EP2566605A1 - Dispositif de filtration à recyclage interne - Google Patents

Dispositif de filtration à recyclage interne

Info

Publication number
EP2566605A1
EP2566605A1 EP11719185A EP11719185A EP2566605A1 EP 2566605 A1 EP2566605 A1 EP 2566605A1 EP 11719185 A EP11719185 A EP 11719185A EP 11719185 A EP11719185 A EP 11719185A EP 2566605 A1 EP2566605 A1 EP 2566605A1
Authority
EP
European Patent Office
Prior art keywords
flat filter
gas
feed
flow
filter modules
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Withdrawn
Application number
EP11719185A
Other languages
German (de)
English (en)
Inventor
Stefan Krause
Ulrich Meyer-Blumenroth
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mann and Hummel Water and Fluid Solutions GmbH
Original Assignee
Microdyn Nadir GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Microdyn Nadir GmbH filed Critical Microdyn Nadir GmbH
Publication of EP2566605A1 publication Critical patent/EP2566605A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/18—Apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/027—Nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/147—Microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/16—Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/08—Flat membrane modules
    • B01D63/082—Flat membrane modules comprising a stack of flat membranes
    • 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
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • 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
    • C02F3/12—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
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/16—Flow or flux control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B01D2311/251—Recirculation of permeate
    • B01D2311/2513—Recirculation of permeate to concentrate side
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/08—Flow guidance means within the module or the apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/12—Specific discharge elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/26—Specific gas distributors or gas intakes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/10—Cross-flow filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/18—Use of gases
    • B01D2321/185—Aeration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/02—Fluid flow conditions
    • C02F2301/028—Tortuous
    • 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 present invention relates to a device and a method for micro, ultra or nanofiltration comprising one or more flat filter modules of parallel and spaced apart flat filter elements and Gasinjektoren a gas lift system for generating a circulating, directed tangentially to the surface of the flat filter elements crossflow flow.
  • Membrane-assisted filtration processes have been used for decades in a large number of industrial and municipal applications, such as wastewater treatment and seawater desalination.
  • a feed overflowed.
  • the pore size of the membranes ranges from about 10 nanometers to several micrometers.
  • the volume through which the feed flows is separated by the membrane from a permeate space.
  • a differential pressure of about 0.1 bar to 100 bar is applied, which causes a mass transport from the flow to the permeate space, wherein permeate (or filtrate) enters the permeate space.
  • Membrane bioreactors (MBR) used for wastewater treatment are preferably operated with a differential pressure in the range from 0.02 to 0.4 bar.
  • the membrane is usually formed as a two-layer composite of a carrier fleece and a porous membrane layer.
  • the porous membrane layer consists of polyethersulfone, polysulfone, polyacrylonitrile, polyvinylidene fluoride, polyamide, polyetherimide, cellulose acetate, regenerated cellulose, polyolefin or fluoropolymer.
  • the porous membrane layer is formed by coating a web or web with polymer solution and precipitating the polymer in a subsequent phase inversion step.
  • a polymer film is suitably stretched to form pores in the polymer film. The stretched polymer film is then laminated to a support web for mechanical stabilization.
  • Filtration membranes produced by these methods are commercially available, for example under the name NADIR ® membranes (MICRODYN-NADIR GmbH, Wiesbaden) or Celgard ® Fiat Sheet Membranes (Celgard Inc., Charlotte, NC, USA).
  • NADIR ® membranes MICRODYN-NADIR GmbH, Wiesbaden
  • Celgard ® Fiat Sheet Membranes Celgard Inc., Charlotte, NC, USA.
  • Membrane modules are equipped with a closed or a single or multi-sided open housing or frame in which flat filter elements or in rare cases wound filters are supported.
  • a membrane module in addition to passages between the filter elements or passages between the turns of the wound filter optionally on the walls of the housing arranged connections for feed, retentate and permeate.
  • the permeate space is bounded by two separate membranes or by two partial surfaces of a one-piece membrane. Between the two membranes or partial surfaces, a porous Permeatspacer is arranged, on the one hand serves as a Stülz Modell for the sensitive membranes on which a transmembrane differential pressure of up to 100 bar loads, and on the other hand provides passages through which the permeate along the inner sides of the Membranes / sections flows off.
  • the permeate space is composed of the entirety of the permeate spaces of all the flat filter elements.
  • a plurality of planar flat filter elements are arranged parallel to one another in a stack. Between each two adjacent flat filter elements spacers are arranged, which keep a passage clear, through which feed and retentate can flow in and out.
