Patent Description:
Wastewaters from domestic and industrial needs are characterized by relative high values of chemical oxygen demand (COD), suspended solids, fats, oil and detergents.

The membrane technology for wastewater has been increasingly studied to develop affordable and efficient solutions. Generally, polymeric membranes for filtration processes are used in order to achieve clear permeate. Membranes made of polymers like polypropylene (PP), polyvinylidine fluoride (PVDF), polyethersulfone (PES), polyacrylonitrile (PAN), polysulfone (PSf) and chlorinated polyethylene (CPE) have an excellent selectivity in water treatment applications. Furthermore they have good chemical and mechanical stability. However, they typically show limited permeability because of their hydrophobic nature. As a consequence, the cost of water flux and treatment is increased due to the fact that more energy is necessary for pumping in order to achieve the filtration.

Modification of membranes to increase permeability while still preserving filtration efficiency can be carried out by blending polymers having suitable properties, e.g. hydrophilic coating, by combination of different organic compounds, like surfactants or organic solvents, or by addition of polymer layers on the active surface of membrane. From a manufacturing point of view, different methods for modifying the membrane surface are employed, like drop-coating, dip-coating, spray-coating, plasma treatment, etc. Among all methods, dip-coating is certainly a straightforward technique for modifying a membrane surface.

Different inorganic nanomaterials have been studied to enhance the performance of membranes, such as zeolites [<NUM>], titanium dioxide [<NUM>], magnesium titanium oxide [<NUM>], silicon dioxide [<NUM>], zirconia [<NUM>], and titanate [<NUM>]. These materials modify the structures and chemical composition of membrane, exhibiting improved surface hydrophilicity, charge, antifouling, salt rejection and anti-scaling and antibacterial properties. Other authors, e.g. Wang et al. [<NUM>], found that sodium maleate (NaMA) and vinil silicone oil (Vi-PDMS) improve the flux of water or oil when they were grafted into PP (polypropylene) pores from UF (ultrafiltration) membranes by using microwave heating, a selective heating method.

In other researches, modification of PP membrane was achieved by employing nanoparticles and hydrophilic additives [<NUM>, <NUM>, <NUM>]. In addition, among the additives, ZnO has increasingly been used since it showed good antibacterial and antimicrobial properties. In this way, Wenten et al. [<NUM>] improved the flux of water and reduced organic fouling when PP membrane prepared by a coating of PSf/PEG400/ZnO via dip-coating was employed in peat water treatment.

It is thus known in the prior art the use of hydrophilic coating to increase water permeability of hydrophobic membranes.

<CIT> [<NUM>] discloses porous substrate materials made of ceramics having extreme wettability to polar or non-polar fluids, such as water and oil. The porous material has a coated surface comprising a low surface energy fluoroalkyl silane that is treated to exhibit at least one type of extreme wettability, wherein the low surface energy fluoroalkyl silane is selected from a group consisting of: heptadecafluoro-<NUM>,<NUM>,<NUM>,<NUM>-tetrahydrodecyl triethoxysilane, heptadecafluoro-<NUM>,<NUM>,<NUM>,<NUM>-tetrahydrodecyl trichlorosilane, heptadecafluoro-<NUM>,<NUM>,<NUM>,<NUM>-tetrahydrooctyl trichlorosilane, tridecafluoro-<NUM>,<NUM>,<NUM>,<NUM>-tetrahydrooctyl triethoxysilane, and nonafluorohexyl triethoxysilane, and combinations thereof.

<CIT> [<NUM>] discloses a membrane made of ceramics with its surface grafted by a hydrophilic polymer. In addition, during the membrane manufacturing, different binders are used like propyl trimethoxy silane coupling agent, polyvinyl alcohol, polyvinyl butyral, epoxy resin, one or more of acrylic resin, and polyurethane.

