as used herein &# 34 ; rejection rate &# 34 ; is the percentage of a particular dissolved material which does not flow through the membrane with the solvent . the rejection rate is equal to 100 minus the percentage of dissolved material which passes through the membrane , i . e . salt passage if the dissolved material is a salt . as used herein &# 34 ; flux &# 34 ; is the flow rate at which solutions pass through the membrane . as used herein &# 34 ; reverse osmosis membrane &# 34 ; is a membrane which has a rejection rate for nacl of from about 95 to about 100 percent . as used herein &# 34 ; nanofiltration membrane &# 34 ; is a membrane which has a rejection rate for nacl of from about 0 to about 95 percent and has a rejection rate for at least one divalent ion or organic compound of from about 90 to about 100 percent . as used herein &# 34 ; divalent ion &# 34 ; is an ion that has lost or gained two electrons and thus has an electric charge of (+ 2 ) or (- 2 ). such ions exist in water solutions upon the addition of inorganic salts . examples of divalent ions include magnesium ions ( mg + 2 ), calcium ions ( ca + 2 ), radium ions ( ra + 2 ), sulfate ions ( so 4 - 2 ), and nitrate ions ( no 3 - 2 ). as used herein &# 34 ; organic compounds &# 34 ; denotes compounds containing carbon and having a molecular weight above about 200 which may be rejected by a nanofiltration membrane . examples of organic compounds include pesticides such as atrazine , monosaccharides such as glucose , chlorinated hydrocarbons , peptides , and soaps containing long chain hydrocarbons . as used herein &# 34 ; polyamide &# 34 ; is a polymer in which amide linkages (-- c ( o ) nh --) occur along the molecular chain . amines useful in this invention include substances such as ammonia optionally substituted with one or more alkyl groups of one to two carbons which alkyl groups may be further optionally substituted with one or more substitutents selected from hydroxy , phenyl , or amino ; butylamine ; cyclohexylamine ; 1 , 6 - hexanediamine and mixtures thereof . preferred substituted ammonia substances include those such as dimethylamine ; trimethylamine ; ethylamine ; triethanolamine ; n , n - dimethyl ethanolamine ; ethylenediamine ; and benzylamine . it has been discovered that by contacting the above amines with the discriminating layer of reverse osmosis or nanofiltration composite membranes in which the discriminating layer comprises a crosslinked polyamide polymer , the flux is increased and the rejection rates for particular substances may be changed . polyamide polymers useful as discriminating layers for reverse osmosis membranes are typically prepared by an interfacial polycondensation reaction between a polyfunctional aromatic amine and a polyfunctional acyl halide as described , for example , in u . s . pat . no . 4 , 277 , 344 . polyamide polymers useful as discriminating layers for nanofiltration membranes are typically prepared by an interfacial polymerization between a piperazine or an amine substituted piperidine or cyclohexane and a polyfunctional acyl halide as described in u . s . pat . nos . 4 , 769 , 148 and 4 , 859 , 384 . another method of preparing polyamide membranes suitable for nanofiltration is by modifying reverse osmosis membranes by the methods and procedures of u . s . pat . nos . 4 , 765 , 897 ; 4 , 812 , 270 ; and 4 , 824 , 574 . these patents involve contacting the reverse osmosis membrane with a strong mineral acid and then a rejection enhancing agent to form the nanofiltration membrane . it is not particularly important when the polyamide discriminating layer is contacted with the amine so long as the polyamide discriminating layer has been formed . for instance , the contacting of the amine with the discriminating layer may be accomplished before the preparation of the discriminating layer into final membrane form . that is the contacting of the amine with the polyamide discriminating layer may be employed after the polyamide has been formed but before the support has been affixed . likewise , the contacting of the amine can be done after the discriminating layer is in its final composite membrane form , as in the case when the membrane is formed directly on the support . the contacting of the amine with the polyamide discriminating layer can even be employed after the composite membrane has been accomplished in a filtration