; then slowly permeating the filter medium by using a calcium chloride solution, so that calcium carbonate precipitates can be generated in the inner pore channels, and proper calcium carbonate can be obtained in the inner pore channels by controlling proper permeation amount, and can occupy a part of the inner pore channels; then the flocculated produced water is used for filtration, and due to the occupation of the internal pore channels, the flocculating constituent and other oil drops and colloids can not occupy the internal pores rapidly any more, a filter cake can be formed on the surface of the filter medium, and the oil drops and the colloids can be prevented from further entering the internal pores in the subsequent filtration process after the filter cake is formed; after the filter cake is initially formed, by slowly percolating with an acidic solution, the calcium carbonate precipitate in the filter cake can be dissolved and brought out of the internal pores while maintaining the surface filter cake, at the same time, the filter cake layer on the surface of the filter medium is maintained, and the removal of the calcium carbonate prefilled in the internal pores is also eliminated, so that the surface filter cake layer can be continuously utilized to perform the filtering function in the subsequent filtering, and the problem of difficult cleaning of the filter medium caused by the occupation of the pores is avoided.
Then, after flocculation and filtration, pollutants which are easy to be eliminated by a conventional physical and chemical method in the wastewater are eliminated, and then the wastewater is subjected to degradation treatment by anaerobic treatment and oxygen deficiency. The treated high COD sewage enters an anaerobic tank and is mixed with the returned activated sludge. The bacteria in the anaerobic tank oxidize and decompose the absorbed organic matters, provide energy, absorb a large amount of phosphorus from the sewage, store the phosphorus in the form of polyphosphate, and discharge the residual sludge out of the system and simultaneously discharge the phosphorus taken in by the bacteria, thereby achieving the aim of removing the phosphorus.
3. The sewage treated by the anaerobic tank automatically flows into an anoxic tank, and heterotrophic facultative microorganisms are mainly utilized in the anoxic tank to carry out denitrification process, and the function is to remove NH in the sewage3N and degrading organic matter. The sewage from the anaerobic tank and the dissolved mixed liquor flowing back from the MBR tank are fully mixed in the tank, denitrification reaction is carried out under the anoxic condition, denitrifying bacteria in the sewage take carbon source organic matters in the original sewage as hydrogen electron donors and nitrate nitrogen as electron acceptors, and nitrogen in the nitrate nitrogen and nitrite nitrogen in the returned mixed liquor is reduced into nitrogen to escape from the water, so that the aim of removing the nitrogen is fulfilled. Meanwhile, the facultative anaerobe in the water can oxidize and decompose macromolecular organic matters which are difficult to degrade by aerobic bacteria into micromolecular organic matters which are easy to degrade, so that the biodegradability of the facultative anaerobe is improved, and favorable conditions are created for aerobic biochemistry.
And sewage automatically flows into an MBR (membrane bioreactor) tank (aerobic tank) from the anoxic tank. The tank utilizes autotrophic aerobic microorganisms to degrade carbon-containing organic matters in the sewage and nitrify ammonia nitrogen in the sewage. An immersed ultrafiltration membrane component is also arranged in the MBR tank, and an aeration system is arranged at the lower part of the component. The sewage is directly filtered by the immersed ultrafiltration membrane to produce water, so that a secondary sedimentation tank can be omitted, the sludge load can be reduced, and the volume load can be improved. Sludge in the MBR tank is periodically lifted to the sludge dewatering machine by a pump, sludge is transported out after being dewatered and is used as solid waste to be subjected to harmless treatment, and desliming sewage flows back to the pretreatment tank to be treated again.
After MBR treatment, main suspended solid, COD in the waste water have been got rid of by a large amount, because still contain inorganic salt in the waste water, can get rid of the inorganic salt in the waste water through the processing of electrodialysis, obtain fresh water and dense water, and fresh water can discharge up to standard, and dense water can obtain the waste salt through the concentration crystallization. Sludge in the MBR can be dried to obtain dried sludge for solid waste treatment.
