the dense membranes suitably have a width from 5 - 2000 μm , and preferably from 5 - 500 μm for most applications . membranes which have a width of more than 5000 μm between opposite filaments of the support layer will tend to rupture even at a small pressure difference between the two sides of such a membrane , unless the membrane thickness is considerable which is undesirable for most applications . the thickness of the dense membranes present in the supporting membrane according to the invention is less than their width and suitably less than the thickness of the filaments ; preferably the thickness of the dense membranes is less than 25 μm , most preferably less than 10 μm . although very small membranes ( having a width of e . g . less than 5 μm ) can usually withstand high pressure differences ( e . g . above 100 bar ) between both sides , even when their thickness is only a few μm , their surface area is usually less than 5 percent of the total surface area of the supported membrane which is too low for most applications . the support layer may comprise any type of non - woven monofilaments which possess sufficient strength and regularity ( thickness and surface smoothness ) provided that the monofilaments are substantially non - soluble in the membrane - forming compound itself and in suitable solvents for said compound . moreover , the monofilaments should preferably be compatible with ( pre ) polymer solutions which are suitably used to form the dense membranes in the supported membranes according to the invention , in order to attain a substantially complete coating of the monofilaments by said solutions . suitable non - woven monofilament support layers comprise a polymeric -, glass fiber - and / or metallic ( e . g . steel ) mesh ; a preferred combination of said materials is a polymer - coated steel mesh having openings of substantially equal size . preferred polymeric compounds include polyesters , such as dacron and terylene ; polyalkylenes which may comprise halogen moieties , such as polytetrafluoroethylene , and cellulose derivatives ( e . g . cellulose acetate or nitro cellulose ). a main advantage of the supported membranes according to the invention , compared with membranes comprising a porous supporting layer extending over the surface of a dense membrane layer , is the possibility to maintain fluid flows directly along both sides of the dense membranes which are now located in the support , thereby substantially reducing or even eliminating concentration polarization in the fluid layers adjacent to the membrane surfaces . consequently , the supported membranes according to the invention can be advantageously applied in dialysis processes wherein the concentration gradient in a plane perpendicular to the membrane surface provides the driving force for the transport of a particular compound through the membrane . furthermore , said supported membranes are excellently suited for application in reverse osmosis processes due to their inherent strength , in particular when the dense membranes have a width from 5 - 100 μm , which makes it possible to maintain pressure differences of more than 10 bar , or even 100 bar , between both sides of the membranes . the supported membranes according to the invention may be used in any configuration known in the art e . g . in the form of flat sheets ; preferably , the supported membranes are spirally wound in such a manner that a fluid flow can be maintained along both sides of the dense membranes . spacers , such as a mesh , a perforated sheet or a porous layer , may be applied between the supported membranes in spirally wound modules . a wide variety of ( pre ) polymers can be applied for the dense membranes which are present in the supported membrane according to the invention . the applied polymers may either comprise thermoplastics , such as polyalkylenes ( in particular polypropylene ) or thermo - hardening compounds , such as ( silicone ) rubbers , resins or fluoro - elastomers ( e . g . polydimethyl siloxane , polyurethane , styrene - butadiene - styrene rubber or fluoro silicone elastomer ). in order to obtain substantially hole - free supported membranes , it is important that a good wetting of the monofilaments is effected by the ( pre ) polymer solution . depending on the combination of monofilament material and polymer solution , treatment of the support layer with a surface active agent such as stearinic acid or polyisobutylene maleic acid anhydride triethylene pentaacetate before coating with the ( pre ) polymer solution can be advantageous . alternatively , a surface active agent can be suitably added to the polymer solution . the concentration of ( pre ) polymer in the polymer solution may be chosen within a wide range , suitably within a range from 1 - 50 % by weight of polymer in solvent , depending on the types of polymer and solvent applied . in case the surface tension of the polymer solution is relatively high , it can be advantageous to use a relatively concentrated polymer solution in order to prevent the formation of holes in the areas of the coated support layer where dense membranes are to be formed . for instance , in case a solution of polypropylene in a solvent with relatively high viscosity and boiling point ( e . g . decaline ) is applied , the concentration of polypropylene in said solvent is preferably at least 5 % by weight . the support layer may be coated e . g . by submerging the layer in the polymer solution or by spraying polymer solution on the layer which is then suitably supported by solid or liquid supporting means . solvent is suitably removed , after coating for the support layer with the polymer solution , by evaporation , preferably at an elevated temperature . in some cases it is possible to remove at least part of the solvent by placing the coated support layer on or in a body of liquid wherein the solvent is soluble and wherein the polymer coating is insoluble . preferably , solvent is removed from the coated support layer at an elevated temperature at which no phase separation occurs in the ( pre ) polymer coating from which the dense membranes are to be formed . in particular when a polypropylene solution is used for preparing dense membranes therefrom , it is important that the temperature should not fall below 120 ° c ., and preferably not below 140 ° c ., during coating of the support layer and during the subsequent evaporation step , in order to avoid crystallization of polypropylene which would give rise to unacceptable pore formation in the membranes thus formed . after having removed at least part , and preferably substantially all of the solvent from the coated supporting layer , a further heat treatment may be applied in particular when thermo - hardening polymers are used , suitably in combination with catalysts and / or cross - linking agents , in the coating . suitably , the heat treatment is carried out at a temperature from 100 °- 160 ° c for a period of 30 minutes - 24 hours . the invention will be further illustrated by means of the following examples . a non - woven monofilament polyester mesh comprising openings having a width of 49 μm was , after cleaning with n - hexane , submerged at a temperature of 20 ° c . in a solution comprising 2 . 5 % by weight of a styrene / butadiene / styrene block copolymer dissolved in cyclohexane , dried at 50 ° c . and again submersed in said solution and dried at 50 ° c . the resulting supported membrane contained 18 g copolymer / m 2 mesh , permitting a carbon dioxide gas flux of 120 m 3 ( s . t . p . )/ bar , m 2 , day through the dense membranes formed in the mesh openings . a similar cleaned polyester mesh as described in example 1 was submerged in a solution comprising 5 % by weight of polypropylene and 1 % by weight of stearinic acid in decalin at a temperature of 150 ° c . which was maintained during drying of the coated mesh . accordingly , dense membranes were obtained which covered 20 % of the total supported membrane area , the remaining area being covered by the monofilaments of the mesh ; the coating amounted to 14 g polypropylene / m 2 mesh . in dialysis experiments carried out with the supported dense membrane at a temperature of 55 ° c ., a flux of n - hexane and n - octane amounting to 0 . 41 and 1 . 27 m 3 / m 2 , day , respectively , was obtained . a steel mesh comprising openings having a width of 2 mm was cleaned with n - hexane and then submerged in a polypropylene - comprising solution as described in example 2 . during drying at 150 ° c . of the steel mesh coated with 23 g polypropylene / m 2 mesh dense membranes were formed which covered 80 % of the total surface area of the supported membrane . in dialysis experiments carried out with said supported membrane at a temperature of 55 ° c ., fluxes of n - hexane and iso - octane amounting to 0 . 30 and 0 . 14 m 3 / m 2 , day , respectively , were obtained . a polytetrafluoroethylene mesh having openings with a width of 50 μm was cleaned with n - hexane and subsequently submerged in a solution comprising 2 . 5 % by weight of poly dimethyl siloxane and 1 % by weight of polyisobutylene maleic acid anhydride triethylene pentaacetate in isooctane , dried at 50 ° c . and cured at 120 ° c . for 4 hours . the resulting supported membrane showed excellent adhesion between the coating and the mesh after wetting with n - hexane .