( i ) from 0 to 95 , preferably from 60 to 80 , weight % of one or more c 4 - 12 vinyl monomers ; ( ii ) from 50 to 2 , preferably from 25 to 10 , weight % of a crosslinking agent ; and ( iii ) from 70 to 3 , preferably from 65 to 15 , most preferably from 60 to 15 , desirably from 50 to 15 weight % of a functionalized monomer containing reactive functional group selected from the group consisting of c 1 - 8 hydroxy esters of c 3 - 6 ethylenically unsaturated carboxylic acids , chloride derivatives thereof , chlorostyrene and c 1 - 8 straight chain , branched or cyclic amines which are unsubstituted or substituted by up to two c 1 - 4 alkyl radicals at the nitrogen atom ; the sum of the weight % of said monomers being 100 weight %. some vinyl monomers include styrene , alpha - methyl styrene , para - methyl styrene and c 1 - 4 alkyl esters of c 3 - 6 unsaturated carboxylic acids . the styrenic monomers such as styrene , alpha - methyl styrene , para - methyl styrene may also be referred to as vinyl aromatic monomers . some c 1 - 4 alkyl esters of c 3 - 6 unsaturated carboxylic acids include methyl methacrylate , ethyl methacrylate , butyl methacrylate , methyl acrylate , ethyl acrylate and butyl acrylate . some crosslinking agents include divinyl benzene , divinyl toluene , di - and tri - acrylates and di - and tri - methacrylates such as pentaerythritol trimethacrylate . the functionalized polymeric supports may be prepared by conventional suspension polymerization techniques . these are well known to those skilled in the art . generally the monomers are dispersed in water as continuous phase using one or more surfactant or suspending agents which may be ionic such as long chain ( e . g . c 12 - 18 ) fatty acids or derivatives thereof ( e . g . sulfonates ) and salts thereof such as for example , dodecyl benzene sulfonate , or a non ionic surfactant such as polyoxyethylene sorbitan fatty acid esters ( such as those sold under the trademark tween ). typically the emulsion also contains a free radical initiator ( such as persulfates ( optionally in the presence of a reducing agent ) or peroxides ). the emulsion is heated to begin polymerization and the polymerization may be completed in a batch process . the selection of the surfactants to some extent controls the particle size of the final particles in the emulsion polymerization . generally the polymeric particles will have a particle size from 0 . 1 to 1000 , preferably from 10 to 300 microns , surface area of greater than 10 , preferably from 100 to 1500 m 2 / g and a pore volume of at least 0 . 2 , preferably at least 0 . 6 cc / g of support . there are several methods which may be used to increase the pore size / volume in the polymeric particles . for example silica may be incorporated into the polymer then dissolved out using a strong base . silica impregnated with a blowing agent may be incorporated into the polymeric particles and then the blowing agent may be activated . the residual silica may again be dissolved from the polymer particles . this technique is disclosed in u . s . pat . no . 5 , 168 , 104 issued dec . 1 , 1992 to li et al . the co - catalysts useful in the present invention are aluminoxanes also sometimes called alumoxanes . the aluminoxane compounds of the present invention have the formula i : r 1 2 alo ( r 1 alo ) m alr 1 2 wherein each r 1 is independently selected from the group consisting of c 1 - 20 hydrocarbyl radicals and m is from 3 to 50 , preferably from 3 to 30 , most preferably from 5 to 30 . most preferably r 1 is selected from the group consisting of c 1 - 6 , most preferably c 1 - 4 straight chained or branched alkyl radicals . suitable alkyl radicals include a methyl radical , an ethyl radical , an isopropyl radical and an isobutyl radical . in some commercially available aluminoxanes r 1 is a methyl radical . in one aspect of the present invention the co - catalyst may be supported on the support in an amount from 0 . 01 to 0 . 8 , preferably from 0 . 01 to 0 . 4 , most preferably from 0 . 02 to 0 . 3 g per g of support ( e . g . 