WO2001051186A1 - Procede et dispositif pour liberer des chemins d'ecoulement dans des modules de filtration - Google Patents

Procede et dispositif pour liberer des chemins d'ecoulement dans des modules de filtration Download PDF

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Publication number
WO2001051186A1
WO2001051186A1 PCT/CH2000/000675 CH0000675W WO0151186A1 WO 2001051186 A1 WO2001051186 A1 WO 2001051186A1 CH 0000675 W CH0000675 W CH 0000675W WO 0151186 A1 WO0151186 A1 WO 0151186A1
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WO
WIPO (PCT)
Prior art keywords
retentate
filtration
membranes
suction
permeate
Prior art date
Application number
PCT/CH2000/000675
Other languages
German (de)
English (en)
Inventor
Eduard Hartmann
Original Assignee
Bucher-Guyer Ag
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 Bucher-Guyer Ag filed Critical Bucher-Guyer Ag
Publication of WO2001051186A1 publication Critical patent/WO2001051186A1/fr

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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
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/04—Backflushing
    • 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

Definitions

  • the invention relates to a method for clearing retentate flow paths of material located therein in filtration modules which are operated in a membrane filtration system in cross-flow mode, flow blockages occurring in these retentate flow paths, and a device for carrying them out.
  • Such methods are used in plants which separate substance mixtures on porous membranes into portions with different particle sizes.
  • the substance mixtures to be separated are guided tangentially along the membranes in flow paths so that the retained parts (retentates) do not deposit on the membranes and clog their pores for the passage of the permeates.
  • the goal of wastewater treatment is the production of fresh water, which should be separated as far as possible from the contaminants.
  • fruit juice production the fruit juice should be separated from the cloudy substances of the fruit mash.
  • a plant for the treatment of water in a circuit with tangential filtration is known from EP 0,433,200 AI (GIE ANJOU-RECHERCHE).
  • This system is used in the filtration and purification of liquids, in particular water, with a circuit for the water to be treated, which comprises at least one membrane for tangential filtration.
  • the task was to provide a system for tangential filtration with membranes with ozone injection, which allows the chemical and internal surface clogging of the membrane to be limited.
  • This system comprises means for introducing an oxidizing gas into the liquid to be treated in the circuit in front of the membrane.
  • Microbubbles of the gas mentioned are of such a size that they generate turbulence in the liquid on the right-hand side of the membrane. Together with the oxidation, these limit the silting up of the membrane mentioned and lead to an improvement in the flow rate and the physico-chemical properties of the filtrate.
  • the system comprises means for introducing chemical reagents and / or adsorbents into the filtration circuit.
  • the mentioned blockages or blockages of the cross-flow channels have partly product-related and partly plant-related causes.
  • the filtration process used is mostly a batch process.
  • a product as retentate is fed from a batch tank via a retentate circulation pump to filter module units, passes through it in cross flow and then returns to the batch tank.
  • the turbid substances retained by the membranes of the module units concentrate over time.
  • the viscosity in the retentate finally increases by a factor of approx. 50 to 50 mPas or higher.
  • the flow behavior of such an ochviscous retentate is then highly pseudoplastic and thixotropic and leads to the blockages mentioned.
  • membranes used for such filtration processes are usually arranged on membrane tubes with a diameter between approx. 1-30 mm and an uninterrupted length between approx. 1-80 m in multi-channel modules.
  • modules a large number of membrane tubes are simultaneously flowed in parallel in the crossflow, the supplied product stream being divided between the individual membrane tubes.
