EP2673074A1

EP2673074A1 - Nanofiltration membrane

Info

Publication number: EP2673074A1
Application number: EP12702837.1A
Authority: EP
Inventors: Martin Mechelhoff; Thomas FRÜH; Christopher Kohl
Original assignee: Lanxess Deutschland GmbH
Current assignee: Lanxess Deutschland GmbH
Priority date: 2011-02-10
Filing date: 2012-02-09
Publication date: 2013-12-18
Also published as: CL2013002318A1; EP2486974A1; US20140175013A1; ZA201306753B; CN103370124A; RU2013141217A; CA2826601A1; WO2012107510A1; CN103370124B; JP2014506531A; BR112013020114A2; AU2012215417A1; JP5909617B2

Abstract

Nanofiltration membrane comprises a porous supporting membrane, where the surface of supporting membrane is coated with an emulsion polymerization prepared polymer particles having a particle diameter of less than 70 nm, preferably 40-50 nm. Independent claims are also included for: (1) producing a nanofiltration membrane having a porous supporting membrane, comprising applying a dispersion (latex) of polymer particles prepared by emulsion polymerization to the supporting membrane and forming a polymer layer on separation-active layer of the support membrane; and (2) use of polymer particles obtained by emulsion polymerization with mean particle diameter less than 70 nm, preferably 40-50 nm for the preparation of a nanofiltration membrane.

Description

Nanofiltration membrane

The invention relates to nanofiltration membranes with a porous support membrane, a process for the preparation of this membrane and their use. For example, in the chemical, food, beverage, electronics and pharmaceutical industries, membranes are used for the separation of solid-liquid mixtures and liquids. In terms of environmental technology, these are also used in the purification of wastewater and the production of drinking water.

Various membrane separation processes are known from the prior art. These include microfiltration, ultrafiltration and nanofiltration, as well as reverse osmosis. These methods are to be assigned to the mechanical separation processes. The separation mechanisms are caused by different membrane structures. They separate by means of membrane pores whose diameters are smaller than those of the particles to be separated.

Another important mechanism in the separation with nanofiltration and reverse osmosis membranes are, in addition to steric effects, the electrostatic interaction of ions in solution or partially dissociated hydrocarbons with corresponding charged groups on the surface of a membrane in aqueous solution. This interaction allows a separation of two substances with a similar particle radius, but different charge or valency. Likewise, separation may occur with membranes having correspondingly small pores, e.g. for nanofiltration or reverse osmosis, based on the different diffusion tendency in the permeation through the membrane of the substances present in a solution.

Known processes for the treatment of liquids under pressure are microfiltration, ultrafiltration and nanofiltration. The pore size of the nano-, ultra- and microfiltration membranes are about 0.001 μπι to 10.0 μπι.

For the characterization of membranes, the retention R with respect to a substance is usually used.

R = w (feed) - w (permeaf) × 100 [%]

w (feed)

where w denotes the mass fraction of any substance.

The retention describes the percentage of a separated substance in the permeate (Latin "permeare"), based on the concentration in the feed also depends on the transmembrane pressure or flow and the concentration of the starting solution. The retentate (Latin "retenere" = retain) contains the increased compared to the feed concentration of the substance to be separated.

This demonstrates the difficulty in assessing the separation properties of a membrane. A rough classification of the membranes is often given by the molecular cut-off (cut-off) along with the flow. This separation limit is equivalent to the molecular weight for which the membrane has a retention of at least 90% and can be very different, especially in the field of nanofiltration depending on the molecular structure of the substances to be separated. The cut-off of nanofiltration membranes is usually <1500 g / mol. Ultrafiltration membranes usually have a cut-off of <about 150 000 g / mol.

Also known are membranes based on organic polymers useful for molecular-level separations, e.g. separation of gases, pervaporation and / or vapor permeation. However, a disadvantage of these polymer membranes is their short lifetime, due to the sensitivity of the polymer membranes

Solvents that swell or destroy the membrane material. Furthermore, the relatively low temperature resistance of current polymer membranes is a problem.

Frequently, ceramic membranes are used, which have a significantly longer life, since they are, depending on the composition, to organic compounds, acids or alkalis are largely inert and also have a higher temperature resistance than polymer materials. Thus, they can also be used for separation tasks in chemical processes, such as e.g. in the vapor permeation, are used. Such ceramic membranes are usually prepared by the so-called sol-gel method or by the dip-coating process so that a total of a multilayer system of ceramic layers of different thicknesses and pore sizes is produced, the top layer, which takes over the actual separation task, the has smallest pores and should be as thin as possible. Due to the low elasticity of ceramic materials, ceramic membranes are sensitive to mechanical stress and break easily. They can not be rolled in contrast to polymer membranes to produce space-saving winding modules. In general, one of the main problems in all known membrane synthesis methods is to control the adjustment of the pore size and the pore shape of the separation-active layer exactly and uniformly and thus to achieve a very narrow pore size distribution.

Polymeric membranes of a wide variety of polymers are available at relatively low cost for wide pH ranges and many applications, but are often not resistant to them organic solvents and at very high and / or very low pH. Also, a permanent temperature resistance at over 80 ° C is rarely given. Although there are many approaches to improve these properties of polymer membranes, but often one of the above requirements is not met. In addition, most polymers are plastically deformable at higher temperatures. This causes compaction of the entire membrane when operated under pressure at higher temperatures. During compaction, the result is that the pore structure of a membrane is completely compressed and thus the filtration resistance is greatly increased. The flow drop is thus induced. Another disadvantage of the usual polymer materials is the poor resistance to organic solvents or oils and the plasticizing effect of the oils on the polymers. As a result, the separation capacity of the membranes is impaired.