1 to 80 , preferably 1 to 40 , most preferably 2 to 30 weight %). in a further aspect the present invention the supported co - catalyst may be used in conjunction with a single site catalyst . typically the catalysts used with the aluminoxane , prepared in accordance with the present invention , comprise a transition metal complex of at least one c 5 - 13 ligand containing a 5 - membered carbon ring having delocalized bonding within the ring and bound to the metal atom through covalent η 5 bonds ; and said ligand being unsubstituted or up to fully substituted with one or more substituents as described below . generally the catalyst may be a single site type catalyst typically comprising a transition metal , preferably an early transition metal ( e . g . ti , v , zr and hf ) and generally having two bulky ligands . in many of the well known single site catalysts typically one of the bulky ligands is a cyclopentadienyl - type ligand . these cyclopentadienyl - type ligands comprise a c 5 - 13 ligand containing a 5 - membered carbon ring having delocalized bonding within the ring and bound to the metal atom through covalent η 5 bonds which are unsubstituted or may be further substituted ( sometimes referred to in a short form as cp ligands ). cyclopentadienyl - type ligands include unsubstituted cyclopentadienyl , substituted cyclopentadienyl , unsubstituted indenyl , substituted indenyl , unsubstituted fluorenyl and substituted fluorenyl . an exemplary list of substituents for a cyclopentadienyl - type ligand includes the group consisting of c 1 - 10 hydrocarbyl radicals ( including phenyl and benzyl radicals ), which hydrocarbyl substituents are unsubstituted or further substituted by one or more substituents selected from the group consisting of a halogen atom , preferably a chlorine or fluorine atom and a c 1 - 4 alkyl radical ; a c 1 - 8 alkoxy radical ; a c 6 - 10 aryl or aryloxy radical ; an amido radical which is unsubstituted or substituted by up to two c 1 - 8 alkyl radicals ; a phosphido radical which is unsubstituted or substituted by up to two c 1 - 8 alkyl radicals ; silyl radicals of the formula — si —( r ) 3 wherein each r is independently selected from the group consisting of hydrogen , a c 1 - 8 alkyl or alkoxy radical , and c 6 - 10 aryl or aryloxy radicals ; and germanyl radicals of the formula — ge —( r ) 3 wherein r is as defined directly above . if there are two such bulky ligands ( i . e . bis - cp ) the catalysts are metallocene - type catalysts . the cp ligand may be bridged to another cp ligand by a silyl bridge or a short chain ( c 1 - 4 ) alkyl radical . the cp - type ligand may be bridged to an amido radical which may be further substituted by up to two additional substituents . such bridged complexes are sometimes referred to as constrained geometry catalysts . broadly , the transition metal complex ( or catalyst ) suitable for use in the present invention has the formula : wherein m is a transition metal preferably selected from the group consisting of ti , v , zr , hf , cr , fe , co , ni and pd , most preferably selected from the group consisting of ti , hf and zr ( as described below ); l is a monoanionic ligand independently selected from the group consisting of a cyclopentadienyl - type ligand , a bulky heteroatom ligand ( as described below ) and a phosphinimine ligand ( as described below ); x is an activatable ligand which is most preferably a simple monoanionic ligand such as alkyl or a halide ( as described below ); n may be from 1 to 3 , preferably 2 or 3 ; and p may be from 1 to 3 , preferably 1 or 2 , provided that the sum of n + p equals the valence state of m , and further provided that two l ligands may be bridged by a silyl radical or a c 1 - 4 alkyl radical . if one or more of the l ligands is a phosphinimine ligand the transition metal complex may be of the formula : wherein m is a transition metal preferably selected from ti , hf and zr ( as described below ); pl is a phosphinimine ligand ( as described below ); l is a monoanionic ligand selected from the group consisting of a cyclopentadienyl - type ligand or a bulky heteroatom ligand ( as described below ); x is an activatable ligand which is most preferably a simple monoanionic ligand such as an alkyl or a halide ( as described below ); m is 1 or 2 ; n is 