EP2274077A1 - Verfahren zur reinigung von filtrationsmembranmodulen sowie membranbioreaktor-system zum aufbereiten von roh- oder abwasser bzw. belebtschlamm - Google Patents
Verfahren zur reinigung von filtrationsmembranmodulen sowie membranbioreaktor-system zum aufbereiten von roh- oder abwasser bzw. belebtschlammInfo
- Publication number
- EP2274077A1 EP2274077A1 EP09737841A EP09737841A EP2274077A1 EP 2274077 A1 EP2274077 A1 EP 2274077A1 EP 09737841 A EP09737841 A EP 09737841A EP 09737841 A EP09737841 A EP 09737841A EP 2274077 A1 EP2274077 A1 EP 2274077A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- particles
- filtration
- membrane
- wastewater
- activated sludge
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 162
- 238000001914 filtration Methods 0.000 title claims abstract description 105
- 239000002351 wastewater Substances 0.000 title claims abstract description 44
- 239000010802 sludge Substances 0.000 title claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000004140 cleaning Methods 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims description 40
- 239000002245 particle Substances 0.000 claims abstract description 100
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- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 8
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 16
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- 230000015572 biosynthetic process Effects 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- SOCTUWSJJQCPFX-UHFFFAOYSA-N dichromate(2-) Chemical compound [O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O SOCTUWSJJQCPFX-UHFFFAOYSA-N 0.000 description 4
- 239000012466 permeate Substances 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
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- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 239000004695 Polyether sulfone Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
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- 150000002896 organic halogen compounds Chemical class 0.000 description 2
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- 230000036284 oxygen consumption Effects 0.000 description 2
- 229920006393 polyether sulfone Polymers 0.000 description 2
- 229920001296 polysiloxane Polymers 0.000 description 2
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000010561 standard procedure Methods 0.000 description 2
- DOBUSJIVSSJEDA-UHFFFAOYSA-L 1,3-dioxa-2$l^{6}-thia-4-mercuracyclobutane 2,2-dioxide Chemical compound [Hg+2].[O-]S([O-])(=O)=O DOBUSJIVSSJEDA-UHFFFAOYSA-L 0.000 description 1
- 238000012935 Averaging Methods 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 229910019093 NaOCl Inorganic materials 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
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- 241000700605 Viruses Species 0.000 description 1
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- 229940010514 ammonium ferrous sulfate Drugs 0.000 description 1
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- 229910000389 calcium phosphate Inorganic materials 0.000 description 1
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- 235000011010 calcium phosphates Nutrition 0.000 description 1
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- 239000003054 catalyst Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
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- 230000002255 enzymatic effect Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- IMBKASBLAKCLEM-UHFFFAOYSA-L ferrous ammonium sulfate (anhydrous) Chemical compound [NH4+].[NH4+].[Fe+2].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O IMBKASBLAKCLEM-UHFFFAOYSA-L 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
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- 238000011065 in-situ storage Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- LNQCJIZJBYZCME-UHFFFAOYSA-N iron(2+);1,10-phenanthroline Chemical compound [Fe+2].C1=CN=C2C3=NC=CC=C3C=CC2=C1.C1=CN=C2C3=NC=CC=C3C=CC2=C1.C1=CN=C2C3=NC=CC=C3C=CC2=C1 LNQCJIZJBYZCME-UHFFFAOYSA-N 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
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- 229910000370 mercury sulfate Inorganic materials 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 235000014593 oils and fats Nutrition 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 235000021317 phosphate Nutrition 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920005597 polymer membrane Polymers 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000011045 prefiltration Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000001878 scanning electron micrograph Methods 0.000 description 1
- YPNVIBVEFVRZPJ-UHFFFAOYSA-L silver sulfate Chemical compound [Ag+].[Ag+].[O-]S([O-])(=O)=O YPNVIBVEFVRZPJ-UHFFFAOYSA-L 0.000 description 1
- 229910000367 silver sulfate Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 230000003442 weekly effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
- B01D65/025—Removal of membrane elements before washing
-
- 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
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
- B01D65/04—Membrane cleaning or sterilisation ; Membrane regeneration with movable bodies, e.g. foam balls
-
- 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
- C02F2303/16—Regeneration of sorbents, filters
-
- 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
Definitions
- the invention relates to a process for the purification of filtration membrane modules, which are used in the treatment of raw or wastewater or activated sludge.