  • the spacers consist for example of washers of a polymeric material, which are arranged between the edge regions or edges, in particular the corners of each two adjacent flat filter elements.
  • a frame or housing equipped with equidistant grooves for receiving the edges of the flat filter elements may be used.
  • MBR membrane bioreactors
  • the wastewater is treated physically, chemically, and biologically in several steps until the wastewater treatment Membrane reached.
  • mechanical-physical pretreatments the wastewater is freed of particles, fibers and coarse materials.
  • coarse filtration large particles that can cause damage to the membranes are removed by rakes and sieves.
  • fine sieves in a size range of 0.05-3 mm are usually used for prefiltration.
  • the wastewater is also freed from heavy particles (eg sand) and oils and fats by means of a sand and fat catcher.
  • the wastewater is treated biologically and chemically.
  • sludge biologically and chemically.
  • microorganisms which enzymatically convert and eliminate high-molecular organic pollutants.
  • the remaining after the enzymatic reaction substances are used by the microorganisms either for cell assembly or for energy production under oxygen consumption.
  • the resulting oxygen consumption is to be covered by a sufficient supply of oxygen, which is why aeration tanks are provided with Belüfrungsurbanen.
  • 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 means that there are no bacteria in the drain of the membrane revitalization system and possibly even viruses are separated by sorption effects. This greatly reduces organic residue contamination.
  • EU Bathing Water Directive [75/160 / EEC, 1975] are complied with by MBR.
  • the solids-free process in both the municipal and in the industrial sector offers a 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 has only a small footprint due to the adjustable high TS content and the elimination of NachGermanbecken.
  • membrane bioreactors Due to the independence of the sedimentation behavior, the activated sludge concentration (biomass concentration, expressed as dry DM substance) over conventional processes.
  • Membrane bioreactors are usually operated with TS concentrations of 8 to 15 g 1.
  • the reactor volume of a membrane bioreactor can be reduced, so that higher volume loads are possible.
  • 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.
  • EP 1 445 240 describes a biological membrane reactor with a cyclically operated ventilation system.
  • the reactor comprises a tank filled with feed with one or more membrane modules, which optionally have flat filter modules made of vertically spaced-apart flat filter elements.
  • the feed is supplied by means of a cyclically operated ventilation system air.
  • the ventilation system has ventilation nozzles, which are arranged in the tank below the flat filter modules.
  • a feed volume is required which is at least twice as large as the free flow volume of the filter modules of the filtration device; Accordingly, the filtration devices have a space or area requirement which corresponds approximately to twice their base area;
  • the object of the present invention is to overcome the above drawbacks and a filtration device with increased filtration efficiency and reduced To create energy and space requirements.
  • the invention aims to reduce the energy requirements of one or more gas lift systems used to generate the crossflow flow.
  • a filtration device is to be provided in which the surfaces of the filtration membranes are cleaned in situ during the ongoing filtration operation and the permeate throughput is maintained at a high level.
  • a device for micro-, ultrafiltration or nanofiltration comprising one or more flat filter modules of parallel and spaced apart flat filter elements and gas injectors of one or more gas lift systems for generating a circulating, tangential to the surface of the flat filter elements directed crossflow flow with at least a riser region in which the crossflow flow substantially vertically still flows up and at least one fall region in which the crossflow flow substantially vertically still flows down, and the riser region 10 to 100% and the fall region 10 to 100% of a flow volume the at least one flat filter module interspersed.
  • (m - n) flat filter modules are equipped with gas injectors of another gas lift system, the gas injectors are equipped with gas outlets and vertical projections of the gas outlets 10 to 100%, preferably 30 to 60% and in particular 45 to 55% of a horizontal cross-sectional area AF of each (m - n) enforce flat filter modules;
  • the device has a housing with side walls and possibly a bottom wall;
  • the housing has at least one supply line for feeding feed and at least one discharge line for discharging feed and / or retentate;
  • the at least one discharge line is designed siphon-like, so that at least part of the feed flows from the interior of the housing through the discharge to the outside flowing feed and / or retentate in the vertical direction upwards;
  • the at least one drain is disposed in an upper third of a sidewall and preferably includes a shutter for retaining solids within the housing;
  • the at least one drain is disposed in the bottom wall and preferably includes a hood for retaining solids inside the housing;
  • flat filter module designates a single flat filter element or a stack of flat filter elements arranged parallel and spaced from one another.
  • a flat filter module according to the invention is equipped with a closed housing or a housing or frame open on one or more sides, in which the flat filter element (s) are held.
