CN110577258A - Constant-pressure cross-flow filtering water treatment process and treatment device using natural force as power - Google Patents
Constant-pressure cross-flow filtering water treatment process and treatment device using natural force as power Download PDFInfo
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- CN110577258A CN110577258A CN201910956885.5A CN201910956885A CN110577258A CN 110577258 A CN110577258 A CN 110577258A CN 201910956885 A CN201910956885 A CN 201910956885A CN 110577258 A CN110577258 A CN 110577258A
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- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 claims description 4
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- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
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- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/102—Permeable membranes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2806—Anaerobic processes using solid supports for microorganisms
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a constant pressure cross flow filtering water treatment process method using natural force as power, which comprises the steps of preparing a frame membrane assembly by using a hollow flat ceramic membrane with hydrophilicity, sealing and superposing the frame membrane assembly to form a membrane assembly, sealing and connecting the membrane assembly with a water inlet pipe, sinking an opening at the lower end of the membrane assembly in raw water to form a sealed filtering channel in the membrane assembly, using the capillary force of the hollow flat ceramic membrane and the siphon force formed by the height of the membrane assembly as filtering pressure, controlling the height of the membrane assembly to enable the filtering pressure value to be smaller than the critical pressure value of the hollow flat ceramic membrane, and sealing one end of a hollow flow collecting hole and communicating the other end of the hollow flow collecting hole with a water collecting pipe. The filter has the advantages that the capillary force and the siphon force are utilized as the filtering pressure without additional pressurization of a water pump, the proper filtering membrane flux is realized, the membrane holes are not blocked, backwashing is almost not needed, the use cost is very low, and the problems of high filtering cost, large investment, easy pollution and difficult regeneration of the ceramic membrane are solved.
Description
Technical Field
The invention relates to a wastewater treatment method and a wastewater treatment device, in particular to a method and a wastewater treatment device for filtering and treating wastewater by taking the capillary force of a flat hydrophilic membrane and the siphon force generated by the height difference of membranes as power.
Background art:
The prior art for treating sewage by using a ceramic flat membrane mainly comprises the following two processes: immersing a flat membrane component in a sewage stock solution, filtering by using a dead end pumped by a pump, intercepting a particle solute in the sewage by a membrane surface, purifying water out through the membrane surface, and backwashing and regenerating after membrane pores of the membrane surface are blocked; the long-term stable filtration flux of the application is generally 5-30L/m2H (domestic sewage); pumping the sewage stock solution in a membrane frame by a pump to pass through the sewage stock solution at positive pressure, forming cross flow with the flat membrane surface through the flat membrane array gaps in the membrane frame, intercepting solute particles by the membrane surface, purifying water by the membrane, and taking away most of the intercepted solute particles by the liquid flow flowing through the membrane surface at high speed, wherein the anti-pollution capacity of the membrane in the filtration and separation mode is better than that of the first type, the long-term stable flux is higher and is about 10-40L/m2H (domestic sewage). However, in both of the above solid-liquid separation methods, the membrane is immersed in raw water and the membrane surface is subjected toThe liquid pressure is larger, the accumulation of pollutants on the membrane surface is thickened, if the pressurization flux is rapidly reduced, the filtration pressure is naturally increased to ensure the water yield, and thus, some small particles easily enter the membrane holes to cause irreversible blockage, so that the filtration separation power (pressure) cannot be constant, and the filtration flux is rapidly reduced along with the thickening of the pollutants all the time in the change, so that the consumption of the backwashing power is increased, and because the accumulation of the pollutants on the membrane surface is thickened, the pressure is naturally increased to ensure the water yield, some small particles easily enter the membrane holes to cause irreversible blockage. The membranes of the two filtration modes are extremely easy to be polluted until irreversible pollution is generated, and the result is that: the power consumption of frequent backwashing is large, the cost of frequent drug washing is high, the efficiency is extremely low, and the practical experience proves that: the backwashing and drug washing results are not ideal, the final stable filtration flux is extremely low, the operation is complex, the membrane maintenance and regeneration difficulty is high, the result is that the project can not normally run, and the membrane component needs to be changed again, so that the membrane pores are easy to block, the stable filtration flux is small, the investment is large, the backwashing frequency is high, the backwashing difficulty is high, the membrane regeneration is difficult, the power consumption is increased, the running cost is high, and the large-scale popularization of the flat ceramic membrane is problematic.
