EP3630339A1 - Structure filtrante monolitique a membrane - Google Patents
Structure filtrante monolitique a membraneInfo
- Publication number
- EP3630339A1 EP3630339A1 EP18732840.6A EP18732840A EP3630339A1 EP 3630339 A1 EP3630339 A1 EP 3630339A1 EP 18732840 A EP18732840 A EP 18732840A EP 3630339 A1 EP3630339 A1 EP 3630339A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- channels
- membrane
- support
- filtration structure
- structure according
- 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.)
- Pending
Links
- 238000005374 membrane filtration Methods 0.000 title claims abstract description 5
- 239000012528 membrane Substances 0.000 claims abstract description 87
- 238000001914 filtration Methods 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 45
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 27
- 229910010272 inorganic material Inorganic materials 0.000 claims abstract description 12
- 239000011147 inorganic material Substances 0.000 claims abstract description 12
- 230000002093 peripheral effect Effects 0.000 claims abstract description 11
- 230000035699 permeability Effects 0.000 claims abstract description 9
- 239000011148 porous material Substances 0.000 claims description 37
- 238000000746 purification Methods 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 abstract description 5
- 239000002245 particle Substances 0.000 description 24
- 229910010271 silicon carbide Inorganic materials 0.000 description 20
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 20
- 238000000034 method Methods 0.000 description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- 239000000843 powder Substances 0.000 description 15
- 239000000203 mixture Substances 0.000 description 14
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 12
- 238000000151 deposition Methods 0.000 description 10
- 230000008021 deposition Effects 0.000 description 10
- 239000012530 fluid Substances 0.000 description 10
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 9
- 229910052753 mercury Inorganic materials 0.000 description 9
- 239000011248 coating agent Substances 0.000 description 7
- 238000000576 coating method Methods 0.000 description 7
- 229910052786 argon Inorganic materials 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- 238000009826 distribution Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 5
- 239000011230 binding agent Substances 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 5
- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- 239000001913 cellulose Substances 0.000 description 3
- 229920002678 cellulose Polymers 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000001125 extrusion Methods 0.000 description 3
- 238000009472 formulation Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000010191 image analysis Methods 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 238000000518 rheometry Methods 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 239000010703 silicon Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 229910003564 SiAlON Inorganic materials 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000005229 chemical vapour deposition Methods 0.000 description 2
- 230000001186 cumulative effect Effects 0.000 description 2
- 239000002270 dispersing agent Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052575 non-oxide ceramic Inorganic materials 0.000 description 2
- 239000006259 organic additive Substances 0.000 description 2
- 229920002451 polyvinyl alcohol Polymers 0.000 description 2
- 238000002459 porosimetry Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- NIPNSKYNPDTRPC-UHFFFAOYSA-N N-[2-oxo-2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 NIPNSKYNPDTRPC-UHFFFAOYSA-N 0.000 description 1
- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910003481 amorphous carbon Inorganic materials 0.000 description 1
- 239000012300 argon atmosphere Substances 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000012982 microporous membrane Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000007750 plasma spraying Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000012465 retentate Substances 0.000 description 1
- 238000001878 scanning electron micrograph Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 239000011863 silicon-based powder Substances 0.000 description 1
- 238000009718 spray deposition Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
-
- 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
- B01D63/06—Tubular membrane modules
- B01D63/066—Tubular membrane modules with a porous block having membrane coated passages
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/50—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition
- B01D29/52—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition in parallel connection
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/08—Fully permeating type; Dead-end filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/02—Details relating to pores or porosity of the membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/02—Details relating to pores or porosity of the membranes
- B01D2325/0283—Pore size
- B01D2325/02834—Pore size more than 0.1 and up to 1 µm
Definitions
- Filters have long been known using ceramic or non-ceramic membranes to filter various fluids, especially polluted water. These filters can work according to the principle of tangential filtration which makes it possible to limit the accumulation of particles, thanks to the longitudinal circulation of the fluid on the surface of the membrane. The particles remain in the flow of circulation whereas the liquid can cross the membrane under the effect of a pressure difference. This technique provides stability of performance and filtration level. It is more particularly recommended for the filtration of fluids heavily loaded with particles and / or molecules.
- US5114581 also discloses a frontal filter with a membrane whose channels can be plugged alternately in a non-regular pattern, and this filter is intended for the filtration of gas or even liquids.
- the presence of a microporous membrane allows the regeneration of the filter against the current and in particular counter-washing.
- no indication is provided in this publication on particular geometries for optimizing the filtration qualities of liquids.
