WO1985000297A1 - Procede et dispositif de separation de substances a l'aide de membranes - Google Patents

Procede et dispositif de separation de substances a l'aide de membranes Download PDF

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Publication number
WO1985000297A1
WO1985000297A1 PCT/EP1984/000201 EP8400201W WO8500297A1 WO 1985000297 A1 WO1985000297 A1 WO 1985000297A1 EP 8400201 W EP8400201 W EP 8400201W WO 8500297 A1 WO8500297 A1 WO 8500297A1
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WO
WIPO (PCT)
Prior art keywords
membrane
working
pressure
medium
concentrate
Prior art date
Application number
PCT/EP1984/000201
Other languages
German (de)
English (en)
Inventor
Robert Kohlheb
Original Assignee
Carl Schleicher & Schuell Gmbh & Co. Kg
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 Carl Schleicher & Schuell Gmbh & Co. Kg filed Critical Carl Schleicher & Schuell Gmbh & Co. Kg
Publication of WO1985000297A1 publication Critical patent/WO1985000297A1/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D13/00—Pumping installations or systems
    • F04D13/02—Units comprising pumps and their driving means
    • F04D13/021—Units comprising pumps and their driving means containing a coupling
    • F04D13/024—Units comprising pumps and their driving means containing a coupling a magnetic coupling
    • 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
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • 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
    • B01D61/06—Energy recovery
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/24—Specific pressurizing or depressurizing means
    • B01D2313/246—Energy recovery means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/60—Specific sensors or sensor arrangements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/62—Displays
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/90—Additional auxiliary systems integrated with the module or 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
    • B01D2313/90—Additional auxiliary systems integrated with the module or apparatus
    • B01D2313/901—Integrated prefilter
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/90—Additional auxiliary systems integrated with the module or apparatus
    • B01D2313/903—Integrated control or detection device
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B1/00—Engines characterised by fuel-air mixture compression
    • F02B1/02—Engines characterised by fuel-air mixture compression with positive ignition
    • F02B1/04—Engines characterised by fuel-air mixture compression with positive ignition with fuel-air mixture admission into cylinder

