Abstract: A discrete catalyst and processes for the alkylation of isoalkanes with alkenes under homogenous fluid conditions. The catalyst is formed by contacting, under fluid conditions, a homogenous fluid containing a paraffin hydrocarbon having from 4 to 12 carbon atoms with a Lewis acid/protic Bronsted acid pair to produce a discrete catalytic complex that is soluble in the fluid. The discrete catalyst is the reaction product of the acid pair and alkanes and includes hydrocarbon ligands of limited chain length rendering it soluble in the fluid. The catalyst is active for the alkylation of isoalkanes, under homogenous fluid conditions.

Abstract: The present invention is directed to novel catalyst compositions, their preparation, and their use in a selective paraffin isomerization process. The solid acid catalyst compositions comprise a zirconium hydroxide support, a Group VIII metal, and a heteropolyacid selected from the group consisting of the exchanged aluminum salt of 12-tungstophosphoric acid, the exchanged salt of 12-tungstosilicic acid, and mixtures thereof. The use of said catalysts in an isomerization process comprises contacting said catalysts with a feed comprising C.sub.n or C.sub.n + paraffins, wherein n=4.

Abstract: .alpha.-alkyl aldehydes having 8 to 17 carbon atoms are obtained from terminal olefins containing one less carbon atom. The olefins are first isomerized in the presence of iron carbonyl and then, without separating out the iron compound, hydroformylated in the presence of rhodium as catalyst.

Abstract: A process of effecting an acid catalyzed reaction wherein a reactant capable of undergoing an acid catalyzed reaction is contacted with an acid functionalized organically-bridged polysilsesquioxane catalyst where all of the acid functionality is covalently bonded to the organic portion of an organically-bridged polysilsesquioxane framework has been developed. The acid functionalized organically-bridged polysilsesquioxane is formed by polymerizing a monomer through sol-gel processing to form an organically-bridged polysilsesquioxane, reacting an acid group onto the organic portion of the organically-bridged polysilsesquioxane, and recovering the acid functionalized product. An embodiment of the invention is where the acid catalyzed reaction is the hydration of olefins, alkylation, acylation, isomerization, or aldol condensation/elimination.

Abstract: A catalyst is provided based on chlorinated eta alumina incorporating platinum and germanium and tin, as well as chlorine. This catalyst can be used in a process for the isomerization of a charge rich in normal C.sub.4 -C.sub.6 -paraffins, without hydrogen recycling.

Abstract: This invention relates to hydrocarbon conversion processes using novel molecular sieve compositions as the catalyst. These molecular sieves contain chromium in the framework structure along with aluminum and silicon. The process of preparing the chromium-containing molecular sieves involves contacting a starting molecular sieve with a solution or slurry of a fluoro salt of chromium under effective process conditions to provide for aluminum extraction and substitution of chromium.

Abstract: Supported non-oxide metal carbide-containing catalysts are provided which comprise: (a) an oxide support, such as alumina or cordierite; (b) a passivating layer of a ceramic, such as silicon carbide; and (c) a non-oxide metal ceramic catalytic component, such as a Group VI metal carbide or nitride, preferably tungsten carbide or molybdenum carbide.

Abstract: Materials which have been prepared by a method which includes the steps of (1) impregnating alumina with a sulfate of at least one metal selected from the group consisting of copper, iron, cobalt, nickel, manganese, zinc and magnesium, (2) calcining the thus-obtained impregnated alumina materials, and (3) heating the calcined materials with AlCl.sub.3 and at least one chlorinated hydrocarbon (preferably CCl.sub.4) at a temperature of about 40.degree.-90.degree. C. are employed as catalysts in the isomerization of C.sub.5 -C.sub.10 cycloalkanes (preferably methylcyclopentane). A select group of the thus-prepared materials are employed as catalysts in the isomerization of C.sub.4 -C.sub.10 alkanes (preferably n-pentane and 2-methylbutane). Preferably, the catalyst preparation method also includes a step of treating the calcined impregnated alumina materials with gaseous hydrogen chloride before they are heated with AlCl.sub.3 and the chlorinated hydrocarbon(s).

Abstract: A catalyst useful for hydroisomerizing wax containing feeds comprises a Group VIII metal on an alumina or silica-alumina support having less than about 35 wt % silica and is surface treated with at least about 0.5 wt % silica or a silica precursor.