Membrane technology plays an important role in the purification of liquid mixtures. In particular, in the extraction of drinking water from seawater by means of reverse osmosis and in product processing increasingly ultra and nanofiltration or reverse osmosis membranes are used.

In membrane processes dilute solutions are usually concentrated and separated organic solvents, water or salt solutions. Either valuable substances or pollutants are obtained in more concentrated and possibly lower-salt solutions, whereby subsequent storage, transport, disposal and further processing can be made more cost-effective. In particular, in wastewater treatment, it is the goal of the membrane treatment to recover the largest part of the volume as permeate in a not or only slightly loaded form. The concentrated retentate can be worked up with less effort in terms of still existing recyclables or disposed of more economically in this concentrated form, for example by combustion. The field of membrane processes involves very different processes. Accordingly, different membranes and their technical designs are available. Technically relevant membrane separation processes are predominantly operated as crossflow filtrations. High shear stresses due to high flow velocities and special module constructions are designed to minimize membrane contamination and reduce concentration polarization.

Commercially available nanofiltration membranes are composite membranes made by interfacial condensation, such as described in US 5,049,167. However, these known membranes can be prepared only very expensive and only in compliance with costly safety measures, since as starting materials z. As carcinogenic diamines and highly reactive acrylic chlorides are used. Such membranes can be configured in many ways, for example as flat film modules, cassette modules, spiral wound modules or hollow fiber modules.

Furthermore, commercial filtration membranes can usually be used only at process temperatures up to about 80 ° C. The object of the present invention is therefore to provide a high-performance nanofiltration membrane which has high thermal stability, good stability in organic and inorganic solvents and at high and low pH values, and also good release properties based on a suitable surface modification. Another object of the invention is also to provide a method by which it is possible to produce defined pore sizes for the respective membranes.

It is known in the art that polymer particles on a porous substrate having a broader pore size distribution can be deposited to obtain a composite membrane having a narrower pore size distribution. The voids between the particles form pores with which separation from a liquid can be performed. The composite membranes thus obtained can be used, for example, as ultrafiltration and

Microfiltration membranes are used.

To achieve the object, therefore, a nanofiltration membrane of the aforementioned type is provided, wherein the surface of the support membrane is coated with polymer particles produced by emulsion polymerization having an average particle diameter <70 nm, preferably between 30 to 65 nm, more preferably between 40 to 50 nm.

It is here between the filtration property of a membrane characterized e.g. by the cut-off, and to distinguish the structure of the filtration membrane.

In the following, the term "nanofiltration membrane" refers to the use of polymer particles in the particle diameter range <100 nm for producing the same. "Nanofiltration membrane" does not imply its separation properties.

Separation, separation properties, separation behavior are used as synonyms. The separation effect is with the help of o. G. Cut-off defined.

Polymer particles and nanoparticles are used as synonyms.

The use of polymer particles prepared by emulsion polymerization with a mean particle diameter <70 nm, preferably between 30 to 65 nm, more preferably between 40 and 50 nm, offers numerous advantages over other polymer particles, since the chemical and physical properties of the polymer particles, such as particle size, particle morphology . Swelling behavior, catalytic activity, hardness, dimensional stability, stickiness, surface energy, aging resistance and impact resistance can be adjusted. This is done on the one hand by the production process, in particular by the polymerization process, as well as by the selection of suitable base monomers and on the other hand by the selection of suitable functional groups whose concentration and settlement area in the polymer particles can be selectively adjusted or tailored within wide limits.

The release-active layer is thus the polymer particles produced by emulsion polymerization with an average particle diameter <70 nm, preferably between 30 to 65 nm, particularly preferably between 40 and 50 nm, layer produced, also referred to as polymer layer, of the nanofiltration membrane according to the invention.

Emulsion polymerization is understood in particular to be a process which is known per se, in which water is used as the reaction medium, in which the monomers used are polymerized in the presence or absence of emulsifiers and free-radical-forming substances to form mostly aqueous polymer latices (see Römpp Lexikon der Chemie, Volume 2) , 10th edition 1997; PA Lovell, MS El-Aasser, Emulsion Polymerization and Emulsion

Polymers, John Wiley & Sons, ISBN: 0 471 96746 7; H. Gerrens, Fortschr. Hochpolym. Forsch. 1, 234 (1959)). In contrast to the suspension or dispersion polymerization, the emulsion polymerization generally gives finer particles which allow a smaller gusset diameter and thus smaller pore sizes in the separation-active layer. Particles of size below 500 nm are by suspension or

Dispersion polymerization generally not accessible, which is why these particles are generally unsuitable for the purposes of this patent application.

Surprisingly, it has now been found that the choice of certain polymer particles no longer requires the use of additional thermal or chemical means for stabilizing the nanofiltration membrane according to the invention.

The choice of monomers sets the glass transition temperature and the glass transition width of the polymer particles. The determination of the glass transition temperature (Tg) and the width of the glass transition (ATg) of the polymer particles is carried out by differential scanning calorimetry (DSC), preferably as described below. For this purpose, two cooling / heating cycles are carried out for the determination of Tg and ATg. Tg and ATg are determined in the second heating cycle. For the determinations, approximately 10-12 mg of the selected polymer particle is placed in a Perkin-Elmer DSC sample container (standard aluminum pan). The first DSC cycle is performed by first cooling the sample to -100 ° C with liquid nitrogen and then heating it to + 150 ° C at a rate of 20K min. The second DSC cycle is started by immediately cooling the sample, as soon as a sample temperature of + 150 ° C is reached. In the second heating cycle, the sample is again heated to + 150 ° C as in the first cycle. The heating rate in the second cycle is again 20K / min. Tg and ATg are determined graphically on the DSC curve of the second heating process. For this purpose, three straight lines are applied to the DSC curve. The 1st straight line is applied to the curve part of the DSC curve below Tg, the 2nd straight line to the curve branch with inflection point passing through Tg and the 3rd straight line to the curve branch of the DSC curve above Tg. In this way, three straight lines with two intersections are obtained. Both intersections are each characterized by a characteristic temperature. The glass transition temperature Tg is obtained as the mean value of these two temperatures and the width of the glass transition ATg is obtained from the difference between the two temperatures.