Based on foretell technology, the utility model provides a device as follows:
the method comprises the following steps:
the sedimentation tank 32 is used for performing pre-filtration treatment on the high-COD wastewater;
the air flotation tank 33 is connected to the sedimentation tank 32 and used for performing air flotation oil removal treatment on the filtrate obtained by the sedimentation tank 32;
a flocculation tank 34 connected to the air flotation tank 33 for performing degradation treatment on the wastewater obtained in the air flotation tank 33;
a solid-liquid separator 36 connected to the flocculation tank 34 for performing solid-liquid separation treatment on the produced water obtained in the flocculation tank 34;
the anaerobic reaction tank 37 is connected with the solid-liquid separator 36 and is used for carrying out anaerobic degradation treatment on the produced water of the solid-liquid separator 36;
an anoxic reaction tank 38 connected to the anaerobic reaction tank 37 for performing anoxic degradation treatment on the wastewater obtained in the anaerobic reaction tank 37;
an MBR reaction tank 39 connected to the anoxic reaction tank 38 for performing MBR aerobic degradation and filtration treatment on the wastewater obtained in the anoxic reaction tank 38;
an electrodialyzer 40 connected to the permeate side of the MBR reaction tank 39 for performing electrodialysis treatment on the filtrate in the MBR reaction tank 39;
an evaporator 42 connected to the concentrated solution obtained in the electrodialyzer 40 for evaporation crystallization to obtain a recovered salt;
and a dryer 43 connected to the bottom of the MBR reaction tank 39 for treating sludge obtained from the MBR reaction tank 39.
In one embodiment, the solid-liquid separator 36 is a media filter, which may be one of a porous ceramic filter, a quartz sand filter, or a manganese sand filter.
In one embodiment, the MBR reactor 39 is a hollow fiber membrane.
In one embodiment, the hollow fiber membrane has a pore size in the range of 20 to 500 nm.
In one embodiment, the fresh water side of the electrodialyzer 40 is connected to a product water basin 41.
Because in the reaction and the filtration process of MBR, can generate more mud, the utility model also provides a be applied to among the foretell effluent treatment plant MBR reactor, radial submerged membrane module, it includes: the device comprises an outer water collecting tank, a membrane wire pre-glue cast block, a central water collecting tank, a connecting pipe, a plug, a rotatable water producing pipe arranged on one side of the central water collecting tank and a driving mechanism for driving the rotatable water producing pipe to rotate; the membrane wires are pre-glued and cast into a plurality of pre-glued casting blocks; one end of the pre-glued cast block is adhered to the groove of the outer water collecting groove, and the other end of the pre-glued cast block is adhered to the groove of the central water collecting pipe in a radial shape; the connecting pipe connects the side wall interface of the outer water collecting tank with the end interface of the central water collecting pipe to form a water passage; the rotatable water producing pipe consists of a rotary joint and a fixed bent pipe; the rotary joint is connected with one side of the central water collecting pipe; the fixed elbow is fixed, and the produced water of the central water collecting pipe led out by the rotary joint is led out; the rotary joint is provided with a transmission mechanism which can rotate through a driving mechanism and drive the whole membrane assembly to rotate. The utility model provides a radial curtain formula membrane module according to the easy problem of gathering a large amount of mud of bottom membrane silk root in the curtain formula membrane module in-service use. The radial curtain type membrane assembly can rotate continuously, the relative direction of the root and sludge sedimentation is continuously converted, the sludge accumulation at the root and the pollution phenomenon on the surface of the membrane are effectively slowed down, the filtering operation can be continuously carried out in a long time, the cleaning period of the assembly is prolonged, and the service life is prolonged.