- said channels being plugged at one or the other of their upstream or downstream end in the direction of circulation of said liquid, to respectively define inlet channels and outlet channels for said liquid, so as to force said liquid through the porous walls separating the inlet and outlet channels;
- D is defined, according to a plane of section perpendicular to the main axis of said structure, by the arithmetic average of the distances di between i portions of the membrane covering each input channel and the output channel closest to each portion i membrane, a portion i being defined as a division of said membrane into at least i parts of equal length, i being greater than 10, or even greater than 20, each di being measured from the central point of the inner surface of the portion of membrane in contact with the inner volume of said inlet channel to the point of the inner wall of an outlet channel closest to said membrane portion.
- Figure 2 According to preferred embodiments of the present invention, which can be combined with one another if necessary:
- the average hydraulic diameter of the channels 0c is between 0.5 and 8 mm, preferably between 0.5 and 7 mm, more preferably between 0.5 and 5 mm, preferably between 0, 5 and 4 mm, more preferably between 0.5 and 3 mm.
- the average thickness of the internal walls p; of the support is between 0.3 mm and 2 mm, preferably between 0.4 mm and 1.4 mm.
- the support has a square, hexagonal or circular base.
- the filter has a length of between 200 and 1500 mm.
- the average thickness of the inner walls pi is between 0.3 and 2 mm.
- the support has an open porosity of between 20 and 70%.
- the average thickness of the membrane t m is in a range from 0.1 to 300 ⁇ , preferably from 10 to 70 ⁇ .
- the membrane has a median pore diameter of between 10 nm and 5 ⁇ , preferably between 30 nm to 5 ⁇ , more preferably between 50 nm and 2000 nm and very preferably between 100 nm and 1000 nm.
- the median pore diameter of the membrane is less than the median pore diameter of the support by at least a factor of 10 (i.e., their ratio is less than 10), or even less by at least one factor 50 or even less by at least a factor of 100.
- the outer peripheral wall of the support is not filtering
- the invention also relates to the use of a filter as defined above for the purification and / or separation of liquids in the field of chemistry, pharmaceutics, food, agri-food, bioreactors, or oil extraction or shale gas.
- the quantities are classically expressed in the units of the international system, namely in meters (m) for quantities D, t m , 0 C , pi and 0 f , and in square meters (m 2 ) for sizes K s and K m .
- the open porosity and the median pore diameter of the support according to the present invention are determined in known manner by mercury porosimetry.
- the porosity corresponding to the pore volume, is measured by mercury intrusion at 2000 bar using a mercury porosimeter such as the Autopore IV series 9500 Micromeritics porosimeter, on a 1 cm 3 sample taken from a block of support, the skin-excluding sample region typically extending up to 500 microns from the block surface.
- the applicable standard is ISO 15901-1.2005 part 1.
- the increase in pressure up to high pressure leads to "push" the mercury into pores of smaller and smaller size.
- the intrusion of mercury is conventionally done in two stages.
- the porosity of the membrane, corresponding to the total pore volume in the membrane, and the median pore diameter of the membrane are advantageously determined according to the invention using a scanning electron microscope.
- the porosity obtained for the membrane by this method can be likened to the open porosity.
- sections of a wall of the support are made in cross section so as to visualize the entire thickness of the coating over a cumulative length of at least 1.5 cm.
- the acquisition of the images is performed on a sample of at least 50 grains, preferably at least 100 grains.
- the area and the equivalent diameter of each of the pores are obtained from the images by conventional image analysis techniques, possibly after a binarization of the image to increase the contrast.
- a measurement of its area is carried out.
- An equivalent diameter of pores or grain is determined, corresponding to the diameter of a perfect disk of the same area as that measured for said particle or for said pore (this operation may possibly be carried out using software especially dedicated Visilog® marketed by Noesis).
- a size distribution of particles or grains or pore diameter is thus obtained according to a conventional distribution curve and a median particle size and / or a median pore diameter constituting the membrane layer are thus determined, this median size or median diameter respectively corresponding to the equivalent diameter dividing said distribution into a first population comprising only particles or pores of equivalent diameter greater than or equal to this median size and a second population comprising particles of equivalent diameter less than this median size or this median diameter.
- the face (or base) downstream is intended to be positioned on the side of the incoming liquid flow (liquid to be filtered) and the face (or base) upstream opposite the flow of liquid entering.
- Support typically has a hydraulic diameter f 0 of 50 to 300 mm, preferably 80-230 mm. The length of the support may be between 200 and 1500 mm.