0 or 1 ; and p is an integer fixed by the valence of the metal m ( i . e . the sum of m + n + p equals the valence state of m ). in one embodiment the catalysts are group 4 metal complexes in the highest oxidation state . for example , the catalyst may be a bis ( phosphinimine ) dichloride complex of titanium , zirconium or hafnium . alternately , the catalyst contains one phosphinimine ligand , one “ l ” ligand ( which is most preferably a cyclopentadienyl - type ligand ) and two “ x ” ligands ( which are preferably both chloride ). the preferred metals ( m ) are from group 4 ( especially titanium , hafnium or zirconium ) with titanium being most preferred . the catalyst may contain one or two phosphinimine ligands which are covalently bonded to the metal . the phosphinimine ligand is defined by the formula : wherein each r 3 is independently selected from the group consisting of a hydrogen atom ; a halogen atom ; c 1 - 20 , preferably c 1 - 10 hydrocarbyl radicals which are unsubstituted by or further substituted by a halogen atom ; a c 1 - 8 alkoxy radical ; a c 6 - 10 aryl or aryloxy radical ; an amido radical ; a silyl radical of the formula : wherein each r 2 is independently selected from the group consisting of hydrogen , a c 1 - 8 alkyl or alkoxy radical , and c 6 - 10 aryl or aryloxy radicals ; and a germanyl radical of the formula : the preferred phosphinimines are those in which each r 3 is a hydrocarbyl radical , preferably a c 1 - 6 hydrocarbyl radical . a particularly preferred phosphinimine is tri -( tertiary butyl ) phosphinimine ( i . e . wherein each r 3 is a tertiary butyl group ). preferred phosphinimine catalysts are group 4 organometallic complexes which contain one phosphinimine ligand ( as described above ) and one ligand l which is either a cyclopentadienyl - type ligand or a heteroligand . as used herein , the term “ heteroligand ” refers to a ligand which contains at least one heteroatom selected from the group consisting of boron , nitrogen , oxygen , phosphorus or sulfur . the heteroligand may be sigma or pi - bonded to the metal . exemplary heteroligands include ketimide ligands , silicone - containing heteroligands , amido ligands , alkoxy ligands , boron heterocyclic ligands and phosphole ligands , as all described below . as used herein , the term “ ketimide ligand ” refers to a ligand which : ( a ) is bonded to the transition metal via a metal - nitrogen atom bond ; ( b ) has a single substituent on the nitrogen atom ( where this single substituent is a carbon atom which is doubly bonded to the n atom ); and ( c ) has two substituents sub 1 and sub 2 ( described below ) which are bonded to the carbon atom . the substituents “ sub 1 ” and “ sub 2 ” may be the same or different . exemplary substituents include hydrocarbyls having from 1 to 20 carbon atoms , silyl groups , amido groups and phosphido groups . for reasons of cost and convenience it is preferred that these substituents both be hydrocarbyls , especially simple alkyls and most preferably tertiary butyl . wherein the — denotes a bond to the transition metal and μ is sulfur or oxygen . the substituents on the si atom , namely r x , r y and r z are required in order to satisfy the bonding orbital of the si atom . the use of any particular substituent r x , r y or r z is not especially important to the success of this invention . it is preferred that each of r x , r y and r z is a c 1 - 2 hydrocarbyl group ( i . e . methyl or ethyl ) simply because such materials are readily synthesized from commercially available materials . the term “ amido ” is meant to convey its broad , conventional meaning . thus , these ligands are characterized by ( a ) a metal - nitrogen bond and ( b ) the presence of two substituents ( which are typically simple alkyl or silyl groups ) on the nitrogen atom . the terms “ alkoxy ” and “ aryloxy ” is also intended to convey its conventional meaning . thus , these ligands are characterized by ( a ) a metal oxygen bond and ( b ) the presence of a hydrocarbyl group bonded to the oxygen atom . the hydrocarbyl group may be a c 1 - 10 straight chained , branched or cyclic alkyl radical or a c 6 - 13 aromatic radical which radicals are unsubstituted or further substituted by one or more c 1 - 4 alkyl radicals ( e . g . 