Definitions

  • the invention relates to a process for the separation of liquids or gaseous multi-media by means of membranes, in which the medium to be treated is first subjected to a working pressure required for the separation and is then passed over the surface of the working membrane.
  • such a process includes both filtration processes with small and smallest membrane pore sizes, in particular microfiltration with pore sizes in the range from 1.0 to 0.1 ⁇ m and ultrafiltration in the range from approximately 0.1 to 0.01 ⁇ m as well as the reverse Understood osmosis.
  • the nutrient media in question can therefore be both cloudy, ie dispersions of solid particles in one liquid phase or a smoke as well as solutions or gas mixtures.
  • the separation of viruses and pyrogens from liquid phases, the desalination of seawater and brackish water or the concentration of industrial wastewater containing radioactive salts are typical examples of the material separation processes of the type in question, which are hereinafter briefly referred to as "membrane processes".
  • the invention further relates to a device for carrying out such membrane processes using a working membrane element which is arranged in a pressure vessel, which has an inlet connection for the medium to be treated by means of a pressure generator, usually a displacement pump, a discharge connection for the permeate or filtrate and a concentrate connection at which the medium concentrated by the membrane treatment and retained in front of the membrane can escape.
  • a pressure generator usually a displacement pump
  • a discharge connection for the permeate or filtrate and a concentrate connection at which the medium concentrated by the membrane treatment and retained in front of the membrane can escape.
  • the fine-pored membranes used to carry out these membrane processes or practically pore-free in the case of reverse osmosis are in some cases quite sensitive structures which, if no precautionary measures are taken, quickly show a significant reduction in flow.
  • the best known and most effective measure for suppressing the flow performance drop of membranes of the type in question can be seen in the fact that the medium to be treated, which is used to achieve the separation effect on the membrane with an overpressure in the range from a few bar to a few 10 bar acted upon. is carried out with the greatest possible flow speed parallel to the surface of the working membrane over this membrane surface.
  • the medium to be treated is subjected to the working pressure by a pressure generator, is pumped under this pressure into a pressure vessel in which the membrane element is arranged, and after which it overflows the surface of the membrane exits the pressure vessel via a throttle device.
  • the medium which is then usually referred to as concentrate or retentate, is returned to the pressure generator after the expansion, behind the throttling device, pressurized again and in turn returned to the pressure vessel and over the working membrane surface.
  • part of the retentate is usually branched off and withdrawn as a concentrate from this circuit.
  • the object of the present invention is to create a method and a device for separating liquids or gaseous multi-material media by means of membranes of the type mentioned at the outset, which enable such membrane processes to be carried out with a lower level of plant technology and which require operational outlay; in particular, means are to be found to reduce the working pressure generator and to reduce the pretreatment effort.
  • This object is achieved by the invention by a process for the separation of liquids or gaseous multi-media, in which the medium to be treated is subjected to a working pressure of a working pressure of a few to a few 10 bar and then passed over the surface of a working membrane, in that the medium subjected to the working pressure is circulated over the surface of the working membrane with only the unavoidable pressure drop due to the flow, so that the working pressure generator only needs to convey the volume flow that is required for the actual membrane process, i.e. only one volume flow of the medium to be treated needs to convey, which is equal to the sum of the volume flows of the concentrate and permeate, which are withdrawn from the system continuously or discontinuously.
  • the volume flow of the mixture of concentrate and injected medium to be treated which is circulated for the purpose of suppressing the blocking of the membrane and for suppressing the flow reduction of the membrane, is circulated in the high-pressure region in front of the working membrane and is returned without being relaxed.
  • an additional pump is required for this circulation, simpler, cheaper and smaller pumps can be used for this purpose, which are characterized in particular by an extremely low energy requirement.
  • the required flow rate in the working pressure generator be reduced by at least a factor of 5 to 10. This, in turn, can in practice reduce the size and energy consumption of the pump used as a working pressure generator by an entire dimension.
  • This circulation volume flow which in practice is at least five to ten times the volume flow actually required for the membrane process and by which the working pressure generator is relieved according to the method according to the invention, is now circulated in the high-pressure region in front of the membrane according to the method according to the invention, namely without leaving this high-pressure area, so that the circulation pump required for this only has an energy requirement which has to compensate for the unavoidable pressure drop in the circuit due to the flow.