Preferably, the polymer particles have a glass transition temperature (Tg) of -85 ° C to 150 ° C, preferably -75 ° C to 110 ° C, more preferably -70 ° C to 90 ° C, on.

The width of the glass transition in the case of the polymer particles used according to the invention is preferably greater than 5 ° C., more preferably greater than 10 ° C. Preferably, the polymer particles produced by emulsion polymerization are rubbery.

Rubbery polymer particles are preferably those based on conjugated dienes such. As butadiene, isoprene, 2-chlorobutadiene and 2,3-dichlorobutadiene, vinyl acetate, styrene or derivatives thereof, 2-vinylpyridine and 4-vinylpyridine, acrylonitrile, acrylamides, methacrylamides, tetrafluoroethylene, vinylidene fluoride, hexafluoropropene, double bond-containing hydroxy, epoxy, amino , Carboxy, and keto compounds.

Preferred monomers or monomer combinations include butadiene, isoprene, acrylonitrile, styrene, alpha-methylstyrene, chloroprene, 2,3-dichlorobutadiene, butyl acrylate, 2-ethylhexyl acrylate, hydroxyethyl methacrylate, glycidyl methacrylate, acrylic acid, diacetone acrylamide, tetrafluoroethylene, vinylidene fluoride and hexafluoropropene. "On the basis" here means that the polymer particles preferably consist of more than 60% by weight, preferably more than 70% by weight, more preferably more than 90% by weight, of the stated monomers.

The polymer particles may be crosslinked or uncrosslinked. The polymer particles may in particular be those based on homopolymers or random copolymers. The terms homopolymers and random copolymers are known to the person skilled in the art and are explained, for example, by Vollmert, Polymer Chemistry, Springer 1973.

The polymer base of the rubber-like, crosslinked or unvarnished polymer particles containing functional groups may in particular serve: BR: polybutadiene,

ABR: butadiene / acrylic acid-C i_ ₄ alkyls stercopolymere,

IR: polyisoprene,

SBR: random styrene-butadiene copolymers having styrene contents of 1-60, preferably 5-50, weight percent,

FKM: fluoro rubber,

ACM: acrylate rubber,

NBR: polybutadiene-acrylonitrile copolymers having acrylonitrile contents of 5-60, preferably 10-60 weight percent, CR: polychloroprene

EAM: ethylene / acrylate copolymers,

EVM: ethylene / vinyl acetate copolymers.

Further preferred polymer particles are thermoplastic and those based on methacrylates, in particular methyl methacrylate, styrene, alpha-methylstyrene and acrylonitrile. The polymer particles preferably have an approximately spherical geometry.

The polymer particles used according to the invention have an average particle diameter of less than 70 nm, preferably between 30 and 65 nm, particularly preferably between 40 and 50 nm.

The average particle diameter is determined by ultracentrifugation with the aqueous latex of the polymer particles from the emulsion polymerization. The method gives a mean value for the particle diameter taking into account any agglomerates. (HG Müller (1996) Colloid Polymer Science 267: 1113-1116 and W. Scholtan, H. Lange (1972) Kolloid-Z and Z. Polymere 250: 782). Ultracentrifugation has the advantage of characterizing the total particle size distribution and calculating various means such as number average and weight average from the distribution curve. The average diameter data used according to the invention relate to the weight average. Diameter data such as dio, d ₅₀ and d ₈₀ can be used. These data mean that 10, 50 or 80% by weight of the particles have a diameter which is smaller than the corresponding numerical value in% by weight. The diameter determination by means of dynamic light scattering is carried out on the latex. Common are lasers operating at 633 nm (red) and 532 nm (green). Dynamic light scattering gives an average of the particle size distribution curve. The average diameter data used according to the invention relate to this mean value. The particles are prepared by emulsion polymerization, wherein the particle size is adjusted in a wide diameter range by varying the starting materials and emulsifier concentration, initiator concentration, liquor ratio of organic to aqueous phase, ratio of hydrophilic to hydrophobic monomers, amount of crosslinking monomer, polymerization temperature, etc. After polymerization, the latices are treated by vacuum distillation or by stripping with superheated steam to separate volatile components, especially unreacted monomers.

For a further work-up of the polymer particles thus prepared, e.g. by coagulation, can be dispensed with. The polymer particles produced by emulsion polymerization according to the invention are at least partially crosslinked in a preferred embodiment.

The crosslinking of the polymer particles produced by emulsion polymerization is preferably carried out by the addition of polyfunctional monomers in the polymerization, e.g. by the addition of compounds having at least two, preferably 2 to 4, copolymerizable C =C double bonds, such as diisopropenylbenzene, divinylbenzene,

Divinyl ether, divinyl sulfone, diallyl phthalate, triallyl cyanurate, triallyl isocyanurate, 1,2-polybutadiene, N, N'-m-phenylene maleimide, 2,4-toluylene bis (maleimide), triallyl trimellitate, glycidyl methacrylate, acrylates and methacrylates of polyvalent, preferably 2- to 4- C2 to C10 alcohols, such as ethylene glycol, 1,2-propanediol, butanediol, hexanediol, polyethylene glycol having 2 to 20, preferably 2 to 8, oxyethylene units, neopentyl glycol,

Bisphenol A, glycerol, trimethylolpropane, pentaerythritol, sorbitol and unsaturated polyesters of aliphatic di- and polyols and maleic acid, fumaric acid, and / or itaconic acid.