- membrane bioreactors MRR
- filtration membrane modules for the treatment of raw or waste water
- the membranes used for filtration consist for example of polymeric materials such as polyethylene, polypropylene, polyethersulfone, polyvinylidene fluoride or similar polymers.
- the pore sizes of the membranes are in the range between 0.001 and 1 ⁇ m for these applications.
- the activation process for wastewater treatment is carried out with a separation of the biomass from the purified water by means of ultrafiltration or microfiltration membranes.
- the polymer membranes are immersed directly in the activated sludge and the treated wastewater is vacuum drawn or drained by gravity.
- the wastewater is treated physically, chemically and biologically in several steps until it reaches the membrane.
- the wastewater is freed of particles, fibers and coarse materials.
- coarse filtration large particles that could cause damage to the membranes are removed by rakes and screens.
- fine sieves in a size range of 0.05-3 mm are usually used as pre-filtration.
- the wastewater is also freed from heavy particles (e.g., sand) and oils and fats by means of a sand and grease trap.
- the wastewater is treated biologically and chemically.
- the activated sludge biologically and chemically.
- biomass contains in its biomass, the enzymatic potential for the implementation of high-molecular pollutants, so that they can be eliminated.
- the dissolved substances are used by the biomass either for cell building or for energy production under oxygen consumption.
- the resulting oxygen consumption must be covered by a sufficient supply of oxygen, which is why aeration tanks with ventilation directions are provided.
- Prerequisite for the function of the process is the retention of biomass in the system. Therefore, the biomass is separated by a membrane filtration of the purified wastewater and returned to the aeration tank. Overgrown animated sludge is removed as excess sludge.
- Various precipitants and flocculants such as ferric chloride or polymers for removing colloidally and particulate dissolved liquid constituents, are usually used in conjunction with a filtration stage.
- MBR solids-free process
- This also means that there are no bacteria in the drain of the membrane revitalization system and possibly even sorbed by sorption effects viruses. This reduces the organic residue contamination due to complete separation.
- the hygienically relevant values of the EU Bathing Water Directive [75/160 / EEC, 1975] are complied with by MBR.
- the solids-free process both in the municipal sector as well as in the industrial sector offers great potential for wastewater reuse.
- water recycling can be achieved through water recycling up to the water cycle closure.
- Another advantage is that this method requires only a small footprint due to the adjustable high TS content and the elimination of secondary sedimentation.
- the activated sludge concentration (biomass concentration, expressed as dry substance TS) can be increased compared to conventional methods.
- Membrane bioreactors are usually operated with TS concentrations of 8 to 15 g / l. In comparison with the conventional activation process, the reactor volume of a membrane bioreactor can be reduced so that higher volume loads are possible.
- membrane bioreactor process which is generally based on the aerobic activation process combined with a membrane filtration unit
- the biomass is recirculated via the membrane filtration unit as a concentrate, while the purified water is separated as filtration permeate.
- membrane fouling A problem with the use of membrane filters in the field of wastewater treatment is the so-called “membrane fouling", which consists in the formation of deposits on the membranes which reduce the flow of the liquid to be purified.
- DE 102 20 916 A1 describes a filtration device and a membrane bioreactor, which are operated in the filtration medium under conditions such that the membrane fouling and deposits on the membrane surfaces are reduced.
- the filtration device for separating the particles from a liquid to a fiber bundle combined hollow fiber membranes, which are traversed from the outside to the inside of the liquid and then the filtered liquid is withdrawn from at least one of the ends of the hollow fiber membranes.
- the filtration device further comprises a gas supply device for purging the outside of the hollow fiber membranes with a gas.
- the fiber bundle is wound on the outer peripheral surface of a carrier of the gas supply device.
- EP 1 734 011 A1 discloses a method for improving the flow in a membrane bioreactor, in which a certain proportion of cationic, amphoteric and zwitterionic polymers or a combination thereof is added.