  • the pressure to be applied for this is around 1 to 3 orders of magnitude lower than the pressure with which the working pressure generator acts on the medium to be treated.
  • the additional investment costs caused by the additional circulation pump are therefore already far overcompensated by the investment costs saved for the working pressure generator, so that the entire considerable operating energy savings in the economic balance sheet are available unabated.
  • the membrane treatment process is carried out in such a way that the medium to be treated is prefiltered through at least one membrane before it reaches the surface of the working membrane.
  • a membrane has an average pore size that is larger than the average pore size of the working membrane.
  • a membrane prefilter and a membrane postfilter are used in front of the actual working membrane.
  • the mean pore size of the membrane prefilter is larger than the mean pore size of the membrane filter and is the average pore size of this membrane post-filter is again larger than the average pore size of the working membrane.
  • the working membrane is a membrane for carrying out the reverse osmosis
  • an ultrafiltration membrane is used as the post-filtration membrane and a microfiltration membrane is used as the prefilter membrane.
  • the medium for the pre-filter membrane hardly needs to be subjected to any noteworthy pressure, whereas for the filtration through the post-filter membrane some pressure is already required in order to achieve a sufficiently high flow rate, according to a further embodiment of the invention the working pressure generator preferably switched between the pre-filter membrane and the post-filter membrane. This has the advantage that no unnecessary pressure drop is generated by connecting the pre-filter membrane in the high-pressure area of the system, ie after the working pressure generator, and that an additional separate pressure generator can be saved for the post-filter membrane.
  • the device for carrying out the method described above essentially consists of a working membrane element which is arranged in a pressure vessel, which in turn is preceded by a pressure generator in which the medium to be treated fed into the pressure vessel is subjected to the working pressure required for the membrane treatment.
  • the working membrane element is preferably a spiral winding element, but can likewise be constructed in a different way, for example as a tubular filter element, labyrinth element or plate filter.
  • the only decisive factor in this connection is that the working membrane element used in each case provides a sufficiently large surface area of the membrane which can be flowed over by the medium to be treated.
  • This membrane treatment arrangement which is customary in this respect is characterized according to the invention by a pump, preferably a turbine centrifugal pump, which is arranged in the pressure vessel in which the working membrane element is also accommodated and whose suction nozzle on the pressure side behind the working membrane element with the concentrate drain and its pressure nozzle with the pressure-side inlet space, inlet area or inlet channel is connected in front of the working membrane element, and by a branch line which connects the suction line of the pump between the concentrate outlet and the suction port of the pump with the concentrate connection of the pressure vessel.
  • the pump arranged in this way in the pressure area of the system within the pressure vessel of the working membrane element thus acts as a circulation pump for the medium to be treated on the pressure side in front of the membrane.
  • this pump is preferably equipped with a turbine drive according to a further embodiment of the invention, the turbine of which is fed via an associated turbine nozzle directly behind the inlet connection of the pressure vessel with that fed into the pressure vessel by the working pressure generator medium to be treated is applied.
  • the turbine pressure drop for the medium fed can be in the order of 0.2 to 8 MPa.
  • the concentrate drain or an additional electric motor can serve as additional drive energy sources for the circulation pump installed in the pressure vessel. If the concentrate outlet is used, it is guided in a separate turbine chamber onto a separate turbine impeller. If an electric motor is provided in addition or alone, it is preferably, but of course not necessarily, arranged outside the pressure vessel.
  • the electric motor for the circulating pump is then preferably, but again also not mandatory, via a coupling which is free of lead-through, for example a magnetic coupling, in order to prevent any technical problems which may occur which may occur when a dynamic seal is formed on a pressure vessel.
  • both an electrical auxiliary drive and an additional turbine drive which can be driven both by external liquid or gaseous pressurized fluids and by utilizing the pressure concentrate discharge, are via a torque limiter, preferably a magnetic coupling, to the turbine which is acted upon by the medium to be treated which is fed in coupled.
  • Figure 1 shows the block diagram of a system for performing the method according to the invention.
  • Figure 2 in axial section and in partial representation the head of the pressure vessel of a device according to the invention.
  • FIG. 3 shows, in axial section and in partial representation, the schematic structure of a foot region of a pressure vessel of the device according to the invention.
  • Fig. 4 is a partial view of the type shown in Fig. 2 in the formation with two turbine wheels.
  • FIG. 1 shows the schematic block diagram of a system for carrying out the method according to the invention.
