CATALYZED VAPOR-PHASE HIDROCYANATION OF DIOLEFINIC COMPOUNDS

Abstract: A catalyzed vapor-phase process for the hydrocyanation of acyclic diolefinic compounds to olefinic nitriles in which the olefinic double bond is not conjugated to the triple bond of the cyano group, wherein a supported catalyst composition comprising at least one multidentate phosphite ligand and zero-valent nickel is preferably used with specially selected or treated supports.

Description: TITLE CATALYZED VAPOR-PHASE HYDROCYANATION OF DIOLEFINIC COMPOUNDS FIELD OF THE INVENTION This invention generally relates to a vapor-phase process for the hydrocyanation of diolefinic compounds to produce nonconjugated acyclic nitriles utilizing zero-valent nickel and a multidentate phosphite ligand as catalysts, and, more particularly, to the utilization of specialized supports for said catalysts. BACKGROUND OF THE INVENTION Catalytic hydrocyanation systems, particularly pertaining to the hydrocyanation of olefins, are known in the art. For example, liquid-phase systems useful for the hydrocyanation of butadiene to form pentenenitriles (PN) are known in the art, e.g., U.S. Patent 3,766,237. As used in that patent, and as will be used herein, the term "pentenenitrile" is intended to mean a cyanobutene. Likewise, "butenenitrile" is intended to mean a cyanopropene. The pentenenitriles so formed are further subjected to hydrocyanation and, in some cases isomerization, to form adiponitrile (ADN), a commercially important material in the manufacture of nylon. Multidentate phosphite ligands complexed to zero-valent nickel and platinum are known to be useful in the liquid-phase hydrocyanation of butadiene, as described by Baker et al., J. Chem. Soc.. Chem. Commun., 1991, pages 803-804. The overwhelming majority of prior art processes for the hydrocyanation of butadiene are conducted in the liquid phase, with all attendant waste disposal problems. Most of the previous approaches toward carrying out vapor-phase hydrocyanation of olefinic compounds have usually started with monoolefinic, not diolefinic, compounds and have given rise primarily to saturated products, which could not be further hydrocyanated. U.S. Patent 5,449,807 describes a catalyzed vapor-phase process for the hydrocyanation of diolefinic compounds comprising, reacting an acylic aliphatic diolefinic compound, preferably butadiene, with HCN in the vapor phase within a temperature range of from about 135°C to about 170°C in the presence of a supported catalyst composition comprising zero-valent nickel and at least one selected bidentate phosphite. Typically, in accordance with U.S. Patent 5,449,807, the zero-valent nickel catalysts are dispersed on silica, alumina or carbon supports in a conventional manner. While the vapor-phase hydrocyanation process described in U.S. Patent 5,449,807 offers many advantages over liquid-phase process for optimum commercial use, the life of the catalyst needs to be prolonged. Therefore, what is needed is a process which provides for longer catalyst life in the vapor-phase hydrocyanation by the selection of catalysts, catalyst supports and catalyst support pre-treatments. Other objects and advantages of the invention will become apparent to those skilled in the art upon reference to the detailed description which hereinafter follows. SUMMARY OF THE INVENTION The present invention provides a process for the vapor-phase hydro¬ cyanation of diolefinic compounds comprising, reacting an acyclic aliphatic diolefinic compound, preferably butadiene, with HCN in the vapor phase within a temperature range of from about 135°C to about 300°C in the presence of a supported catalyst composition comprising zero-valent nickel and at least one multidentate phosphite ligand selected from the group consisting of compounds represented by Formulas I and II: Formula I wherein each R 1 , R 2 , R 3 , R 4 , R 5 , and R 6 are independently, H, a branched or straight chain alkyl of up to 12 carbon atoms, or OR 7 , wherein R 7 is a C j to C 12 alkyl; Formula II wherein each R 8 is, independently, H, a primary, secondary or tertiary hydrocarbyl of 1 to 12 carbon atoms, or B, where B is a substituent of the formula wherein x is an integer from 1 to 12; and each