Abstract: A process for producing high quality lubricants by the hydrocracking and hydroisomerization of petroleum waxes uses a catalyst which is based on an ultra-large pore crystalline material. The crystalline material exhibits unusually large pores of at least 13 .ANG. diameter and a high sorption capacity demonstrated by its benzene adsorption capacity of greater than about 15 grams benzene/100 grams at 50 torr and 25.degree. C. The crystalline material is characterized by an X-ray diffraction pattern with at least one d-spacing greater than about 18 .ANG. and in a particularly preferred form, a hexagonal arrangement of pores of at least 13 .ANG. diameter which can be indexed with a d.sub.100 value greater than about 18 .ANG.. The hydrocracking catalysts based on these materials are capable of producing lube products with a high VI of at least 120 and usually higher, values of 135 and higher e.g. 143.

Abstract: Isomerization catalyst compositions are prepared by heating aluminum chloride, at least one of several metal salts (preferably CuSO.sub.4), at least one of several inorganic support materials (alumina, silica, aluminum phosphate and combinations thereof) and at least one chlorinated hydrocarbon (preferably CCl.sub.4) at a temperature of about 40.degree.-90.degree. C. The dried catalyst compositions are used for the isomerization of C.sub.5 -C.sub.10 cycloalkanes and/or C.sub.4 -C.sub.10 alkanes.

Abstract: In one embodiment, C.sub.4 -C.sub.10 alkanes and/or C.sub.5 -C.sub.10 cycloalkanes are isomerized in the presence of a catalyst which has been prepared by heating AlCl.sub.3, at least one aluminum sulfate-containing support material and at least one chlorinated hydrocarbon (preferably CCl.sub.4) at about 40.degree.-90.degree. C., followed by separating the formed solid from the chlorinated hydrocarbon.In another embodiment, C.sub.5 -C.sub.10 cycloalkane(s) are isomerized in the presence of a catalyst which has been prepared by heating AlCl.sub.3, at least one sulfur-containing acid (H.sub.2 SO.sub.4 and/or ClSO.sub.3 H and/or FSO.sub.3 H and/or CF.sub.3 SO.sub.3 H) and at least one chlorinated hydrocarbon (preferably CCl.sub.4) at about 40.degree.-90.degree. C., followed by separating the formed solid from the chlorinated hydrocarbon.

Abstract: An isomerization zone process is disclosed that combines a deisohexanizer with a PSA separation section to provide a product stream comprising methylbutane and dimethylbutane. The process combines a methylpentane and normal hexane recycle stream, a normal pentane recycle stream and a fresh feedstream to provide a combined feedstream that is charged to an isomerization zone. The effluent from the isomerization zone is stabilized and passed to a deisohexanizer. A sidecut stream carries the methylpentane and normal hexane recycle stream from the deisohexanizer. Hydrocarbons having a higher boiling point than the sidecut stream are withdrawn as a bottoms stream from the deisohexanizer. An overhead carries normal pentane, methylbutane and dimethylbutanes to the PSA separation section. An extract stream is recovered as the normal pentane recycle stream. The raffinate from the PSA provides a high octane isomerate stream comprising mainly methylpentane and dimethylbutanes.

Abstract: Alkylaromatic hydrocarbons are produced in a process which comprises concentrating a feed aromatic hydrocarbon into a sidecut stream removed from a fractionation column. A feed acyclic olefin is then admixed with the aromatic hydrocarbon and passed through an alkylation reaction zone operated at optimum alkylation conditions. The reaction zone effluent is returned to the fractionation column to recover the product and to recycle untreated feed aromatics. This technique can be applied to hydrocarbon conversion processes in general to obtain benefits of catalytic distillation while operating the reaction zone at conditions not suitable for catalytic distillation. Hydrogen and other light gases are preferably separated from the reaction zone effluent by cooling and vapor-liquid separation external to the column.

Abstract: This invention relates to molecular sieve compositions and processes for using the molecular sieves. The molecular sieves have a three-dimensional microporous crystalline framework structure of tetrahedral oxide units of AlO.sub.2, SiO.sub.2, TiO.sub.2 and/or FeO.sub.2. These molecular sieves can be prepared by contacting a starting zeolite with a solution or slurry of a fluoro salt of titanium and/or iron under effective process conditions to extract aluminum from the zeolite framework and substitute titanium and/or iron. The molecular sieves can be used as catalysts in hydrocarbon conversion processes and other processes.