<CIT>[<NUM>] discloses a method of manufacturing reverse osmosis membranes having a high permeation flux. The membrane includes: a porous support and a polyamide active layer formed on the porous support and including zeolite, modified on the surface with a compound having at least one functional group selected from a group consisting of an amino group and a glycidyl group.

<CIT> [<NUM>] discloses the use of silane-modified silica filter media such as rice hull ash for separating protein and capturing particulates, simultaneously. The object of this disclosure is to filter a sample through filter media whose surface has been modified with one or more silanes. The disclosed methods allow simultaneously to capture the particulate by filtration and bind soluble materials onto the silica filter media.

<CIT> discloses a manufacturing method of a composite membrane having a hydrophilic coating layer on hydrophobic support membrane. In particular, the hydrophobic support membrane is immersed in an aqueous solution containing hydrophilic polymer. The support membrane is used for increasing the mechanical resistance and durability of the filter membrane.

<CIT> [<NUM>] discloses polyvinylidene fluoride (PVDF) and polysulfone (PSf) membranes with pore sizes of <NUM> coated with specific amino silanes: <NUM>-aminopropyl triethoxy silane, <NUM>-aminopropyl trimethoxy silane, aminoethyl aminopropyl triethoxy silane, aminoethyl aminopropyl trimethoxy silane, and different thiol-silanes such as <NUM>-mercaptopropyl triethoxy silane, <NUM>-mercapto propyl trimethoxy silane, which change the hydrophobic properties of the composite film. Additionally, a tannin solution is employed to adjust the pH between <NUM> and <NUM>.

<CIT> discloses a hydrophilic polypropylene membrane comprising a polymeric microporous membrane coated with a hydrophilic coating of vinyltrimethoxysilane and inorganic particles.

<CIT> discloses a hydrophilic coated membrane for water treatment. The membrane coating comprises organomethoxysilanes.

Among the substrate materials, PP is one of the most favourable candidates for membranes thanks to its availability, easy processing, durability and low cost, and has been widely used for ultrafiltration (UF) [<NUM>]. However, PP, as mentioned above, have limitations in water treatment due to poor hydrophilic property [<NUM>, <NUM>]. To overcome this problem, it was reported that polymerization with hydrophilic monomers can be used for modifying supporting PP substrates in thin film composite membranes [<NUM>]. For achieving durable and high permeability, chemical affinity between hydrophilic coating and membrane or membrane's substrate is essential. This is especially applicable to the case where PP is membrane material and not only support material.

Accordingly, the present inventors have found that a polypropylene (PP) membrane coated with organomethoxysilane overcomes the drawbacks disclosed in the state of the art and, in particular, has a high permeability capacity for liquids, in particular water.

In a first aspect, the present invention relates to a polypropylene (PP) membrane coated with an organomethoxysilane alone or combined with oxide particulates according to claim <NUM>.

In a second aspect, the present invention relates to a method for manufacturing the polypropylene membrane according to the first aspect of the invention.

In a third aspect, the present invention relates to a device comprising the polypropylene membrane according to the first aspect of the invention.

In a fourth aspect, the present invention relates to different uses of the polypropylene membrane according to the first aspect of the invention or the device according to the third aspect of the invention.

In this disclosure and in the claims, terms such as "comprises," "comprising," "containing" and "having" are open-ended terms and can mean "includes," "including," and the like; while terms like "consisting of" or "consists of" refer to the mentioned elements after these terms and others which are not mentioned are excluded.

Unless otherwise explained, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs. The singular terms "a", "an", and "the" include plural referents unless context clearly indicates otherwise. Similarly, the word "or" is intended to include "and" unless the context clearly indicate otherwise.

In a preferred embodiment, said oxide particulates are selected from graphene oxide micro- or nano-particles and titanium oxide micro- or nano-particles.

In another preferred embodiment, said PP membrane has a pore size ranging from <NUM> to <NUM>, preferably ranging from <NUM> to <NUM>.