- the proportion of added polymers is 10 to 2000 ppm, based on the total membrane bioreactor volume.
- the polymers have a molecular weight of 10,000 to 20,000,000 Da.
- the addition of the above-mentioned polymers should, in particular, reduce inorganic fouling which results from the precipitation of limestone CaCO 3 from the wastewater to be purified on the membrane surfaces.
- the pH increases, which in turn promotes the precipitation of calcium phosphate and iron oxide. Precipitation of carbonates and phosphates in wastewater takes the form of small particles retained on the membrane surfaces.
- membrane fouling results in a decrease in flow and permeability due to precipitation of bioactive solids, colloids, attachment of particles or macromolecular particles to the membrane surface. It is difficult to accurately describe the fouling process due to the heterogeneity of the activated sludge. Factors such as the characteristics of the biomass, the extracellular polymeric substance, pore size, surface characteristics and membrane material, and the Construction of the filtration membrane modules and operating conditions affect fouling growth. For example, biofouling is most common in nanofiltration and reverse osmosis. The reason is that the membranes can not be disinfected with chlorine to kill bacteria. Biofouling is mainly due to the complex growth behavior of the bacteria.
- microorganisms The type of microorganisms, their growth rate and concentration on the membranes depends mainly on the critical factors such as temperature, pH, dissolved oxygen concentration and the presence of organic and inorganic nutrients. It should be noted that the microorganisms get into the filtration plants via the air and / or water.
- pretreatment of the raw or waste water before flowing into the activated sludge by means of various filtration steps, as mentioned above, including fine mesh with a mesh width of 0.5 to 3 mm are used.
- the liquid to be purified is circulated along the membrane surface, with submerged modules having venting devices installed underneath the membrane modules that induce upward flow.
- Dry Cleaning The steps are used to prevent or at least reduce membrane fouling. Dry cleaning is required to remove the membrane fouling layers on and within the membranes. Dry cleaning causes significant operating costs as the membranes are out of service during cleaning and therefore additional membranes must be installed. Furthermore, it is disadvantageous that the chemicals used, such as, for example, sodium hydrochlorite NaOCl, impair the environment and contribute to the formation of adsorbable organic halogen compounds (AOX). In addition, an additional infrastructure is needed for the chemical cleaning (pumps, chemical tanks, leakage measurements, protective equipment, ...) which is costly. Often, the membranes are chemically cleaned in a separate cleaning tank to save chemicals because these cleaning tanks have small volumes.
- AOX adsorbable organic halogen compounds
- the membrane module must be removed from the filtration tank or tank and installed in the cleaning tank or tank. In the cleaning tank / tank then the chemical cleaning takes place. The operating personnel must be trained to handle these chemicals and the dry-cleaners are labor-intensive. Overall, the dry cleaning represents a significant cost and environmental factor.
- VA TECH WABAG GmbH Vienna, author: F. Klegraf, entitled “Control of Fouling and Scaling on Submerged Filtration Systems in Membrane Aeration Systems”
- abrasive, inert, inorganic, porous materials described which can dissolve deposits on the surface of the membrane by continuous action. This application is not uncontroversial, because it must be feared that the abrasive forces not only remove the deposits but also damage the sensitive surfaces of the membranes.
- expanded clay is mentioned, which is introduced into the reactor. Through sieves, the expanded clay is retained in the reactor. The turbulence introduced into the reactor with the purging air is sufficient to homogenize the expanded clay in the system.
- the increase in filtration efficiency can be measured, and by carefully increasing the concentration of expanded clay in the activated sludge, the setpoint of filtration performance can be achieved 75% after 40 days of test.
- the further increase in the expanded clay concentration in the reactor does not entail a lasting improvement in the filtration results.
- the density of porous expanded clay increases with time due to water absorption. As a result, the expanded clay particles are heavier and settle within the reactor and circulate due to the liquid flow only slightly. To stimulate the circulation of expanded clay particles, then larger amounts of compressed air are required, which, however, due to the increased supply of compressed air in the liquids to be cleaned other process parameters adversely affected can be, for example, the compliance with predetermined oxygen target values, considerably more difficult.