Abstract: A process for isomerizing a paraffin feed comprising contacting the feed with a strong, solid acid catalyst comprising a sulfated Group IVB metal oxide and at least one Group VIII metal in the presence of hydrogen and an adamantane compound.

Abstract: An isomerization zone process is disclosed that combines a deisohexanizer with a PSA separation section to provide a product stream comprising methylbutane and dimethylbutane. The process combines a methylpentane and normal hexane recycle stream, a normal pentane recycle stream and a fresh feedstream to provide a combined feedstream that is charged to an isomerization zone. The effluent from the isomerization zone is stabilized and passed to a deisohexanizer. A sidecut stream carries the methylpentane and normal hexane recycle stream from the deisohexanizer. Hydrocarbons having a higher boiling point than the sidecut stream are withdrawn as a bottoms stream from the deisohexanizer. An overhead carries normal pentane, methylbutane and dimethylbutanes to the PSA separation section. An extract stream is recovered as the normal pentane recycle stream. The raffinate from the PSA provides a high octane isomerate stream comprising mainly methylpentane and dimethylbutanes.

Abstract: This invention deals with a hydrocarbon conversion process using a crystalline oxysulfide composition. The crystalline oxysulfide composition has a three-dimensional microporous framework structure of at least MO.sub.2, MS.sub.2, and MOS tetrahedral units, having an intracrystalline pore system and an empirical formula expressed in molar ratios:(M.sub.s Al.sub.t P.sub.u Si.sub.v)S.sub.w O.sub.2-wwhere M is at least one metal selected from the group consisting of metals which: 1) can be incorporated into the framework structure of a microporous molecular sieve and 2) form hydrolytically stable sulfides; s, t, u, v and w are the mole fractions of M, Al, P, Si and S respectively. The values of s, t, u and v are chosen such that when t is greater than zero u is greater than zero, s+t+u+v=1 and when s=1, M is only a combination of gallium and germanium.

Abstract: This invention deals with a crystalline oxysulfide composition, a process for preparing the composition, a catalyst using the composition and processes using the composition. The crystalline oxysulfide composition has a three-dimensional microporous framework structure of at least MO.sub.2, MS.sub.2, and MOS tetrahedral units, having an intracrystalline pore system and an empirical formula expressed in molar ratios:(M.sub.s Al.sub.t P.sub.u Si.sub.v)S.sub.w O.sub.2-wwhere M is at least one metal selected from the group consisting of metals which: 1) can be incorporated into the framework structure of a microporous molecular sieve and 2) form hydrolytically stable sulfides; s, t, u, v and w are the mole fractions of M, Al, P, Si and S respectively. The oxysulfide composition is prepared by contacting a molecular sieve having an empirical formula: (M.sub.s Al.sub.t P.sub.u Si.sub.v)O.sub.

Abstract: A solid strong acid catalyst useful for hydrocarbon reactions, especially for the skeletal isomerization of paraffinic hydrocarbons is provided by supporting sulfate (SO.sub.4) and at least one member selected from Group VIII metals on a support consisting of hydroxides and oxides of Group IV metals and Group III metals and mixtures thereof and then calcining and stabilizing the catalyst.

Abstract: Compositions containing sulfuric acid and one or more of certain chalcogen-containing compounds in which the chalcogen compound/H.sub.2 SO.sub.4 molar ratio is below 2 contain the mono-adduct of sulfuric acid which is catalytically active for promoting organic chemical reactions. Suitable chalcogen-containing compounds have the empirical formula ##STR1## wherein X is a chalcogen, each of R.sub.1 and R.sub.2 is independently selected from hydrogen, NR.sub.3 R.sub.4, and NR.sub.5, at least one of R.sub.1 and R.sub.2 is other than hydrogen, each of R.sub.3 and R.sub.4 is hydrogen or a monovalent organic radical, and R.sub.5 is a divalent organic radical. Such compositions are useful for catalyzing organic reactions such as oxidation, oxidative addition, reduction, reductive addition, esterification, transesterification, hydrogenation, isomerication (including racemization of optical isomers), alkylation, polymerization, demetallization of organometallics, nitration, Friedel-Crafts reactions, and hydrolysis.