- a plurality of channels parallel to the main axis of the support is formed in the inner portion of the support. These channels, also called filter channels, are plugged at either end to define inbound channels and outgoing channels in the direction of fluid flow.
- the incoming channels thus have an inlet face (upstream in the fluid flow direction) unobstructed and an outlet face plugged.
- the outgoing channels thus have a clogged face upstream face in the direction of flow of the fluids) -bouchée and an unobstructed face downstream front side of the filtration structure.
- It is formed of a porous inorganic material, in particular a non-oxide ceramic material, such as SiC, in particular recrystallized SiC, SiO 3 N 4 , SiO 2 ON 2 , SiAlON, BN or a combination thereof.
- Its porosity is typically from 10 to 70% and the median pore diameter from 10 nm to 5 ⁇ m, preferably between 50 nm and 1 ⁇ m (1 micrometer).
- the permeability of the membrane K m is preferably from 10 -19 to 10 -14 m 2 . It typically has an average thickness t m from 0.1 to 300 ⁇ , preferably from 1 to 200 ⁇ , more preferably from 10 to 80 ⁇ .
- the filter according to the invention can be obtained by any technique well known to those skilled in the art.
- a conventional manufacturing process generally comprises the main steps of manufacturing the support and then deposition of the membrane.
- the support is preferably obtained by extruding a paste through a die and followed by drying and baking to sinter the support material and obtain the porosity and mechanical strength characteristics necessary for the support. application.
- a recrystallized SiC support it may in particular be obtained according to the following manufacturing steps: mixing a mixture comprising particles of silicon carbide with a purity greater than 98% and having a particle size such that 75% by weight of the particles has a diameter greater than 30 ⁇ m, the median diameter by mass of this size fraction measured by laser particle size being less than 300 ⁇ .
- the mixture also comprises an organic binder of the cellulose derivative type. Water is added and kneaded to obtain a homogeneous paste whose plasticity allows extrusion, the die being configured to obtain the monoliths according to the invention,
- the plugging of the monoliths can be carried out according to well-known techniques, for example those described in FIG. WO 2004/065088,
- the material obtained has an open porosity of 20 to 70%, preferably 40 to 50% by volume and a median pore diameter of the order of 5 nm to 50 ⁇ m, preferably 100 nm to 40 ⁇ m, more preferably from 5 to 30 ⁇ .
- the filter support is then coated with a membrane.
- the membrane may be deposited according to various techniques known to those skilled in the art: deposition from suspensions or slips, chemical vapor deposition (CVD) or thermal spray deposition, for example plasma projection (plasma spraying).
- CVD chemical vapor deposition
- plasma spraying plasma projection
- the membrane layer or layers are deposited by coating from slip or suspension.
- the membrane can be obtained by the deposition of several successive layers.
- the membrane rests on a first layer, called a primary layer, deposited in direct contact with the substrate.
- the primary acts as a layer of attachment.
- the slip used for the deposition of the primer preferably comprises between 30 and 70% by weight of SiC grains having a median diameter of 1 to 30 ⁇ , the complement being, for example, a metal silicon powder, silica and / or carbon powder.
- the viscosity of the slips is typically from 0.01 to 0.8 Pa.s, preferably from 0.05 to 0.7 Pa.s, measured at 22 ° C. under a shear rate of 1 s -1 according to the standard. DIN 53019-1: 2008 Slips can typically comprise from 0.1 to 1% of the mass of water of thickening agents preferably selected from cellulose derivatives, and may typically comprise from 0.1 to 5% of the weight of the slurry.
- the slip may also comprise from 0.01 to 1% of the SiC powder mass of selected dispersing agents of Preferably, one or more layers of slip may be deposited in order to form the membrane.
- the deposition of a slip layer typically makes it possible to obtain a membrane with a thickness of 0.1 to 80 ⁇ , but thicker membranes typically of 100 to 300 ⁇ can be e obtained by the deposition of several successive layers of slip.
- the thus coated support is then dried at room temperature typically for at least 30 minutes and then at 60 ° C for at least 24 hours.
- the supports thus dried are sintered at a firing temperature of typically between 1000 and 2200 ° C. under a non-oxidizing atmosphere, preferably under argon so as to obtain a membrane porosity measured by image analysis of 10 to 70% by volume and a median equivalent pore diameter measured by image analysis from 10 nm to 5 ⁇ .
- the periphery of the support is preferably coated with a membrane, in addition to the internal surface of the inlet channels.