The organomethoxysilane of the present invention has the formula (I):
<CHM>
wherein, independently, R1 is a C1-<NUM> alkyl group; R2 is a C1-<NUM> alkyl group; R3 is a C1-<NUM> alkyl group;.

In a particular preferred embodiment, independently of R2 and R3, R1 is methyl.

In a particular preferred embodiment, independently of R1 and R3, R2 is ethyl.

In a particular preferred embodiment, independently of R1 and R2, R3 is methyl.

In a particular preferred embodiment, independently, R1 = R3 = methyl and R2 = ethyl.

"Alkyl" in the context of the present invention means a branched or lineal alkyl group, preferably a lineal alkyl group, for example, a butyl, propyl, ethyl or methyl group.

In a further preferred embodiment, the organomethoxysilane is <NUM>-[methoxy(polyethyleneoxy)<NUM>-24propyl]trimethoxy silane.

In another preferred embodiment, the PP membrane further comprises at least one layer over the organomethoxysilane coating and/or at least one layer under the PP membrane.

It is noted that any of the embodiments disclosed herein for the PP membrane according to the first aspect of the invention can be taken alone or combined with any other embodiment disclosed herein unless the context specifies otherwise.

In a second aspect, the present invention relates to a method for manufacturing the PP membrane according to any of embodiments disclosed according to the first aspect of the invention, comprising the steps of:.

In a preferred embodiment of the second aspect, the organomethoxysilane solution in step a) is combined with oxide particulates. Preferably, said oxide particulates are selected from graphene oxide micro- or nano-particles and titanium oxide micro- or nano-particles.

In another preferred embodiment of the second aspect, said PP membrane has a pore size ranging from <NUM> to <NUM>, preferably ranging from <NUM> to <NUM>.

The organomethoxysilane has the formula (I):
<CHM>
wherein, independently, R1 is a C1-<NUM> alkyl group; R2 is a C1-<NUM> alkyl group; R3 is a C1-<NUM> alkyl group;.

In a further preferred embodiment of the second aspect, the organomethoxysilane is <NUM>-[methoxy(polyethyleneoxy)<NUM>-24propyl]trimethoxy silane.

In another preferred embodiment of the second aspect, the PP membrane further comprises at least one layer over the organomethoxysilane coating and/or at least one layer under the PP membrane.

In another preferred embodiment of the second aspect, in the mixture of alcohol and water of step a), the alcohol is preferably ethanol or isopropanol, more preferably ethanol. Preferably, the ratio between alcohol and water is from <NUM>:<NUM> to <NUM>:<NUM> (v/v), wherein the alcohol is preferably ethanol or isopropanol, more preferably ethanol.

In another preferred embodiment of the second aspect, the hydrolysis reaction is catalysed particularly by a Brønsted acid such as, for example, hydrochloric acid, sulfuric acid, sulfurous acid, phosphoric acid, phosphorous acid, nitric acid, nitrous acid, perchloric acid, chlorous acid, as well as any organic Brønsted acid, such as formic acid, acetic acid, butyric acid, glutaric acid as well as mixtures of the above mentioned Brønsted acids. Glacial acetic acid is preferably used.

In another embodiment of the method according to the second aspect, the method further comprises the step d) of spray coating the PP membrane with oxide particulates when the organomethoxysilane does not contain oxide particulate in the solution of step a). Preferably, said oxide particulates are selected from graphene oxide micro- or nano-particles and titanium oxide micro- or nano-particles.

In another preferred embodiment of the method according to the second aspect, the fixing process in said step c) is carried out by heating the PP membrane at a temperature between <NUM> and <NUM>, or by applying UV light over the PP membrane, or a combination thereof.

In another preferred embodiment of the method according to the second aspect, said method further comprises a final step of removing the excess of organomethoxysilane. Preferably, said step of removing the excess of organomethoxysilane is carried out by washing with deionized water, acetone or ethanol or under ultrasound, or a combination thereof.