operation as long as the membrane is still operable . if the membrane is to be contacted after it is in final membrane form , then the shape and composition of the membrane should be such that the polyamide discriminating layer is capable of being contacted with the above - described amine compounds . a variety of membrane shapes are commercially available and useful in the present invention . these include spiral wound , hollow fiber , tubular , or flat sheet type membranes . in regard to the composition of the membrane , often the discriminating layer has hygroscopic polymers other than the polyamide coated upon the surface of the discriminating layer . among these polymers are polymeric surfactants , polyvinyl alcohol , and polyacrylic acid . the presence of these polymers will generally not affect the invention so long as the amine and the polyamide discriminating layer come into contact . likewise , the material of construction of the porous support of the composite membrane is not critical to the invention . any porous support that provides physical strength to the discriminating layer may be employed . typical support materials that are known in the art include cellulose esters , polysulfones , polyether sulfones , polyvinyl chloride , chlorinated polyvinyl chloride , polystyrenes , polycarbonates , polyacrylonitriles , and polyesters . a particularly preferred class of support materials are polysulfones . preparation of such supports are described in u . s . pat . nos . 3 , 926 , 798 ; 4 , 039 , 440 ; and 4 , 277 , 344 . in most polyamide membranes , as the flux that the membrane is capable of increases , the rejection rate for ions decreases , i . e ., the membrane becomes less selective . this invention may be used in this manner to convert a reverse osmosis membrane into a nanofiltration membrane . this is generally accomplished as disclosed below by contacting the discriminating layer with the disclosed amines under sufficient conditions , for example , for a long enough period of time and a high enough concentration , to increase the flux and alter the rejection rate . however , the invention may also be used to increase the flux of a reverse osmosis membrane and substantially maintain the rejection rate for nacl , i . e ., not lower the rejection rate for nacl more than 10 percent , preferably not more than 5 percent , more preferably not more than 2 percent . this is accomplished via contacting the discriminating layer with the disclosed amines , but varying either the amine employed , the concentration , the time of contact , the temperature of contact , the ph , or combinations thereof from that used when changing a reverse osmosis membrane to a nanofiltration membrane . the general guidelines provided below will enable one skilled in the art to utilize the invention without undue experimentation to either change a reverse osmosis membrane to a nanofiltration membrane or increase the flux of a reverse osmosis membrane and substantially maintain the rejection rate for nacl . as mentioned above , the degree that the flux of the membrane is increased or enhanced may be controlled by varying the particular amine employed , the concentration of the amine , the time of contact between the discriminating layer and amine , the temperature of the contact , the ph of the amine solution , or combinations thereof . in general the above conditions should be such that the flux of the membrane is increased at least about 10 percent , preferably at least about 20 percent , most preferably at least 50 percent . as the flux is increased , the selectivity of the membrane may change , i . e ., the membrane may allow univalent ions such as sodium to pass through the membrane at a higher rate while only rejecting divalent ions and organic compounds . the amine used to treat the polyamide discriminating layer may be in solution , neat , or even a gas phase so long as it can be contacted with the polyamide . gas phases may typically be employed for lower molecular weight amines such as ammonia , methylamine , and dimethylamine . the solvent may be any solvent in which the amine is soluble so long as the flux enhancement and the performance of the membrane is not hindered by contact with the solvent . typical solvents may include water and organic compounds such as alcohols and hydrocarbons provided the support is not dissolved by the solvent . generally , because of its ease of handling and its availability , water is employed if a solvent is desired . the extent that the flux of the membrane is enhanced when treated with the amines of this invention varies depending upon the particular amine employed . at least one general trend applies in most situations , however . the trend being that the more functional groups which are present on the amine , e . g ., alcohol and / or amino groups , the greater the increase in flux . correspondingly , the concentration of the amine and time of contact are interrelated and effect the degree of flux enhancement . the minimum length of time that a particular amine is required to be contacted with the discriminating layer for an increase in flux depends to a great extent upon the concentration of the amine . generally , the higher the concentration of the amine , the shorter the necessary length of contacting time to increase the flux . in most cases , the concentration of the amine should be at least about 5 , preferably at least about about 20 , most preferably at least about 50 , to about 100 percent by weight . the minimum time of contact can be from at least about 15 seconds , preferably at least about one minute , more preferably at least about 30 minutes when contacted at ambient temperatures . in general , the longer the time of contact and the higher the concentration of the amine , the greater the increase in flux . after a prolonged time of contact , the flux will reach its maximum increase and no longer increase . at this point , the membrane may be used or continued to be stored in the amine . the time to reach the maximum increase varies depending upon the particular amine employed , the concentration of the amine , and the temperature of contact but is ascertainable by one skilled in the art without undue experimentation by utilizing the general trends disclosed above . for most amines and concentrations , the flux of the membrane will be maximized once the discriminating layer has been contacted for about 5 days with the amine . if it is desired to shorten the minimum length of time of contact , then the surface temperature of the polyamide discriminating layer may be increased . although this applies generally , it is particularly advantageous if low concentrations of an amine which might require a long contacting time are being employed . although temperatures from about 0 ° to about 30 ° c . are most conveniently used , increased temperatures may shorten the necessary contacting time . the increased temperatures should not be so high that the membrane &# 39 ; s performance is reduced , i . e ., not above about 130 ° c . typical temperatures which will hasten the flux effect of the membrane are at from at least about 30 ° c ., preferably at least about 60 ° c . to about 130 ° c . these temperatures may be reached by contacting the amine with the polyamide discriminating layer in a device such as an oven or a dryer . typical ovens or dryers which may be employed include convection , infrared , or forced air dryers . the ph of the amine solution to be contacted with the polyamide is not a critical aspect of the invention . however , the ph should not be so low that the particular amine being employed precipitates out of solution . on the other hand , the ph should not be so high that the polyamide discriminating layer is degraded or performance is negated . preferably , a ph of about 7 to about 12 is useful in the method of the present invention and for some amines higher phs may increase the degree of flux enhancement . the method used to contact the amine with the discriminating layer may be any which allows the amine to become associated with the polyamide for a sufficient time to increase the flux . for instance , the polyamide may be partially or totally immersed or soaked in the amine or amine solution . the amine or amine solution may also be passed through , sprayed onto , or rolled onto the discriminating layer . although the aforementioned methods may also be useful when the amine is a gas , the contacting of a gaseous amine with the discriminating layer is advantageously accomplished in a closed vessel to minimize the amount of amine employed . reverse osmosis membranes ( ft - 30 ™ available from filmtec corporation ) are contacted with triethanolamine of various aqueous concentrations at 60 ° c . as shown in table 1 for 1 hour . the membranes are then stored in water at room temperature until tested for flux , as measured in both gallons per foot per day ( gfd ) and liters per meter square per hour ( l / m 2 - hr ), and percent salt passage ( 100 - rejection rate ) using 2000 parts per million ( ppm ) aqueous sodium chloride ( nacl ) solution and a transmembrane pressure of 225 pounds per square inch ( psi ) which is 1 . 