2 , 6 di - tertiary butyl phenoxy ). boron heterocyclic ligands are characterized by the presence of a boron atom in a closed ring ligand . this definition includes heterocyclic ligands which also contain a nitrogen atom in the ring . these ligands are well known to those skilled in the art of olefin polymerization and are fully described in the literature ( see , for example , u . s . pat . nos . 5 , 637 , 659 ; 5 , 554 , 775 ; and the references cited therein ). the term “ phosphole ” is also meant to convey its conventional meaning . “ phospholes ” are cyclic dienyl structures having four carbon atoms and one phosphorus atom in the closed ring . the simplest phosphole is c 4 ph 4 ( which is analogous to cyclopentadiene with one carbon in the ring being replaced by phosphorus ). the phosphole ligands may be substituted with , for example , c 1 - 20 hydrocarbyl radicals ( which may , optionally , contain halogen substituents ); phosphido radicals ; amido radicals ; or silyl or alkoxy radicals . phosphole ligands are also well known to those skilled in the art of olefin polymerization and are described as such in u . s . pat . no . 5 , 434 , 116 ( sone , to tosoh ). the term “ activatable ligand ” or “ leaving ligand ” refers to a ligand which may be activated by the aluminoxane ( also referred to as an “ activator ”) to facilitate olefin polymerization . exemplary activatable ligands are independently selected from the group consisting of a hydrogen atom ; a halogen atom , preferably a chlorine or fluorine atom ; a c 1 - 10 hydrocarbyl radical , preferably a c 1 - 4 alkyl radical ; a c 1 - 10 alkoxy radical , preferably a c 1 - 4 alkoxy radical ; and a c 5 - 10 aryl oxide radical ; each of which said hydrocarbyl , alkoxy , and aryl oxide radicals may be unsubstituted by or further substituted by one or more substituents selected from the group consisting of a halogen atom , preferably a chlorine or fluorine atom ; a c 1 - 8 alkyl radical , preferably a c 1 - 4 alkyl radical ; a c 1 - 8 alkoxy radical , preferably a c 1 - 4 alkoxy radical ; a c 6 - 10 aryl or aryloxy radical ; an amido radical which is unsubstituted or substituted by up to two c 1 - 8 , preferably c 1 - 4 alkyl radicals ; and a phosphido radical which is unsubstituted or substituted by up to two c 1 - 8 , preferably c 1 - 4 alkyl radicals . the number of activatable ligands depends upon the valency of the metal and the valency of the activatable ligand . the preferred catalyst metals are group 4 metals in their highest oxidation state ( i . e . 4 + ) and the preferred activatable ligands are monoanionic ( such as a halide — especially chloride or c 1 - 4 alkyl — especially methyl ). one useful group of catalysts contain a phosphinimine ligand , a cyclopentadienyl ligand and two chloride ( or methyl ) ligands bonded to the group 4 metal . in some instances , the metal of the catalyst component may not be in the highest oxidation state . for example , a titanium ( iii ) component would contain only one activatable ligand . as noted above , one group of catalysts is a group 4 organometallic complex in its highest oxidation state having a phosphinimine ligand , a cyclopentadienyl - type ligand and two activatable ligands . these requirements may be concisely described using the following formula for the preferred catalyst : wherein : m is a metal selected from ti , hf and zr ; pl is as defined above , but preferably a phosphinimine wherein r 3 is a c 1 - 6 alkyl radical , most preferably a t - butyl radical ; l is a ligand selected from the group consisting of cyclopentadienyl , indenyl and fluorenyl ligands which are unsubstituted or substituted by one or more substituents selected from the group consisting of a halogen atom , preferably chlorine or fluorine ; c 1 - 4 alkyl radicals ; and benzyl and phenyl radicals which are unsubstituted or substituted by one or more halogen atoms , preferably fluorine ; x is selected from the group consisting of a chlorine atom and c 1 - 4 alkyl radicals ; m is 1 ; n is 1 ; and p is 2 . in one embodiment of the present invention the transition metal complex