R 9 and R 10 are independently, H, OR 1 1 wherein R 1 ' is a C] to Cj 2 alkyl or a primary, secondary or tertiary hydrocarbyl of 3 to 12 carbon atoms and wherein R 10 can be ortho, meta or para to the oxygen; and wherein x is an integer from 1 to 12; and wherein when said multidentate phosphite ligand is selected from the group consisting of compounds represented by Formulas I and II, the catalyst support is selected from carbon, heated to a temperature of at least 600°C in an inert atmosphere for at least 2 hours, or an organic polymer, to produce acyclic, preferably 3- and 4-pentenenitriles, in which the olefinic double bond is not conjugated with the cyano group. The process may be carried out continuously or batchwise. In the above definitions for Formula I and Formula II, the terms "secondary" and "tertiary" refer to the carbon atom attached to the aromatic ring. In addition, for purposes of the present disclosure and claims, the terms "alkenenitrile", "pentenenitrile", and "butenenitrile" are intended to mean, respectively, a cyanoalkene in which the carbon atom of the cyano group is the first carbon; a cyanobutene; and a cyanopropene. When 1,3-butadiene (BD) is utilized as the starting material, the inventive vapor-phase hydrocyanation process produces a mixture of pentenenitriles (PN) consisting essentially of 3 -pentenenitrile (3PN), 4-pentenenitrile (4PN) and 2 -methyl -3 -butenenitrile (2M3BN). Small amounts of dinitriles (DN) and of a dimer of 1,3-butadiene, 2-vinylcyclohexene (VCH) are also sometimes produced. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Catalysts useful in the practice of the present invention consist essentially of the multidentate phosphite complexes detailed above. When the catalysts are selected from those of Formula I and Formula II, they can be supported on conventional carriers of silica, alumina, carbon, or other suitable supports, as well as the specialized supports discussed hereinbelow. Commonly used techniques for treatment of supports with metal catalysts can be found in B. C. Gates, Heterogeneous Catalysis. Vol. 2, pp. 1-29, Ed. B. L. Shapiro, Texas A & M University Press, College Station, Texas, 1984. Alternately, a given support can be prepared with a uniformly dispersed coating of zero-valent nickel metal and then can be treated with a multidentate phosphite ligand. Typically, in accordance with this invention, the zero-valent nickel catalysts are dispersed on the chosen support at concentrations sufficient to produce a supported catalyst composition containing 0.3% wt. to 1.0% wt. Ni. For prolonged catalyst life, when the catalysts are selected from those of Formula I and Formula II, they should be supported on catalyst supports selected from heat-treated carbon or organic polymeric supports. The carbon utilized can be any form of commercially available paniculate carbon, but the carbon must be heated in an inert atmosphere to at least 600°C, and preferably to at least 800°C, for at least 2 hours, and preferably at least 4 hours, prior to contact with the catalyst and subsequent use. After the carbon has been heat-treated and cooled, the catalyst can be applied thereto by dispersion of the catalyst in an organic liquid, such as toluene or tetrahydroturan, and contact of this dispersion with the heat-treated carbon support. The organic polymeric supports of choice are those with thermal stabilities greater than 200°C, for example, polydivinylbenzene/polyacrylonitrile and cross-linked polystyrene and copolymers or blends thereof. In the case of organic polymeric supports, the catalyst of choice can be dispersed therewith in the same manner as utilized for heat-treated carbon supports. The catalysts are then loaded into tubular reactors, and a gaseous diolefinic compound, e.g., butadiene, and HCN is passed continuously over the solid catalysts at temperatures sufficiently high to maintain the starting materials as well as the reaction products in the vapor phase. The temperature range is generally from about 135°C to about 300°C and preferably from about 145°C to 200°C. The temperature must be high enough to maintain all the reactants and products in the vapor phase but low enough to prevent deterioration of the catalyst. The