- the ascending speed of the particles is determined by the size of the resulting air bubbles, but not by the amount of air introduced.
- the object of the invention is to provide such conditions for a process for the purification of filtration membrane modules, which are used in the treatment of raw or wastewater or activated sludge, in which the deposits caused by the membrane fouling are greatly reduced and mechanical damage to the membranes is largely avoided.
- the operating costs should be reduced and the flow of the wastewater to be cleaned through the membranes should be kept constant for a long time.
- This object is achieved in that the filter membrane module to be cleaned, introduced into a cleaning tank / tank or arranged in a filtration tank / tank, is surrounded by a liquid containing non-porous, biologically resistant particles and gas introduction into circulation is added and that the surface located on the outer surfaces of the membranes of the filtration membrane module, the so-called membrane fouling, is mechanically removed by the particles.
- the process for treating raw or wastewater or activated sludge comprises the steps of mechanical, physical and chemical pretreatment of the raw or wastewater or activated sludge,
- a membrane bioreactor system having one or more filtration tanks, in each of which at least one submerged filtration membrane module is arranged,
- the particles circulating within the filtration tank carry out an upward movement induced by gas inflow, in particular by compressed air, and a downward movement caused by gravity.
- the non-porous particles are made of inert polymer material having a density of 1.0 to 1.5 kg / dm 3 .
- inert is here and below synonymous with “biologically resistant” or not degradable by the bacteria used in activated sludge.
- the polymer material is advantageously selected from the group consisting of polypropylene, mineral particles containing, polycarbonate blends, thermoplastic polyurethane elastomers, polymethyl methacrylate, polybutylene terephthalate, polyoxymethylene, polyethylene, polyvinyl chloride.
- the particles have an average diameter of less than 5 mm and have a spherical, cylindrical or lenticular shape.
- particles are used whose surface has an average roughness Rtm of less than 40 ⁇ m, preferably less than 30 ⁇ m, and in particular less than 20 ⁇ m.
- the average roughness Rtm is determined by averaging the roughness Rt (DIN EN ISO 4287) of several particles.
- a membrane bioreactor system with a filtration tank / tank is provided with at least one submerged filtration membrane module.
- the system is characterized by the fact that the raw or wastewater or the activated sludge in the filtration tank contains non-porous, biologically resistant particles.
- the distance between two membranes in the filtration membrane module is up to 8 mm and the mean diameter of the particles (granules) is less than 5 mm.
- a supply device for gas, in particular compressed air is provided, whose compressed air flow moves the particles upwards between the membranes.
- the maximum specific surface loading of the membranes in the filtration membrane module is 1 to 80 l / (m 2 xh). It can be seen that the permeability, as the ratio of the specific surface area of the membrane to the transmembrane pressure in the filtration membrane modules, is constant over more than 6 months of operation.
- the method achieves the advantages that a mechanical removal of the membrane fouling layers takes place without additional chemical cleaning, that the flow of the liquid to be cleaned through the membranes remains constant over a period of several months, abrasive damage of the membrane surfaces by particles occurs only to a very small extent and thus the operating costs can be reduced because the intervals for cleaning the membrane surfaces are extended.
- membranes which already have a fouling layer characterized by a very low permeability and high transmembrane pressures
- the membrane module is installed in a cleaning container and the liquid in the cleaning container particles are added, which are set in motion.
- the membranes are cleaned by the particles inside the cleaning tank.
- the particles can remain in the cleaning tank and be reused, resulting in further cost savings. Subsequently, the cleaned membrane modules can be reinstalled for filtration operation.
- FIG. 1 is a schematic representation of a membrane bioreactor system with a filtration device
- Fig. 8 is an electron micrograph of a membrane surface, the fouling layer was removed without the participation of particles.
- FIG. 1 schematically shows a membrane bioreactor system 1 for treating raw or waste water, a denitrification device 4, a nitrification device 6 and a filtration tank 11 in which a plurality of filtration membrane modules 12a, 12b, 12c .... are located.