More specifically, the MBR module is structured as shown in FIGS. 3-8:
as shown in fig. 3, a radial submerged membrane module comprises an outer water collecting tank 1 and a central water collecting pipe 3, wherein the outer water collecting tank 1 is annular, the central water collecting pipe 3 is positioned in the middle of the outer water collecting tank 1, membrane wires 26 are distributed between the central water collecting pipe 3 and the outer water collecting tank 1, one end of each membrane wire 26 is fixed on the central water collecting pipe 3, the other end of each membrane wire 26 is fixed on the outer water collecting tank 1, an internal channel is communicated with the outer water collecting tank 1, and central water collecting pipe connectors 7 at two ends can be used as module water producing ports; the membrane wires 26 are evenly divided into a plurality of bundles, two ends of each bundle are sealed with glue, and the glue is pre-cast into a plurality of m membrane wire pre-cast blocks 2; one end of the membrane wire pre-glue cast block 2 is adhered with the outer side water collecting groove 8, and the other end is adhered with the central water collecting pipe groove 9 in a radial shape to form a fan shape; the connecting pipe 4 connects the side wall interface 5 of the outer water collecting groove with the end interface 6 of the central water collecting pipe to form a water passage.
As shown in fig. 6, the plug threaded end of the plug 19 is connected with the central water collecting pipe connecting port 7 at one end for sealing, and the plug end cap 16 of the plug 19 is supported by the supporting frame 17; referring to fig. 4, the rotatable water producing pipe 20 is composed of a rotary joint 12 and a fixed elbow 11; the rotary joint 12 is connected with the central water collecting pipe connecting port 7 at one side; the fixed elbow 11 is fixed on the support frame 17, and the produced water of the central water collecting pipe 3 led out from the rotary joint 12 is led out from the total water outlet 10; the rotary joint 12 is provided with a transmission mechanism 14 which can be connected by a driving mechanism 22 and a chain 21 to rotate and drive the whole radial submerged membrane module 18 to rotate, as shown in fig. 6. In the structure, the connecting pipes 4 are distributed around the annular water collecting tank 1 in a dispersing way, on one hand, the effect of collecting produced water in the annular water collecting tank 1 to the central pipe is achieved, on the other hand, the effect of supporting the annular water collecting tank 1 and the central pipe is achieved, the whole membrane assembly can form a disk taking the central pipe as an axis, the disk can rotate in a vertical plane through supporting on a support, the change effect of gravity is utilized, mud at the root is removed in the rotating process, the radial curtain type membrane assembly can rotate continuously, the relative direction of the root and the mud sedimentation is converted continuously, the accumulation of the mud at the root is effectively slowed down, the phenomenon of the pollution on the surface of the membrane is avoided, the filtering operation can be carried out continuously in a long time, the cleaning period of the assembly is prolonged, and the.
The method of making the radial submerged membrane module of the present invention is described in the examples below.
As shown in fig. 3, the radial submerged membrane module comprises an outer water collecting tank 1, a membrane wire pre-glued cast block 2, a central water collecting pipe 3 and a connecting pipe 4, and the manufacturing process comprises the following steps: the end parts of 200 membrane filaments 26 are coated with a hole plugging medium PEG2000 to plug the membrane filament water flow channel, so that the sealant is prevented from entering the inner hole. The method comprises the following steps of selecting a cylindrical gel casting mold 24 with a cavity structure, wherein the cylindrical gel casting mold 24 is only provided with an upper end opening, placing a cylindrical membrane wire pre-gel casting block 29 on the upper portion of the cylindrical gel casting mold 24, enabling the cross section of the cylindrical membrane wire pre-gel casting block 29 to be cylindrical, being provided with more pore channels inside and used for embedding a membrane wire 26, arranging a gel inlet 25 at the bottom of the cylindrical gel casting mold 24, coating a proper amount of release agent on the inner wall of the cylindrical gel casting mold 24, and arranging and neatly placing the membrane wire 26 with one end provided with a blocked hole in the gel casting mold. Pouring the hard pouring sealant 27 into the epoxy resin from the bottom glue inlet 25, pouring the epoxy resin with the height 7cm away from the bottom end of the membrane wire, and standing until the hard pouring sealant 27 is solidified. Then, the soft pouring sealant 28 is poured slowly from the opening of the cylindrical rubber casting mold 29 to a depth of 1cm, and then the soft pouring sealant 28 is kept standing until the soft pouring sealant is solidified. One end of the cylindrical membrane wire pre-glue casting block 29 after being cured is slowly removed from the mold, and the hard pouring glue 27 with the thickness of 1cm at the end part is cut off to open the inner hole of the membrane wire 26 to form a water flow channel. The cylindrical membrane wire pre-gel casting block 29 is turned upside down, and the other end is prepared according to the same steps, and the prepared cylindrical membrane wire pre-gel casting block 29 is shown in fig. 6. And then, one end of each cylindrical membrane wire pre-glue cast block 29 is bonded with the outer side water collecting groove 8 of one side one by one, and the other end of each cylindrical membrane wire pre-glue cast block is sequentially rotated by 90 degrees to be bonded with the corresponding central water collecting pipe groove 9 one by one, so that all the cylindrical membrane wire pre-glue cast blocks 29 are bonded with the outer side water collecting groove 8 and the central water collecting pipe groove 9 according to the step. And finally, connecting one end of each of the 3 connecting pipes 4 with an outer side water collecting tank side wall interface 5, and connecting the other end with a corresponding central water collecting pipe end interface 6.