particular preferred temperature depends to some extent on the catalyst being used, the diolefinic compound being used, and the desired reaction rate. The operating pressure is not particularly critical and can conveniently be from about 1-10 atmospheres (101.3 to 1013 kPa). No practical benefit is obtained when operating above the upper limit of this pressure range. HCN and/or diolefinic compound starting materials can be delivered as a neat vapor or as a preheated solution in a solvent, such as acetonitrile or toluene. Under atmospheric pressure, using nitrogen or another inert gas as a carrier, temperatures of from about 140-160°C are typically used. Nitrogen is preferred because of its low cost. Gaseous oxygen, water vapor, or other gaseous substance which could react with the HCN, the zero-valent nickel catalyst, or the starting diolefinic compound should be avoided. The reaction products are liquid at room temperature and are conveniently recovered by cooling. Branched 2-methyl-3- butenenitrile can be separated from linear 3 -pentenenitrile and 4-pentenenitrile by distillation. Zero-valent nickel is known to the art and can be made in a number of ways. Most common zero-valent nickel species, which can be used to form the catalytic compositions useful in the present invention, are derived from Ni(0) complexes containing o-tritolylphosphite, p-tritolylphosphite, cyclooctadiene, and ethylene. Ni(0) can also be prepared by reduction of Ni(II) compounds with molecular hydrogen, or other reducing agents, in the presence of appropriate ligands (e.g., where Ni(NO 3 ) 2 is reduced by H 2 to provide Ni(0) on silica gel). Moreover, Ni(0) complexes containing multidentate ligands can be prepared from reduction of Ni(II) compounds (e.g., where Ni(ligand "A")(ethylene) is prepared) and Ni metal and a multidentate ligand. Other zero-valent nickel species known to those skilled in the art can be successfully used as well. The actual catalyst is a complex of zero-valent nickel with the multidentate ligand, which is formed when those two materials are combined. An effective catalyst requires at least one mole of multidentate ligand for one gram- atom of zero-valent nickel. The diolefinic compound reactants used in this invention include primarily conjugated diolefins containing from 4 to 10 carbon atoms; for example 1,3-butadiene and ris and trans-2,4-hexadienes. Butadiene is especially preferred by reason of its commercial importance in the production of adiponitrile. Other suitable diolefinic compounds include diolefinic compounds substituted with groups which do not deactivate the catalyst, for example, cis and trans- 1 ,3- pentadienes. The following Formulas III and IV illustrate suitable representative starting diolefinic compounds; and Formulas V, VI, and VII represent the products obtained from 1,3-butadiene and HCN. CH 2 =CH-CH=CH 2 (1,3-butadiene) III R 12 CH=CH-CH=CHR 13 IV wherein each one of R 12 and R 13 , independently, is H or a C] to C 3 alkyl. NC-CH 2 -CH=CH-CH 3 V (3PN) CH 2 =CH-CH 2 -CH 2 -CN VI (4PN) CN H 2 C c C CH 3 H H VII (2M3BN) It will be recognized that Compound III is a special case of Formula IV, where each one of R 12 and R 13 is hydrogen. In the practice of the hydrocyanation process of the present invention, a reactor, such as a tubular reactor, is charged in an inert atmosphere with the desired supported Ni(0) (Ligand) catalyst. The reactor feed and exit lines are preferably purged with an inert gas, such as N 2 , Ar, or He. The reactor is then heated to the desired temperature, either under a continuous flow of inert gas or sealed from the ambient atmosphere. The reactor is fed with the desired diolefinic compound and HCN. These may be fed together or separately, either neat or as solutions in suitable solvents, such as acetonitrile or toluene. When the reactants are fed continuously, an inert gas carrier normally is employed as well. The diolefinic compound, HCN and any solvent are passed through a heated portion of feed line heated to the reaction temperature to ensure complete vaporization. The gaseous product mixture exiting the reactor can be passed, if desired, through a heated gas sampling loop of a gas chromatograph for perodically monitoring