  • flat filter modules are provided without a frame, wherein adjacent flat filter elements are mechanically coupled in each case by a connecting permeate tube and / or by spacers.
  • the spacers are preferably formed as cylindrical or rectangular spacers made of a polymeric material and arranged in the edge region and in particular at the corners of two adjacent flat filter elements.
  • the spacers are coupled by means of clips (clips) or adhesive bonds with the flat filter elements.
  • the housing, frame or spacers provide mechanical stability to the flat filter module and protect the sensitive membranes of the flat filter elements from cracking under tensile or compressive loading.
  • the term "supply volume” designates the free, i.e. volume fraction of a flat filter module which can be flowed through by a liquid.
  • flow volume number x area X distance.
  • a free volume fraction of the size area x distance / 2 is assumed for the two outer flat filter elements of the flat filter module.
  • the size of the flow volume corresponds approximately to the outer volume of the flat filter module minus the product of number, area and thickness of the flat filter elements.
  • the terms “rising area” and “falling area” designate predetermined partial volumes of the flow volume of the flat filter elements, wherein the riser areas are acted upon by the gas injectors of one or more gas lift systems with a gas such as air.
  • a gas lift system mammoth pumps are preferably used.
  • mammoth pumps are especially often used for circulating liquids with a solids content, in particular of activated sludge in sewage treatment plants.
  • a gas lift system such as a mammoth pump, upward flow is created by localized injection of a delivery gas into a fluid to be delivered.
  • the gas lift system comprises one or more gas injectors designed as hollow bodies, in particular as tubes, with one or more, preferably planar, gas outlets or gas nozzles. Due to the injected gas, the density of the liquid is reduced locally, due to the Archimedes principle of gravity, ie upward buoyancy acts.
  • conveying gas is preferably used air which is blown by means of a pressure-generating device, such as a blower, a compressor or the like under slight overpressure in the liquid.
  • gas lift systems include a pipe or riser having a lower intake port and an upper exhaust port. The outlet opening is vented to the surrounding atmosphere, so that the conveying gas which is blown into the liquid between the suction opening and the outlet opening can escape.
  • the riser delimits the conveying or rising region, in which the liquid is conveyed upwards, from a surrounding liquid volume.
  • a riser is not mandatory.
  • gas lift systems are usually used without riser. In this case, air is blown into the activated sludge or feed at predetermined points within the clarifier, with riser regions forming in the liquid volume located above the injection points with fluid flowing upwards.
  • the cross-section or the lateral extent of the riser areas is determined by the respective lateral arrangement of the gas outlets or gas nozzles of the gas injectors of the / of the gas lift system / s.
  • the transport gas blown into the riser areas rises to the surface of the liquid and is released into the atmosphere, whereby the density of the near-surface liquid rises to its normal value.
  • the volume penetrated by the downflowing or sinking liquid is referred to below as the drop zone.
  • the liquid volume in the rise region differs from the liquid volume in the fall region by an increased content of gas bubbles.
  • the use of two gas lift systems or pressure-generating devices such as blowers or compressors provided.
  • the adjustable valves are arranged in the supply lines of the gas lift system or in the flat filter modules.
  • a blower / compressor can be used to apply gas to a first part of the flat filter modules, while a second part is disconnected from the gas supply.
  • the second parts of the flat filter modules is supplied with gas, while the first part is disconnected from the gas supply. Accordingly, a first and second part of the flat filter modules can be alternately charged with gas.
  • a method for micro-, ultra- or nanofiltration of liquids by means of a device comprising one or more flat filter modules of parallel and spaced apart flat filter elements and gas injectors of one or more gas lift systems, wherein a circulating, directed tangentially to the surface of the flat filter elements Crossflow Flow is generated with at least one riser region in which the crossflow flow substantially vertically still flows up, and at least one case region in which the crossflow flow substantially vertically still flows down, and the rise range 10 to 100% and the fall range 10 to 100% of a flow volume of the at least one flat filter module interspersed.
  • Figure 1 is a clarifier with several interconnected filtration devices.
  • Fig. 2 shows a known filtration device
  • FIG. 3 shows a first filtration device according to the invention
  • Figs. 4-5 are partial perspective views of the filtration device of Fig. 3;
  • FIGS. 6-8 show further embodiments of filtration devices according to the invention.
  • FIG. 9 Feed and retentate inlets and outlets;
  • FIG. 9 Feed and retentate inlets and outlets;
  • FIG. 11 shows a filtration device with flat filter modules, in which alternately gas can be injected.