Disclosure of Invention
Aiming at the problems in the prior art, the invention analyzes the reasons of the problems as follows: flat sheet membrane filtration belongs to the field of microfiltration, in which there are three kinetic operating zones, whether they are flat sheet membranes or tubular membranes: supercritical, critical, and subcritical regions; the subcritical pressure refers to the filtering pressure of the hollow flat membrane which can maintain filtering and can not be blocked, when the filtering pressure is less than the subcritical pressure, the filtering is operated in a subcritical region, the membrane filtering and transmembrane pressure difference are kept stable, the membrane pollution speed is very low, the pollution is reversible pollution, the filtering is operated for a long time under the condition that the membrane flux is relatively stable, a certain stable filtering amount can be kept in the long-time filtering operation, the blockage is avoided, and frequent back washing is not needed; when the filtration pressure is greater than the subcritical pressure and less than the critical pressure, the filtration is operated in the critical zone, and the system is operated in the critical zonewhen the membrane filter operates for a period of time under a low pollution rate, the operating pressure is linearly and slowly increased, and finally becomes rapid in the later period, so that the filtration flux is reduced, and membrane pollution is generated; when the filtration pressure is higher than the critical pressure, the filtration enters a supercritical region, the transmembrane pressure difference is rapidly increased and unstable, part of irreversible pollution is formed, the membrane flux is rapidly reduced in a short time, the filtration operation needs to be frequently stopped for high-pressure backwashing, the peak value of the membrane flux is reduced after each flushing, a sawtooth shape with a constantly reduced peak line is formed, and the average membrane flux in the time is 10L/m2H is less than h, and the running cost for treating the domestic sewage is more than 1 yuan/cubic meter. In summary, under certain operating conditions, the filtration pressure is in the critical region, especially in the subcritical region, and the membrane flux is maintained in the critical flux region, preferably in the subcritical flux region, so that the high membrane flux can be maintained for long-term stable operation. And from the operating pressure point of view: when the operating (filtration) pressure is below the critical pressure, the membrane flux increases with increasing pressure, and above this value, membrane fouling is exacerbated, which is difficult to achieve in practical operation of a dynamically controlled filtration system in which the filtration pressure is kept constant below the critical pressure or sub-critical pressure.
Aiming at the problems of high investment cost, low flux, easy pollution, difficult regeneration and high operation cost of the hydrophilic flat membrane, particularly the hydrophilic hollow plate-type ceramic membrane, which are encountered in large-scale popularization and use in the prior art, the invention provides a method for solving the problems, and the principle of the method is as follows: the method does not need additional pumping pressure as filtering power, but utilizes siphon force generated by the height drop of raw water and capillary force of the hydrophilic membrane as filtering pressure (namely the power value of filtered water), and controls the filtering pressure to be always positioned in a critical pressure area, preferably in a subcritical area by adjusting the lamination height of the membrane assembly and changing the magnitude of the siphon force.
The invention relates to a constant-pressure cross-flow filtering water treatment process method using natural force as power, which comprises the steps of preparing a frame membrane assembly by using a hollow flat ceramic membrane with a hydrophilic membrane, sealing and superposing the frame membrane assembly to form a membrane assembly, sealing and connecting the upper end of the membrane assembly with the upper end of a water inlet pipe, sinking an opening at the lower end of the membrane assembly in raw water to form a sealed filtering channel in the membrane assembly, using siphon force formed by capillary force and height of the hollow flat ceramic membrane as filtering power, controlling the height of the membrane assembly to enable the filtering pressure value to be smaller than the critical pressure value of the ceramic membrane, and sealing one end of a hollow flow collecting hole in the hollow flat ceramic membrane and communicating the other end of the hollow flow collecting hole.
further, in order to improve the filtering effect, the lower end of the membrane assembly is provided with an air vibration box with a support frame, the lower end of the support frame is fixed in the raw water box and is immersed in the raw water, and the support frame is preferably an elastic support frame.
Furthermore, a water distributor is hermetically arranged at the upper end of the membrane assembly, a honeycomb pore plate is arranged at the lower end of the water distributor, and the upper end of the water distributor is hermetically connected with the upper end of the water inlet pipe.
Furthermore, the water inlet pump is a high-flow low-lift water pump.
Furthermore, a backwashing device is arranged on the raw water tank.
further, the height difference between the uppermost layer purified water outlet and the lowermost layer purified water outlet of the membrane assembly is less than 2.5 meters or less than 5.4 meters.
When the invention lies in: firstly, when the filtration is operated in a subcritical pressure area, the binding force between dirt on the surface of the membrane and the membrane is weak, the dirt on the surface of the membrane is very easy to be taken away by shear flow formed on the surface of the membrane and is not easy to be polluted, and the membrane is reversibly polluted even if the dirt is polluted, so that the membrane is very easy to regenerate; the raw liquid is pumped to a water distributor at the top of the membrane group by a large-flow low-lift water pump, water falls freely by gravity to cover the surface of a wetting membrane, at the moment, the liquid is sucked into the membrane capillary by the capillary force of membrane capillaries, after the membrane capillary is completely filled, a membrane water collecting cavity is filled with water, finally, a water purifying pipe is filled with water and is discharged through a water purifying drain pipe under the action of the siphon force of the water purifying water collecting pipe, meanwhile, the liquid scours the surface of the membrane to generate cross flow, the water flow and the membrane generate shearing motion, the influences of membrane pollution and concentration difference polarization can be greatly reduced, pollutants on the surface of a hollow flat plate membrane are easily scoured and removed, and the last critical low constant pressure filtration effect is added, so that the membrane pollution is extremely.