- the filter according to the invention can be used for various applications for the purification of liquids and / or the separation of particles or molecules from a liquid.
- the filter according to the invention makes it possible to maximize the flow of filtrate independently of the viscosity of the liquid to be filtered. It can be used to filter liquids having, for example, a dynamic viscosity of 0.1 to 20 mPa.s or even 50 mPa.s.
- the dynamic viscosity of the fluid to be filtered can be measured at 20 ° C. under a shear gradient. 1 s "1 in accordance with DIN standard 53019-1: 2008.
- the present invention especially relates to the use of such a filter as described above for the purification of water production from oil extraction or It is also used in various industrial processes for the purification and / or separation of liquids in the chemical, pharmaceutical, food, agri-food or bioreactor fields, as well as in pool waters.
- Figure 1 illustrates an overview of a common filter (or filter) structure.
- Figure 2 is a front view of a portion of the upstream face of the filter which further illustrates the subject of the present invention.
- Figures 3 to 10 are also front views of a portion of the upstream face of the filter whose channel configuration is different.
- Figures 11 and 12 illustrate two modes of implementation of a filter according to the present invention.
- FIG. 1 illustrates a filter with frontal filtration comprising a support 1 of cylindrical shape having a main axis (X), an upstream face 2 and a downstream face 3, according to the direction of flow of the liquid to be filtered.
- a plurality of channels parallel to the main axis (X) are formed in the inner part of the support and separated from each other by porous internal walls, comprising input channels 4 open on the upstream face and output channels. 5 open on the downstream face, in the direction of circulation of the liquid.
- the inlet channels 4, opening on each of the upstream 2 and downstream 3 bases, are covered on their inner surface by a membrane (not shown in FIG. 1) and are plugged on their downstream face 3.
- the outlet channels 5 are blocked on their upstream face 2.
- FIG. 2 is a view of the upstream face of a filter for illustrating in more detail the object of the present invention.
- FIG. 2 shows a central input channel 4 and several output channels 5 of the filter, as well as the filtering membrane 6 lining the inside of each input channel.
- This membrane is divided into i portions of equal length, as shown in FIG. 2.
- a distance d1 is determined from the central point 7 of the inner surface of the membrane portion in contact with the internal volume of said channel. inlet to the point 8 of the inner wall of an outlet channel closest to said membrane portion.
- different outlet channels 5 can and should be considered as a function of the position of the membrane portion i and the capping configuration and the geometry of the channels.
- the relevant distance D is the arithmetic average of the dies thus determined for all the portions i of all the input channels of each monolith.
- the number of portions chosen in the section plane is advantageously chosen according to the configuration of the channels and the number of output channels with respect to each input channel, but must be sufficient to be representative of the average path of the liquid coming from an inlet channel to an outlet channel, through the porous wall of the support.
- the number of di measurements per channel is greater than 10, or even greater than 20, preferably greater than 50, or even greater than 100. According to the invention, at least 20, preferably at least 50, are thus determined. or 100 di distances per input channel, for the calculation of D.
- FIG. 3 is a front view of the upstream face of a filtration filter whose inlet and outlet channels are of square section, according to a first configuration of the closure of the channels.
- Figures 8 to 10 are front views of the upstream face of a filter filter whose inlet and outlet channels are of hexagonal section, according to several configurations of the closure of the channels.
- Figures 11 and 12 illustrate two modes of operation of such filters:
- Figure 11 illustrates a longitudinal section (in a plane passing through the main axis) of a filter structure (or filter) inserted into a compartment (housing).
- Figure 12 shows a longitudinal section of a filter immersed in a reservoir of the liquid to be filtered.
- the raw monolith obtained is then dried to bring the water content not chemically bound to less than 1% by weight, then baked under argon to a temperature of 2100 ° C which is maintained for 5 hours.
- the support obtained has an open porosity of 35% and a median pore diameter of about 10 ⁇ , as measured by mercury porosimetry.
- the channels of the monolith are alternately blocked according to well-known techniques, for example described in application WO 2004/065088. So as to obtain a geometry capping as shown in Figure 3.
- the outer peripheral wall of the support is made non-filtering.
- the membrane separating layer (the membrane) is obtained from a slip whose mineral composition is as follows: 67% by weight of the powder of metallic silicon grains whose median diameter D50 is about 4 micrometers, 33% ) amorphous carbon powder whose median diameter D 50 is about 1 micrometer.