  • FIG. 1 schematically shows a plan view of a clarification tank 1 filled with activated sludge or feed 2 with a plurality of filtration devices 3 interconnected via permeate lines 6, each containing one or more stacked flat filter modules 4 of flat filter elements 5.
  • the Penneat space of each flat filter element 5 is connected to one of the permeate lines 6 such that permeate flows out of the Penneatraum via the Permeattechnischen 6 and, as indicated by directional arrows 7, can be derived.
  • Filtration devices 3 commonly used in the prior art typically have a box-shaped frame open at the bottom and top, which serves as a supporting structure for the flat filter modules 4.
  • the frame may be formed as a housing with 1 to 4 side walls.
  • FIG. 2 shows a sectional view of a known filtration device 3 with a flat filter module 4 of flat filter elements 5 and side walls 300.
  • a distance between each two adjacent flat filter elements 5 is denoted by D.
  • gas injectors 100 of a gas lift system are arranged below the flat filter module 4 arranged.
  • the gas injectors 100 are connected via lines (not shown) with a blower or a compressor through which a gas, in particular air under low pressure and with a predetermined flow rate (m 3 / h) is supplied.
  • the gas injectors 100 are equipped with gas outlets through which the gas in the form of bubbles 110 is discharged into the activated sludge or feed 2.
  • the gas bubbles 110 By the gas bubbles 110, the local density of the feed 2 is reduced, so that it is displaced according to the Archimedian principle or is exposed to a vertically upward buoyancy force. As a result, a continuous vertical upward and tangential to the surface of the flat filter elements 5 directed crossflow flow forms, which is indicated in Fig. 2 by directional arrows 200.
  • the upward flowing feed 2 is replaced by "fresh" more or less gas-free feed 2, which flows from the area below the gas injectors 100. Accordingly, a circulating flow is formed with upwardly directed crossflow portions 200 and downflow backflows 210.
  • the gas injectors 100 and the gas outlets are arranged below the flat filter modules 4 such that the upwardly directed crossflow flow 200 passes through the entire flow volume of the flat filter module 4, while the downstream return flow 210 is located outside, ie in the feed 2 surrounding the feed device 3 ,
  • the clarifier 1 or the filtration devices 3 are dimensioned relative to one another such that the sum of the throughput volumes of all flat filter modules 4 corresponds approximately to half of the feed volume 2 contained in the clarifier 1. If this volume ratio is approximately maintained, then the feed 2 is circulated in the ratio 1: 1 in the case of the crossflow recirculation 200, 210. This situation is reproduced to scale in FIG. 1, wherein the surface 8 is approximately as large as the cross-sectional area of a flat filter module 4 and the sum of the cross-sectional areas of all flat filter modules 4 and the surrounding surfaces 8 corresponds to the cross-sectional area of the clarifier 1.
  • FIG. 3 shows a first filtration device 10 according to the invention with a housing with side walls 11, a flat filter module 4 with flat filter elements 5 and gas injectors 13, which are connected to a gas lift system.
  • the pressure-generating device of the gas lift system which is preferably a blower and the supply lines from the pressure-generating device to the gas injectors 13 are not shown in Fig. 3 in order to keep the representation clearly.
  • one or more filtration devices are supplied by one or more, in particular by two pressure-generating devices.
  • the invention relates on the one hand filtration devices with gas injectors 13 and ports for connecting the gas injectors 13 with a network of one or more pressure-generating devices and on the other hand filtration devices, which also have a dedicated pressure-generating device in addition to the gas injectors 13.
  • the distance between each two adjacent flat filter elements 5 is designated D in FIG.
  • the filtration device 10 differs from known devices in that a circulating crossflow flow 50, 60 is substantially limited to the internal volume of the filtration device 10, wherein a riser portion of the gas lift system 10 to 80% of the flow volume of the flat filter module 4 and a falling area of the gas lift system 90th to 20% of the flow volume of the flat filter module 4 interspersed.
  • FIG. 3 shows optional gas injectors 13 '(drawn with dashed lines) which can be connected to a further gas lift system and can be supplied with gas independently of the gas injectors 13.
  • the gas injectors 13 and 13 ' are provided for alternate operation which allows the direction of the circulating crossflow flow 50, 60 to be reversed.
  • a reversal of the direction of the circulating crossflow flow 50, 60 is advantageous in the use of granules for the mechanical cleaning of the membrane surfaces.