the progress of the reaction. Alternatively, the gaseous effluent can be cooled to about 0°C to 25°C in order to condense all products to liquids. The flow rate of the diolefinic compound preferably is such that its mole ratio to catalyst, per hour of continuous feed, is about 5:1 to 100:1. The mole ratio of the diolefinic compound to HCN normally is at least about 1:1. The hydrocyanation reaction is preferably carried out without a solvent. If any solvent is used, the solvent should be gaseous at the reaction temperature and pressure and inert towards the diolefinic compound, HCN, and the catalyst. Such solvents include hydrocarbons such as hexane, benzene, toluene or xylene, or nitriles such as acetonitrile. EXAMPLES This invention is now illustrated by the following non-limiting examples of certain preferred embodiments thereof, wherein all parts, proportions, and percentages are by weight, unless otherwise indicated. In the Examples, Ligand "PE-1 " is the ligand of Formula II, where x is 1 and each R 10 is CH 3 , each R 9 is isopropyl and each R 8 is B, and Ligand "A" is the ligand of Formula I, where each R l , R 2 , R 3 and R 4 is H, R 5 is OCH 3 , and each R6 is t-butyl. EXAMPLE 1 Synthesis of Silica-supported Ni[OTTP] 2 CH 2 =CH 2 + PE-1 where OTTP is o-tritolyl phosphite and the Ligand "PE-1 " is the ligand of Formula II, where x =1 and each R 8 is B, each R 9 is isopropyl and each R 10 is methyl A 2 g sample of Johnson Mathey Co. silica (300 m 2 /g, 8/12 mesh) was dried under flowing N 2 at 200°C for 2 hours, then cooled to ambient temperature in a N 2 -filled glove box. The 2 g of dried silica was combined with 0.21 g (0.125 mmole) Ligand PE- 1 , 0.10 g (0.125 mmole) Ni(OTTP) 2 CH 2 =CH 2 and 10 mL dry tetrahydrofuran (THF) and the mixture was stirred for 15 minutes. Solvent THF was evaporated under vacuum to provide the silica-supported Ni(0) catalyst used for Example 5 in Table 1. EXAMPLE 2 Synthesis of polydivinylbenzene/polyacrylonitrile-supported Ni(0) (Ligand "A")CH 2 =CH 2 , where the Ligand "A" is of Formula I, where each R 1 , R 2 , R 3 , R 4 , is H, each R 5 is OCH 3 and each R 6 is t-butyl All operations were carried out in a nitrogen atmosphere. Into a glass vial were placed 0.385 g (1.5 mmoles) of Ni(acetylacetonate) 2 , 1.18 g (1.5 mmoles) of Ligand "A" and 20 mL toluene. Next, ethylene was bubbled through the solution. Then, 2.3 mL of a 1.9 M (25%) solution of (C 2 H 5 ) 3 A1 (4.4 mmoles) in toluene was added dropwise, while ethylene still was being introduced into the solution. After several more minutes, the ethylene flow was stopped and the vial was sealed with a septum. The reaction contents were stirred overnight. The next day, about half of the solvent was removed by evaporation at a reduced pressure. A portion of the solid reaction product was recovered by filtration. Methanol was added to precipitate additional solid reaction product. Recovered solid product was dried under vacuum to yield 0.78 g of a gold-colored powder. A 31 P NMR spectrum of the final product exhibited a major singlet at 169.9 ppm {Ni(Ligand "A")CH 2 =CH 2 } and a minor singlet at 162.8 ppm {Ni(Ligand "A") 2 } . A 10 g sample of Johns Manville Chromasorb 104 ( polydivinyl-benzene/ polyacrylonitrile, 60/80 mesh) was dried in flowing N 2 at 150°C for 1 hour, then cooled to ambient temperature in a N 2 -filled glove box. Next, 8 g of the dried Chromasorb 104 was combined with 0.44 g (0.50 mmole) Ni(0)(Ligand "A")CH 2 =CH 2 and 20 mL dry THF and was stirred for 10 minutes. Solvent THF was evaporated under vacuum to provide the Chromasorb 104-supported Ni(0) catalyst used for Example 6 in Table 1. EXAMPLE 3 Synthesis of polydivinylbenzene/polyacrylonitrile-supported Ni(0) (Ligand "A") 2 , where the Ligand "A" is of Formula I, Where each R 1 , R 2 , R 3 , R 4 , is H, each R 5 is OCH 3 and each R 6 is t-butyl A 2 g sample of Chromasorb 104 ( polystyrene/polyacrylonitrile, 60/80 mesh), dried as in Example 2, was combined with 0.20 g (0.47 mmole) Ni(0)(Ligand "A") 2 and 10 mL dry THF and was stirred for 15 minutes. Solvent THF was evaporated under vacuum to provide the Chromasorb 104-supported Ni(0) catalyst used for Example 7 in Table 1. EXAMPLE 4 Synthesis of carbon-supported