The membrane wire pre-gel ingot may also be replaced with a rectangular parallelepiped, cylindrical or prism shape, as shown in fig. 8.
The oily wastewater treated in the following examples is wastewater produced in an oil field, and the water quality is as follows: the salt content is 1240mg/L, the oil content is 780mg/L, and the COD content is 5300 mg/L.
Example 1
Firstly, carrying out inclined plate sedimentation on the wastewater extracted from the oil field to remove larger solid suspended matters in the wastewater, and continuously treating the wastewater through air flotation to enable oil drops to float upwards and skim off; adding 30ppm of polyaluminium chloride flocculant into the deoiled wastewater for flocculation, filtering through a porous ceramic filter to remove floccules, and continuously performing anaerobic and anoxic treatment on the filtrate, wherein the dissolved oxygen concentration in the anaerobic process is below 0.5mg/L, the wastewater temperature is 30-35 ℃, the pH value is 7-7.5, and the retention time is 35 hours; the concentration of dissolved oxygen in the anoxic process is below 0.5mg/L, the temperature of the wastewater is 30-35 ℃, the pH value is 6.5-7.5, and the retention time is 18 hours. And the treated wastewater is sent into an aerobic reaction tank for reaction treatment, and meanwhile, a hollow fiber membrane filtering component is arranged in the aerobic reaction tank and used for filtering reaction liquid in real time, and the dissolved oxygen is 3-5mg/L and the retention time is 15 hours in the MBR aerobic reaction treatment process. The feed liquid after reaction is subjected to electrodialysis desalination treatment, and the current intensity in the electrodialysis process is 120mA/cm2The fresh water is discharged after reaching the standard, and the waste salt is obtained after the concentrated water is evaporated and crystallized; sludge in the MBR reaction process is dried to obtain a sludge cake as solid waste.
Example 2
Firstly, carrying out inclined plate sedimentation on the wastewater extracted from the oil field to remove larger solid suspended matters in the wastewater, and continuously treating the wastewater through air flotation to enable oil drops to float upwards and skim off; adding 30ppm polyaluminium chloride flocculant into the deoiled wastewater for flocculation, filtering by a porous ceramic filter to remove floccules, and continuously passing the filtrate through anaerobic and anoxic positionsThe concentration of dissolved oxygen in the anaerobic process is below 0.5mg/L, the temperature of wastewater is 30-32 ℃, the pH value is 7-7.5, and the retention time is 30 hours; the concentration of dissolved oxygen in the anoxic process is below 0.5mg/L, the temperature of the wastewater is 30-32 ℃, the pH value is 6.5-7.5, and the retention time is 15 hours. And the treated wastewater is sent into an aerobic reaction tank for reaction treatment, and meanwhile, a hollow fiber membrane filtering component is arranged in the aerobic reaction tank and used for filtering reaction liquid in real time, and the dissolved oxygen is 3-5mg/L and the retention time is 12 hours in the MBR aerobic reaction treatment process. The feed liquid after reaction is subjected to electrodialysis desalination treatment, and the current intensity in the electrodialysis process is 80mA/cm2The fresh water is discharged after reaching the standard, and the waste salt is obtained after the concentrated water is evaporated and crystallized; sludge in the MBR reaction process is dried to obtain a sludge cake as solid waste.