  • Such granules which preferably consist of polymeric particles having a specific gravity in the range of 1.0 to 1.5 kg / dm, are carried along by the recirculating crossflow flow 50, 60, gently removing abrasive fouling deposits continuously formed on the membrane surfaces . Due to gravity acting on the granules, the rates of granule particles differ relative to the membrane surface in the rise and fall regions, i.e., the granularity of the particles. in the upflow or downflow crossflow flow significantly from each other. Accordingly, their cleaning effect differs, with the higher relative speed of the granulate particles in the falling areas effecting a more effective removal of the fouling coverings. By reversing the direction of the circulating crossflow flow 50, 60 at regular time intervals, it is possible to ensure uniform cleaning of the membrane surfaces over the entire flow volume of the filtration device.
  • FIG. 4 shows a partial perspective view of the filtration device 10.
  • the gas injectors 13 have gas outlets 14 on their upper side facing the filtration module 4.
  • Vertical projections 140 of the gas outlets 14 pass through defined regions of the flow volume of the flat filter module 4.
  • Each of the vertical projections 140 corresponds to the "ideal" path of a gas bubble rising from one of the gas outlets 14 to the flat filter module 4 without lateral deflection. Due to turbulence in the liquid 2, the actual path of each ascending gas bubble deviates from the vertical one Projection 140 off.
  • the gas injectors 13 are preferably designed in such a way that their gas outlets 14 are arranged in horizontally aligned contiguous surface areas and are uniformly spaced laterally from one another.
  • the lateral distance of adjacent gas outlets 14 is 0.2 to 50 mm, so that the associated bubble cones superimpose or unite after an ascent of 1 to 10 cm.
  • FIG. 5 shows a horizontal cross-sectional area AF of the flat filter module 4 with a length of A and a width of F, the cross-sectional area AF being indicated merely by a small shaded partial area in order to provide a perspective view of other parts of FIG. 5 not to obscure.
  • the proportion of the cross-sectional area AF penetrated by the vertical projections 140 of the gas outlets 14 is 10 to 80%, preferably 30 to 60% and in particular 45 to 55%. According to the arrangement shown in Fig. 5, these conditions correspond to the following mathematical relations:
  • the gas outlets 14 may be arranged in any desired manner such that their vertical projections 140 pass through a continuous partial surface or a plurality of partial surfaces of any shape, separated from one another by approximately 2 to 4 separate parts. According to the invention, however, the symmetrical configuration shown in FIGS. 3 to 5 with two rectangular partial surfaces arranged below the left and right sides of the flat filter module 4 is preferred.
  • the gas injectors 13 have a common construction in the prior art and include pipes whose walls have numerous openings and the outside of which is enveloped by an elastic, liquid-impermeable membrane with fine slits. The elastic membrane is biased such that the fine slots serving as gas outlets 14 behave as one-way valves.
  • a bypass circuit is formed in the liquid volume 2 surrounding the filtration device 10.
  • the shunt circuit 80 is formed because, on the one hand, permeate which flows out of the flat filter elements 5 is replaced by feed or surrounding liquid 2 and, on the other hand, because part of the circulating crossflow flow 50, 60 with the liquid volume surrounding the filtration device 10 2 interacts.
  • the gas lift system of the filtration device (s) is designed such that it is suitable to deliver a gas flow of 0.1 to 0.5 m per m membrane surface of the flat filter elements and hour in the activated sludge or feed 2.
  • the pressure-generating device of the gas lift system such as a blower or a compressor is equipped with a controllable drive, which allows the per unit time of delivered gas (m 3 / h) to control and on the for the entire membrane surface of one or more of the invention Filtration devices required value.
  • the pressure-generating unit is designed so that it generates the pressure required at the gas injectors for gas delivery even at high delivery rates to overcome the hydrostatic pressure of the feed 2 and the ⁇ ffhungswiderstand the gas outlets.
  • the volume flows of the various liquids converted in the filtration device are approximately in the following ratio:
  • feed feed 4x to 6x permeate flow
  • Relation (i) states that the volume of the crossflow flowing through the flat filter modules per unit time, that is to say the feed which flows aiif- and downwards or recirculates in the rise and fall areas, is 100 to 300 times the permeate volume discharged from the flat filter modules.
  • relation (ii) states that the volume of the (fresh) feed supplied per unit time is 4 to 5 times the permeate volume.