The crosslinking of the polymer particles can be achieved directly during the emulsion polymerization, such as by copolymerization with crosslinking multifunctional compounds or by subsequent crosslinking as described below. Direct crosslinking during emulsion polymerization is preferred. Preferred multifunctional comonomers are compounds having at least two, preferably 2 to 4, copolymerizable C =C double bonds, such as diisopropenylbenzene, divinylbenzene, divinyl ether, divinylsulfone, diallyl phthalate, triallyl cyanurate, triallyl isocyanurate, 1,2-polybutadiene, N, N'-m- Phenylene maleimide, 2,4-toluylenebis (maleimide) and / or triallyl trimellitate. In addition, the acrylates and methacrylates of aliphatic amines, epoxides and polyhydric, preferably 2- to 4-valent C 2 to C 10 alcohols such as ethylene glycol, 1,2-propanediol, butanediol, hexanediol, polyethylene glycol having from 2 to 20, preferably 2 to 8 oxyethylene units, neopentyl glycol, bisphenol A, glycerol, trimethylolpropane, pentaerythritol,

Sorbitol with unsaturated polyesters of aliphatic di- and polyols and maleic acid, fumaric acid, and / or itaconic acid.

The crosslinking during the emulsion polymerization can also be carried out by continuing the polymerization up to high conversions or in the monomer feed process by polymerization with high internal conversions. Another possibility is to carry out the emulsion polymerization in the absence of regulators.

For the crosslinking of the uncrosslinked or the weakly crosslinked polymer particles following the emulsion polymerization, it is best to use the latices which are obtained in the emulsion polymerization. Suitable crosslinking chemicals are, for example, organic peroxides, such as dicumyl peroxide, t-butylcumyl peroxide, bis (t-butyl-peroxy-isopropyl) benzene, di-t-butyl peroxide, 2,5-ditmethylhexane-2,5-dihydroperoxide, 2, 5-dimethylhexine-3,2,5-dihydroper-oxide, dibenzoyl peroxide, bis (2,4-dichlorobenzoyl) peroxide, t-butyl perbenzoate and organic azo compounds such as azo-bis-isobutyronitrile and azo-bis-cyclohexanenitrile and di and polymercapto compounds such as dimercaptoethane, 1,6-dimercaptohexane, 1,3,5-trimercaptotriazine and mercapto-terminated polysulfide rubbers such as mercapto-terminated reaction products of bis-chloroethylformal with sodium polysulfide.

The optimum temperature for carrying out the postcrosslinking is of course dependent on the reactivity of the crosslinker and can be carried out at temperatures from room temperature to about 180 ° C., optionally under elevated pressure (see Houben-Weyl, US Pat.

Methods of Organic Chemistry, 4th Edition, Volume 14/2, page 848). Particularly preferred crosslinking agents are peroxides.

The crosslinking of rubbers containing C =C double bonds to polymer particles can also be described in dispersion or emulsion with simultaneous, partial, possibly complete, hydrogenation of the C =C double bond by hydrazine as described in US Pat. No. 5,302,696 or US Pat. No. 5,442,009 or other hydrogenating agents, for example Organometallhydridkomplexe done.

Before, during or after postcrosslinking, an agglomeration of particles may possibly be carried out. The crosslinked polymer particles used according to the invention expediently have toluene at 23 ° C insoluble fractions (gel content) of at least about 70 wt .-%, more preferably at least about 80 wt .-%, particularly preferably 90 wt .-%, more preferably at least about 98 wt .-% on. The insoluble in toluene content is determined in toluene at 23 °. Here, 250 mg of the polymer particles are swollen in 25 ml of toluene for 24 hours with shaking at 23 ° C. After centrifugation at 20,000 rpm, the insoluble fraction is separated and dried. The gel content results from the quotient of the dried residue and the weight and is given in percent by weight.

The crosslinked polymer particles used also suitably have a swelling index of less than about 80, more preferably less than 60, more preferably less than 40, in toluene at 23 ° C. Thus, the swelling indices of the polymer particles (Qi) may more preferably be between 1 and 20 and 1-10. The swelling index is calculated from the weight of the solvent-containing polymer particles swollen in toluene at 23 ° for 24 hours (after centrifugation at 20,000 rpm) and the weight of the dry polymer particles: Qi = wet weight of the polymer particles / dry weight of the polymer particles.

To determine the swelling index, 250 mg of the polymer particles are allowed to swell in 25 ml of toluene with shaking for 24 h. The gel is centrifuged off and weighed and then dried at 70 ° C to constant weight and weighed again.

Preferably, the support membrane is made of an inorganic or organic material. Moreover, it is advantageous that the support membrane is chemically and / or mechanically stable.

It should be pH stable and also in organic solvents, such as aldehydes, ketones, mono- and polyhydric alcohols, benzene derivatives, halogenated hydrocarbons, ethers, esters, carboxylic acids, cyclic hydrocarbons, amines, amides, lactams, lactones, sulfoxides, Alkanes, alkenes. Preferably, a support membrane is selected which is chemically stable in the following solvents: acetone, toluene, benzene, water, tetrahydrofuran, dimethylformamide, dimethyl sulfoxide, N-methylpyrrolidone, N-ethylpyrrolidone, pyridine, methanol, ethanol, propanol, isopropanol, butanol, isobutanol, pentane , Hexane, heptane, octane, nonane, decane, methyl ethyl ketone, diethyl ether, dichloromethane, tetrachloroethane, carbon tetrachloride, methyl tert-butyl ether, chlorobenzene, dichlorobenzene, trichlorobenzene, nitrobenzene, ethyl acetate, cyclohexane.