- the mixture is mixed in a deionized water solution, the amount of water representing approximately 50% of the total mass of the mixture.
- the supports are then dried at ambient temperature for 10 minutes and then at 60 ° C. for 12 hours. The thus dried supports are then baked in Argon at a temperature of 1470 ° C. for 4 hours at ambient pressure under argon.
- the primer and the membrane are deposited according to the same process.
- the slurry is introduced into a stirred tank at 20 rpm. After a light vacuum de-aeration phase, typically 25 mbar, while maintaining stirring, the tank is put in slight overpressure of about 0.8 bar in order to coat the interior of the support from the bottom to the high. This operation takes only a few seconds for a 300 mm long stand.
- the slip comes to coat the inner wall of the channels of the support and the excess is then discharged by gravity immediately after deposition.
- this primer layer does not affect the filtration performance of the filter, given its porosity characteristics (median pore diameter and overall porosity) greater than that of the membrane itself. which alone plays the role of a separating layer.
- the coated support is then dried at ambient temperature for 30 minutes and then at 60 ° C. for 30 hours.
- the thus dried coated carrier is then sintered at a temperature of 1300 ° C under an Argon atmosphere for 4 hours to obtain 40% membrane porosity with a median pore diameter of 100 nm.
- a filter was prepared in the same way as that of Example 1-1 except that the plugging is carried out according to the configuration described in FIG.
- a filter was prepared in a manner identical to that of Example 1-1 except that the die was modified in order to obtain channels with a hydraulic diameter of 2.6 mm and an average thickness of internal walls of 800 microns. .
- the mixture for the extrusion of the support comprises 65% by weight of a first silicon carbide particle powder having a median diameter of approximately 1 1 ⁇ and 35% by weight of a second powder of carbide particles. silicon having a median diameter of about 0.9 ⁇ .
- a membrane layer of silicon carbide membrane is then deposited on the inner wall of the channels according to the method described below:
- a primer of attachment of the separating layer is constituted in a first step, from a slip whose mineral formulation comprises 30% by weight of a black SiC grain powder (Sika DPF-C) whose median diameter D50 is about 11 micrometers, 20% by weight of a black SiC grain powder (SIKA FCP-07) whose median diameter D50 is about 2.5 microns, and 50% water. deionized.
- a slurry of the material constituting the separating layer is also prepared, the formulation of which comprises 40% by weight of SiC grains (d 50 around 0.6 micrometer) and 60% of demineralized water.
- the rheology of the slips has been adjusted by adding the organic additives at 0.7 Pa.s under a shear rate of ls -1 , measured at 22 ° C. according to the DINC33-53019 standard.
- the slip is introduced into a tank with stirring (20 rpm). After a light vacuum de-aerating phase (typically 25 millibars) while maintaining stirring, the tank is pressurized approximately 0.7 bar in order to coat the interior of the support from its lower part until at its upper end. This operation takes only a few seconds for a support of 30 cm in length. Immediately after coating the slip on the inner wall of the support channels, the excess is removed by gravity.
- the carriers are then dried at room temperature for 10 minutes and then at 60 ° C for 12h and the channels are capped in the same manner as for the series of Examples 1-1 to 1-3.
- the thus dried supports are then baked in argon at a temperature of 1540 ° C. for 2 hours at ambient pressure.
- a filter was prepared in a manner identical to that of Example 2-1 with the difference that the die was modified to obtain channels with a hydraulic diameter of 1.9 mm and a wall thickness of 635 microns.
- the raw monolith obtained is baked to a temperature of 2200 ° C.
- the support obtained has an open porosity of 50% and a median pore diameter of about 35 ⁇ .
- a filter was prepared in the same manner as in Example 2-1 except that the die was modified to obtain a hexagonal structure as shown in FIG. 8, the channels of which have a hydraulic diameter of 2, 0 mm and an average thickness of internal walls of 600 micrometers.
- the raw monolith obtained is baked to a temperature of 2130 ° C.
- the support obtained has an open porosity of 40% and a median pore diameter of about 9 ⁇ .
- the preparation of the separating membrane is carried out as for example 2.1 but the coated supports are then baked in argon at a temperature of 1480 ° C. instead of 1540 ° C.
- Examples 1-3, 2-1 and 3-4 according to the invention correspond to optimal structures whose configuration also depends on the physical characteristics of the membrane and the support. These examples highlight the importance of adapting the pattern and the number of incoming and outgoing channels of the filter according to the physical parameters of the filter, such as the shape of the channels, the average thickness of the internal walls, the average thickness of the membrane, the median pore diameter of the membrane and the porosity of the membrane or the support, so as to obtain a distance D according to the invention to maximize the flow of filtrate.