  • feed volume retentate volume + permeate volume
  • FIG. 6 shows a further example of a filtration device 10 'according to the invention, which is based on the design principle shown in FIGS. 3 to 5, wherein a rise region comprises 10 to 80%, preferably 30 to 60% and in particular 45 to 55% of the flow volume of a Flat filter module 4 and a fall range 90 to 20%, preferably 70 to 40% and in particular 55 to 45% of the flow volume of the flat filter module 4 passes.
  • the riser region is characterized in that gas injectors 13 with gas outlets are arranged below the flat filter elements 5 of the flat filter module 4.
  • the filtration device 10 ' comprises a housing with four substantially closed side walls 11 and is provided on an upper side with orifices 17, which define a derivative 16 for feed and / or retentate.
  • the orifices 17 prevent solids, such as optionally used granules for cleaning the surfaces of the flat filter elements 5, from being flushed out of the interior of the filtration device 10 '.
  • the specific gravity of the optional granules is greater than the specific gravity of water, which is 1 kg / dm. Accordingly, granulate particles are suspended in the liquid 2 only in the riser region of the crossflow flow 50, 60 or carried upward. Near the surface of the liquid at the reversal points of the crossflow flow 50, 60, the granulate particles are carried down or fall down by gravity.
  • the orifices 17, which are preferably designed as flat, horizontally arranged wall elements in the manner shown in FIG. 6, represent a practically insurmountable barrier for the granulate particles.
  • Gas injectors 13 are arranged in a bottom region of the filtration device 10 '. Below the gas injectors 13 is a bottom wall 12 with leads or passages 15th intended for feed.
  • the filtration device 10 ' comprises a subframe 18 which rests on the bottom 400 of a container for the liquid 2 to be cleaned and determines the vertical position of the gas injectors 13 and the flat filter module 4 in the liquid 2.
  • the further reference symbols of FIG. 6 have the same meaning as explained above in connection with FIG. 3.
  • the filtration device 20 comprises a housing with four substantially closed side walls 21 and a bottom wall 22.
  • the filtration device 20 is preferably arranged in the liquid 2 to be filtered so that the upper edges of the side walls 21 protrude beyond the surface of the liquid to be filtered 2 and the inner volume of the filtration device 20 is substantially completed with respect to the surrounding liquid volume 2.
  • at least one supply line 25 and one discharge line 26 are provided, which are each arranged in one or more of the side walls 21.
  • the at least one supply line 25 is mounted in a lower third of the filtration device 20 approximately at the level of the gas injectors 13 of the gas lift system.
  • the discharge line 26 is preferably arranged in an upper third of the filtration device 20 below and near the surface of the liquid 2.
  • a volume flows through the supply line 25 per unit of time into the interior of the filtration device which corresponds at least to the amount of liquid discharged as permeate from the flat filter module 4.
  • a bypass circuit 80 is formed whose current strength depends on the intensity of the internal crossflow flow 50, 60 and the geometry and arrangement, but in particular on the internal cross section of the supply and discharge lines 25, 26.
  • the shunt circuit 80 determines the volume of liquid that is exchanged per unit time between the interior of the filtration device 20 and the surrounding liquid 2. By appropriate dimensioning of the inner cross sections of the leads 25 and the leads 26, this exchange volume can be regulated.
  • the discharge line 26 is provided with a diaphragm 27.
  • the specific gravity of the material constituting the granules is greater than the specific gravity of water. Accordingly the granules are suspended in the liquid 2 only in the riser region of the crossflow flow 50, 60 or mit Hoodt upward. Near the surface of the liquid at the reversal points of the crossflow flow 50, 60, the granulate particles are carried down or fall down by gravity.
  • a discharge of the granular particles in the discharge line 26 can be effectively prevented by means of a diaphragm 27, which is preferably formed in the manner shown in Fig. 7 as a concave element which surrounds the passage of the discharge line 26 through the wall 21 and has an upper edge , which is located above the passage of the discharge line 26.
  • the filtration device 30 comprises a housing with four substantially closed side walls 31 and a bottom wall 32.
  • the filtration device 30 is preferably arranged in the liquid 2 to be filtered such that the upper edges of the side walls 31 protrude beyond the surface of the liquid to be filtered 2 and the inner volume of the filtration device 30 is compared to the surrounding liquid volume 2 is substantially complete.
  • at least one supply line 35 and a discharge line 36 is provided.
  • the at least one feed line 36 is preferably tubular with an inlet opening near the surface of the liquid 2 and a passage to the filtration device 30 in a lower third of one of the side walls 31 near gas injectors 13 of a gas lift system.
  • the derivative 36 is disposed in the bottom wall 32.