may have the formula : [( cp ) q m [ n ═ p ( r 3 )] b x c wherein m is the transition metal ; cp is a c 5 - 13 ligand containing a 5 - membered carbon ring having delocalized bonding within the ring and bound to the metal atom through covalent η 5 bonds and said ligand being unsubstituted or up to fully substituted with one or more substituents selected from the group consisting of a halogen atom , preferably chlorine or fluorine ; c 1 - 4 alkyl radicals ; and benzyl and phenyl radicals which are unsubstituted or substituted by one or more halogen atoms , preferably fluorine ; r 3 is a substituent selected from the group consisting of c 1 - 10 straight chained or branched alkyl radicals , c 6 - 10 aryl and aryloxy radicals which are unsubstituted or may be substituted by up to three c 1 - 4 alkyl radicals , and silyl radicals of the formula — si —( r ) 3 wherein r is c 1 - 4 alkyl radical or a phenyl radical ; l is selected from the group consisting of a leaving ligand ; q is 1 or 2 ; b is 1 or 2 ; and the valence of the transition metal —( q + b )= c . the catalysts systems in accordance with the present invention may have a molar ratio of aluminum from the aluminoxane to transition metal from 5 : 1 to 1000 : 1 , preferably from 5 : 1 to 300 : 1 , most preferably from 30 : 1 to 300 : 1 , most desirably from 50 : 1 to 120 : 1 . in a further embodiment of the present invention the above noted catalyst may be supported on the above noted polymeric support . the catalyst may be loaded on the support to provide from 0 . 01 to 5 , preferably from 0 . 05 to 2 , most preferably from 0 . 1 to 1 weight % of transition metal per g of support . in a further embodiment of the present invention the aluminoxane and the above noted catalyst may be premixed in the ratios specified above ( e . g . from 5 : 1 to 1000 : 1 , preferably from 5 : 1 to 300 : 1 , most preferably from 30 : 1 to 300 : 1 , most desirably from 50 : 1 to 120 : 1 ) and the resulting mixture may be supported on the functionalized polymeric catalyst support . these ratios may be broadly used with the catalyst and activator regardless of the sequence of deposition on the support . in supporting the aluminoxane , catalyst or mixture on the polymeric support conventional techniques may be used . the support in a hydrocarbyl diluent may be contacted with the aluminoxane or the catalyst or a mixture thereof in the same or a compatible hydrocarbyl solvent or diluent . the resulting treated polymeric support may be separated from the bulk of the solvent or diluent by decanting or by drying typically from room temperature ( 20 ° c .) to about 60 ° c ., preferably under vacuum ( of less than about 10 torr ) optionally while passing an inert gas such as nitrogen through the separated support and diluent / solvent . it should be noted the polymeric support may swell in the solvent or diluent but should not readily dissolve because it is crosslinked . it may be possible to spray dry the polymeric support together with the aluminoxane and or catalyst . inert hydrocarbon solvents typically comprise a c 4 - 12 hydrocarbon which may be unsubstituted or substituted by a c 1 - 4 alkyl group , such as butane , pentane , hexane , heptane , octane , cyclohexane , methylcyclohexane or hydrogenated naphtha . an additional solvent is isopar e ( c 8 - 12 aliphatic solvent , exxon chemical co .). the polymerization in accordance with the present invention may be conducted in a liquid phase as either a slurry or solution polymerization conducted in an inert diluent or solvent , or gas phase polymerization . the difference between slurry and solution polymerization being whether the resulting polymer is soluble in the liquid phase . solution and slurry polymerization processes are fairly well known in the art . these processes are conducted in the presence of an inert hydrocarbon solvent typically a c 4 - 12 hydrocarbon which may be unsubstituted or substituted by a c 1 - 4 alkyl group such as butane , pentane , hexane , heptane , octane , cyclohexane , methylcyclohexane or hydrogenated naphtha . an additional solvent is isopar e ( c 8 - 12 aliphatic solvent , exxon chemical co .). the polymerization may be conducted