Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
  • C08G67/00—Macromolecular compounds obtained by reactions forming in the main chain of the macromolecule a linkage containing oxygen or oxygen and carbon, not provided for in groups C08G2/00 - C08G65/00
  • C08G67/02—Copolymers of carbon monoxide and aliphatic unsaturated compounds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/18—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms
  • B01J31/1805—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms the ligands containing nitrogen
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
  • B01J31/2404—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
  • B01J31/2404—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring
  • B01J31/2409—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring with more than one complexing phosphine-P atom
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F15/00—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table
  • C07F15/0006—Compounds containing elements of Groups 8, 9, 10 or 18 of the Periodic Table compounds of the platinum group
  • C07F15/006—Palladium compounds
  • C07F15/0066—Palladium compounds without a metal-carbon linkage
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/02—Compositional aspects of complexes used, e.g. polynuclearity
  • B01J2531/0238—Complexes comprising multidentate ligands, i.e. more than 2 ionic or coordinative bonds from the central metal to the ligand, the latter having at least two donor atoms, e.g. N, O, S, P
  • B01J2531/0241—Rigid ligands, e.g. extended sp2-carbon frameworks or geminal di- or trisubstitution
  • B01J2531/0247—Tripodal ligands, e.g. comprising the tris(pyrazolyl)borate skeleton, "tpz", neutral analogues thereof by CH/BH exchange or anionic analogues of the latter by exchange of one of the pyrazolyl groups for an anionic complexing group such as carboxylate or -R-Cp
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/824—Palladium

Definitions

• This invention relates to the production of linear alternating polymers of carbon monoxide and at least one ethylenically unsaturated hydrocarbon. More particularly, the invention relates to a method of making novel catalyst compositions and a novel process for the production of such polymers employing the catalyst compositions in the process.
• the invention relates to homogeneous catalysts for copolymerization of carbon monoxide and alpha olefins, methods for preparing these catalysts, and a process of copoly erizing alpha- olefins and carbon monoxide using these catalysts. More particularly, the invention relates to a homogeneous catalyst useful for making polymers containing carbon monoxide and olefins in interpolymerized form.
• the polymer will have C3 units randomly scattered through the olefinic portion of the polymer.
• the C3 units do not interfere with or disrupt the linear alternating structure of the polymer in that only one olefinic unit is located between two carbonyl goups .
• Pd, Co or Ni are given as the transition metal sources with anions that could be used including hexafluorophosphate (PFg ⁇ ) , trichloroacetate and tetrafluoroborate (BF ⁇ ) which are respectively the conjugate anions of hexafluorophosphoric acid, trichloroacetic acid and tetrafluoroboric acid.
• PFg ⁇ hexafluorophosphate
• BF ⁇ tetrafluoroborate
• U.S. Patent 4,804,739 describes the use of catalysts based on palladium as the transition metal source and quaternary phosphonium salts for the anion source. These catalysts reduce the amount of metallic residues in the product.
• the catalyst compositions generally consist of a palladium(II) salt (such as a halide or acetate) , a strong organic acid (such as trifluoroacetic, p-toluenesulfonic acid) and a bidentate phosphine (such as, 1,3- bisfdiphenylphosphino]propane) .
• U.S. 4,831,114 discloses the use of a catalyst containing a Group VIII metal, an anion of a non-hydrohalogenic acid having a pKa more than about 2 but less than 4, and certain bidentate hydrocarbyl phosphine ligands.
• the composition is described as exhibiting greater reactivity at lower reactor temperatures.
• EPO application 0 396 268 Al describes the use of a catalyst including a palladium(II) salt, a bidentate amine, phosphine, arsine or stibene and specified anions. Quinone was added as an oxidant to prevent reduction of the transition metal. Quinones are described as being useful in maintaining catalyst stability.
• EP 0 061 337-A1 teaches a catalytic process for hydrogenation of unsaturated organic compounds in a two phase aqueous/organic medium, in which the catalytic complex is dissolved in the aqueous phase.
• Rhodium catalysts are preferred, but [Pd (water soluble phosphines ligand) 2 (octone) 2 ] +2 is also mentioned as a suitable pre-formed complex for use as a hydrogenation catalyst.
• EP 0 450 707 Al teaches use of certain palladium (0) complexes in the production of isoprenyl-alkylethers from isoprene.
• U.S. Patent 4,866,128 teaches another approach for controlling the melting range of olefin/carbon monoxide polymers by blending them with other polymers. Only limited success has been achieved by this technique due to the apparent incompatibility of the ethylene/carbon monoxide copolymer with other materials, even under melt processing conditions. See, for example, US Patents 4,904,728 and 4,954,570.