  • a malfunction occurs. e.g. If the power supply is interrupted, the viscosity of the retentate increases very quickly due to the lack of material shear. After a short interruption, it is usually no longer possible to restart all membrane pipes connected in parallel; the blockages mentioned can no longer be released, at least in some membrane pipes. If the filtration can be continued with a few membrane tubes, the viscosity in the blocked membrane tubes increases even further.
  • Tubular filtration membranes on polymer material are preferably used in straight parts with a maximum length of 3 m. These straight parts are with
  • connection sheets connected to longer series open the connecting bends and try to flush the blockage with a water lance.
  • the object of the invention is to design the generic method for clearing retentate flow paths in such a way that the disadvantages of known methods and devices described above are largely eliminated.
  • the method according to the invention for clearing retentate flow paths of the type mentioned at the outset is characterized by the fact that, by lowering the pressure of the material present on the retentate side of the membranes to a value below a pressure below the permeate side of the membranes, blocking retentate fractions together with from the permeate side of the membranes the membranes of material flowing back are sucked off on the retentate side.
  • the retentate-side release of the membranes with at least one sensor is monitored and the suction process is automatically ended after a predetermined proportion of blocking retentate components have been extracted.
  • FIG. 1 is a schematic representation of a simple cross-flow filtration system with means according to the invention for clearing a retentate flow path
  • FIG. 2 shows a schematic illustration of a further cross-flow filtration system with means according to the invention for clearing several retentate flow paths
  • Fig. 3 is a diagram of processes when clearing a retentate flow path according to the invention in a filtration module.
  • this system comprises a container 1 for a product 2, which is to be filtered.
  • the product 2 is fed to a filtration module 5 in a manner known per se via a connecting line 3 and a feed pump 4.
  • the filtration module 5 comprises porous membranes 6, which are used in microfiltration or ultrafiltration according to their separation limit.
  • the product is separated into a permeate as a filtrate and a retentate.
  • a discharge line 7 is provided for the permeate and an outlet line 8 for the retentate. Via the outlet line 8, a throttle valve 9 and a throttle valve 10, the retentate returns to the container 1 with the product 2, as a result of which, in a manner known per se, a closed retentate circuit given is.
  • a feed line 11 is arranged on the container 1 for supplying the product 2.
  • a filtration system described so far is known. It is preferably operated in such a way that the product 2 is first filled up to a level 12 in the container 1 via the feed line 11 and that there is still a constant amount of work, batch or batch for processing in the container 1.
  • the container 1 is therefore also referred to as a batch tank 1. 1 thus operates in batch mode.
  • the product 2 in the container 1 reaches ever higher degrees of thickening.
  • the porous membranes 6 in the filtration module 5 are preferably arranged on support tubes, as shown in FIG. 3 in detail.
  • product 2 flows through the inside of the support tubes in the filtration module 5 (core-side feeding) and the permeate is discharged from the outside of the support tubes via the discharge line 7 after penetration of the membranes 6.
  • a shut-off valve 13 is arranged between the outlet of the feed pump 4 and the inlet of the filtration module 5, and the outlet of the feed pump 4 can be fed back into the batch tank 1 via a further shut-off valve 14 and a short-circuiting return line 15 via the throttle valve 10.
  • the input of the filtration module 5 is via another
  • Shut-off valve 16 and a further return line 17 are connected to the inlet of the feed pump 4, and a further shut-off valve 18 is arranged between this inlet of the feed pump 4 and the batch tank 1.
  • shut-off valves 18, 13 and the throttle valve 9 are open and the shut-off valves 16, 14 are closed.
  • the shut-off valves 18, 13, 9 are closed and the shut-off valves 16, 14 are opened.
  • the suction effect of the feed pump 4 then reduces the pressure of the material 2 present on the retentate side of the membranes 6 to a value below a pressure present on the permeate side of the membranes 6.