Example 3
Firstly, carrying out inclined plate sedimentation on the wastewater extracted from the oil field to remove larger solid suspended matters in the wastewater, and continuously treating the wastewater through air flotation to enable oil drops to float upwards and skim off; adding 30ppm of polyaluminium chloride flocculant into the deoiled wastewater for flocculation, filtering through a porous ceramic filter to remove floccules, and continuously performing anaerobic and anoxic treatment on the filtrate, wherein the dissolved oxygen concentration in the anaerobic process is below 0.5mg/L, the wastewater temperature is 34-38 ℃, the pH value is 7-7.5, and the retention time is 40 hours; the dissolved oxygen concentration in the anoxic process in the step 4 is below 0.5mg/L, the wastewater temperature is 35-48 ℃, the pH value is 6.5-7.5, and the retention time is 24 hours. And the treated wastewater is sent into an aerobic reaction tank for reaction treatment, and meanwhile, a hollow fiber membrane filtering component is arranged in the aerobic reaction tank and used for filtering reaction liquid in real time, and the dissolved oxygen is 3-5mg/L and the retention time is 18 hours in the MBR aerobic reaction treatment process. The feed liquid after reaction is subjected to electrodialysis desalination treatment, and the current intensity in the electrodialysis process is 140mA/cm2The fresh water is discharged after reaching the standard, and the waste salt is obtained after the concentrated water is evaporated and crystallized; sludge in the MBR reaction process is dried to obtain a sludge cake as solid waste.
Example 4
The difference between this example and example 3 is that a media filter is pretreated; firstly, the waste water produced in the oil field is treatedSettling by an inclined plate, removing larger solid suspended matters, and continuously treating the wastewater by air floatation to enable oil drops to float upwards and skim off; adding 30ppm of polyaluminium chloride flocculant into the deoiled wastewater for flocculation, filtering the wastewater through a porous ceramic filter, pretreating the porous ceramic filter before filtering the flocculation production water, soaking a filter cake of the filter into 15wt% of sodium carbonate solution to enable the pore channels to contain the sodium carbonate solution, naturally drying the filter, repeating the steps for one time, slowly percolating 5wt% of calcium chloride solution into the filter to enable calcium carbonate precipitate to be formed in the pore channels, filtering the flocculation production water, enabling the surface of the filter to form a filter cake layer, slowly percolating 10wt% of hydrochloric acid, dissolving the precipitate in the pore channels, and continuing to filter the flocculation production water; continuously carrying out anaerobic and anoxic treatment on the filtrate, wherein the dissolved oxygen concentration in the anaerobic process is below 0.5mg/L, the wastewater temperature is 30-35 ℃, the pH value is 7-7.5, and the retention time is 35 hours; the concentration of dissolved oxygen in the anoxic process is below 0.5mg/L, the temperature of the wastewater is 30-35 ℃, the pH value is 6.5-7.5, and the retention time is 18 hours. And the treated wastewater is sent into an aerobic reaction tank for reaction treatment, and meanwhile, a hollow fiber membrane filtering component is arranged in the aerobic reaction tank and used for filtering reaction liquid in real time, and the dissolved oxygen is 3-5mg/L and the retention time is 15 hours in the MBR aerobic reaction treatment process. The feed liquid after reaction is subjected to electrodialysis desalination treatment, and the current intensity in the electrodialysis process is 120mA/cm2The fresh water is discharged after reaching the standard, and the waste salt is obtained after the concentrated water is evaporated and crystallized; sludge in the MBR reaction process is dried to obtain a sludge cake as solid waste.