It has been found that the nanofiltration membrane according to the invention is stable, in particular also in the pH range of 10-14 and / or 1-4. For the application of the membrane, it is also useful that the support membrane is made of a material which is temperature stable both at room temperature and in typical application process temperatures. A temperature stability of 50 to 200 ° C, preferably between 70 and 150 ° C and 80 to 120 ° C is also conceivable. For example, micro-glass fiber webs, metal fleeces, dense glass fiber fabric or metal fabric, as well as ceramic or carbon fiber fleeces or fabrics can be used as the inorganic, permeable support membrane. The skilled person will appreciate that all other known, preferably flexible, provided with open pores or openings in the appropriate size materials can be used as support membranes. Also, ceramic composite materials may be used, such as inorganic support materials of an oxide selected from A1 ₂ 0 ₃ , titanium oxide, zirconium oxide or silicon oxide. Also preferably, the inorganic support membrane comprises a material selected from ceramic, SiC, Si ₃ N ₄ , carbon, glass, metal or semimetal. Furthermore, organic polymer materials having sufficient chemical and thermal resistance can be used as the supporting membrane, such as polyimide, polytetrafluoroethylene, polyvinylidene fluoride, polyetherimide, polyetherketone,

Polyetheretherketone, polyethersulfone, polybenzimidazole, polyamide.

Preferably, the support membranes have a pore size of less than 500 nm. More preferably, they have a pore size of less than 100 nm and most preferably less than 50 nm. More preferably, the pore size of the supporting membrane is smaller than the middle one

Particle diameter of the polymer particles.

Preferably, the thickness of the support membrane 5 to 100 μιη, more preferably from 20 to 80 μιη, most preferably from 30 to 60 μιη.

Preferably, the polymer particles produced by emulsion polymerization are at least partially functionalized by the addition of polyfunctional monomers in the polymerization. The polyfunctional monomers may be selected from the group consisting of: compounds having at least two, preferably 2 to 4, copolymerizable C =C double bonds, such as diisopropenylbenzene, divinylbenzene, divinyl ether, divinylsulfone, diallyl phthalate, triallyl cyanurate, triallyl isocyanurate, 1,2- Polybutadiene, N, N'-m-phenylene maleimide, 2,4-toluylene bis (maleimide), triallyl trimellitate, acrylates and methacrylates of aliphatic amines, epoxides and polyhydric, preferably 2- to 4-valent C 2 to C 10 alcohols, such as ethylene glycol, propanediol 1,2, butanediol, hexanediol, polyethylene glycol with 2 to 20, preferably 2 to 8 oxyethylene units, neopentyl glycol, Bisphenol A, glycerol, trimethylolpropane, pentaerythritol, sorbitol and unsaturated polyesters of aliphatic di- and polyols and maleic acid, fumaric acid, and / or itaconic acid.

The separation-active layer of the nanofiltration membrane according to the invention preferably has at least one monolayer of the polymer particles having the average particle diameter <70 nm, preferably between 30 and 65 nm, particularly preferably between 40 and 50 nm.

A preferred embodiment of the nanofiltration membrane according to the invention has a separating active layer with 0.1 to 20 μπι thickness, in which case several layers of the polymer particles are superimposed.

Preferably, the thickness of the separation-active layer is at most as thick as the support membrane. Another invention is the production process of the invention

A nanofiltration membrane wherein a dispersion (latex) of polymer particles prepared by emulsion polymerization is applied to the support membrane and a polymer layer (release active layer) is formed on the support membrane.

It was found that the dispersion used is largely monodisperse, i. H. According to the method of dynamic light scattering, 95.4% of the polymer particles are in a size class with a deviation of ± 7 nm.

Preferably, the process is carried out continuously.

The aqueous dispersion preferably has polymer particles with an average particle diameter <70 nm, preferably between 30 and 65 nm, particularly preferably between 40 and 50 nm, the dry rubber content after the polymerization being at least 20%, preferably at least 25%, especially preferably at least 30%, based on the total volume of the polymer.

The concentration of latices to a dry rubber content of not more than 65% based on the total volume of the polymer is also conceivable for the preparation. The determination of the dry rubber content is carried out as follows:

The dry rubber content is determined with a halogen moisture meter, e.g. the Mettler Toledo Halogen Moisture Analyzer HG63. Here, a latex is dried at a temperature of 140 ° C and weighed continuously. The measurement is considered complete when the weight loss is less than 1 mg / 50 sec.

The dry rubber content after the polymerization is preferably at most 65 based on the total volume of the polymer. Preferably, the latex with the polymer particles is applied to the support membrane by means of a nozzle.

In a subsequent step, the nanofiltration membrane formed in this way is dried. It is conceivable that the nanofiltration membrane formed in this way can additionally be crosslinked, whereby the polymer particles are connected to one another and / or to the support membrane. Usually, chemical (covalent and / or ionic) as well as physical types of crosslinking are induced by electromagnetic (e.g., UV), thermal, and / or radioactive radiation. All conventional crosslinking aids can be used.

This further reduces the pore size and modifies the filtration properties.

Another invention is the use of polymer particles produced by emulsion polymerization with average particle diameters <70 nm, preferably between 30 to 65 nm, more preferably between 40 to 50 nm for the preparation of a nanofiltration membrane.

Another invention is the use of the nanofiltration membrane for the food industry, the chemical industry and the biochemical industry. This list is not limiting.