Abstract: Process for the isomerization of a hydrocarbon feed containing hydrocarbons comprising at least 4 carbon atoms, which process comprises isomerizing a hydrocarbon stream; separating the isomerisate thus obtained into a hydrogen-containing gas and a hydrocarbon effluent; separating from the hydrocarbon effluent a product stream containing branched hydrocarbons, leaving non-product hydrocarbons, and passing at least part of these hydrocarbons again to the isomerization step, in which process at least part of the feed is added to at least part of the isomerisate before the isomerisate is separated into the hydrogen-containing gas and the hydrocarbon effluent.

Abstract: Upon a pressure vessel reactor, lower alkanes such as methane and propane subjected to temperatures of up to 800 K and pressures up to 70,000 psi (467 MPa), isomerize even in the absence of catalyst to produce a variety of alkanes, alkenes, cycloalkanes and aromatic hydrocarbons containing up to twelve carbon atoms.

Abstract: An integrated process for the production of a refinery gasoline pool with enhanced octane value from a pentane and hexane containing feedstock by first contacting with an isomerization catalyst; fractionating the resulting product into an iC.sub.5 product stream forming part of said refinery gasoline pool and a bottom stream containing nC.sub.5, nC.sub.6, mono-branched C.sub.6 and dibranched C.sub.6 ; passing said bottom stream through an adsorption bed with dibranched C.sub.6 passing thru unabsorbed; desorbing nC.sub.5, nC.sub.6 and monobranched C.sub.6 from the absorption bed; and recycling the desorbed nC.sub.5, nC.sub.6 and monobranched C.sub.6 to the isomerization zone.

Abstract: A improved process is provided for upgrading light olefins from hydrocarbon cracking, such as light crackate gas containing ethene, propene and other C.sub.1 -C.sub.4 lower aliphatics. The process comprises the steps of: maintaining an oligomerization reactor containing a fluidized bed of zeolite catalyst particles in a low severity reactor bed at oligomerization temperature conditions by passing hot olefinic gas upwardly through the fluidized catalyst bed under throughput rate conditions sufficient to convert at least 50 wt % of lower olefins to hydrocarbons in the C.sub.5 -C.sub.10 range; maintaining turbulent fluidized bed conditions through the fluidized bed by passing fresh ethene-rich feedstream gas upwardly through the fluidized catalyst bed and adding thereto sufficient recycled light byproduct gas to maintain a minimum gas velocity; cooling reaction effluent from the conversion zone to provide light gas byproduct and liquid hydrocarbon reaction product rich in C.sub.5 -C.sub.

Abstract: The benzene content in a gasoline pool is reduced by a process that hydrogenates a benzene-containing isomerization zone feedstream. In addition to reducing the benzene concentration, the hydrogenation zone is also used to heat the isomerization zone feed and thereby eliminate the need for an isomerization zone heater. The process employs mild saturation conditions which eliminates hydrocracking and prevents the loss of isoparaffin yield. Additional cyclic hydrocarbons produced by the saturation of benzene can be processed in the isomerization zone for ring opening to increase the available paraffinic feedstock or the isomerization zone can be operated to pass the cyclic hydrocarbons through to a product recovery section.

Abstract: Waxy distillates, or raffinates containing from as little as 10% wax but more typically about 30% wax or more are upgraded by a process comprising the steps of hydrotreating the waxy oil under conditions which convert less than 20% of the feed into products boiling lower than the feed to reduce the sulfur and nitrogen content of the oil followed by hydroisomerizing the hydrotreated waxy oil to reduce the wax content and increase the viscosity index. This oil having a waxy content of less than 30%, preferably less than 25%, can now be more easily dewaxed using conventional solvent dewaxing procedures. The advantage of the present process resides in the increased yield and/or stability of oil as compared to other upgrading, dewaxing processes which convert wax to light products. The isomerization catalyst is preferably a low fluorine content catalyst, more preferably a noble metal on 0.1 to less than 2 wt % fluorine on alumina catalyst, most preferably a noble Group VIII metal (e.g.