at temperatures from about 20 ° c . to about 250 ° c . depending on the product being made , this temperature may be relatively low such as from 20 ° c . to about 180 ° c ., typically from about 80 ° c . to 150 ° c . and the polymer is insoluble in the liquid hydrocarbon phase ( diluent ) ( e . g . a slurry polymerization ). the reaction temperature may be relatively higher from about 180 ° c . to 250 ° c ., preferably from about 180 ° c . to 230 ° c . and the polymer is soluble in the liquid hydrocarbon phase ( solvent ). the pressure of the reaction may be as high as about 15 , 000 psig for the older high pressure processes or may range from about 15 to 4 , 500 psig . in the gas phase polymerization of a gaseous mixture comprising from 0 to 15 mole % of hydrogen , from 0 to 30 mole % of one or more c 3 - 8 alpha olefins , from 15 to 100 mole % of ethylene , and from 0 to 75 mole % of an inert gas at a temperature from 50 ° c . to 120 ° c ., preferably from 75 ° c . to about 110 ° c ., and at pressures typically not exceeding 3447 kpa ( about 500 psi ), preferably not greater than 2414 kpa ( about 350 psi ). suitable olefin monomers may be ethylene and c 3 - 20 mono - and diolefins . preferred monomers include ethylene and c 3 - 12 alpha olefins which are unsubstituted or substituted by up to two c 1 - 6 alkyl radicals . illustrative non - limiting examples of such alpha olefins are one or more of propylene , 1 - butene , 1 - pentene , 4 - methyl - 1 - pentene , 1 - hexene , 1 - heptene , 1 - octene and 1 - decene . the polymers prepared in accordance with the present invention have a good molecular weight . that is , weight average molecular weight ( mw ) will preferably be greater than about 30 , 000 ranging up to 10 7 , preferably 10 5 to 10 7 . hydrogen may be used in the polymerization to control the molecular weight of the polymer . the polyethylene polymers which may be prepared in accordance with the present invention typically comprise not less than 60 , preferably not less than 70 , most preferably not less than 80 weight % of ethylene and the balance of one or more c 4 - 10 alpha olefins , preferably selected from the group consisting of 1 - butene , 1 - hexene and 1 - octene . the present invention will now be illustrated by the following non - limiting examples . in the examples unless otherwise indicated parts means part by weight ( i . e . grams ) and percent means weight percent . the suspension medium , 1 . 0 l water containing 95 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round - bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask at room temperature while stirring . the dispersed medium consisted of 7 . 5 g of hema , 31 . 5 g of styrene , 11 g of dvb , 40 g of toluene , 1 . 2 g of hydrophobic fumed silica and 0 . 7 g of aibn . the mixture was then stirred at 400 rpm as the temperature was increased to 58 ° c . ; the temperature was kept at 58 ° c . for 18 hours while stirring . the temperature was then raised to 68 ° c . and kept at this temperature for 16 hours while stirring . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration . the polymer beads were washed several times with water and then dispersed in 300 ml of a 4n naoh aqueous solution containing 50 ml of methanol . the suspension was shaken in a parr shaker at room temperature for one day . the polymer beads were filtered from the suspension by vacuum filtration and washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone . the beads were dried in air at room temperature and sieved . the 30 - 100 μm fraction was used as catalyst support . the suspension medium , 1 . 0 l water containing 80 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask which was at 50 ° c . while stirring . the dispersed medium consisted of 15 g of hema , 24 g of styrene , 11 g of dvb , 40 g of toluene , 5 . 0 g of ptmg and 0 . 7 g of aibn . the mixture was then stirred at 350 rpm as the temperature was increased to about 60 ° c . ; the temperature was kept at about 60 ° c . for 24 hours while stirring . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone . the beads were dried in air at room temperature and sieved . the 35 - 80 μm fraction was used as catalyst support . the suspension medium , 1 . 