  • the discharge line 36 is designed siphon-like, so that from the interior of the filtration device 30 flows through the discharge line 36 to the outside flowing feed and / or retentate at least a portion in the vertical direction upwards.
  • the drain 36 comprises a hood 37 for retaining granules so that it is not discharged from the filtration device 30.
  • the filtration devices 10, 20 and 30, analogous to the filtration device 10 'shown in Fig. 6 are equipped with a base 18.
  • the gas injectors 13 shown in Figures 3 to 8 are tubular, wherein the longitudinal axis of each gas injector 13 is substantially aligned in a horizontal plane and in a direction parallel to the lower edges of the flat filter elements 5 direction. Notwithstanding the exemplary embodiments of FIGS. 3 to 8, according to the invention, filtration devices are also provided in which the longitudinal axis of each Gas injector 13 is substantially aligned in a horizontal plane and in a direction perpendicular to the lower edges of the flat filter elements 5 extending direction.
  • FIG. 9 shows further examples according to the invention of inlets and outlets for feed and retentate.
  • Fig. 9 (a) Shown in Fig. 9 (a) is a siphon-like tubular feed line 250 arranged in a lower third of a side wall 21 of a filtration device of the type shown in Fig. 7.
  • the flow from a surrounding liquid volume into the interior of the filtration device is indicated by a directional arrow 81.
  • FIG. 9 (b) shows a siphon-like tubular discharge line 260 which is arranged in an upper third of a side wall 21 of a filtration device constituted analogously to FIG. 7.
  • the flow from the interior of the filtration device to the surrounding liquid volume is indicated by a directional arrow 82.
  • a siphon-like tubular drain 360 which is disposed in a bottom wall 32 of a filtration device of the type shown in Fig. 8.
  • the flow from the interior of the filtration device to the surrounding liquid volume is indicated by a directional arrow 83.
  • FIG. 9 further embodiments of feed and discharge lines for feed and retentate are provided according to the invention, in which a passage through a side or bottom wall of the filtration device is surrounded by a retention box with four walls such that a liquid flows outwardly from the interior of the filtration device to a surrounding fluid volume, travels a vertical leg in a direction opposite to gravity.
  • the filtration device 40 comprises m flat filter modules 4, 4 ', of which n flat filter modules 4 are equipped with gas injectors 13 of a gas lift system.
  • the letters m and n denote natural numbers that have the following conditions
  • the remaining (m - n) flat filter modules 4 ' have no gas injectors.
  • a gas such as Air injected into the flat filter modules 4, so that in these an upwardly directed crossflow flow 70 is formed, which in turn induces a downward crossflow flow 71 in adjacent flat filter modules 4 '.
  • the gas injectors 13 are equipped with gas outlets 14 whose vertical projections pass through 10 to 100%, preferably 30 to 60% and in particular 45 to 55% of a horizontal cross-sectional area AF of each of the n flat filter modules 4.
  • the (m-n) flat filter modules 4 ' are connected to gas injectors 13' of a further gas lift system.
  • This arrangement makes it possible to inject gas into the flat filter modules 4 or 4 'alternately by means of the gas injectors 13 or 13'. Accordingly, an upwardly directed crossflow flow 70 or a downwardly directed crossflow flow 71 can alternately be produced in the flat filter modules 4 or in the flat filter modules 4 '.
  • the flat filter modules 4 and 4 ' are spaced apart to illustrate the modular structure of the devices 40 and 41.
  • the space required, the device 40, 41 is reduced and the downflowing flow of feedflow 71 concentrated on the respective designated flat filter modules.
  • a flat filter module 4 and a flat filter module 4 * are arranged side by side in the filtration devices 40 and 41.
  • arrangements are provided in which a flat filter module 4 or 4 'is surrounded on its four sides by four flat filter modules 4' and 4, respectively (checkered arrangement).
  • the filtration devices 10 ', 20, 30, 40, 41 contain granules which circulates with the crossflow flow 50, 60 inside the filtration devices 10', 20, 30, 40, 41 and at the surfaces the flat filter elements 5 adhering residues, especially a biological fouling layer (membrane fouling) mechanically removed.
  • the granules consist of non-porous particles of a polymeric material having a density of 1.0 to 1.5 kg / dm 3 , preferably 1.0 to 1.3 kg / dm 3 , and in particular 1.0 to 1.1 kg / dm 3 .
  • the polymeric material is selected from the group comprising polypropylene containing mineral particles, polycarbonate blends, polyurethane thermoplastic elastomers, polymethyl methacrylate, polybutylene terephthalate, polyoxymethylene, polyethylene, and polyvinyl chloride.