- the denitrification device 4 raw or waste water is introduced via a supply line 2, after it has been previously chemically-mechanically pretreated. Furthermore, nutrients enter the activation stage via a line 3.
- the filtration tank 11 for example, five filtration membrane modules are arranged, of which three filtration membrane modules 12a, 12b and 12c are in operation, as will be explained in more detail below.
- filtration membrane modules are acted upon via a supply device 5 for gas, in particular for compressed air, at the lower end of the respective filtration membrane modules with compressed air.
- gas in particular for compressed air
- the excess sludge is transported out of the filtration tank 11.
- the upper ends of the filtration membrane modules are connected to a raw or waste water return line. Furthermore, the water purified from the biologically active material is withdrawn from the filtration tank by means of a pump in the permeate line.
- FIG. 2 schematically shows a section through a filtration tank 11 containing a filtration membrane module 12.
- the distance between two adjacent in a filtration membrane module 12 ter membranes 7 and 8 is up to 8 mm.
- non-porous, resistant particles 9 are registered, which are present as granules.
- the supply device 5 for gas, in particular compressed air, can be found at the lower end of the filtration membrane module 12.
- the gas or air bubbles rising from the supply device 5 flow up between the membranes of the filtration membrane module 12 and carry the particles 9 whose density is 1.0 to 1.5 kg / dm 3 .
- the particles 9 outside of the filtration membrane module 12 descend downward due to gravity. In this way, a circulation of the particles 9 is achieved, which mechanically ablate the forming membrane fouling layers on the membrane surfaces during the high flow, wherein an abrasive damage to the membrane surfaces is almost completely avoided.
- the non-porous particles 9 are made of inert polymer material and have, as already mentioned, a density of 1.0 to 1.5 kg / dm 3 .
- the density of the polymer material is 1.00 to 1.40 kg / dm 3 and, in particular, the density of the polymer material is 1.00 to 1.10 kg / dm 3 .
- the polymer material is selected from a group comprising polypropylene containing mineral particles, polycarbonate blends, thermoplastic polyurethane elastomers, polymethyl methacrylate, polybutylene terephthalate, polyoxymethylene, polyethylene, polyvinyl chloride. The criteria for the selection of the particles are summarized in Table 1 below.
- Each of the filtration membrane modules 12 (a, b, c.) Shown in Figure 1, when their permeability decreases significantly, are removed from the filtration tank and placed in a purification tank similar to the filtration tank for purification.
- the cleaning tank contains a liquid, preferably pure water, which contains non-porous, biologically resistant particles of the same nature as the particles in the filtration tank.
- the liquid is circulated with the introduction of gas, in particular with air injection, so that the particles mechanically remove the deposit located on outer surfaces of the membranes of the filtration membrane module, the so-called membrane fouling.
- Table 1 Criteria for Particle (Granules) Selection
- the polymer material of the particles 9 is preferably polypropylene (PP) filled with minerals (PPTV20).
- the particles 9 have an average diameter of less than 5 mm, in particular from 1.5 to 3.5 mm.
- the median diameter of polypropylene (PP) filled with minerals (PPTV20) is in the range of 2.0 to 3.0 mm.
- the particles 9 are produced from the respective polymer material by means of known granulate processes. For example, a possibly mixed with fillers powder of the respective polymer or copolymer is liquefied and injected through a nozzle into a precipitation bath. In this case, essentially spherical, lens or cylindrical polymer particles 9 are produced, in which fillers are optionally embedded. The polymer particles 9 produced are then sieved and dried. The size and surface quality of the particles can be adjusted by the diameter of the nozzle openings, the pressure, the composition of the precipitation bath and the process temperature in wide ranges.
- the particles 9 have a surface with an average roughness Rtm of less than 40 ⁇ , preferably less than 30 ⁇ m, and in particular less than 20 ⁇ m.
- the average roughness Rtm of the particles 9 is determined according to DIN EN ISO 4287.