  • the low-viscosity material which then flows back from the permeate side of the membranes 6 through the membranes 6 releases the blocking of the material 2 in the carrier tubes of the membranes 6 and is together with the blocking material 2 on one side from the inlet of the filtration module 5 via the feed pump 4 and the return lines 17, 15 sucked into the batch tank 1.
  • the feed pump 4 is advantageously equipped on the pressure side with a throttle valve 50 and on the suction side with a vacuum probe 51, which is in a controlling operative connection 52 with the throttle valve 50.
  • the suction vacuum of the feed pump 4 can thus be restricted by throttling on the pressure side in such a way that no cavitation and thus no cavitation damage to the Feed pump 4 occur.
  • a tank 21 for a solvent is connected to the discharge line 7 via a further shut-off valve 20.
  • Permeate, water, alkalis, acids, chlorine or enzymes are preferably suitable as such solvents.
  • a further shut-off valve 22 is arranged on the discharge line 7, which is closed when the retentate flow paths are cleared.
  • a permeate back pressure can be introduced into the discharge line 7 via a further shut-off valve 23 by means of a liquid or a gas, which supports the backflow according to the arrow 19.
  • FIG. 3 The processes involved in clearing a retentate flow path in a filtration module are shown in detail in FIG. 3.
  • a bundle of support tubes for the porous membranes 6 is arranged, the inner sides of which are flowed through in parallel with the product via a feed line.
  • a pressure pl, with pl ⁇ p2, or a partial vacuum, under which the retentate is located, has now been generated on the inside of the carrier tube 25, for example with a crossflow filtration system according to FIG. 2, by aspirating the retentate on both sides.
  • 3 shows flows at the two ends of the interlocking 2 'the permeate 26 due to the partial vacuum p1 through the membrane 6 back inward and thereby removes solids 2''from the interlocking 2'.
  • the blocking 2 ′ is broken down and the retentate flow path is cleared again.
  • This breakdown of the blockages 2 ' is particularly effective here because not only is p2 set larger pl, but a partial vacuum, eg 0.2 bar, is used for pl, which loosens the blockages 2' by reducing internal friction.
  • FIG. 2 shows a schematic representation of a further cross-flow filtration system with means for clearing several retentate flow paths, components in FIG. 1 corresponding to FIG. 2 having the same reference numerals as in FIG. 1.
  • the system according to FIG. 2 comprises four filtration modules 5 ', 5' ', 5' '', 5 '' '', to which the product 2 is fed in parallel from the batch tank 1 via the connecting line 3 and the feed pump 4.
  • the retentate circuit is closed by the output line 8 to the batch tank 1 common to all filtration modules.
  • the filtration modules 5 ', 5'',5''', 5 ''' according to FIG. 2 give the permeate 26 directly to the Surroundings.
  • This permeate 26 is collected here by an unpressurized trough 30, from which it is discharged with an overflow line 7 'when a level 31 is reached.
  • the tub 30 has a removable cover 32 and at the bottom an emptying opening 7 ′′, to which a shut-off valve 22 for emptying and a further shut-off valve 22 ′ for a residual drain are connected.
  • An opening for an inlet 21 ′ of a solvent or of permeate is provided in the lid 32, so that the permeate level can be filled up to level 31. Then they stand Filtration modules 5 ', 5'',5''', S '''' under a pressure p2 according to the surrounding liquid column of the permeate 26.
  • Level 31 is selected so that the filtration modules with the permeate sides of their membranes are completely immersed in the permeate, so that when sucking back into the retentate flow paths, no air is sucked in, which in certain cases would not solve the blockages as well.
  • weak blockages however, it was found that the permeate sides of the membranes can also be surrounded by air and that the retentate can nevertheless be suctioned off.
  • the use of such non-pressurized troughs 30 is particularly advantageous in the case of large filtration modules, such as those by winding up longer ones
  • Pipe membranes with filtration areas of over 100 m can be built.
  • the filtration system according to FIG. 2 has further devices, the function of which can be controlled by a number of shut-off valves.