The invention will be explained in more detail below by means of examples: EXAMPLES

Preparation of Polymer Particles Type 1 and 2

The following starting materials were used for the preparation of the polymer particles. In Table 1, formulation ingredients are based on 100 parts by weight of the monomer mixture.

Monomers i) butadiene (99%, destabilized) of Lanxess Deutschland GmbH

2) Acrylonitrile (99% stabilized with hydroquinone monomethyl ether), the Merck KGaA 3) styrene (98%) of KMF Laboratory Chemistry GmbH

4) trimethylolpropane trimethacrylate (96%) from Aldrich; Product number: 24684-0;

(Abbreviation: TMPTMA)

5) Hydroxyethyl methacrylate (97% from Arcos, abbreviation: HEMA) emulsifiers

Disproportionated rosin acid (abbreviated as HS) - calculated as the free acid starting from the amount of Dresinate® 835 used (Abieta Chemie GmbH; D-86358 Gersthofen)

The Dresinate® 835 batch used was characterized by the solids content and by the emulsifier components present as the sodium salt, as the free acid and as the neutral. The solids content was determined according to the procedure described by Maron, S. H .; Madow, B.P .; Borneman, E. "The effective equivalent of certain rosin acids and soaps" Rubber Age, April 1952, 71-72.

The mean value of three aliquots of the Dresinate® 835 batch used was found to be 71% by weight solids.

The emulsifier moieties present as the sodium salt and as the free acid were determined by titration according to the procedure described by Maron, SH, Ulevitch, IN, Eider, ME Fatty and Rosin Acids, Soaps, and Their Mixtures, Analytical Chemistry, Vol. 21, 6, 691-695 Method determined.

To determine (in an example) 1.213 g Dresinate® 835 (71% pure) dissolved in a mixture of 200 g of distilled water and 200 g of distilled isopropanol, treated with an excess of sodium hydroxide solution (5 ml 0.5 N NaOH) and with 0.5 N hydrochloric acid back titrated. The titration course was followed by potentiometric pH measurement. The evaluation of the titration curve was carried out as described in Analytical Chemistry, Vol. 21, 6, 691-695.

Three aliquots of the Dresinate® 835 batch used were averaged:

Gesamtemulgatorgehalt: 2.70 mmol / g dry matter _T

Na salt: 2.42 mmol / g dry mass

Free acid: 0.28 mmol / g dry mass

With the aid of the molar masses for the sodium salt of disproportionated abietic acid (324 g / mol) and the molar mass for the free disproportionated abietic acid (302 g / mol), the proportions by weight of Na salt, free acid and unperfected portions of the Dresinate® used 835 batch calculated:

Sodium salt of disproportionated rosin acid: 78.4% by weight

Free disproportionated rosin acid: 8.5% by weight

Unrecorded Shares (Neutrals) 13, 1 wt% In the following formulations, the amounts of Dresinate® 835 used in the polymerizations were converted into free acid (abbreviated as HS) and as wt. Parts based on 100 parts by weight of monomers. In this conversion, the neutral body was not considered.

To reconstruct the conversion of the amounts of disproportionated abietic acid (HS) indicated in Table 1 on the basis of the amounts of Dresinate 835® used, the following Table 1 is added:

Table 1:

Partially hydrogenated tallow fatty acid - abbreviated as FS (Edenor "HTiCT N from Cognis Oleo Chemicals)

The Gesamtemulgatorgehalt and the average molecular weight of Edenor ^® HTiCT used N-batch were titrimetrically determined using the following methods: Maron, SH, Ulevitch, IN, Eider, ME "Fatty and Rosin Acids, soaps, and Their Mixtures, Analytical Chemistry, Vol 21, 6, 691-695; Maron, SH; Madow, BP; Borneman, E. "The effective equivalent of certain rosin acids and soaps" Rubber Age (1952), 71 71-2) The titration (in one example, 1.5 g Edenor® HTiCT N in a mixture of 200 g distilled water and 200 g of distilled isopropanol, treated with an excess of 15 ml of NaOH (0.5 mol / 1) and titrated back with 0.5 M hydrochloric acid.

Here, was obtained as a mean of three aliquots of the Edenor ^® used HTiCT N-Charge:

Gesamtemulgatorgehalt: 3.637 mmol / g dry matter _T

Molecular weight (free acid): 274.8 mg / mmol In the following formulations, the amounts of partially hydrogenated tallow fatty acid used (as commercially available) were reported as "free acid = FS".

The calculation of the amounts necessary for the adjustment of the given in the tables degrees of neutralization was carried out on the basis of the titrimetrically determined contents of the various constituents of the Dresinate® used 835- and Edenor ^® HTiCT N-batches. The neutralization grades were adjusted with potassium hydroxide.

regulator

⁸⁾ tert-dodecyl mercaptan of the Chevron Phillips Chemical Company LP (Sulfole 120 ^®)

The preparation of the polymer particles was carried out by emulsion polymerization in a 20 1 autoclave with stirrer. For the polymerization runs, 4.3 kg of monomers were used with 0.34 g of 4-methoxyphenol (Arcos Organics, Item No. 126001000, 99%). The total emulsifier and total water amounts given in the table (minus the amounts of water required for the preparation of the aqueous premix and p-menthane hydroperoxide solutions, see below) were initially introduced together with the emulsifiers and the necessary amounts of potassium hydroxide in the autoclave.