- the molding or impression material used is a silicone-based precision impression material, for example highly viscous condensation-crosslinking polysiloxane according to DIN 13 913 A2, ISO 4823 or Elastosil Ml 470 (Wacker-Chemie GmbH). After the impression material has cured, the hemisphere of the impression By means of a DIN EN ISO 3274 compliant stylus instrument (eg Hommel Tester T 4000) a primary profile is recorded.
- the measuring tip of the stylus device is placed as centrally as possible through the respective impression of a particle 9.
- the spherical, lens or cylindrical surface contour and any existing long-wave surface structure of the particles 9 or the corresponding impressions in the impression material is removed by software-based filtering according to DIN EN ISO 11562 from the measured primary profile to a roughness profile and the total height Rt (maximum Height between the highest peak and the deepest valley).
- the average roughness Rtm is determined as the mean value of the roughnesses Rt of the at least 12 molded particles.
- Table 2 summarizes the diameters and density of selected particles for pure water testing.
- the membrane bioreactor system 1 shown schematically in Figure 1 was operated with synthetic waste water at about 25 ° C.
- the pilot plant was operated for several months using the aforementioned three parallel filtration tanks with the modules 1a2a, 12b and 12c.
- effluent water quality was recorded for turbidity and COD concentration, operating conditions for activated sludge solids content, activated sludge concentration TS, temperature, pH and membrane conditions such as flow, transmembrane pressure TMP, permeability.
- the resulting sludge load is 0.1 kg COD / kg TS / d.
- the activated sludge concentration is up to 15 g / l.
- Chemical Oxygen Demand (COD) is a measure of the sum of all substances present in water that can be oxidized under certain conditions. It indicates the amount of oxygen in mg / l that would be needed for its oxidation if oxygen were the oxidant.
- COD Chemical Oxygen Demand
- a water sample is strongly acidified with sulfuric acid and heated with a predetermined precise amount of strong oxidant potassium dichromate, with the addition of silver sulfate as a catalyst. The amount of dichromate consumed is calculated by determining the remaining dichromate and from this the equivalent amount of oxygen O 2 is calculated.
- the chloride For chloride-containing samples, the chloride must first be removed or masked with mercury sulfate so that oxidation to chlorine does not erroneously increase the reading.
- the remaining amount of dichromate is determined ditremetically with ammonium ferrous sulfate solution and ferroin indicator according to the German standard methods.
- the COD determination is usually carried out by means of so-called cuvette rapid tests. These test kits already contain all the necessary reagents and require very little laboratory equipment. The dichromate consumption is determined photometrically - in contrast to the German standard method - and the corresponding special photometer also shows the result converted as oxygen in mg / l.
- the chemical oxygen demand serves in particular as a sum parameter for quantifying the load of waste water with organic substances. It covers both biodegradable and non-biodegradable organic substances, but also some inorganic substances.
- the pilot plant was operated with synthetic water with a long sludge retention time of more than 50 days.
- the hydraulic retention time was less than 10 hours.
- High recirculation rates were set in the filtration tanks.
- the flocculation and activated sludge volume index of the activated sludge were low. Since the filtration efficiencies partly also depends on the structure of the activated sludge, the filterability of the sludge used was low.
- the flow rate and transmembrane pressure were recorded continuously and the permeability, that is, the flow divided by the transmembrane pressure, was calculated and used as an indicator of the current membrane state and the membrane fouling situation.
- FIG. 4 the result of a cleaning is shown.
- a cleaning already provided with a fouling layer membranes is possible.
- a filtration membrane module which had a permeability of only 20% of its initial permeability, was in a cleaning tank with water and an addition of 1 to 10 kg / m 3 , in particular about 3 to 5 kg / m 3 granules with about 10 to 14 hours Air fumigated, so that the particles circulated. After completion of the cleaning, the module was put back into operation and showed its initial permeability.
- FIG. 5 shows an electron micrograph of a fresh membrane material, for example a polyethersulfone membrane with a pore size of 0.05 ⁇ m. There are no surface defects.
- the membranes of a filtration membrane module exhibit slight abrasive effects that can be recognized as physical injuries to the membrane surface.
- Fig. 7 shows electron micrographs of membranes installed in the reference line operating without particle recirculation. These membranes show no physical damage and their membrane surfaces are consistent with the membrane surfaces of fresh membranes.