In another preferred embodiment of the method according to the second aspect, the concentration of organomethoxysilane in the final solution of step a) is from <NUM> to <NUM> % by weight.

In another preferred embodiment of the method according to the second aspect, the ratio of ethanol:water in step a) is <NUM>:<NUM> (v:v).

In another preferred embodiment of the method according to the second aspect, the step a) is carried out for <NUM> to <NUM> minutes.

In another preferred embodiment of the method according to the second aspect, the step b) is carried out for <NUM> to <NUM> minutes.

In another preferred embodiment of the method according to the second aspect, the step c) is carried out for <NUM> to <NUM> minutes.

It is noted that any of the embodiments disclosed herein for the manufacture of the PP membrane according to the second aspect of the invention can be taken alone or combined with any other embodiment disclosed herein unless the context specifies otherwise.

In a third aspect, the present invention relates to a device comprising the PP membrane as defined in any of the embodiments according to the first aspect of the invention.

In a fourth aspect, the present invention relates to the use of the device according to third aspect of the invention for a filtration, osmosis, concentration or dialysis process, or a combination thereof.

Preferably, the filtration process is applied to the filtration of a fluid. More preferably, said fluid is selected from blood and water. Most preferably, said fluid is water.

In the context of the present invention, by "water" is understood water from seawater, municipal wastewater, brackish water and industrial process water such as cooling, heating and boiler water treatment.

In another preferred embodiment, the osmosis process is reverse osmosis.

In another preferred embodiment, the concentration process is applied to particles or microorganisms.

In another preferred embodiment, the filtration process is applied to MBR (membrane bioreactor).

A number of examples will be provided below that are intended to illustrate the invention and in no way limit the scope of the invention, which is established by the attached claims.

<NUM>-[Methoxy(polyethyleneoxy)<NUM>-24propyl]trimethoxysilane (Tech <NUM>) of the organomethoxysilane chemical family (OS). Ethanol absolute was purchased from Scharlau and acetic acid was provided by Sigma-Aldrich. A PP membrane filter from laboratory (pore size = <NUM>, diameter <NUM>) was supplied by Filter-Lab® (FLAB®), a PP membrane filter from laboratory (pore size = <NUM>, diameter <NUM>) was supplied by Scharlab® (GVB®) and a commercial PP membrane filter like Fluytec® membrane (pore size = <NUM>) was provided by Fluytec Filtration Technologies®.

Firstly, an OS-containing solution was prepared. The OS was dissolved at <NUM> wt % in <NUM>:<NUM> ethanol:water with <NUM> % glacial acetic acid as a catalyst. After <NUM> hydrolysis time, the solution was ready. The PP membrane was immersed (dip-coating) in the OS-containing solution for <NUM>-<NUM>. After this time, the modified membrane was treated at <NUM> for <NUM> in a convection oven.

Dynamic contact angle measurements on the membrane was evaluated using a Drop Shape Analyzer-DSA100 (Krüs GmbH) in order to measure the surface wetting characteristics. The results from these measurements are representatives of the hydrophilicity of each membrane.

The static and the sliding Contact Angle (CA) measurements were carried out with drops of <NUM>µl volume. An image was taken of each drop and subsequently the contact angles were evaluated. Software ImageJ was used for calculating the angles. Static CA was first measured and then sliding CA. In all experiments, tilting was up to <NUM>° to study advancing CA (θa) and receding CA (θr). Furmidge (see <FIG>) assumed the footprint of the drop to be rectangular during sliding, which may be a source of error, but he found the equation to be sufficiently accurate to be able to account for sliding drops on a flat surface [<NUM>]. The difference between θa and θr is known as hysteresis.

Water flux experiments were conducted using a batch set-up system and continuous set-up system. Both schematic diagrams of the test can be found in <FIG>, respectively.

The water flux refers to the volume of deionized water passing through a unit membrane area per unit time and is defined as: <MAT> where Flux is the permeate flux (LMH), Vfiltrated is the volume of deionized water employed in the experiment, Smembrane is the effective membrane area (<NUM><NUM>) and Tfiltration is the running time (h).