After temperature control of the reaction mixture to 15 ° C in the listed polymerization batches each 50% freshly prepared aqueous Premix solutions (4%) were added to the autoclave. These premix solutions consisted of:

0.284 g of ethylenediaminetetraacetic acid (Fluka, article number 03620),

0.238 g of iron (II) sulfate * 7 H ₂ O (Riedel de Haen, item number: 12354) (without

Calculated water of crystallization)

0.576 g of Rongalit C, Na formaldehyde sulfoxylate 2-hydrate (Merck-Schuchardt,

Article number 8.06455) (calculated without water of crystallization) as well

0.874 g trisodium phosphate * 12 H ₂ O (Acros, article number 206520010) (without

Calculated water of crystallization).

For the activation of the listed polymerizations, 5 g were used for the styrene-containing type and 1.7 g of p-menthane hydroperoxide (Trigonox NT 50 from Akzo-Degussa) for the acrylonitrile-containing type, which were emulsified in 200 ml of the emulsifier solution prepared in the reactor.

When reaching 30% conversion, the remaining 50% of the premix solution was added. The temperature control during the polymerization was carried out by adjusting the coolant quantity and the coolant temperature in the temperature ranges indicated in the tables.

Upon reaching a polymerization conversion of more than 85% (usually: 90% to 100%), the polymerization was stopped by adding an aqueous solution of 2.35 g of diethylhydroxylamine (DEHA, Aldrich, Article No. 03620).

Removal of volatiles

To remove volatile constituents from the latex, the latex was subjected to steam distillation under atmospheric pressure. The polymer particles thus prepared are used for a nanofiltration membrane according to the invention.

Table 2 shows the recipe of the polymer particles produced; the following indices are used: i) butadiene (unstabilized)

2) acrylonitrile (99% stabilized with hydroquinone monomethyl ether), Merck KGaA 3) styrene (stabilized with 100 to 150 ppm of 4-tert-butylpyrocatechol)

4) trimethylolpropane trimethacrylate (96% from Aldrich)

5) hydroxyethyl methacrylate (97% from Arcos)

6) Amount calculated from the amount of Dresinate 835 calculated

disproportionated rosin acid (abbreviated as HS)

Edenor HTiCT N from Oleo Chemicals (abbreviated as FS)

tert-dodecylmercaptan (Sulfol® 120 from Chevron Phillips)

The properties of the particles produced are shown in Table 3. Table 2:

Table 3:

Production of the nanofiltration membrane according to the invention with polymer particles of type 1 or with polymer particles of type 2

As a supporting membrane strongly cross-linked polyimide was used. This membrane was coated using a slot die in the bead-coating process with an aqueous dispersion of rubbery polymer particles of types 1 or 2. The support membrane was led under the nozzle at a speed of 2 m / min. The distance of the nozzle to the support membrane was 100 μιη. The wet film thickness of the latex layer was estimated at 30 μm, which results in a dry film thickness of the separating active layer of about 10 μm. The drying was carried out at room temperature under atmospheric pressure for about 30 minutes. Nanofiltration membrane type 1 (with polymer particles type 1) and nanofiltration membrane type 2 (with polymer particles type 2) were produced.

In the case of the nanofiltration membrane type 2 according to the invention, the crosslinking of the polymer particles was additionally carried out after the drying. As the crosslinking agent, 1,6-hexamethylene diisocyanate (HDI) was used. First, the membrane was rinsed with acetone followed by n-hexane. Then a solution of 2 wt% HDI and 0.2 wt% was added.

Dioctyl-Zinnlaureat in n-hexane applied to the membrane. After a reaction time of 20 minutes at 25 ° C, the reaction solution was removed and the membrane rinsed with acetone.

Determination of filtration properties

The filtration properties of the nanofiltration membranes according to the invention were measured using a model system of polystyrene oligomers in various solvents. The

Oligomers had molecular weights between about 230 and 1100 g / mol. After passing through a sufficiently large amount of permeate, samples of retentate and permeate were taken and determined by HPLC, the respective concentration of the oligomers by chromatography. From the resulting concentrations of the respective oligomers, their retention by the membrane and thus the molecular weight cut-off can be determined.

Filtration properties of the nanofiltration membrane of the invention type 1

Table 4 shows the values for the retention of polystyrene oligomers by a nanofiltration membrane according to the invention, type 1, the separation-active layer consisting of polymer particles of type 1, which have not been additionally crosslinked. The solvent chosen was acetone. The separation of the styrene oligomers took place at 25 ° C. and a pressure of 30 bar. The flow rate was determined to be 11 l / (m ² h). Table 4:

The nanofiltration membrane according to the invention thus has a cut-off of about 1000 g / mol in the test system defined here, since a 90% retention has been measured here. Thus, the membrane is suitable for nanofiltration.

Filtration properties of the nanofiltration membrane type 2 according to the invention

Table 5 contains values for the retention of polystyrene oligomers by a type 2 nanofiltration membrane according to the invention, wherein the release active layer consists of polymer particles type 2 which have been additionally crosslinked by 1,6-hexamethylene diisocyanate. The values for filtration in three different solvents (acetone, tetrahydrofuran (THF) and toluene) are given. Flows of 7 to 11 l / (m ² h) were measured at a temperature of 25 ° C and a pressure of 30 bar.

Table 5:

Molecular weight / LM: toluene LM: THF LM: acetone

g / mol retention /% retention /% retention /%

236 - 42 34

295 52 50 45

395 73 71 66 495 82 79 76

595 88 85 84

695 91 87 87

795 93 89 89

895 95 89 91

995 96 90 92

1095 96 91 93

From the measured values shown here, it can be seen that after crosslinking of the polymer particles, the cut-off of this membrane is at 700 to 800 g / mol, so that the membrane can be used for nanofiltration. The values are only slightly dependent on the selected solvent. The membranes of the invention have been used in all

Solvents no dissolution phenomena shown.