Ni(0) (Ligand "A") 2 , where the Ligand "A" is of Formula I, Where each R 1 , R 2 , R 3 , R 4 , is H, each R 5 is OCH 3 and each R 6 is t-butyl A 2 g sample of carbon (EM Co., 1050 m 2 /g, 20-35 mesh) was heated under flowing He by ramping the temperature in 90 minutes to 850°C, holding at 850°C for 5 hours, and then cooling to ambient temperature in a N -filled glove box. 1 g of the heat-treated carbon was combined with 0.10 g (0.24 mmole) Ni(0)(Ligand "A") 2 and 10 mL dry THF and was stirred for 15 minutes. Solvent THF was evaporated under vacuum to provide the carbon-supported Ni(0) catalyst used for Example 8 in Table 1. COMPARATIVE EXAMPLE 4A Synthesis of a carbon-supported Ni(0) (Ligand "A") 2 , where the Ligand "A" is of Formula I, Where each R 1 , R 2 , R 3 , R 4 , is H, each R 5 is OCH 3 and each R 6 is t-butyl A 2 g sample of carbon (EM Co., 1050 m 2 /g, 20-35 mesh) was heated under flowing N 2 at 200°C for 1 hour, then cooled to ambient temperature in a N 2 -filled glove box. 1 g of the heat-treated carbon was combined with 0.10 g (0.24 mmole) Ni(0)(Ligand "A*') 2 and 10 mL dry THF and was stirred for 15 minutes. Solvent THF was evaporated under vacuum to provide the carbon- supported Ni(0) catalyst used for Comparative Example 8 A in Table 1. EXAMPLES 5-COMPARATIVE 8A Vapor-Phase Hydrocyanation of Butadiene (BD) An empty 0.25-inch (0.64 cm) diameter, 15-inch (37.5 cm) Jong stainless steel tubular reactor was placed in a nitrogen-filled glove box. A plug of glass wool was placed in the bottom end of the reactor, followed by the amount and type of Ni(0) catalyst shown in Table 1. A thermocouple was inserted into the top of the reactor. Both ends of the reactor were sealed with metal fittings, and the reactor was removed from the glove box and connected to stainless steel reactor feed lines purged with nitrogen. The feed streams of nitrogen, butadiene (BD), HCN and toluene solvent were preheated to 145°C to ensure complete vaporization. The reactor was heated in a split tube furnace to the temperatures shown in Table 1. Gaseous effluent from the reactor passed through a heated sampling valve which permitted periodic on-line gas chromatographic analyses of products. Feed solutions of weighed amounts of butadiene in toluene also contained weighed amounts of acetonitrile which served as an internal gas chromatograph (GC) standard. GC analyses were done on a 30 m DB-23 capillary columnn of a 0.32 mm internal diameter, supplied by J&W Scientific, Folsom, California. The stationary phase was cyanopropyl (50%) methylpolysiloxane. Table 1 shows the specific reaction conditions and summarizes the results. TABLE 1 Vapor Phase BD HCN Runs Feed Catalyst Catalyst Feed L/min Temp. Elapsed Ex No. (Support) g. % Ni mmole/hr N 2 °C Time (Hr.) BD HCN 5 Ni(OTTP) 2 CH 2 =CH + L 1.02,0.31 .51 0.26 10 145 1 L=Ligand "PE-l" (Silica) Example 1 NiLCH 2 =CH 2 1.02, 0.35 .69 0.32 10 145 L=Ligand "A" (Chromasorb 104) Example 2 NiL 2 1.01 ,0.32 .65 0.33 10 145 L=Ligand "A" (Chromasorb 104) 47 Example 3 56 NiL 1.03,0.32 .66 0.33 10 145 L=Ligand "A" t In the above Table, percent conversion to pentenenitriles (PNs) was calculated as (measured GC area % for PNs/GC area % for acetonitrile) x (GC response factor for PNs) x (g of acetonitrile fed per hour/mmoles of BD fed per hour) x 100. Response factor is the number, characteristic for each compound, required for converting area percent to weight percent/molecular weight of PNs. Percent conversion to DNs was determined as (measured GC area % for DNs)/(GC area % for acetonitrile) x (GC response factor for DNs) x (g of acetonitrile fed per hour./mmoles of BD fed per hour) x 100. Percent selectivity to (3PN + 4PN + 2M3BN) was determined as (GC area % for 3PN + 4PN + 2M3BN)/(GC area % for PNs + DNs) x 100. Although particular embodiments of the present invention have been described in the foregoing specification, it will be understood by those skilled in the art that the invention is capable of numerous modifications, substitutions and rearrangements without departing from the spirit or essential attributes of the invention. Reference should be made to the appended claims, rather than to the foregoing specification, as indicating the scope of the invention.