  • the individual components of this system shown are provided with ISO codes which have the following meaning:
  • the medium to be treated passes through an inlet line 1 and an actuator 2 provided with an overflow stop to a prefilter 3, which is a combination filter comprising a poured, wound or sintered activated carbon filter 4 and a microfiltration membrane 5.
  • the pre-filter 3 can be backwashed and cleaned via a drain valve 6 and can be aerated on the filtrate side via an aeration valve 7.
  • the filtrate leaving the pre-filter 3 can be provided with an additive, for example with a marking substance, a reactant or a process additive, via an auxiliary feed line 8 and a three-way ball valve 9. The proper functioning of the filter 3 is monitored with a downstream manometer 10.
  • the pre-filter 3 is followed by a pressure generator 11, which in the exemplary embodiment shown here is designed as a centrifugal pump driven by an electric motor 12 with a downstream check valve 13.
  • a post-filter 14 is connected, which consists of an outer flexible and flexible hose 15 and an inner elastic membrane filter hose 16. While the membrane filter 5 of the pre-filter 3 has an average pore size of 0.45 ⁇ m, the elastic membrane filter tube 16 of the post-filter 14 has an average pore size of 0.1 ⁇ m. While working membrane poisons such as free chlorine, ozone or oxygen in the pre-filter on the activated carbon and in the membrane pre-filter all particles up to 0.45 ⁇ m, e.g. partly radioactive substances, colloidal suspensions, organic residues and partly bacteria, are retained all bacteria in particular are retained on the post-filter 14.
  • the elastic design of the secondary filter 14 also serves to dampen pulsation and noise, in particular when the pressure generator 11 is a piston displacement pump.
  • the post-filter 14 is monitored with the aid of a manometer 17 and a sampling tap 18.
  • the actual membrane treatment in the exemplary embodiment described here, is reverse osmosis, in assembly 19, referred to here briefly as "turbo module", which is essentially constructed from a pressure vessel 20, a working membrane element 21, a concentrate circulation line 22 and a circulation pump 23.
  • the working membrane can of course also be an ultrafiltration membrane or a microfiltration membrane. It is only necessary to ensure that the membrane 16 of the secondary filter 14 has an average pore size which is larger than the average pore size of the membrane of the membrane element 21, and that the average pore size of the membrane 5 of the pre-filter 3 in turn has a larger pore size than that Membrane 16 of the night filters 14.
  • the circulation pump 23 is designed in the manner described in more detail below as a turbine centrifugal pump which is equipped with an auxiliary electric motor 24.
  • the filtrate circuit line 22 is equipped with a flow monitor
  • the permeate or filtrate is passed through a permeate drain line
  • the quality of the permeate is monitored by means of a conductivity sensor 28.
  • the concentrate removed continuously via a concentrate discharge line 29 and monitored by means of a manometer 30 and a flow monitor 31 is continuously withdrawn from the concentrate flow circulated in the turbo module 19 via a two-way valve 32, the setting of which determines the withdrawal ratio of concentrate to permeate.
  • the electrical control and energy supply of the entire system takes place via a central control and regulating unit 33.
  • FIG. 2 shows a schematic representation of the head of the turbo module 19 shown in FIG. 1 with the cut membrane element 21 and the circulation pump 23.
  • the circulation pump 23 is designed as a turbo centrifugal pump and essentially consists of the pump impeller 34, the turbine impeller 35, which can be acted upon by the turbine nozzle 36, and the auxiliary electric motor 24, which is coupled to the shaft of the turbine impeller 35 via a magnetic coupling 37.
  • the electric auxiliary motor 24 is located outside the pressure vessel 20, but it is. connected to it by means of a mounting plate 38 to form an integral structural unit and by a cover 39 protected from mechanical influences.
  • the pressure vessel 20 has an inlet connection 40 for the medium to be treated with pressure by means of the pressure generator, an outlet connection 41 for the permeate (FIG. 3) and a concentrate connection 42 (FIG. 2), on which the membrane treatment concentrated and pressure side medium retained in front of the membrane can be drawn off continuously in a branch stream.
  • the suction port 43 of the circulation pump 23 is connected via the concentrate circulation line 22, which is also the suction line for the pump 23, to the concentrate outlet space 44 on the pressure side behind the working membrane element 21, while the pressure port 45 of the circulation pump 23 is connected to the inlet space 46 in front of the working membrane element 21.
  • the concentrate flow is indicated by the flow arrow K
  • the flow of the medium to be treated is indicated by the flow arrow E.
  • the suction line 22 of the circulation pump 23 is connected to the concentrate connection 42 via a branch line 47.
  • the turbine wheel 50 is acted upon by a turbine nozzle 51 with the high pressure concentrate under operating pressure from the concentrate branch line 47.
  • the concentrate running off the turbine wheel 50 is led as a low-pressure concentrate via a low-pressure concentrate line 52 to a separate concentrate connection, where it is removed from the system as a concentrate stream.
  • the concentrate auxiliary turbine described in the exemplary embodiment shown in FIG. 4 is also connected to the shaft of the main turbine 23 via a magnetic coupling 37.