  • the shut-off valve 18 at the outlet of the batch tank 1, throttle valve 9 at the retentate outlet of the filtration modules 5 ', 5' ', 5' '', 5 '' '', shut-off valve 13 between the feed pump 4 and the inlet of the filtration modules 5 ', 5 '', 5 '' ', 5' ''', and shut-off valve 14 between the outlet of the feed pump 4 and the batch tank 1 correspond to those of the system according to FIG. 1.
  • a second return line 33 for sucking off the retentate via a shut-off valve 34, a special suction pump 35 with a vacuum probe 53 and a further shut-off valve 36 are arranged in the batch tank 1 according to FIG. 2.
  • a suction line 37 with a shut-off valve 38 is arranged between the inlet and outlet of the filtration modules 5 ', 5'',5''', 5 '''', which allows switching between one-sided and two-sided suction. If the retentate is not to be fed into batch tank 1, it can be discharged via a shut-off valve 39 at the outlet of the suction pump 35 or via a shut-off valve 40 at the outlet of the feed pump 4.
  • shut-off valve 34 is closed and the shut-off valves 16, 14, 10 are opened. If suction is to be carried out on both sides at the retentate inlet and at the retentate outlet of the filtration modules 5 ', 5' ', 5' '', 5 '' '', the shut-off valve 38 is also opened.
  • a line 45 for the addition of a viscous liquid is arranged at the inlet of the feed pump 4 via a shut-off valve 44.
  • This addition should take place because, depending on the type of pump, the suction effect of the feed pump 4 is improved by simultaneously feeding a highly viscous auxiliary liquid slowly. Concentrated clear apple juice is suitable as such auxiliary liquid in screw eccentric pumps.
  • the filtration system In order to identify the release of the retentate flow paths and the function, the filtration system according to FIG. 2 has a pressure sensor 41 at the input of the filtration modules, and a turbidity sensor 42 and 43 at the outputs of the feed pump 4 and the suction pump 35. These turbidity sensors 42 or 43 no longer indicate cloudiness, if no blocking retentate portions, but only clear permeate is sucked off.
  • the suction process for example with water on the permeate side, lasts until the material extracted on the retentate side becomes clear. This process can vary depending on the type of constipation and the
  • Membrane tube length can last from a few minutes to a few hours. Depending on the equipment of the filtration system, no manual work is required and the process can be monitored using the turbidity sensors 42 or 43.
  • the temperature of the solvent is preferably selected between 20 ° C and 80 ° C depending on the material base of the membrane support tubes.
  • the procedure for clearing is based on a
  • the microfiltration module used has the following specification: Number of parallel membrane tubes 4 pieces inner diameter of the membrane tubes 5.5 mm wall thickness of the membrane tubes 2 mm
  • Cloudy apple concentrate with a proportion of soluble dry matter 20% by weight
  • Retentate temperature 50 ° C average retentate speed 2.5 m / s retentate inlet pressure 6 bar
  • Postage can be automated
  • Water lances can be flushed out without failure due to blockages.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne une installation de filtration à courant transversal comportant un module de filtration (5) pourvu d'une membrane de filtration (6) présentant un côté rétentat et un côté perméat, un contenant (1) pour la substance (2) à filtrer, et une pompe d'alimentation (4) placée entre le contenant (1) et le module de filtration (5). Les parties de rétentat solides créant des obstructions dans les chemins d'écoulement de rétentat sont éliminées sur le côté rétentat de la membrane de filtration (6). Cette élimination est réalisée par le fait que, au moyen d'un raccord côté aspiration de la pompe d'alimentation (4), la pression côté rétentat est abaissée sur la membrane de filtration (6) dans une mesure telle que le perméat refoulé depuis le côté perméat, à travers la membrane de filtration (6), enlève les éléments obstructeurs et est aspiré par l'intermédiaire de la pompe d'alimentation (4) avec les parties de rétentat créant l'obstruction. Grâce au fait que l'on n'utilise pas de réservoirs à perméat résistant à la pression, on obtient des modules de grande taille économiques avec une complexité d'appareillage relativement simple.
PCT/CH2000/000675 2000-01-13 2000-12-20 Procede et dispositif pour liberer des chemins d'ecoulement dans des modules de filtration WO2001051186A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH62/00 2000-01-13
CH622000 2000-01-13