the invention is characterized in that the operation pressure is as follows: the siphon force of the hydrophilic membrane is used as a basis to be coupled with the siphon force generated by the natural height drop of the raw water, and the height drop of the membrane assembly is adjusted (actually, the height difference of the upper and lower purified water outlets is adjusted), so that the filtering operation can be controlled to operate at a certain pressure value in a subcritical area or a critical area, the binding force between dirt on the surface of the membrane and the membrane is extremely weak, the dirt is easily taken away by shear flow and is not easily polluted, the pollution is reversible, and the membrane is easily regenerated; thirdly, a large-flow low-lift water pump is used for pumping the stock solution to a water distributor on the top of the membrane group, then the water freely falls down to impact the surface of the membrane through the gravity to generate cross flow, the water flow and the membrane surface generate shearing motion, the influence of membrane pollution and concentration difference polarization can be greatly reduced, pollutants on the surface of the flat membrane are easily washed away and removed, and the last critical low constant pressure filtration effect is added, so that the membrane pollution is extremely low.
The invention utilizes the capillary force of the hydrophilic membrane and the filtration power formed by the siphon force to be a certain value below the critical pressure, thereby realizing the perfect combination of low constant pressure operation and a cross flow mechanism, leading the sewage purification treatment method to have the advantages of operational feasibility, stability and huge cost, and even possibly bringing revolutionary popularization prospect to the hydrophilic flat ceramic membrane.
The present invention adopts bauxite, cordierite, quartz, kaolin, ball clay or their composition as base material to produce hydrophilic ceramic film, and uses them to prepare surface film material (ultrafiltration and microfiltration), so that it can greatly reduce the cost of ceramic film, and its cost is identical to that of hydrophilic ceramic film adopting SiC and alpha-Al in existent technology2O3Carrier material made of fused corundum and SiC and Al2O3、SiO2、TiO2、ZrO2And ZnO or the composition of the ZnO and the ZnO are used for preparing the surface film, and the cost of the surface film is reduced to more than 500 yuan/square and less than 100 yuan/square, so that the problems of high price and large investment of the hollow flat sheet film are solved.
The invention adopts organic materials such as ABS, U-PVC, PP and the like to manufacture the frame body and the membrane component by injection molding, has simple structure, can greatly reduce the cost of the membrane component, and basically uses 304 in the prior art#The frame body is made of stainless steel, the flat ceramic membrane water collecting plug is made of materials such as ABS, U-PVC and the like, and the membrane component is formed by a large water collecting pipe, an aeration pipe, a backwashing pipe and the like which are made of materials such as a quick connecting piece, a nylon pipe, PP, PVC, PC and the like; long working procedure, complex structure, more and expensive raw materials,
The plastic membrane component consists of two parts of a frame body and a hollow flat ceramic membrane, the front part of each membrane component structure is provided with a filtering and purifying area, and the rear part of each membrane component structure is provided with a purified water collecting cavity, so that the plastic membrane component has simple structure and low cost, and compared with the prior art, the cost of raw materials and accessories of the membrane component is 150 yuan/m plus 100-2Reduced to 30 yuan/m2The following.
The invention mainly adopts constant pressure filtration in a subcritical pressure value area, wherein siphon suction is determined by the siphon principle through the altitude difference of a discharge port of a water purification collecting pipe and a membrane assembly and filtration flux and effect field tests, an operation area below subcritical pressure can stabilize filtration flux without generating membrane pollution, in the prior art, no matter cross flow or dead end filtration is performed by pumping, the pressure is always changed, the filtration flux is also always changed, the filtration flux starts to be very large but quickly decreases, and the membrane flux cannot be recovered along with the time extension until the membrane flux is blocked and cannot be operated. Even if a constant pressure pump is used as a power source, the filtration flux is sharply reduced along with the increase and the thickening of the membrane surface pollution, the filtration cost is too high, the membrane is not practical, the pressure can be easily controlled by using the siphon suction force (determined by the height difference), the pressure is constant by determining the height difference, the filtration flux is constant because the membrane is not easy to be polluted and the filtration flux is combined with a cross-flow filtration mechanism, although the initial flux is not large for pumping filtration, the stable flux (30-100L/m)2H) a steady flux (5-20L/m) in comparison with suction filtration2H) is much larger, and the filtering mode has low running cost, controllable operation, simplicity and small investment.
The invention utilizes abundant capillary channels in the hydrophilic membrane, when solvent (water) contacts the surface of the membrane, the solvent (water) is immediately absorbed into the capillary in the membrane by the force of the capillary in the membrane, the force is a natural force, the former filtration and separation mechanism is not fully known and utilized, and the natural force and the filtration power are in the same direction and are consistent, so that the running cost can be greatly reduced by fully utilizing the natural force and the filtration power.
The invention adopts a water pump with low lift and large flux to supply water with small hydrodynamic loss, distributes water uniformly by a water distributor, freely falls down to fully wet and cover and scour the membrane surface to generate shearing motion, thereby forming cross-flow filtration, no pressure or micro-positive pressure exists in a filtration channel, the membrane is in a non-pressure or low-pressure state, the filtration mechanism has low requirement on the membrane strength, and raw water does not need to fill the whole membrane cavity space channel. In the prior art, cross-flow filtration is adopted, water is pumped by a high-power water pump to pass through an inner membrane hole (a tube membrane) or a membrane surface (a flat membrane) at a high speed, raw water is completely filled in a channel or a membrane cavity space channel, a high-pressure water environment is formed simultaneously, a membrane or a membrane frame is always in high tensile stress or pressure stress, water is pressed into or extruded out of the membrane, and the membrane is in the high pressure of the water environment, so that separation of solute and solution is formed.