  • the particles of the granules have an average diameter of less than 5 mm, in particular from 1.5 to 3.5 mm.
  • the particles 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 plasticized and injected through a nozzle into a precipitation bath. In this case, essentially spherical, lens or cylindrical polymer particles are produced in which fillers are optionally embedded.
  • the polymer particles produced are then sieved and dried.
  • the size and surface quality of the particles can be adjusted in a wide range via the diameter of the nozzle openings, the pressure, the composition of the precipitation bath and the process temperature.
  • the particles have a surface with an average roughness Rtm of less than 40 ⁇ , preferably less than 30 ⁇ , and in particular less than 20 ⁇ .
  • the average roughness Rtm of the particles is determined in accordance with DIN EN ISO 4287. For Durcli entry the measurement is first taken of at least 12 of the particles by means of a molding compound a half-page impression.
  • 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).
  • a primary profile is recorded on the half-sided concave markings of the particles by means of a DIN EN ISO 3274 compliant stylus instrument (eg Hommel Tester T 4000).
  • the measuring tip of the stylus instrument is placed as centrally as possible through the respective impression of a particle.
  • the spherical, lens or cylindrical surface contour and any existing long-wave surface structure of the particles or the corresponding imprints 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 its total height Rt (maximum height between the highest peak and the deepest valley). Finally, the average roughness Rtm is determined as the mean value of the roughnesses Rt of the at least 12 molded particles.
  • the concentration of the granules in the filtration devices 10 ', 20, 30 is, based on the liquid volume 1 to 10 kg m 3 , in particular about 3 to 5 kg / m 3 .

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Nanotechnology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Organic Chemistry (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Filtering Of Dispersed Particles In Gases (AREA)

Abstract

L'invention concerne un dispositif de micro-, ultra- ou nano-filtration, qui comprend un ou plusieurs modules de filtration plats constitués d'éléments de filtration plats (5) agencés parallèlement et espacés les uns des autres, et des injecteurs de gaz (14) d'un ou de plusieurs systèmes de siphon de gaz (13) pour la formation d'un courant à écoulement transversal en circulation, orienté tangentiellement à la surface des éléments de filtration plats, comprenant au moins une zone ascendante, dans laquelle le courant à écoulement transversal s'écoule essentiellement verticalement vers le haut, et au moins une zone descendante, dans laquelle le courant à écoulement transversal s'écoule essentiellement verticalement vers le bas, la zone ascendante prévalant sur 10 à 100 % et la zone descendante sur 10 à 100 % d'un volume d'avancée du ou des modules de filtration plats.
EP11719185A 2010-05-06 2011-04-28 Dispositif de filtration à recyclage interne Withdrawn EP2566605A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010019505.7A DE102010019505B4 (de) 2010-05-06 2010-05-06 Filtrationsvorrichtung mit interner Rezirkulation
PCT/EP2011/002129 WO2011137990A1 (fr) 2010-05-06 2011-04-28 Dispositif de filtration à recyclage interne

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EP2566605A1 true EP2566605A1 (fr) 2013-03-13

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US (1) US10040030B2 (fr)
EP (1) EP2566605A1 (fr)
CN (1) CN102917774B (fr)
DE (1) DE102010019505B4 (fr)
WO (1) WO2011137990A1 (fr)

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CA2798889A1 (fr) * 2011-12-16 2013-06-16 Meurer Research Inc. Methode et systeme de nettoyage des filtres a membrane
US20140238936A1 (en) * 2013-02-28 2014-08-28 Genesys International Limited Reverse osmosis and nanofiltration membrane cleaning
DK178159B1 (en) 2014-02-03 2015-07-06 Sani Membranes Aps Filter plate assembly
FR3030481B1 (fr) * 2014-12-23 2017-01-20 Bfg Env Tech Dispositif mobile de traitement biologique des eaux usees du type a bioreacteur.
DK180105B1 (en) 2018-03-08 2020-05-04 Sani Membranes Aps A FILTER-PLATE WITH EXTERNAL FLOW AREA

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DE102010019505B4 (de) 2016-09-29
CN102917774B (zh) 2016-07-06
US10040030B2 (en) 2018-08-07
WO2011137990A1 (fr) 2011-11-10
CN102917774A (zh) 2013-02-06
DE102010019505A1 (de) 2011-11-10
US20130043189A1 (en) 2013-02-21

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