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WO2001051186A1 true WO2001051186A1 (fr) 2001-07-19

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003082449A1 (fr) * 2002-04-03 2003-10-09 Bucher-Guyer Ag Dispositif de filtration a flux transversal et procede de fonctionnement associe
WO2003084650A1 (fr) * 2002-04-10 2003-10-16 Bucher-Guyer Ag Installation de filtration a courant transversal
WO2004067146A1 (fr) * 2003-01-27 2004-08-12 Bucher-Guyer Ag Procede et dispositif de filtrage de flux transversal
WO2004069377A1 (fr) * 2003-01-29 2004-08-19 Bucher-Guyer Ag Dispositif de filtrage de flux transversal et procede pour le faire fonctionner
DE102011056633A1 (de) 2011-12-19 2013-06-20 Highq-Factory Gmbh Verfahren zum Reinigen eines Filters

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0335648A2 (fr) * 1988-03-31 1989-10-04 Koch Membrane Systems, Inc Procédé pour conduire des installations de séparation à membranes
EP0427376A2 (fr) * 1989-11-08 1991-05-15 Koch Membrane Systems, Inc Système de séparation à membrane et procédé de fonctionnement
EP0479492A1 (fr) * 1990-10-04 1992-04-08 Koch Membrane Systems, Inc Dispositif de séparation par membrane et procédés pour le fonctionnement et le nettoyage d'un tel dispositif
EP0526372A1 (fr) * 1991-07-26 1993-02-03 Societe De Traitements Hydrex S.N.C. Procédé et dispositif de décolmatage de membranes de filtration
JPH06238134A (ja) * 1993-02-15 1994-08-30 Hitachi Plant Eng & Constr Co Ltd 回転平膜分離装置
US5647988A (en) * 1994-05-30 1997-07-15 Kubota Corporation Method of back-washing submerged-type ceramic membrane separation apparatus

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0335648A2 (fr) * 1988-03-31 1989-10-04 Koch Membrane Systems, Inc Procédé pour conduire des installations de séparation à membranes
EP0427376A2 (fr) * 1989-11-08 1991-05-15 Koch Membrane Systems, Inc Système de séparation à membrane et procédé de fonctionnement
EP0479492A1 (fr) * 1990-10-04 1992-04-08 Koch Membrane Systems, Inc Dispositif de séparation par membrane et procédés pour le fonctionnement et le nettoyage d'un tel dispositif
EP0526372A1 (fr) * 1991-07-26 1993-02-03 Societe De Traitements Hydrex S.N.C. Procédé et dispositif de décolmatage de membranes de filtration
JPH06238134A (ja) * 1993-02-15 1994-08-30 Hitachi Plant Eng & Constr Co Ltd 回転平膜分離装置
US5647988A (en) * 1994-05-30 1997-07-15 Kubota Corporation Method of back-washing submerged-type ceramic membrane separation apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN vol. 018, no. 619 (C - 1278) 25 November 1994 (1994-11-25) *

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003082449A1 (fr) * 2002-04-03 2003-10-09 Bucher-Guyer Ag Dispositif de filtration a flux transversal et procede de fonctionnement associe
WO2003084650A1 (fr) * 2002-04-10 2003-10-16 Bucher-Guyer Ag Installation de filtration a courant transversal
WO2004067146A1 (fr) * 2003-01-27 2004-08-12 Bucher-Guyer Ag Procede et dispositif de filtrage de flux transversal
WO2004069377A1 (fr) * 2003-01-29 2004-08-19 Bucher-Guyer Ag Dispositif de filtrage de flux transversal et procede pour le faire fonctionner
DE102011056633A1 (de) 2011-12-19 2013-06-20 Highq-Factory Gmbh Verfahren zum Reinigen eines Filters
WO2013092606A1 (fr) 2011-12-19 2013-06-27 Highq-Factory Gmbh Procédé de nettoyage d'un filtre
US9855529B2 (en) 2011-12-19 2018-01-02 Highq-Factory Gmbh Method for cleaning a filter

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