The invention can improve the purified water yield and reduce the filtration operation cost by increasing the stacking height or the layer number of the membrane assembly, and the water feeding amount and the filtration water yield of the water pump are tested as follows: the purification proportion is more than 30 percent of the single water feeding amount (water inlet amount of the water inlet pipe) (namely 70 percent of the single water feeding amount returns to the original water tank, and 30 percent of raw water is purified and filtered to become purified water which is discharged into the purified water tank); the invention can also apply: the water distributor is used for continuously feeding raw water, after the water distributor contains water, the upper ends of the membrane assemblies are sealed by water, the lower end air vibration frame is partially immersed below the liquid level of a raw water tank (pool) and is also sealed by the liquid level, the membrane assemblies are sealed by sealing rubber pads, a filtering channel assembled by a plurality of membrane assemblies is also in a closed space state, when the water continuously and freely falls, the sealing channel is in a micro-positive pressure state, the naturally generated micro-positive pressure (about 20 Pa) is consistent with the direction of the filtering pressure, and the membrane is in a naturally generated micro-positive pressure space.
The invention utilizes the impact force generated by the free falling body of water to drive the membrane frame to vibrate, thereby causing the stock solution of the membrane to generate severe shearing friction and further reducing the membrane pollution: the method comprises the following steps: the air vibration box (figure 5) and the membrane assembly and the water distributor arranged on the air vibration box are arranged on a support frame with certain elasticity, so that raw water washes membranes from top to bottom in sequence, finally residual liquid falls into the raw water tank to generate wave returning, a membrane frame and an inner membrane are impacted by water, the support frame can generate 0.1-5 cm vibration under the action of micro positive pressure and filtering pressure, the frequency of shearing frequency of the membranes and the raw water is increased, the difficulty of staying and attaching sludge particles on the surface of the membranes is increased, the operation energy consumption can be reduced to the minimum by fully utilizing the capillary force and the high siphon force of the hydrophilic membranes and the micro positive pressure generated by water falling and draining, and almost all power loss of the whole machine is the power loss of the circulating water inlet pump; secondly, a low constant pressure filtration mechanism and a cross flow filtration mechanism in a subcritical region are combined, water flow impact is fully utilized to enable the membrane to vibrate, the membrane is hardly polluted, backwashing, drug washing, aeration and other conventional operations are hardly needed, the use cost is very low, the running cost of domestic sewage can be controlled below 0.2 yuan/cubic meter, and the normal flux can reach 30L/m2H or more, the problems of high cost, large investment, easy pollution, difficult regeneration and difficult use of the ceramic membrane are basically solved, and another new ceramic membrane sewage treatment process is developed.
The invention seals the bottom of the air vibration tank (or the membrane frame) by adjusting the liquid level of the raw water in the raw water tank, can randomly adjust the interior of the membrane frame to be in an oxygenated state or an anoxic state, and can also adjust the depth of the raw water in the raw water tank to adjust the raw water to be in an anaerobic and facultative oxygen consumption state, and the water distribution of the water pump belongs to aerobic operation, thus forming an integrated process of nitrification and denitrification biochemical treatment process and filtration separation treatment.
The filtering method is subcritical low pressure and constant pressure filtering, a subcritical pressure value of 0.035MPa and a critical pressure value of 0.065MPa are determined by testing an alumina membrane and a membrane plate with a membrane hole of 0.01-100 mu m on site, the filtering pressure is that the sum of the capillary force and the potential energy generated by the height difference is smaller than the critical pressure value, preferably smaller than the subcritical pressure value, and the filtering pressure value is determined by adjusting the siphon force (the height of the membrane component or the height position of a water collecting pipe discharge port).
The capillary force refers to the acting force which can make the liquid wetting the tube wall of the capillary tube naturally rise. This force is directed in the direction in which the concave surface of the liquid is oriented, and its magnitude is proportional to the surface tension of the liquid and inversely proportional to the capillary radius.
first, calculation of capillary force h ═ 2 γ Cos α/(ρ gr), (water column):
The raw water temperature is 25 ℃, the raw water density rho is 1000kg/m3, and the membrane aperture r of the hydrophilic ceramic membrane is 0.001 multiplied by 10－3（m），
When the film material is an aluminum oxide film, the contact angle of the pores of the hydrophilic ceramic film is about 45 degrees, and the surface tension y is 7.2 multiplied by 10－3(kg/m), g 9.8 (acceleration of gravity).
The capillary force h is 2 γ Cos α/(ρ gr) is 2 × 7.2 × 10－3×cos45°/（1000×9.8×0.001×10－3) 14.4 × 0.707/9.8-1.0388 m water column-0.01 MPa (calculated as 1 MPa-101.97 m water column)
And secondly, the siphon force Q of the raw water is equal to delta h multiplied by rho, and delta h is the height difference of a siphon (the height difference between a water inlet end and a water outlet end).