55 megapascals ( mpa ). the results are shown in table 1 . table 1__________________________________________________________________________performance when contacted with different concentrations oftriethanolamine ( tea ) for 1 hour at 60 ° c . treatment flux flux % salt ( volume flux flux std . dev . std . dev . % salt pass . rejectionpercent ) gfd l / m . sup . 2 - hr gfd l / m . sup . 2 - hr pass . std . dev . rate (%) __________________________________________________________________________100 % tea 62 . 35 36 . 68 7 . 79 4 . 58 8 . 99 6 . 24 91 . 01 66 % tea 48 . 03 28 . 25 0 . 34 0 . 20 2 . 33 0 . 14 97 . 67starting membrane 36 . 44 21 . 44 0 . 87 0 . 51 1 . 54 0 . 49 98 . 46__________________________________________________________________________ reverse osmosis membranes ( ft - 30 ™ available from filmtec corporation ) are contacted with 100 percent triethanolamine at 60 ° c . for various amounts of time as shown in table 2 . the membranes are then stored in water at room temperature until tested for flux and percent salt passage using a 2000 ppm aqueous nacl solution and a transmembrane pressure of 225 psi which is 1 . 55 mpa . the results are shown in table 2 . table 2__________________________________________________________________________performance when contacted with 100 % triethanolamine ( tea ) for different amounts of time at 60 ° c . length flux flux % % saltof flux flux std . dev . std . dev . salt rejection pass . treatment gfd l / m . sup . 2 - hr gfd l / m . sup . 2 - hr pass . rate (%) std . dev . __________________________________________________________________________60 min . 61 . 54 36 . 20 3 . 17 1 . 86 1 . 75 98 . 25 0 . 1240 min . 60 . 11 35 . 36 4 . 58 2 . 70 1 . 98 98 . 02 0 . 4720 min . 55 . 8 32 . 82 1 . 15 0 . 68 2 . 10 97 . 90 0 . 17starting membrane 37 . 77 22 . 22 3 . 40 2 . 00 1 . 45 98 . 55 0 . 19__________________________________________________________________________ reverse osmosis membranes ( ft - 30 ™ available from filmtec corporation ) are contacted with one molar solution of butylamine , cyclohexylamine , 1 , 6 - hexanediamine and benzylamine for five days at 25 ° c . reverse osmosis membranes ( ft - 30 ™ available from filmtec corporation ) are contacted with one molar solution of 1 , 6 - hexanediamine and benzylamine for one day at 25 ° c . the above treated membranes are then stored in water at room temperature until tested for flux and percent salt passage using 2000 ppm aqueous nacl solution and transmembrane pressure of 225 psi which is 1 . 55 megapascals ( mpa ). the results are shown in table 3a and 3b . table 3a______________________________________five days 5 days 5 days % of flux flux % salt rejection initial gfd l / m . sup . 2 - hr pass . rate flux______________________________________startingmembraneaverage 37 . 4905 22 . 0532 1 . 502 98 . 498std dev 1 . 4095 0 . 8291 0 . 112butyl amineaverage 48 . 3086 28 . 4168 2 . 766 97 . 234 128 . 86 % std dev 3 . 77934 2 . 22314 0 . 124cyclo hexylamineaverage 51 . 4335 30 . 2550 4 . 931 95 . 069 137 . 19 % std dev 5 . 32809 3 . 13417 0 . 3491 , 6 - hexanediamineaverage 49 . 1316 28 . 9009 3 . 158 96 . 842 131 . 05 % std dev 3 . 4174 2 . 0102 0 . 390benzyl amineaverage 62 . 0229 36 . 4841 9 . 051 90 . 949 165 . 44 .% std dev 1 . 2882 0 . 7578 1 . 186______________________________________ table 3b______________________________________one day 1 day 1 day flux flux % salt rejection gfd l / m . sup . 2 - hr pass . rate______________________________________starting membraneaverage 36 . 2623 21 . 3308 1 . 07879 98 . 92121std dev 1 . 52969 0 . 89981 0 . 087241 , 6 - hexane diamineaverage 40 . 9509 24 . 0888 1 . 12219 98 . 7781std dev 2 . 92659 1 . 72152 0 . 02112benzyl amineaverage 43 . 2974 25 . 4691 3 . 35476 96 . 64524std dev 4 . 40101 2 . 58882 0 . 