Example 5
The difference between this example and example 3 is that a media filter is pretreated; firstly, carrying out inclined plate sedimentation on the wastewater extracted from the oil field to remove larger solid suspended matters in the wastewater, and continuously treating the wastewater through air flotation to enable oil drops to float upwards and skim off; adding 20ppm polyaluminium chloride flocculant into the deoiled wastewater for flocculation, filtering by a porous ceramic filter, pretreating the porous ceramic filter before filtering the flocculated produced water, soaking a filter cake of the filter in 12wt% sodium carbonate solution to ensure that the pore channel contains carbonic acidNaturally drying the sodium solution, repeating the steps once, slowly percolating 2wt% of calcium chloride solution into the filter to form calcium carbonate precipitate in the pore channel, filtering the flocculation water to form a filter cake layer on the surface of the filter, slowly percolating 5wt% of hydrochloric acid to dissolve the precipitate in the pore channel, and continuously beginning to filter the flocculation water; continuously carrying out anaerobic and anoxic treatment on the filtrate, wherein the dissolved oxygen concentration in the anaerobic process is below 0.5mg/L, the wastewater temperature is 30-32 ℃, the pH value is 7-7.5, and the retention time is 30 hours; the concentration of dissolved oxygen in the anoxic process is below 0.5mg/L, the temperature of the wastewater is 30-32 ℃, the pH value is 6.5-7.5, and the retention time is 15 hours. And the treated wastewater is sent into an aerobic reaction tank for reaction treatment, and meanwhile, a hollow fiber membrane filtering component is arranged in the aerobic reaction tank and used for filtering reaction liquid in real time, and the dissolved oxygen is 3-5mg/L and the retention time is 12 hours in the MBR aerobic reaction treatment process. The feed liquid after reaction is subjected to electrodialysis desalination treatment, and the current intensity in the electrodialysis process is 80mA/cm2The fresh water is discharged after reaching the standard, and the waste salt is obtained after the concentrated water is evaporated and crystallized; sludge in the MBR reaction process is dried to obtain a sludge cake as solid waste.
Example 6
The difference between this example and example 3 is that a media filter is pretreated; firstly, carrying out inclined plate sedimentation on the wastewater extracted from the oil field to remove larger solid suspended matters in the wastewater, and continuously treating the wastewater through air flotation to enable oil drops to float upwards and skim off; adding 40ppm of polyaluminium chloride flocculant into the deoiled wastewater for flocculation, filtering the wastewater through a porous ceramic filter, pretreating the porous ceramic filter before filtering the flocculation production water, soaking a filter cake of the filter into 18wt% of sodium carbonate solution to enable the pore channels to contain the sodium carbonate solution, naturally drying the filter, repeating the steps for one time, slowly percolating 4wt% of calcium chloride solution into the filter to enable calcium carbonate precipitate to be formed in the pore channels, filtering the flocculation production water, enabling the surface of the filter to form a filter cake layer, slowly percolating 8wt% of hydrochloric acid to enable the precipitate in the pore channels to be dissolved, and continuing to filter the flocculation production water; the filtrate is continuously treated by anaerobic and anoxic treatment, whichIn the anaerobic process, the concentration of dissolved oxygen is below 0.5mg/L, the temperature of wastewater is 34-38 ℃, the pH value is 7-7.5, and the retention time is 40 hours; the dissolved oxygen concentration in the anoxic process in the step 4 is below 0.5mg/L, the wastewater temperature is 35-48 ℃, the pH value is 6.5-7.5, and the retention time is 24 hours. And the treated wastewater is sent into an aerobic reaction tank for reaction treatment, and meanwhile, a hollow fiber membrane filtering component is arranged in the aerobic reaction tank and used for filtering reaction liquid in real time, and the dissolved oxygen is 3-5mg/L and the retention time is 18 hours in the MBR aerobic reaction treatment process. The feed liquid after reaction is subjected to electrodialysis desalination treatment, and the current intensity in the electrodialysis process is 140mA/cm2The fresh water is discharged after reaching the standard, and the waste salt is obtained after the concentrated water is evaporated and crystallized; sludge in the MBR reaction process is dried to obtain a sludge cake as solid waste.