When the aperture of the ceramic membrane is 0.001 multiplied by 10 < -3 > m, the critical pressure value is 0.065MPa and the subcritical pressure value is 0.035MPa through test, and the setting is as follows:
When the critical pressure (X) value is 0.065MPa, the filtration is in the critical zone,
When the subcritical pressure (Y) value is 0.035MPa, the filtration is in the subcritical region.
Thirdly, to ensure that the raw water can be filtered in a critical area, particularly a subcritical area, a filtering pressure value formed by capillary force and siphon force should satisfy the following relational expression:
h + Q is less than or equal to X or h + Q is less than or equal to Y, wherein X is 0.065MPa and Y is 0.035MPa
Then: q is less than or equal to X-h, and delta h is less than or equal to X-h, 0.065-0.01 is 0.055MPa, so that the delta h is 0.055 multiplied by 101.97/1 is 5.4(m),
Q is not more than Y-h, Δ h × ρ is not more than Y-h 0.035-0.01 ═ 0.025MPa, resulting in Δ h 0.025 × 101.97/1 ═ 2.5m (m).
From the above results, it was found that when the raw water temperature was 25 ℃, the raw water density ρ was 1000kg/m3, and g-9.8 was the acceleration of gravity, the membrane pore diameter of the hydrophilic ceramic membrane was 0.001 × 10－3m (1 um), when the film material is an aluminum oxide film, the contact angle of the pores of the hydrophilic ceramic film is about 45 degrees, and the surface tension gamma is 7.2 multiplied by 10－3(kg/m), the height difference between the uppermost layer purified water outlet and the lowermost layer purified water outlet of the ceramic membrane assembly is adjusted to be less than 5.4m, so that the filtering pressure value formed by capillary force and siphon force is less than or equal to 0.065MPa, and the filtering is operated in a critical region. Preferably, the height difference between the uppermost layer purified water outlet and the lowermost layer purified water outlet of the ceramic membrane assembly is adjusted to be within the range of less than 2.5m, so that the filtering pressure value formed by capillary force and siphon force is ensured to be less than or equal to 0.035MPa, and the filtering is operated in a subcritical region; namely, the height difference between the purified water outlet on the uppermost membrane module 9 and the purified water outlet on the lowermost membrane module of the regulating and controlling membrane assembly is below 2.5 meters or below 5.4 meters.
Therefore, the process method can fully utilize the capillary force and the height difference siphon force of the membrane as the membrane filtration pressure as long as the membrane material is proper and the height of the membrane assembly is reasonably adjusted, the pressure of the water pump can pump the raw water into the uppermost membrane assembly without additional pressurization of the water pump, the capillary force and the siphon force can be utilized as the filtration pressure, the proper filtration membrane flux can be ensured, the membrane pores can not be blocked, the conventional operations such as backwashing, drug washing, aeration and the like are hardly needed, the use cost is very low, the domestic sewage operation cost can be controlled below 0.2 yuan/cubic, and the normal flux can reach 30L/m2H or more, and basically solves the problems of high cost, large investment, easy pollution, difficult regeneration and difficult use of the ceramic membrane.
The water distributor has the same appearance size and assembly size as the membrane module; water inlets are reserved on the periphery or the upper part; the lower part in the water distributor is provided with one or two layers of sieve plates which are mainly used for uniformly dispersing water flow; the middle upper part in the water distributor is a cavity which is mainly used for temporarily containing water and holding water, and the sieve pores of the water distributor mainly have a round shape, a square shape, a triangular shape, a pentagonal shape and a multi-pore shape, wherein the water is distributed by the long strip-shaped sieve pores.
The membrane modules are horizontally placed, a plurality of membrane modules are assembled into a row from bottom to top, and the membrane module frames are sealed by rubber sealing ring gaskets; hollow flat membranes are arranged in parallel in the membrane frame, the distance between the membranes is 5-50 mm, and water flow channels are arranged between the membranes and the inner wall of the membrane frame; a support frame for bearing the membrane module is arranged in the raw water storage tank, and the large-scale project is a water storage tank; the bottom of the lower side of the water storage tank is provided with a sludge discharge gate, the upper part of the water storage tank is provided with a raw water inlet gate, and the bottom of the raw water storage tank is provided with a stirrer; the water storage tank is provided with a bearing platform, and the bearing platform is provided with a large-flow water feeding pump, a back washing pump or an air compressor for air washing, a raw water suction pump, an automatic control system and the like.