09992______________________________________ reverse osmosis membranes ( ft - 30 ™ available from filmtec corporation ) are contacted with 100 percent triethanolamine at 60 ° c . for various amounts of time as shown in table 4 . the membranes are then tested for flux and percent passage using a 2000 ppm aqueous nacl solution , a 1000 ppm aqueous mgso 4 solution , a 0 . 5 percent aqueous glucose solution , and a transmembrane pressure of 120 psi which is 0 . 83 megapascals ( mpa ). the results are shown in table 4 . table 4__________________________________________________________________________length of nacl nacl mgso . sub . 4 mgso . sub . 4 glucosetreatment salt rejection flux flux salt rejection glucose rejection std . dev . with tea pass . rate gfd l / m . sup . 2 - hr pass . rate pass . rate glucose__________________________________________________________________________ 10 min 3 . 33 % 96 . 67 % 25 . 61976 15 . 07044 0 . 0 % 100 . 0 % 2 . 81 % 97 . 19 % 0 . 36 % 10 min 5 . 05 % 94 . 95 % 36 . 5628 21 . 5075 0 . 0 % 100 . 0 % 2 . 57 % 97 . 43 % 0 . 14 % 30 min 7 . 57 % 92 . 43 % 44 . 62176 26 . 24809 0 . 31 % 99 . 69 % 3 . 76 % 96 . 24 % 0 . 08 % 30 min 6 . 75 % 93 . 25 % 39 . 15984 23 . 03520 3 . 70 % 96 . 30 % 4 . 95 % 95 . 05 % 0 . 22 % 120 min 11 . 91 % 88 . 09 % 54 . 29148 31 . 93616 0 . 26 % 99 . 74 % 4 . 90 % 95 . 10 % 0 . 08 % 120 min 13 . 22 % 86 . 78 % 55 . 4616 32 . 6245 0 . 0 % 100 . 0 % 2 . 81 % 97 . 19 % 0 . 16 % starting membrane 3 . 31 % 96 . 69 % 23 . 68992 13 . 93524 0 . 70 % 99 . 30 % 3 . 28 % 96 . 72 % 0 . 29 % starting membrane 3 . 15 % 96 . 85 % 22 . 50492 13 . 23819 1 . 12 % 98 . 88 % 11 . 64 % 88 . 32 % 0 . 12 % __________________________________________________________________________ a nanofiltration membrane ( nf - 45 ™ available from filmtec corporation ) is contacted with 100 percent triethanolamine at 60 ° c . for one hour . the membrane is then stored in water at room temperature until tested for flux and percent salt passage using a 2000 ppm aqueous nacl solution and a transmembrane pressure of 225 psi . the results are shown in table 5 . table 5______________________________________ flux % salt rejection flux l / m . sup . 2 - hr pass . rate______________________________________starting membraneaverage 44 . 8122 26 . 3601 32 . 777 67 . 223std dev 1 . 71086 1 . 00639 20 . 241tea at 60 ° c . 1 hr . average 94 . 6887 55 . 6992 33 . 194 66 . 806std dev 13 . 5823 7 . 9896 3 . 864______________________________________ reverse osmosis membranes ( ft - 30 ™ available from filmtec corporation ) are contacted with the various solutions in table 6 for 20 minutes at 90 ° c . each of the three membranes is then tested to determine the rejection rate of atrazine , magnesium sulfate ( mgso 4 ) calcium chloride ( cacl 2 ), and sodium chloride ( nacl ) using the transmembrane pressures and concentrations listed in table 6 . the results are shown in table 6 . table 6__________________________________________________________________________ 130 psi (. 90 mpa ) 10 ppm 2000 ppm 130 psi (. 90 mpa ) 250 psi ( 1 . 7 mpa ) atrazine mgso4 cacl2 300 ppm 2000 ppm nacl rejection rejection flux rejection flux rejection flux rate % rate % flux ( gfd ) l / m . sup . 2 - hr rate % flux ( gfd ) l / m . sup . 2 - hr rate % flux l / m . sup . 2__________________________________________________________________________ - hr 4 % naoh , 70 % tea , 74 . 5 , 68 . 3 99 . 6 , 99 . 6 68 . 5 , 60 . 8 40 . 3 , 35 . 8 93 . 6 , 95 . 9 113 , 128 66 . 5 , 75 . 3 69 . 9 , 66 . 3 126 , 74 . 1 , 82 . 9ph 13 . 25 1 . 8 % naoh , 70 % tea , 85 . 8 , 85 . 1 99 . 6 , 99 . 6 56 . 8 , 56 . 3 33 . 4 , 33 . 1 98 . 1 , 98 . 4 105 , 105 61 . 8 , 61 . 8 80 . 92 , 79 115 , 67 . 6 , 66 . 5ph 12 . 55100 % tea , ph 10 . 44 91 . 6 , 93 . 2 99 . 6 , 99 . 9 48 . 7 , 47 . 9 28 . 6 , 28 . 2 99 . 2 , 98 . 5 94 . 2 , 88 . 5 55 . 4 , 52 . 1 87 . 8 , 86 . 5 96 , 56 . 5 , __________________________________________________________________________ 60 . 6 reverse osmosis membranes ( ft - 30 available from filmtec corporation ) are contacted with a 50 percent solution of triethanol amine ( tea ) for 20 minutes at both 50 ° c . and 70 ° c . as shown in table 7 . the average flux and average rejection rate as measured with a transmembrane pressure of 150 psi and a 2000 ppm , nacl solution are shown in table 7 below . table 7______________________________________flux flux rejection ( gfd ) ( l / m . sup . 2 - hr ) rate nacl______________________________________50 ° c . 29 . 09 17 . 11 98 % 70 ° c . 49 . 23 28 . 96 89 % ______________________________________