Abstract: This invention relates to a process for increasing the octane of a refinery gasoline pool by segregating components of a feed stream to increase the value of select components by isomerization and to prevent isomerization of other components already having a high octane value. The preferred feed stream of this process comprises di-branched paraffins, mono-methyl-branched paraffins and normal paraffins. Two or more different separatory sieves are used prior to isomerization. A first separatory shape-selective molecular sieve has a pore size of 4.5.times.4.5A or smaller to adsorb normal paraffins. A second separatory shape-selective molecular sieve has a pore size of 5.5.times.5.5 to 4.5.times.4.5A but excluding 4.5.times.4.5A. These sieves may be situated in a series flow arrangement. Normal paraffins are adsorbed by the first sieve. Mono-methyl-branched paraffins are adsorbed by the second sieve.

Abstract: A combined reforming and isomerization process wherein at least a portion of the hydrogen produced in the reforming process is passed with a C.sub.5 -C.sub.6 range normal paraffin feedstock to an isomerization zone, containing an isomerization catalyst, at isomerization condition to produce an isomerized C.sub.5 -C.sub.6 product stream and passing the C.sub.5 -C.sub.6 isomerized product stream to a reformate separation zone (hydrogen stripping and topping zones) and recovering at least a major portion of the isomerized C.sub.5 -C.sub.5 product stream with the reformate for use as a high octane gasoline product.

Abstract: The invention concerns a combined process of catalytically hydroreforming a heavy naphtha in at least one reaction zone (10) and catalytically hydroisomerizing a light naptha in at least one reaction zone (34).The invention is characterized in that the hydrogen produced in the hydroreforming unit (line 27) is used to isomerize the light naphtha, the obtained reformate and isomerate being fractionated preferably together in the same stabilization column (51 in FIG. 1).A better thermal integration, a better recovery of light hydrocarbons and a lowering of the utilities requirements and investments, as compared with units operating separately, are thus achieved.

Abstract: The improved, heterogeneous catalysts are in the form of gas-impervious, hollow, thin-walled spheres (10) suitably formed of a shell (12) of metal such as aluminum having a cavity (14) containing a gas at a pressure greater than atmospheric pressure. The wall material may be, itself, catalytic or the catalyst can be coated onto the sphere as a layer (16), suitably platinum or iron, which may be further coated with a layer (18) of activator or promoter. The density of the spheres (30) can be uniformly controlled to a preselected value within .+-.10 percent of the density of the fluid reactant such that the spheres either remain suspended or slowly fall or rise through the liquid reactant.

Abstract: This invention relates to a process for the production of an isomerate gasoline blending component where the octane value of the isomerate is increased relative to prior art processes utilizing single separatory sieves. After respective isomerization of feed streams comprising C.sub.6 or C.sub.6.sup.+ normal paraffins, a multiple separatory sieve is located to selectively adsorb unreacted normal paraffins and mono-methyl-branched paraffins from an isomerate product stream. The preferred first separatory sieve is exemplified by a calcium 5A sieve which can adsorb normal paraffins while allowing mono-methyl-branched paraffins and more higly branched paraffin to pass to a second separatory sieve. The second sieve comprises a shape-selective zeolite having a pore size intermediate 5.5.times.5.5 and 4.5.times.4.

Abstract: Catalytically-active metallic glasses containing at least one element from a subgroup of the periodic system and at least one element from a main group of the periodic system. Process for the production of catalytically-active metallic glasses where the metallic glass is produced from at least one element from a subgroup of the periodic system and at least from one element from a main group of the periodic system. The metallic glasses are activated by self-activation or by an oxidative and/or reductive treatment. The catalytically-active metallic glasses can be used as hydrogenation oxidation or isomerization catalysts.

Abstract: Control of an isomerization process is based on a known relationship between the octane number and temperature of a reaction at equilibrium; and a predetermined relationship between octane number and temperature of the reaction product of a reactor using a specific catalyst. In use, measurements of actual octane number and temperature are compared with the octane number and temperature of a reaction at equilibrium to determine if the reaction is at equilibrium. If the reaction is not at equilibrium, a control signal is developed to restore equilibrium. Thus control of an isomerization process is accomplished so as to substantially maximize the efficiency of the isomerization process both from a production standpoint and from an energy usage standpoint by maintaining the isomerization reaction at desired equilibrium conditions. Also, for a dual reactor system, the differential temperature between the two reactors is manipulated so as to maintain more favorable isomerization conditions in the tail reactor.