The membrane module is a small module, a plurality of small modules are combined from bottom to top to form a membrane module aggregate, and the aggregate also becomes a water fluid channel; the height of the liquid level of the water storage tank can be adjusted according to needs, when the liquid level of the sewage rises above the bottom surface of the air vibration membrane frame (or the membrane frame), the interior of a channel of the membrane frame is in an anoxic state, when the liquid level of the sewage drops below the bottom surface of the membrane frame, the channel of the membrane frame is connected with air, and the interior of the channel of the membrane frame is in an oxygenated state, so that the height can be adjusted according to needs; in addition, when the film is anoxic and in a working state, the residual liquid of the free falling body impacts the liquid level, the lower liquid level can generate surge under the action of a reaction force, the circulation is repeated, micro positive pressure and micro negative pressure can be generated in the channel of the film frame to act on the surface of the film back and forth, the dirt on the surface of the film can be further loosened, and the film can be easily washed away under the impact of falling liquid, so that the anti-pollution capability of the film surface is enhanced; the membrane module frame is internally provided with a water collecting cavity (figure 4) and a purified water outlet, and the best water collecting cavity is arranged at the lowest part of the water collecting cavity of each membrane module frame.
When the system is in a working state, facultative bacteria or oxygen consuming bacteria are planted on the surface of the membrane, a layer of biological bacteria membrane layer is formed on the surface of the membrane, and the double functions of filtration and separation and biochemical reaction are performed in the working process, so that the water quality can be further purified; the lowermost part of the membrane module can be provided with an air vibration box, the size and the assembly size of the air vibration box are the same as those of the membrane module, and high-pressure air can be pressed into the air vibration box to vibrate the membrane module at a certain frequency when necessary; the combined height of the membrane modules is determined by the flow of the upper water pump, namely the flow of the upper water pump flows down through the water distributor and can be fully wetted or covered on the membrane surfaces in all the membrane frame channels.
The invention can also combine the filtration pressure formed by the capillary force of the hydrophilic flat membrane and the siphon force of the height difference potential energy with a cross-flow mechanism without a suction pump, thereby saving a large amount of operation energy consumption, skillfully ensuring that the filtration power source can be constant in a subcritical area and can not exceed an adjacent pressure value, ensuring that the membrane pollution is extremely small during working, the membrane pollution is reversible even if the membrane is polluted, the regeneration is extremely easy, and the filtration flux is large, stable and constant.
The invention is provided with a backwashing system, when the filtering treatment time is too long, the biological bacteria layer on the surface of the membrane is too thick, and the filtering flux is seriously influenced to be reduced, the membrane module is started, and the membrane module (module) is arranged on a supporting frame fixed on a water storage tank and also can be arranged on a supporting frame with certain elasticity; after raw water is treated by the device, the concentration of residual water is improved, the residual water falls into the water storage tank again, sludge can be gradually precipitated, and the sludge flows back to the biochemical tank through a sludge conveyor at the bottom of the tank (tank) for further nitrification and denitrification, so that the stability of the water quality in the water storage tank (tank) is ensured.
The hollow flat ceramic membrane is a cheap silicon-aluminum or magnesium ceramic membrane, and the chemical composition range is as follows: SiO 22 ：10-80(%)、Al2O3：80-10(%)、MgO：0.1-15（%）、CaO:0.1-5(%)、KNaO:0.1-10(%)、TiO2:0.1-5(%)、Fe2O3:0.1-3(%)、LiO20-3(%), the others: 0-3 (%); the mineral composition is as follows: mullite: 0-85 (%), corundum: 0-50 (%), quartz (cristobalite): 0-60 (%), glass phase: 0.5-40 (%), cordierite: 0-80 (%); the hollow flat ceramic membrane material can be: corundum, mullite, high-alumina, quartz, cordierite or their composition; the pore diameter range of the hydrophilic membrane or the inorganic ceramic membrane is as follows: 0.01-100 um; asymmetric membranes, symmetric membranes (uniform membranes) are also possible.
the invention provides a treatment device for realizing a constant-pressure cross-flow filtered water treatment process method taking natural force as power, which comprises a membrane component 9, a water inlet pipe, a water inlet pump 4, a water collecting pipe 12 and a raw water tank 2, wherein the membrane component is formed by alternately placing hollow flat ceramic membranes with hydrophilic membranes in a frame body, the membrane component is sealed and superposed to form a membrane assembly, the upper end of the membrane assembly is hermetically connected with the upper end of the water inlet pipe, the lower end opening of the membrane assembly is submerged in raw water in the raw water tank 2, so that a sealed filtering channel can be formed in the membrane assembly, one end of a hollow flow collecting hole in each hollow flat ceramic membrane is closed, the other end of the hollow flow collecting hole is open and is communicated with the water collecting cavity and the water collecting pipe, and the height of a purified.
Furthermore, the treatment device also comprises an aeration back-flushing device, the aeration back-flushing device comprises a back-flushing pump, a back-flushing water inlet pipe 19, a back-flushing pipe 5, a back-flushing air inlet pipe 14 and an aeration pipe 30, one end of the back-flushing water inlet pipe is connected with the purified water tank, the other end of the back-flushing water inlet pipe is connected with the back-flushing pump, the other end of the back-flushing pipe is connected with the water collecting pipe, one end of the aeration pipe is connected with an air washing air compressor 32, and the other end of the aeration pipe is provided with aeration.
Furthermore, the hollow collecting hole open end in the hollow flat ceramic membrane in each group of membrane modules is connected with a water collecting tank, and the water collecting tank is connected with the purified water outlet and then communicated with the water collecting pipe.