The dry commercial membranes and dry modified membrane were weighted using a five-digit balance.

The surface chemical compositions of the membranes were analysed by X-ray photoelectron spectroscopy (XPS, Axis Supra, Kratos) with Al and Kα line as an X-ray source. Commercial supports, supports modified with OS, were analysed before and after water flux experiments.

The surface of the commercial membranes and the modified membranes were analyzed by scanning electron microscopy (FEG-SEM, Inspect F, FEI Systems) to evaluate the change in the structure of the membranes. The samples were covered with a copper foil for observation with SEM, using the Sputter Coater Orion <NUM> HV. To evaluate the change in pore size, on the Fluytec® membrane the pore size was studied by filtering a solution containing particles between <NUM>-<NUM>. The pore size of the OS-modified GVB membrane was evaluated with a solution of Escherichia Coli.

In order to show the suitability of the membrane material for the purpose of the present invention, materials other than polypropylene were tested for permeability:.

It was observed that PVDF had less permeability after being coated with organomethoxysilane in the same as conditions as in the present invention.

PSf, PES and PA are indeed very hydrophobic materials and did not show permeability being coated or not coated with organomethoxysilane.

The first experiment studied the water flux went through the commercial supports. The readings of the permeability of Fluytec® (F) and Filter-LAB® (FLAB) were <NUM> and <NUM>/m<NUM>h, respectively. Supports were then modified with OS and water flux was evaluated in batch set-up. The results correspond to at least of three replicates. Table <NUM> and Table <NUM> show these results for Fluytec® and FLAB®, respectively. As shown, water flux increased with the amount of OS over surface.

The surface-wetting properties of the commercial supports before and after treatment were studied by water CA measurements. Commercial Fluytec® and FLAB® membranes have a contact angle (CA) of <NUM>° and <NUM>°, respectively. On the other hand, Fluytec® and FLAB® modified with <NUM> % OS have a CA of <NUM>° and <NUM>°, respectively.

The results show that OS decreases about <NUM> % the CA for FLAB®, but the change is negligible for Fluytec® (see <FIG>).

Table <NUM> shows the variation of average water CA measurements for Fluytec® and Fluytec®-<NUM> % OS. Firstly, static CA was studied and then θa and θr for tilt angle of <NUM>° were measured. The values correspond to different times of permeation: before filtration, after filtration and <NUM> hours after filtration, when the supports were dry. In case of commercial Fluytec®, the increase of CA just after filtration and <NUM> later is <NUM> % and <NUM> %, respectively. On the other hand, the most significant result is observed for Fluytec®-<NUM> % OS. The modified membrane abruptly increases water flux and according to the permeability study, Fluytec®-<NUM> % OS absorbs the water drop in <NUM> seconds.

The same study was carried out for FLAB®. These results are shown in.

Table <NUM>. Compared to Fluytec®, FLAB® is more hydrophobic. When the surface of contact angle equipment, where FLAB® is located, increases from <NUM> until <NUM> °, the drop deposited over surface FLAB® falls down. This fact proves the low attraction between the water and FLAB® surface. After filtration, once FLAB® is wet, this situation is not observed anymore. In this case, the drop remains attached over surface for <NUM>° tilt. θa and θr are <NUM>° and <NUM>°, respectively. In addition, <NUM> hours after filtration permeability experiments, FLAB® recovers the initial properties, since static CA is similar to values obtained with commercial filter and the water drop slides when tilt reaches <NUM>°. In contrast, FLAB® - <NUM> % OS is slightly more hydrophilic than FLAB®, as static CA is lower than that for commercial FLAB in all experiments (before, after and <NUM> hours after filtration). In addition, when tilt achieves <NUM>°, the water drop remains attached to surface (it does not slide), indicating that the OS changes the hydrophilic properties. Finally, the last row in <NUM> summarizes the water flux for commercial FLAB® and FLAB® - <NUM> % OS. FLAB® - <NUM> % OS shows an increase of <NUM> % with respect to the initial untreated (not covered with OS) commercial filter.