0 l water containing 80 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask which was at 50 ° c . while stirring . the dispersed medium consisted of 25 g of hema , 14 g of styrene , 11 g of dvb , 40 g of toluene , 5 . 0 g of ptmg and 0 . 7 g of aibn . the mixture was then stirred at 350 rpm as the temperature was increased to about 60 ° c . ; the temperature was kept at about 60 ° c . for 24 hours while stirring . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone . the beads were dried in air at room temperature and sieved . the 35 - 80 μm fraction was used as catalyst support . the suspension medium , 1 . 0 l water containing 80 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask which was at 50 ° c . while stirring . the dispersed medium consisted of 30 g of hema , 9 g of styrene , 11 g dvb , 40 g of toluene , 5 . 0 g of ptmg , and 0 . 7 g of aibn . the mixture was then stirred at 400 rpm as the temperature was increased to about 60 ° c . ; the temperature was kept at about 60 ° c . for 24 hours while stirring . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone . the beads were dried in air at room temperature and sieved . the 20 - 50 μm fraction was used as catalyst support . the suspension medium , 1 . 0 l water containing 80 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask which was at 60 ° c . while stirring . the dispersed medium consisted of 40 g of hema , 10 g of ptma , 35 g of toluene , 6 . 0 g of hydrophobic 5 μm spherical silica particles , and 0 . 5 g of aibn . the mixture was then stirred at 250 rpm as the temperature was increased to about 62 ° c . ; the temperature was kept at about 62 ° c . for 18 hours while stirring . the temperature was increased to 80 ° c . and kept at 80 ° c . for an additional 12 hours while stirring at 250 rpm . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then dispersed in 300 ml of an aqueous 4 n sodium hydroxide solution , containing 50 ml of methanol , and shaken in a parr shaker at room temperature for 24 hours . the beads were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone . the beads were dried in air at room temperature and sieved . the 90 - 200 μm fraction was used as catalyst support . the suspension medium , 1 . 0 l water containing 80 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask which was at 50 ° c . while stirring . the dispersed medium consisted of 58 g of styrene , 22 g dvb , 80 g of 2 - butanol , and 1 . 6 g of aibn . the mixture was then stirred at 350 rpm as the temperature was increased to about 60 ° c . ; the temperature was kept at about 60 ° c . for 24 hours while stirring . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone . the beads were dried in air at room temperature and sieved . the 120 - 400 μm fraction was used as catalyst support . the suspension medium , 1 . 0 l water containing 100 g of acacia , was placed into a 2 l round bottom flask equipped with a stirrer and a reflux condenser . the round bottom flask was placed into a thermostated vessel . a dispersed medium , which contained the monomers , was added to the 2 l flask which was at 50 ° c . while stirring . the dispersed medium consisted of 39 g of styrene , 11 g dvb , 40 g of toluene , 1 . 6 g of hydrophobic silica particles , 1 ml of chloroform , and 0 . 7 g of aibn . the mixture was then stirred at 400 rpm as the temperature was increased to about 60 ° c . ; the temperature was kept at about 60 ° c . for 24 hours while stirring . the mixture was cooled and the polymer beads , which had been formed , were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then dispersed in 300 ml of an aqueous 4 n sodium hydroxide solution , containing 50 ml methanol , and shaken in a parr shaker at room temperature for 24 hours . the beads were filtered from the suspension by vacuum filtration and were washed several times with water . the beads were then soaked in methanol for several hours followed by several washings in water and then acetone followed by drying in air . the beads were dried in air at room temperature and sieved . the 80 - 400 μm fraction was used as catalyst support . the support i prepared in example 1 was dried under a high vacuum at room temperature for 4 hours , 80 ° c . for 5 hours and further at room temperature overnight , with intermittent purging with nitrogen gas . in a flask were placed 5 . 