- non-porous particles prevents the formation of membrane fouling layers largely due to mechanical erosion and thereby the permeability of the membranes is kept constant over long periods of time.
- turbidity measurements In the treated wastewater, it was determined by turbidity measurements that neither sludge nor other particles are present in the effluent water.
- a cleaning of already contaminated membranes can be achieved by the addition of particles. The observed minor physical damage of the membranes by the particles does not affect the separation of the biomass from the purified water.
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- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
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Abstract
Description
Claims
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DE200810021190 DE102008021190A1 (de) | 2008-04-29 | 2008-04-29 | Verfahren zur Reinigung von Filtrationsmembranmodul sowie Membranbioreaktor-System zum Aufbereiten von Roh- oder Abwasser bzw. Belebtschlamm |
PCT/EP2009/002944 WO2009132797A1 (de) | 2008-04-29 | 2009-04-23 | Verfahren zur reinigung von filtrationsmembranmodulen sowie membranbioreaktor-system zum aufbereiten von roh- oder abwasser bzw. belebtschlamm |
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EP2274077A1 true EP2274077A1 (de) | 2011-01-19 |
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EP09737841A Withdrawn EP2274077A1 (de) | 2008-04-29 | 2009-04-23 | Verfahren zur reinigung von filtrationsmembranmodulen sowie membranbioreaktor-system zum aufbereiten von roh- oder abwasser bzw. belebtschlamm |
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US (1) | US8580115B2 (de) |
EP (1) | EP2274077A1 (de) |
CN (1) | CN102015077A (de) |
DE (1) | DE102008021190A1 (de) |
WO (1) | WO2009132797A1 (de) |
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AU2010204829A1 (en) | 2009-01-13 | 2011-07-28 | Access Business Group International Llc | Gravity feed water treatment system |
DE102009028165B4 (de) * | 2009-07-31 | 2017-03-30 | Endress+Hauser Conducta Gmbh+Co. Kg | Verfahren und Vorrichtung zur automatisierten Bestimmung des chemischen Sauerstoffbedarfs einer Flüssigkeitsprobe |
JP2012166142A (ja) * | 2011-02-14 | 2012-09-06 | Hitachi Plant Technologies Ltd | 膜分離活性汚泥システム及び膜分離活性汚泥方法 |
JP5605802B2 (ja) * | 2011-02-14 | 2014-10-15 | 株式会社日立製作所 | 平膜ろ過装置及び平膜ろ過方法 |
DE102011114634A1 (de) | 2011-10-04 | 2013-04-04 | Mn-Beteiligungs Gmbh | Abrasionsbeständige Membran und Verfahren zu ihrer Herstellung |
CA2798889A1 (en) | 2011-12-16 | 2013-06-16 | Meurer Research Inc. | Method and system for cleaning membrane filters |
RU2666867C2 (ru) * | 2012-09-21 | 2018-09-12 | Ди.Си. УОТЕР ЭНД СЬЮЭР ОТОРИТИ | Способ и устройство для обработки воды с использованием сеток |
CN102897896B (zh) * | 2012-09-29 | 2014-02-26 | 北京碧水源膜科技有限公司 | 一种管式膜生物反应器 |
FR3015463B1 (fr) * | 2013-12-20 | 2016-01-29 | Veolia Water Solutions & Tech | Procede de traitement d'eau sur membranes integrant une adsorption sur materiau pulverulent adsorbant et des moyens permettant de limiter l'abrasion des membranes. |
CN106458668A (zh) * | 2014-03-04 | 2017-02-22 | 氧膜有限公司 | 一种膜曝气生物膜反应器(mabr) |