Claims: WHAT IS CLAIMED IS: 1. A process for the vapor-phase hydrocyanation of diolefinic compounds comprising, reacting an acyclic aliphatic diolefinic compound with HCN in the vapor phase within a temperature range of from about 135°C to about 300°C in the presence of a supported catalyst composition comprising zero-valent nickel and at least one multidentate phosphite ligand selected from the group consisting of compounds represented by Formulas I and II: Formula I wherein each R 1 , R 2 , R 3 , R 4 , R 5 , and R 6 are independently, H, a branched or straight chain alkyl of up to 12 carbon atoms, or OR 7 , wherein R 7 is a C ] to C 12 alkyl; Formula II wherein each R 8 is, independently, H, a primary, secondary or tertiary hydrocarbyl of 1 to 12 carbon atoms, or B, where B is a substituent of the formula wherein x is an integer from 1 to 12; and each R 9 and R 10 are independently, H, OR 1 wherein R 1 * is a Cj to Cι 2 alkyl or a primary, secondary or tertiary hydrocarbyl of 3 to 12 carbon atoms and wherein R 10 can be ortho, meta or para to the oxygen; and wherein x is an integer from 1 to 12; to produce acyclic pentenenitriles in which the olefinic double bond is not conjugated with the cyano group. 2. The process of Claim 1 wherein the catalyst support is selected from the group consisting of silica, alumina and carbon. 3. The process of Claim 1 wherein the catalyst support is selected from the group consisting of heat-treated carbon, heated to a temperature of at least 600°C in an inert atmosphere for at least 2 hours, and an organic polymer. 4. The process of Claim 3 wherein the carbon support is heated to at least 800°C. 5. The process of Claim 3 wherein the carbon support is heated for at least 4 hours. 6. The process of Claim 3 wherein the organic polymer support is selected from the group consisting of polydivinylbenzene/polyacrylonitrile, cross- linked polystyrene and copolymers and blends thereof. 7. The process of Claim 1 wherein the acyclic aliphatic diolefinic compound is selected from the group consisting of 1,3-butadiene, cis-2,4- hexadiene, and trans-2 ,4-hexadiene . 8. The process of Claim 1 wherein the temperature range is from about 145°C to about 200°C. 9. The process of Claim 1 wherein the acyclic pentenenitriles produced include 3 -pentenenitrile and 4-pentenenitrile. 10. A supported catalyst composition comprising zero-valent nickel and at least one multidentate phosphite ligand selected from the group consisting of compounds represented by Formulas I and II: Foπnula l wherein each R 1 , R 2 , R 3 , R 4 , R 5 , and R 6 are independently, H, a branched or straight chain alkyl of up to 12 carbon atoms, or OR 7 , wherein R 7 is a C] to C 12 alkyl; Formula II wherein each R 8 is, independently, H, a primary, secondary or tertiary hydrocarbyl of 1 to 12 carbon atoms, or B, where B is a substituent of the formula wherein x is an integer from 1 to 12; and each R 9 and R 10 are independently, H, OR 1 1 wherein R 1 ' is a C \ to C ]2 alkyl or a primary, secondary or tertiary hydrocarbyl of 3 to 12 carbon atoms and wherein R 10 can be ortho, meta or para to the oxygen; and wherein x is an integer from 1 to 12. 11. The catalyst composition of Claim 10 wherein the catalyst support is selected from the group consisting of silica, alumina and carbon. 12. The catalyst composition of Claim 10 wherein the catalyst support is selected from the group consisting of heat-treated carbon, heated to a temperature of at least 600°C in an inert atmosphere for at least 2 hours, and an organic polymer. 13. The catalyst composition of Claim 12 wherein the carbon support is heated to a temperature of at least 800°C. 14. The catalyst composition of Claim 12 wherein the carbon support is heated for at least 4 hours. 15. The catalyst composition of Claim 12 wherein the organic polymer support is selected from the group consisting of polydivinylbenzene/polyacrylonitrile, cross-linked polystyrene and copolymers and blends thereof. 16. A catalyst support for use with a catalyst composition comprising heat-treated carbon, heated to a temperature of at least 600°C in an inert atmosphere for at least 2 hours. 17. A catalyst support for use with a catalyst composition comprising an organic polymer selected from the group consisting of polydivinylbenzene/polyacrylonitrile, cross-linked polystyrene and copolymers and blends thereof. 18. The catalyst support of Claim 16 wherein the carbon is heated to a temperature of at least 800°C. 19. The catalyst support of Claim 16 wherein the carbon is heated for at least 4 hours.

Inventors: DRULINER JOE DOUGLAS, HERRON NORMAN, DRULINER, JOE, DOUGLAS, HERRON, NORMAN
Applicants: DRULINER JOE DOUGLAS, DU PONT, HERRON NORMAN, DRULINER, JOE, DOUGLAS, E.I. DU PONT DE NEMOURS AND COMPANY, HERRON, NORMAN
Application year: 1997
Main classification: C07C253
IPC codes: B01J31, C07C253, C07C255