Abstract: Process for the hydroisomerization of petroleum waxes by contacting said waxes with hydrogen at hydroisomerization conditions using a catalyst comprising at least one hydrogenating metal or compound thereof present on at least one refractory oxide which has been treated with from 0.1 to 30% w, calculated on refractory oxide, of at least one reactive metal compound of Group 2a, 3a, 4a and/or 4b of the Periodic Table of the Elements.

Abstract: Natural gasoline of low octane value derived from natural gas is upgraded to higher octane value by means of catalyst consisting essentially of trifluoromethanesulfonic acid at temperatures between about 80.degree. C. and about 120.degree. C., and preferably between about 100.degree. C. and about 120.degree. C.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a catalyst composite comprising from about 5 weight percent to about 95 weight percent of a silica polymorph consisting of crystalline silica, said silica polymorph after calcination in air at 600.degree. C. for one hour, having a mean refractive index of 1.39.+-.0.01 and a specific gravity at 25.degree. C. of 1.70.+-.0.05 g/cc and at least 5 weight percent to about 95 weight percent Ziegler alumina.

Abstract: A new porous zeolite, a method of making same and the use thereof in catalytic conversion of organic compounds. The new product has a composition, expressed in terms of moles of anhydrous oxides per 100 moles of silica as follows:(0-2.5)M.sub.2/n O:(0- 2.5)Al.sub.2 O.sub.3 :(100)SiO.sub.2wherein M is at least one cation having a valence n and wherein the zeolite is characterized by the distinctive X-ray powder diffraction pattern as shown in Table 1 herein. The new zeolite is prepared from a reaction mixture comprising a source of silica, a source of organic compounds of Group VB, alkali metal cations, water and with or without a source of alumina.

Abstract: A process for the isomerization of acyclic hydrocarbons and alkylaromatic hydrocarbons is disclosed. The mixed-phase feed stream is heated and the liquid-phase portion of the feed stream is simultaneously vaporized by indirect heat exchange against the effluent of the reaction zone. Prior to this exchange, the effluent of the isomerization zone is heated in a fired heater to a temperature above that employed in the reaction zone. The inventive concept eliminates the need to pass mixed-phase feed streams through fired multi-pass heaters.

Abstract: A process is described for producing methyl tert.-butyl ether from butane-containing light hydrocarbon mixtures. The n-butane is isomerized to isobutane which is dehydrogenated to an isobutene/isobutane molar ratio of 0.4 to 2:1, the isobutene in the mixture is etherified with methanol to form methyl tert.-butyl ether and the residual isobutane is recycled for dehydrogenation. After the isomerization step, the n-butane and isobutane can be separated and the n-butane recycled. The product containing methyl tert.-butyl ether can be used as a gasoline additive.

Abstract: A hydrocarbon conversion process for the production of motor fuel blending stocks from propane and butane is disclosed. Preferably a charge stream comprising a mixture of C.sub.3 -C.sub.4 saturated hydrocarbons is split into a C.sub.3 stream passed into a dehydrogenation zone and a C.sub.4 stream passed into an isostripper column. Normal butanes are removed from the isostripper and passed into an isomerization zone, with product isobutane being concentrated by fractionation in the isostripper. Isobutane and propylene from the dehydrogenation zone are then reacted in an alkylation zone which produces C.sub.5 -plus product hydrocarbons. The effluent of the alkylation zone enters the isostripper. The product stream and a propane-containing stream are withdrawn from the isostripper, with the propane-containing stream being passed into a second separation zone. Alternative butane fractionation systems are disclosed.

Abstract: Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with an acidic multimetallic catalytic composite comprising a combination of catalytically effective amounts of a platinum group component, a nickel component, a zinc component, and a halogen component with a porous carrier material. The platinum group, zinc, nickel, and halogen components are present in the multimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal, about 0.01 to about 5 wt. % zinc, about 0.05 to about 5 wt. % nickel, and about 0.1 to about 3.5 wt. % halogen.

Abstract: A composition comprising an ion exchange resin, a metal selected from the transition group of elements bound to said resin and an organic linking compound which has at least one moiety which is ionically bonded to said resin and which further has at least one moiety which is coordinately bonded to said metal.