Abstract

Procédé et dispositif de séparation de substances d'un milieu de substances multiples fluides ou gazeuses à l'aide de membranes (21) dans un conteneur à pression (20) avec prétraitement et conduction du milieu à traiter dans un circuit de circulation. Le milieu à traiter mélangé avec un concentré est mis en circulation par une pompe séparée (23) avec une énergie minimum et un grand débit après avoir effectué une préfiltration (23) à l'aide des membranes et après chargement en utilisant une pression de travail sans réduction de pression par vanne régulatrice à l'intérieur de la zone haute pression. De la sorte, le générateur de pression de travail (11) peut être ajusté à un débit qui est juste égal à la somme du débit du perméat et du débit du concentré, et qui ne contient aucune fraction du circuit de circulation.
PCT/EP1984/000201 1983-07-01 1984-07-02 Procede et dispositif de separation de substances a l'aide de membranes WO1985000297A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19833323725 DE3323725A1 (de) 1983-07-01 1983-07-01 Einrichtung, energiesparende modulkonfiguration, verfahren und anordnung fuer membrantechnologiezwecke
DEP3323725.5 1983-07-01

Publications (1)

Publication Number Publication Date
WO1985000297A1 true WO1985000297A1 (fr) 1985-01-31

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1984/000201 WO1985000297A1 (fr) 1983-07-01 1984-07-02 Procede et dispositif de separation de substances a l'aide de membranes

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DE (1) DE3323725A1 (fr)
WO (1) WO1985000297A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988006475A1 (fr) * 1987-03-06 1988-09-07 Szuecs Laszlone Procede et appareil servant a traiter des fluides contenant des substances etrangeres au moyen d'un equipement de filtrage a membrane
WO2000001471A1 (fr) * 1998-07-06 2000-01-13 Bolsaplast, S.A. Dispositif a faible consommation de dessalement d'eau salee par osmose inverse
CN1064380C (zh) * 1997-08-13 2001-04-11 李卫 聚四氟乙烯软带单面活化处理方法

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2810256B1 (fr) 2000-06-14 2003-03-07 Vallee De L Aigues S I V A Soc Dispositif de filtration integrant une boucle de circulation
FR2903617B1 (fr) 2006-07-17 2009-03-20 Vallee De L Aigues Sarl Soc In Procede de controle d'un dispositif de filtration tangentielle et dispositif correspondant

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3369667A (en) * 1966-03-08 1968-02-20 Universal Water Corp Reverse osmosis apparatus having feed recirculation means
US3505215A (en) * 1968-10-10 1970-04-07 Desalination Systems Method of treatment of liquids by reverse osmosis
US3708069A (en) * 1970-08-13 1973-01-02 Aqua Chem Inc Reverse osmosis membrane module and apparatus using the same
FR2180478A1 (en) * 1972-04-18 1973-11-30 Rhone Poulenc Sa Water demineralsn - by ultra filtration followed by reverse osmosis
US3836458A (en) * 1971-09-27 1974-09-17 Carborundum Co Water purification means
FR2227892A1 (fr) * 1973-05-03 1974-11-29 Dorr Oliver Inc
DE2622461A1 (de) * 1976-05-20 1977-11-24 Didier Werke Ag Verfahren und vorrichtung zur durchfuehrung der umgekehrten osmose
WO1980000310A1 (fr) * 1978-08-07 1980-03-06 Allied Water Corp Procede et systeme de purification de l'eau
GB1603747A (en) * 1978-05-23 1981-11-25 Keefer B Rotary reverse osmosis or ultrafiltration apparatus and method

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3756408A (en) * 1972-06-15 1973-09-04 Osmonics Inc Separation system
DE2801018A1 (de) * 1978-01-11 1979-07-19 Jenaer Glaswerk Schott & Gen Hochdruck-ultrafiltrations-anlage

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3369667A (en) * 1966-03-08 1968-02-20 Universal Water Corp Reverse osmosis apparatus having feed recirculation means
US3505215A (en) * 1968-10-10 1970-04-07 Desalination Systems Method of treatment of liquids by reverse osmosis
US3708069A (en) * 1970-08-13 1973-01-02 Aqua Chem Inc Reverse osmosis membrane module and apparatus using the same
US3836458A (en) * 1971-09-27 1974-09-17 Carborundum Co Water purification means
FR2180478A1 (en) * 1972-04-18 1973-11-30 Rhone Poulenc Sa Water demineralsn - by ultra filtration followed by reverse osmosis
FR2227892A1 (fr) * 1973-05-03 1974-11-29 Dorr Oliver Inc
DE2622461A1 (de) * 1976-05-20 1977-11-24 Didier Werke Ag Verfahren und vorrichtung zur durchfuehrung der umgekehrten osmose
GB1603747A (en) * 1978-05-23 1981-11-25 Keefer B Rotary reverse osmosis or ultrafiltration apparatus and method
WO1980000310A1 (fr) * 1978-08-07 1980-03-06 Allied Water Corp Procede et systeme de purification de l'eau

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988006475A1 (fr) * 1987-03-06 1988-09-07 Szuecs Laszlone Procede et appareil servant a traiter des fluides contenant des substances etrangeres au moyen d'un equipement de filtrage a membrane
CN1064380C (zh) * 1997-08-13 2001-04-11 李卫 聚四氟乙烯软带单面活化处理方法
WO2000001471A1 (fr) * 1998-07-06 2000-01-13 Bolsaplast, S.A. Dispositif a faible consommation de dessalement d'eau salee par osmose inverse

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