Claims

claims

Nanofiltration membrane with a porous support membrane, characterized in that the surface of the support membrane is coated with polymer particles produced by emulsion polymerization having an average particle diameter of less than 70 nm, preferably between 30-65 nm, more preferably between 40-50 nm coated.

Nanofiltration membrane according to claim 1, characterized in that the support membrane consists of an inorganic or organic material.

Nanofiltration membrane according to claim 2, characterized in that the pore size of the supporting membrane is less than 500 nm, preferably less than 100 nm and particularly preferably less than 50 nm.

Nanofiltration membrane according to claim 3, characterized in that the pore size of the supporting membrane is smaller than the average particle diameter of the polymer particles.

Nanofiltration membrane according to claim 4, characterized in that the thickness of the supporting membrane 5 to 100 μιη, preferably 20 to 80 μιη and most preferably from 30 μιη to 60 μιη.

Nanofiltration membrane according to claim 5, characterized in that the polymer particles produced by emulsion polymerization are rubbery.

Nanofiltration membrane according to claim 6, characterized in that the rubbery polymer particles are those based on conjugated dienes such as butadiene, isoprene, 2-chlorobutadiene and 2,3-dichlorobutadiene, vinyl acetate, styrene or derivatives thereof, 2-vinylpyridine and 4-vinylpyridine, acrylonitrile, Acrylamides, methacrylamides, tetrafluoroethylene, vinylidene fluoride, hexafluoropropene, double bond-containing hydroxy, epoxy, amino, carboxy, and keto compounds.

Nanofiltration membrane according to claim 7, characterized in that the polymer particles have a glass transition temperature (Tg) of -85 ° C to 150 ° C, preferably - 75 ° C to 110 ° C, particularly preferably -70 ° C to 90 ° C.

Nanofiltration membrane according to claim 8, characterized in that the polymer particles produced by emulsion polymerization are at least partially crosslinked.

10. nanofiltration membrane according to claim 9, characterized in that the polymer particles produced by emulsion polymerization are at least partially functionalized by the addition of polyfunctional monomers in the polymerization.

The nanofiltration membrane according to claim 10, characterized in that the polyfunctional monomers are selected from the group consisting of:

Compounds with at least two, preferably 2 to 4, copolymerizable C =C double bonds, such as diisopropenylbenzene, divinylbenzene, divinyl ether, divinylsulfone, diallyl phthalate, triallyl cyanurate, triallyl isocyanurate, 1,2-polybutadiene, N, N'-m-phenylene maleimide, 2,4- Toluylenebis (maleimide), triallyl trimellitate, acrylates and methacrylates of aliphatic amines, epoxides and polyhydric, preferably 2- to 4-valent C 2 to C 10 alcohols, such as ethylene glycol, 1,2-propanediol, butanediol, hexanediol, polyethylene glycol of 2 to 20, preferably 2 to 8 oxyethylene units, neopentyl glycol, bisphenol A, glycerol, trimethylolpropane, pentaerythritol, sorbitol and unsaturated polyesters of aliphatic di- and polyols and maleic acid, fumaric acid, and / or itaconic acid.

12. nanofiltration membrane according to claim 11, characterized in that the

Polymer particles have an approximately spherical geometry.

13. nanofiltration membrane according to claim 12, characterized in that the

Polymer particles in toluene at 23 ° C insoluble fractions of at least about 70 wt .-%, preferably at least about 80 wt .-%, more preferably 90 wt .-%, more preferably at least about 98 wt .-%.

14. nanofiltration membrane according to claim 13, characterized in that the

Polymer particles in toluene at 23 ° C have a swelling index of less than about 80, preferably 60 and more preferably 40.

15. nanofiltration membrane according to claim 14, characterized in that the

Layer thickness of the nanofiltration membrane at least one monolayer of the polymer particles having the average particle diameter less than 70 nm, preferably 30- 65 nm, more preferably 40-50 nm (separation active layer).

16. nanofiltration membrane according to claim 15, characterized in that the separation-active layer has a layer thickness of 0.1 μιη to 20 μιη.

17. nanofiltration membrane according to claim 16, characterized in that the separation-active layer is at most as thick as the thickness of the support membrane.

18. A process for producing a nanofiltration membrane with a porous

Supporting membrane according to one of the preceding claims, characterized in that a dispersion (latex) of produced by emulsion polymerization Polymer particles applied to the support membrane and a polymer layer (separation active layer) is formed on the support membrane.

19. The method according to claim 18, characterized in that the method is carried out continuously.

20. The method according to claim 19, characterized in that the dispersion is monodisperse.

21. The method according to claim 20, characterized in that the dispersion

Polymer particles having an average particle diameter of less than 70 nm, preferably 30-60 nm, particularly preferably 40-50 nm, wherein the dry rubber content (dry rubber content) after polymerization at least 20%, preferably at least 25%, particularly preferably at least 30% on the total volume of the polymer.

22. The method according to claim 21, characterized in that the dry rubber content

(Dry Rubber content) after the polymerization is a maximum of 65% based on the total volume of the polymer.

23. The method according to claim 22, characterized in that the application of the

Polymer particles is carried out by means of a nozzle.

24. The method according to claim 23, characterized in that the nanofiltration membrane is dried in a subsequent step.

25. The method according to claim 24, characterized in that the separation-active layer of

Nanofiltration membrane is additionally crosslinked.

26. Use of polymer particles produced by emulsion polymerization having an average particle diameter of less than 70 nm, preferably 30-60 nm, more preferably 40-50 nm for the preparation of a nanofiltration membrane according to any one of the preceding claims.

27. Use of the nanofiltration membrane according to one of the preceding claims for the food industry, the chemical industry, biochemical industry.