The water quality of the treated water produced in the steps is as follows:
it can be seen from the above table that, through the utility model discloses a processing method can realize handling the oil field produced water of high COD value, makes waste water up to standard. In example 1, the media filter in the media filtration process was pretreated so that the internal clogging of the porous media during the filtration process was less likely to occur and the water flux of the media filter was attenuated more slowly in one-cycle filtration process than in example 4.
Claims (10)
1. An immersed membrane module, comprising:
the outer water collecting tank (1) is annular;
the central water collecting pipe (3) is positioned in the middle of the outer water collecting tank (1);
the membrane filaments (26) are multiple in number, one end of each membrane filament (26) is fixed on the central water collecting pipe (3), the other end of each membrane filament is fixed on the outer side water collecting groove (1), and a channel in the membrane filament (26) is communicated with the outer side water collecting groove (8) fixed on the outer side water collecting groove (1);
the number of the connecting pipes (4) is multiple, one end of each connecting pipe is connected to the outer water collecting tank (1), the other end of each connecting pipe is connected to the central water collecting pipe (3), and the outer water collecting tank groove (8) is communicated with the central water collecting pipe (3) through the connecting pipes (4);
a rotatable water producing pipe (20) connected to the central water collecting pipe (3) for collecting the produced water of the inner channel of the membrane filaments (26);
the driving mechanism (22) is used for driving the whole outer side water collecting tank (1) to rotate through the central water collecting pipe (3);
and the support frames (17) are connected to two ends of the central water collecting pipe (3) and are used for supporting the membrane component.
2. Submerged membrane module according to claim 1, characterised in that the drive mechanism (22) rotates the central collector pipe (3) by means of a chain (21).
3. The submerged membrane module according to claim 1, characterised in that a number of outer sump side wall interfaces (5) are provided outside the outer sump (1), the outer sump side wall interfaces (5) communicating with the outer sump groove (8).
4. The submerged membrane module according to claim 1, characterised in that the number of outer sump side wall interfaces (5) is 3-8.
5. The submerged membrane module according to claim 1, characterised in that the connecting pipe (4) is connected to the outside sump side wall connection (5).
6. The submerged membrane module according to claim 1, characterised in that the central header (3) is located in the centre of the outer header (1) and perpendicular to the plane of the outer header (1), and the top projection of the outer header (1) is located at the centre line of the central header (3).
7. The submerged membrane assembly according to claim 1, characterised in that the membrane filaments (26) are in the outer header groove (8) and fixed between the outer part of the membrane filaments (26) and the outer header groove (8) by a hard potting compound (27).
8. The submerged membrane assembly according to claim 1, characterized in that the central water collecting pipe (3) is provided with a central water collecting pipe groove (9) at the periphery, the ends of the membrane filaments (26) are placed in the central water collecting pipe groove (9), and the outer part of the membrane filaments (26) and the central water collecting pipe groove (9) are fixed through a hard pouring sealant (27).
9. The submerged membrane module according to claim 1, characterised in that the membrane filaments (26) are external pressure type hollow fibre membrane filaments, internal pressure type hollow fibre membrane filaments, self-supporting hollow fibre membrane filaments, hollow fibre membrane filaments with an internal lining tube or hollow fibre membrane filaments with internal stiffening ribs.
10. The submerged membrane module according to claim 1, characterised in that the membrane filaments (26) are divided into a plurality of bundle-like strands, each strand forming a fan-like shape with respect to each other.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113943048A (en) * | 2021-11-30 | 2022-01-18 | 北控水务(中国)投资有限公司 | Membrane bioreactor and membrane bioreactor filtering method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113943048A (en) * | 2021-11-30 | 2022-01-18 | 北控水务(中国)投资有限公司 | Membrane bioreactor and membrane bioreactor filtering method |
| CN113943048B (en) * | 2021-11-30 | 2023-09-05 | 北控水务(中国)投资有限公司 | Membrane bioreactor and membrane bioreactor filtering method |
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