US20160096146A1 (en) * | 2014-10-07 | 2016-04-07 | Derek Oxford | Microfiltration systems for cleaning waste water |
US10023481B2 (en) | 2014-10-17 | 2018-07-17 | Clemson University | Materials and methods for reducing biofouling in water treatment membrane systems |
CN113244774A (zh) | 2014-10-22 | 2021-08-13 | 科氏分离技术解决方案公司 | 使用膜束封罩和脉冲曝气的膜组件系统以及操作方法 |
CN107530636A (zh) * | 2015-03-31 | 2018-01-02 | 水技术国际有限责任公司 | 用于处理废水的增强膜生物反应器方法 |
USD779631S1 (en) | 2015-08-10 | 2017-02-21 | Koch Membrane Systems, Inc. | Gasification device |
CN105600921B (zh) * | 2015-12-18 | 2018-10-30 | 南京大学 | 一种填料老化生物膜的原位活化方法 |
US11117821B2 (en) * | 2016-12-06 | 2021-09-14 | Grundfos Holding A/S | Multi-parameter enhancement of membrane bioreactor process efficiency by biomass selection and selective biomass wasting |
DE102017116156B4 (de) * | 2017-07-18 | 2019-06-27 | Kay Gunther Gabriel | Filtrationssystem |
CN107935077A (zh) * | 2017-12-21 | 2018-04-20 | 深圳市沃泰克环保设备有限公司 | 一种净水器滤芯 |
JP7082681B2 (ja) * | 2018-11-15 | 2022-06-08 | 旭化成株式会社 | 多孔質膜を用いたろ過方法 |
CN110078245A (zh) * | 2019-06-06 | 2019-08-02 | 淄博博立特冷冻空调设备有限公司 | 一种大循环倍率浓水回流膜法废水回收回用系统 |
CN112387118B (zh) * | 2019-08-19 | 2023-06-30 | 北京奥博水处理有限责任公司 | 一种在线自清洗陶瓷膜过滤器 |
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JPH11300350A (ja) * | 1998-04-23 | 1999-11-02 | Kantou Regional Constr Bureau Ministry Of Constr | 膜処理装置および河川水浄化システム |
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JPH0574357A (ja) | 1991-09-13 | 1993-03-26 | Nec Corp | 多空胴クライストロン |
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JP3821566B2 (ja) | 1998-01-16 | 2006-09-13 | 株式会社クボタ | 膜分離活性汚泥処理方法 |
DE19953459A1 (de) * | 1999-11-05 | 2001-05-10 | Gva Ges Fuer Verfahren Der Abw | Reinigungssystem für Abwasserbehandlungsanlagen |
DE10220916A1 (de) | 2002-05-10 | 2003-11-27 | Sfc Umwelttechnik Gmbh Salzbur | Hohlfasermembran-Filtrationsvorrichtung und deren Verwendung bei der Reinigung von Abwasser sowie Membranbioreaktor |
JP2005074357A (ja) * | 2003-09-02 | 2005-03-24 | Ngk Insulators Ltd | 膜分離活性汚泥法における膜洗浄方法 |
CN100563798C (zh) * | 2005-02-25 | 2009-12-02 | 日本碍子株式会社 | 膜分离活性污泥法中的膜洗净方法 |
US8017014B2 (en) | 2005-06-01 | 2011-09-13 | Nalco Company | Method for improving flux in a membrane bioreactor |
DE102006008453A1 (de) * | 2006-02-17 | 2007-08-23 | Itn Nanovation Ag | Reinigungsverfahren für Abwässer |
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2008
- 2008-04-29 DE DE200810021190 patent/DE102008021190A1/de not_active Withdrawn
-
2009
- 2009-04-23 CN CN2009801154432A patent/CN102015077A/zh active Pending
- 2009-04-23 WO PCT/EP2009/002944 patent/WO2009132797A1/de active Application Filing
- 2009-04-23 US US12/988,667 patent/US8580115B2/en not_active Expired - Fee Related
- 2009-04-23 EP EP09737841A patent/EP2274077A1/de not_active Withdrawn
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JPH11300350A (ja) * | 1998-04-23 | 1999-11-02 | Kantou Regional Constr Bureau Ministry Of Constr | 膜処理装置および河川水浄化システム |
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DE102008021190A1 (de) | 2009-11-05 |
WO2009132797A1 (de) | 2009-11-05 |
CN102015077A (zh) | 2011-04-13 |
US20110042308A1 (en) | 2011-02-24 |
US8580115B2 (en) | 2013-11-12 |
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