- the filters according to the invention thus dimensioned are characterized by an optimized and maximum flow of the filtrate as can be seen from the results reported in Table 1.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Porous Artificial Stone Or Porous Ceramic Products (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1754822A FR3066924B1 (fr) | 2017-05-31 | 2017-05-31 | Structure filtrante a membrane |
PCT/FR2018/051257 WO2018220332A1 (fr) | 2017-05-31 | 2018-05-31 | Structure filtrante monolitique a membrane |
Publications (1)
Publication Number | Publication Date |
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EP3630339A1 true EP3630339A1 (fr) | 2020-04-08 |
Family
ID=62044757
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP18732840.6A Pending EP3630339A1 (fr) | 2017-05-31 | 2018-05-31 | Structure filtrante monolitique a membrane |
Country Status (6)
Country | Link |
---|---|
US (1) | US20200156008A1 (fr) |
EP (1) | EP3630339A1 (fr) |
JP (1) | JP7191861B2 (fr) |
CN (1) | CN110678251A (fr) |
FR (1) | FR3066924B1 (fr) |
WO (1) | WO2018220332A1 (fr) |
Family Cites Families (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4069157A (en) | 1975-11-20 | 1978-01-17 | E. I. Du Pont De Nemours And Company | Ultrafiltration device |
US4060488A (en) | 1975-11-20 | 1977-11-29 | E. I. Du Pont De Nemours And Company | Particulate membrane ultrafiltration device |
US4417908A (en) * | 1982-02-22 | 1983-11-29 | Corning Glass Works | Honeycomb filter and method of making it |
US5114581A (en) * | 1991-01-10 | 1992-05-19 | Ceramem Corporation | Back-flushable filtration device and method of forming and using same |
JP4723173B2 (ja) | 2003-01-20 | 2011-07-13 | 日本碍子株式会社 | ハニカム構造体の製造方法 |
JP2004306020A (ja) * | 2003-03-24 | 2004-11-04 | Ngk Insulators Ltd | セラミックフィルタ |
US7491373B2 (en) * | 2006-11-15 | 2009-02-17 | Corning Incorporated | Flow-through honeycomb substrate and exhaust after treatment system and method |
US8814974B2 (en) * | 2007-08-24 | 2014-08-26 | Corning Incorporated | Thin-walled porous ceramic wall-flow filter |
EP2065575B1 (fr) | 2007-11-29 | 2012-08-15 | Corning Incorporated | Filtre en nids d'abeille à écoulement à travers des parois ayant une grande capacité de stockage et une faible contre-pression |
WO2009121366A2 (fr) | 2008-04-03 | 2009-10-08 | Povl Kaas | Unité de filtration avec banc filtrant |
JP5253261B2 (ja) | 2009-03-26 | 2013-07-31 | 日本碍子株式会社 | アルミナ質多孔質及びその製造方法 |
GB2526310A (en) * | 2014-05-20 | 2015-11-25 | Imp Innovations Ltd | Monolith |
JP2016093794A (ja) | 2014-11-14 | 2016-05-26 | 日本碍子株式会社 | セラミックフィルタ |
FR3045398A1 (fr) * | 2015-12-18 | 2017-06-23 | Saint-Gobain Centre De Rech Et D'Etudes Europeen | Filtre monolithique |
-
2017
- 2017-05-31 FR FR1754822A patent/FR3066924B1/fr active Active
-
2018
- 2018-05-31 US US16/617,718 patent/US20200156008A1/en not_active Abandoned
- 2018-05-31 WO PCT/FR2018/051257 patent/WO2018220332A1/fr active Application Filing
- 2018-05-31 EP EP18732840.6A patent/EP3630339A1/fr active Pending
- 2018-05-31 CN CN201880035930.7A patent/CN110678251A/zh active Pending
- 2018-05-31 JP JP2019566335A patent/JP7191861B2/ja active Active
Also Published As
Publication number | Publication date |
---|---|
JP2020521634A (ja) | 2020-07-27 |
US20200156008A1 (en) | 2020-05-21 |
FR3066924A1 (fr) | 2018-12-07 |
JP7191861B2 (ja) | 2022-12-19 |
FR3066924B1 (fr) | 2019-07-12 |
WO2018220332A1 (fr) | 2018-12-06 |
CN110678251A (zh) | 2020-01-10 |
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