Drawings
Figure 1 is a schematic front view of the present invention,
Figure 2 is a schematic diagram of the top view structure of the invention,
figure 3 is a schematic view of the structure of the water distributor from the top,
FIG. 4 is a schematic view of a partial cross-sectional structure of a membrane module,
FIG. 5 is a schematic diagram of a cross-sectional structure of a membrane module,
Figure 6 is a schematic view of the frame structure,
fig. 7 is a partial sectional structural view of a-a of fig. 1.
In the figure, 1, a raw water main pipe 2, a raw water tank 3, a backwashing pump 4, a water inlet pump 5, a backwashing pipe 6, a raw water inlet pipe I7, a water distributor 8, a sieve plate 9, a membrane component 10, a water outlet valve 11, a purified water outlet 12, a water collecting pipe 13, a raw water inlet pipe II 14, a backwashing air inlet pipe 15, raw water 16, an air vibration tank 17, a purified water outlet 18, a purified water tank 19, a backwashing water inlet pipe 20, a sewage outlet 21, a membrane surface 22, a hollow collecting hole 23, a hollow flat ceramic membrane 24, a left support plate 25, a right support plate 26, a plug 27, a water collecting tank 28, a frame 29, a flange 30, an aeration pipe 31, a support frame 32 and an air washing.
Detailed Description
In the figure, a processing device for realizing a constant-pressure cross-flow filtered water treatment process method using natural force as power comprises a membrane component 9, a water inlet pipe, a water inlet pump 4, a water collecting pipe 12 and a raw water tank 2, wherein the water inlet pipe consists of a raw water inlet pipe I6 and a raw water inlet pipe II 13, the membrane component is formed by arranging hollow flat ceramic membranes 23 with hydrophilic membranes in a frame 28 at intervals, the gas vibration tank 16 can be arranged at the bottommost part of the membrane component, the size and the assembly size are the same as those of the membrane component, and high-pressure air can be pressed into the gas vibration tank to vibrate the membrane component module at a certain frequency when necessary; the hollow flat ceramic membranes are spaced by 5-50 mm, three layers of hollow collecting holes 22 (or two or more layers) are arranged on the hollow flat ceramic membranes, the left end hollow collecting hole is sealed by a plug 26 and is arranged on a left support plate 24 of the frame body, the right end hollow collecting hole is opened and is arranged on a right support plate 25, the membrane surface 21 of the hollow flat ceramic membranes is provided with micropores, a water collecting tank 27 is connected on the right support plate 25 in a sealing way, the hollow collecting hole 22 on the first membrane component is directly communicated with the water collecting pipe 12, or the hollow collecting hole is connected with the water collecting tank 27, the water collecting tank is communicated with the water collecting pipe 12 through a purified water outlet 11 and a water outlet valve 10, one end of the water collecting pipe is provided with a purified water outlet 17, the end part is connected to the purified water tank 18, each membrane component is connected with a screw rod through a flange 29 on the frame body to form, the upper end of the membrane assembly can be directly connected with a raw water inlet pipe I6, preferably is connected with a water distributor 7 in a sealing way, the lower end of the water distributor is provided with a honeycomb-shaped sieve plate 8, the water distributor is then connected with the raw water inlet pipe I6, the sieve holes are round, square, triangular or hexagonal, the upper end of the water inlet pipe is connected in a sealing way, the lower end opening of the membrane assembly is sunk in raw water in a raw water tank 2, so that a sealed filtering channel can be formed in the membrane assembly, a support frame 31 (preferably an elastic support frame) for bearing the membrane assembly can be further arranged in the raw water tank (tank), the bottom of the lower side of the raw water tank is provided with a sewage discharge port 20; in addition, the original water tank is provided with a bearing platform which is provided with a large-flow upper water inlet pump, a back washing pump or an air compressor for air washing, an automatic control system and the like; one end of a hollow flow collecting hole of the hollow flat ceramic membrane sheet is closed, the other end of the hollow flow collecting hole is open and communicated with a water collecting pipe, and the height of a water purifying and draining port 17 on the water collecting pipe is lower than that of the bottom surface of the lowest membrane module. The treatment device also comprises an aeration backwashing device, the aeration backwashing device comprises a backwashing pump 3, a backwashing water inlet pipe 19, a backwashing pipe 5, a backwashing air inlet pipe 14 and an aeration pipe 30, raw water 15 in the raw water main pipe 1 is sent into the water distributor through a raw water inlet pipe II 13 and a water inlet pump 4, one end of the backwashing water inlet pipe is connected with the water purification tank according to the height of the raw water in the raw water tank, the other end of the backwashing water inlet pipe is connected with the backwashing pump, one end of the backwashing pipe is connected with the backwashing pump, the other end of the backwashing pipe is connected with the water collecting pipe, one end of the aeration pipe is connected with an air washing air compressor 32, and the other.