In addition, the same study is performed for GVB®. These results are shown in Table <NUM>. Compared to Fluytec® and FLAB® this filter is more hydrophobic. When the surface of the contact angle equipment, where GVB® is located, increases from <NUM> to <NUM>°, the drop deposited on the GVB® surface falls. This fact demonstrates the low attraction between water and the GVB® surface. After filtration, once GVB® is wet, this situation is no longer observed. In this case, the drop remains attached on the surface for a tilt of <NUM>°. θa and θr are <NUM>° and <NUM>°, respectively. In addition, <NUM> hours after the filtration permeability experiments, GVB® recovers the initial properties, since the static CA is similar to the values obtained with the commercial filter and the water drop slides when the inclination reaches <NUM>°. In contrast, GVB® - <NUM>% OS, is initially slightly more hydrophobic than FLAB®, since the static CA is higher than that for FLAB®. Furthermore, when the tilt reaches <NUM>°, the water drop remains attached to the surface (it does not slide), which indicates that the OS changes the hydrophilic properties. Finally, the last row of Table <NUM> summarizes the water flow for GVB® commercial and GVB® - <NUM>% OS. GVB® - <NUM>% OS shows an increase of <NUM>% over the initial untreated commercial filter (not covered with OS).

Weight studies were then carried out in order to make sure that OS still remains on the support after filtration experiments. These experiments are summarized in Table <NUM>. The results show that a weight increase of <NUM> %, <NUM> % and <NUM> % was observed in Fluytec®, FLab® and GVB® membranes, respectively, after applying <NUM> % OS.

In order to assess the long term effect of OS over the membrane and consequently the performance stability and durability, we performed experiments with the batch set-up. <FIG>shows the flux resulting from flowing <NUM> of deionized water through the OS modified Fluytec® PP membrane at different steps until the flux reached a saturation value. The experiment was performed in four steps or stages. After each of them, the membrane was dried for <NUM> hours at room temperature, before undergoing the subsequent stage. In the figure, the water flux of commercial Fluytec® is not shown as the value is too low for the scale of Y-Axis (<<NUM> LMH - see Table <NUM>). In addition, <FIG>shows the weight corresponding to the "dry" state of the mebrane after each permeation sequence. We can observe that the water flux and the membrane weight decrease with the number of sequences. This fact probably indicates that during the permeation study the OS in excess on the membrane surface is removed and the membrane surface loses part of the hydrophilicity acquired just after the coating. In addition, at the end of the <NUM> sequences, the Fluytec®-<NUM>% OS showed a stable value of permeability and much higher water flux than that of the commercial Fluytec®. At the same time, it only showed a slightly increased weight, indicating that the OS in excess was likely to be removed until forming a monolayer or a few layers after the applied permeability sequences (see Table <NUM>).

<FIG> and Table <NUM> collect the results for FilterLAB® modified with <NUM> % OS. At the beginning of experiments, FilterLAB-<NUM>% OS shows a weight increase of <NUM>% with respect to commercial FilterLAB®. The first filtration with <NUM> has the highest water flux. Third and fourth runs show stable values in terms of water flux and membrane weight. This indicates that all OS in excess was likely removed, remaining a self-assembly monolayer of OS over the surface. In addition, if these results are compared with the results of flux and weight summarized in Table <NUM>, it can be concluded that OS modified the membrane surface and improved the water flux about <NUM> % with respect to commercial FLAB membrane.

To further investigate the stability of the OS coated PP membranes, measurements in a continuous set-up were carried out. Table <NUM> summarizes the initial water flux (measured with batch set-up) for initial commercial membranes and OS modified membranes.