55 g of a mao solution ( 4 . 47 weight % al in toluene ) and 15 ml of toluene . while the solution was stirred at room temperature , 1 . 5 g of support i was added slowly . the mixture was stirred for 16 hours at room temperature . to this mixture , 0 . 034 g of tri - tert - butyl phosphiniminate indenyl titanium dissolved in 4 ml of toluene was added . the mixture was stirred for 2 hours at room temperature and further for 2 hours at 45 ° c . the solvent was then removed by applying a high vacuum , to provide a free - flowing powder . same as example 8 except that the support ii obtained in example 2 was used . same as example 8 except that the support iii obtained in example 3 was used . same as example 8 except that the support iv obtained in example 4 was used . same as example 8 except that the support v obtained in example 5 was used . same as example 8 except that the support vi obtained in example 6 was used . same as example 8 except that the support vii obtained in example 7 was used . same as example 8 , except that a commercial styrene - divinylbenzene copolymer ( chromosorb 101 purchased from chromatographic specialties inc .) was used . same as example 8 , except that an xpo - 2408 silica manufactured by w . r . grace davison that was dehydrated by heating at 200 ° c . under air for 2 hours and further at 600 ° c . under nitrogen for 6 hours was used . the support i obtained in example 1 was dried under a high vacuum for 4 hours at room temperature , 80 ° c . for 5 hours and further at room temperature overnight , with intermittent purging with nitrogen gas . in a flask , 58 mg of bis ( n - butyl cyclopentadienyl ) zirconium was dissolved in 25 ml of toluene . to this solution was added 1 . 27 g of a mao solution ( 13 . 75 weight % al in toluene ). the mixture was stirred at room temperature for 30 minutes . the solution was then added to 1 . 38 g of the support i in example 1 . the mixture was stirred at 45 ° c . for 90 minutes . the solvent was removed by applying a high vacuum to provide a free - flowing powder . same as example 17 except that the support vii obtained in example 7 was used . in a 2 liter autoclave reactor , 160 g of nacl was added for use as seedbed . the reactor was heated to 100 ° c . and thoroughly purged with ethylene gas . approximately 0 . 40 ml of tri - isobutyl aluminum in n - hexane solution ( 0 . 40 mmol ) and 3 ml of 1 - hexene were injected into the reactor . after the reactor was cooled down to 90 ° c . and pressurized with 100 psig of ethylene , 10 ˜ 30 mg of a supported catalyst a ˜ e or j was added and the reactor was pressurized with 200 psig of ethylene . the polymerization was proceeded for 60 minutes with temperature maintained at 90 ° c . and pressure at 200 psig by feeding ethylene continuously into the reactor . the reaction was terminated by rapidly venting the reaction gases and cooling the reactor to room temperature . the polymer was recovered and the catalyst activity ( gram of polymer / gram of catalyst ) was determined ( table 2 ). same as examples 19 , but the supported catalyst f prepared in example 13 was used . same as examples 19 , but the supported catalyst g prepared in example 14 was used . same as examples 19 , but the supported catalyst h prepared in example 15 was used . same as examples 19 , but the supported catalyst i prepared in example 16 was used . same as examples 19 , but the supported catalyst k prepared in example 18 was used . the results show the following . using the supports of the present invention , it is possible to prepare a supported single - site type catalyst having a much higher activity than that of the same catalyst supported on polymer particles containing no functional groups . with levels of cross - linking agent of about 20 to 25 % and hema levels from 15 to 60 weight %, the supported catalyst prepared according to the invention show good activities that are comparable or better than that of the same catalyst supported on silica .