Claims (12)
1. The constant pressure cross flow filtering water treatment process using natural force as power is characterized by comprising the following steps: the treatment process method comprises the following steps: make the frame membrane module with the hollow dull and stereotyped ceramic diaphragm that has hydrophilicity, seal the stack with the frame membrane module and form the membrane sub-assembly, with membrane sub-assembly upper end and inlet tube upper end seal and link to each other, membrane sub-assembly lower extreme opening sinks in raw water, makes the interior sealed filtration passageway that forms of membrane sub-assembly, utilizes the capillary force of hollow dull and stereotyped ceramic diaphragm and the high siphon force that forms of membrane sub-assembly to regard as filtration pressure jointly, through the height of controlling the membrane sub-assembly, makes the filtration pressure value be less than critical pressure value or be less than subcritical pressure value, the last cavity current collection hole one end of hollow dull and stereotyped ceramic diaphragm seals, the other end communicates with.
2. The process for filtering water according to claim 1, wherein the process comprises the following steps: the capillary force of the hollow flat ceramic membrane and the siphon force formed by the height of the membrane assembly are used as the filtering pressure, and the filtering pressure value is smaller than the critical pressure value or smaller than the subcritical pressure value by controlling the height of the membrane assembly and is integrated with the coupling cross-flow filter to filter the raw water.
3. The process for filtering water according to claim 1, wherein the process comprises the following steps: the membrane assembly is characterized in that a water distributor is hermetically arranged at the upper end of the membrane assembly, a honeycomb pore plate for shunting is arranged at the lower end of the water distributor, and the upper end of the water distributor is hermetically connected with a water inlet pipe.
4. The process for filtering water according to claim 1, wherein the process comprises the following steps: the aperture of the hollow flat ceramic membrane is 0.01-100 microns.
5. The process for filtering water according to claim 1, wherein the process comprises the following steps: when the membrane material is an alumina membrane, the membrane aperture of the hydrophilic ceramic membrane is 0.001 multiplied by 10 < -3 > m, the contact angle of the pores of the hydrophilic ceramic membrane is about 45 degrees, and the height difference between the uppermost layer purified water outlet and the lowermost layer purified water outlet of the membrane assembly is less than 2.5 meters or less than 5.4 meters.
6. The process for filtering water according to claim 1, wherein the process comprises the following steps: the hollow flat ceramic membrane is a silicon-aluminum or magnesium ceramic membrane, and the chemical composition range is as follows: SiO 22 ：10-90%、Al2O3：10-95%、MgO：0.1-15%、CaO:0.1-5%、KNaO:0.1-10%、TiO2:0.1-5%、Fe2O3:0.1-3%、LiO20-3%, others: 0 to 3 percent.
7. the process for filtering water according to claim 1, wherein the process comprises the following steps: the hollow flat ceramic membrane mineral composition is as follows: mullite: 0-85%, corundum: 0-50%, quartz: 0-80%, glass phase: 0.5-40%, cordierite: 0 to 95 percent.
8. The process for filtering water according to claim 1, wherein the process comprises the following steps: the membrane module forms a membrane assembly according to layers, and frame bodies of the membrane module are sealed by rubber sealing ring gaskets; hollow flat ceramic membranes (23) are arranged in parallel in the frame body, the space between the hollow flat ceramic membranes is 5-50 mm, and water flow scouring channels are arranged between the membranes and the inner wall of the frame body.
9. The process for filtering water according to claim 1, wherein the process comprises the following steps: the lower end of the membrane assembly is provided with an air vibration box (16) with a support frame, the lower end of the support frame is fixed in the raw water tank (15) and is submerged in the raw water or on the water surface, and the support frame is an elastic support frame (31).
10. The treatment device for realizing the constant-pressure cross-flow filtration water treatment process method taking natural force as power comprises a membrane module (9), a water inlet pipe, a water inlet pump (4), a water collecting pipe (12) and a raw water tank (2), wherein the membrane module is formed by placing hollow flat ceramic membranes with hydrophilic membranes in a frame at intervals, the membrane module is sealed and superposed to form a membrane assembly, the upper end of the membrane assembly is connected with the upper end of the water inlet pipe in a sealing way, the lower end opening of the membrane assembly is submerged in raw water (15) in the raw water tank (2), so that a sealed filtration channel can be formed in the membrane assembly, and one end of a hollow flow collecting hole in the hollow flat ceramic membrane is sealed, and the other end of the hollow flow collecting hole is open and communicated with the water collecting.
11. The processing apparatus of claim 10, wherein: the treatment device also comprises an aeration backwashing device, the aeration backwashing device comprises a backwashing pump, a backwashing water inlet pipe (19), a backwashing pipe (5), a backwashing air inlet pipe (14) and an aeration pipe (30), one end of the backwashing water inlet pipe is connected with the water purification tank, the other end of the backwashing water inlet pipe is connected with the backwashing pump, one end of the backwashing pipe is connected with the backwashing pump, the other end of the backwashing pipe is connected with the water collecting pipe, one end of the aeration pipe is connected with the air washing air compressor (32), and the other end of the aeration pipe is provided with aeration holes and is positioned at the.
12. The processing apparatus of claim 10, wherein: the hollow collecting hole open end in the hollow flat ceramic membrane (23) in each group of membrane modules (9) is connected with a water collecting tank, and the water collecting tank is connected with a purified water outlet (11) and then communicated with a water collecting pipe.
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