<FIG> shows water flux for Fluytec® and FLAB® membranes modified with <NUM> % OS when the experiments were carried out with continuous set-up. The first sequence consisted of measuring the water flux for <NUM> hours. After this, the membranes were soaked in deionized water for <NUM> hours. Finally, the membranes were measured again for <NUM> hours of continuous operation. In these experiments, we can consider that the water flux is kept constant.

<FIG> does not show the value of water flux for commercial Fluytec® since, with continuous set-up, the water does not flow through the membrane due to its hydrophobicity.

<FIG> shows the same experiment for FilterLAB® and FLAB® <NUM> % OS. The FilterLAB®-<NUM>% OS showed a much higher permeability (<NUM>%) than that of the commercial FilterLAB®.

Finally, when comparing the performance between continuous and batch set-ups depicted in <FIG> and <FIG>, we observed that continuous set-up shows an improvement in water flux because the membrane is keeping always wet.

<FIG> shows the XPS for Fluytec® and FLAB® (A); and, Fluytec® <NUM>% OS and FLAB®- <NUM> % OS before (B) and after (C) being employed in water flux experiments. The major peak at binding energy (B. ) of <NUM> eV is attributed to C-C bond and peak at B. of <NUM> eV corresponds to oxygen. Graphics corresponding to Fluytec® shows three spectres: up, denotes the first sheet; int, denote intermedia sheet; and, down, denote the third sheet, since this membrane has three sheets. In case of FLAB®, graphics show only two spectres: up, denote the top surface; and, down, denote the bottom surface, since FLAB® consists of only one sheet. As shown in <FIG>, commercial supports do not show the O peak in the XPS. This fact is due to the fact that PP has only C and H in its structure. <FIG>shows XPS for support modified with OS (Fluytec®-<NUM>% OS and FLAB® (R)-<NUM> %OS). In these experiments, O peak is shown indicating that the OS has been deposited over surface. Finally, <FIG> C shows XPS for Fuytec®-<NUM>% OS and FLAB®-<NUM> %OS before being employed in water flux experiments. This analysis shows that after water filtration was carried out, the OS remained over the membrane surface.

In the study of pore size modification, a <NUM>/L solution of polystyrene particles of equal spherical size and greater than <NUM> is prepared. The initial particle solution had a value of <NUM> ± <NUM> NTU (Nephelotimetric Turbidity Unit). After filtering this solution using the Fluytec - <NUM>% OS membrane, the NTU reading was zero. In this sense, the modified Fluytec retains particles larger than <NUM>.

The GVB-<NUM>% OS membrane was evaluated in the elimination of E. Colis were determined using the Colibert-<NUM> test (ISO <NUM>-<NUM>: <NUM>). The results are expressed as the most probable number of coliforms (MPN) per <NUM>, being the limit of quantification <NUM> MPN/<NUM>. The starting point is a solution of <NUM> MPN/<NUM> of E. In the experiment, <NUM> is filtered. In the final analysis, <NUM> MPN/<NUM> was obtained. This fact indicates that the membrane retained the E. Coli from the medium.

Finally, Table <NUM> shows the water permeation capacities as measured employing other materials: PVDF, PSf, PA and PES. The table summarizes the permeability evaluated in batch set-up with unmodified support and supports modified with OS. Last column corresponds to flux water improvement with respect to the commercial membrane. In these experiments, the permeation capacities were not improved in any case.

Claim 1:
A polypropylene (PP) membrane coated with an organomethoxysilane alone or combined with oxide particulates, wherein said organomethoxysilane has the formula (I):
<CHM>
wherein, independently, R1 is a C1-<NUM> alkyl group; R2 is a C1-<NUM> alkyl group; R3 is a C1-<NUM> alkyl group,
wherein a is <NUM>, <NUM> or <NUM>, and
wherein X-Y is <NUM> - <NUM>, <NUM> - <NUM>, <NUM>-<NUM>, or <NUM> - <NUM>.