• Such a catalyst would provide flexibility in controlling the melt flow characteristics of this polymer and terpolymers by varying the olefinic component and would permit the preparation of polymers which range from completely amorphous to highly crystalline.
• Pd(II) is palladium having a valence of +2;
• S is a synthesis solvent; is a monodendate, bidendate or tridendate ligand or ligands having one or more bonding sites;
• x is an integer from 1 to 3 and is equal to the total number of ligand bonding sites;
• A is a weakly or non-coordinating anion capable or stabilizing the complex in its cationic form; and n is 1 or 2 and y is 2 or 1; provided that
• the organometallic complex is not (tris(acetonitrile)palladium(II)triphenylphosphine) , (bis(acetonitrile)palladium(II) is(triphenylphosphine) ) , ( (acetonitrile)palladium(II)tris (triphenylphosphine) ) or
• a first method of preparing the catalyst compositions comprises the steps of:
• a second method of preparing the catalyst composition comprises the steps of:
• a third method of preparing the catalyst compositions comprises the steps of: (a) contacting a palladium dihalide and a metal containing salt and a synthesis solvent to form a solution; and
• the new catalyst compositions are useful for the copolymerization of carbon monoxide and at least one ethylentically unsaturated hydrocarbon to produce linear alternating polymers.
• the rate of polymerization is enhanced by including an alcohol, such as methanol, in the polymerization mixture.
• the catalyst compositions of the current invention are generally prepared by reacting together a source of palladium, appropriate solvent and anion followed by partial or complete substitution of the solvent by an appropriate ligand.
• the anion is preferably that of a strong acid, i.e., an anion of an acid having a pKa of less than 2 for those acids having a measurable pKa, and preferably consists of tetrafluoroborate, tetraphenylborate, perchlorate, hexafluorophosphate, trifluoromethanesulfonate, or a mixture thereof.
• a strong acid i.e., an anion of an acid having a pKa of less than 2 for those acids having a measurable pKa
• a strong acid i.e., an anion of an acid having a pKa of less than 2 for those acids having a measurable pKa
• a strong acid i.e., an anion of an acid having a pKa of less than 2 for those acids having a measurable pKa
• the solvent used in the synthesis of the catalyst must not decompose the palladium metal complex or any of the reactants.
• the following compounds are useful as synthesis solvents: acetonitrile, benzonitrile, propionitrile, 1,4-dioxane, dimethylformamide, hexamethylphosphoramide, pyridine, 1-piperidinecarbonitrile, dimethoxyether, aniline, dimethylsuIfoxide, 1,2-dimethoxyethane, diethylether, tetrahydrofuran, or a mixture of at least two thereof.
• the source of anion is preferably that of a strong acid.
• acids and salts are nitrosium tetrafluoroborate, tetrafluoroboric acid, silver perchlorate, perchloric acid, sodium tetraphenylborate, sodium hexafluorophosphate, and silver trifluoromethanesulfonate.
• the ligands used to partially or completely displace the synthesis solvent molecules can be mono-, bi, tri- or tetradentate.
• Suitable coordinating ligands include, for example, aliphatic or aromatic substituted nitrogen containing compounds, phosphines, arsines and stibines.
• the ligand or ligands employed are substantially water insoluble, meaning in this context and in the claims that the resulting catalyst complex is less soluble in water than in a non-aqueous inert solvent useful for dissolving the catalyst in the process described herein for producing alternating linear copolymers of carbon monoxide and at least one alpha olefin.
• the coordinating ligand is 1,3- bis(diphenylphosphino)propane or 1,1,1- tris(diphenylphosphinomethyl)ethane.
• Ligands can be employed in the catalyst compositions which are generally covalently bound nucleophilic groups to the palladium atom and provide stability to the complex. These are selected from monodentate, bidentate or tridentate ligands of nitrogen, phosphorus, arsenic or antimony. Suitable monodentate ligands are of the formula
• R 1 , R 2 and R ⁇ are independently organic radicals of from 1 to 20 carbon atoms selected from a group consisting of akyl, aryl, alkaryl or alkoxyaryl. Preferably each aryl, alkaryl or alkoxyaryl of consists of 6 to 14 carbon atoms. Examples of such organic radicals are phenyl, p-methylphenyl, o-methoxyphenyl, p-methoxyphenyl, o- dimethoxyphenyl and 2,6-dimethylphenyl.
• Suitable atoms for Z include nitrogen, phosphorus, arsenic and antimony, preferably nitrogen or phosphorus.
• Examples of monodentate ligands include triphenyl phosphine, diphenylmethylphosphine, dimethylphenylphosphine, tris(o- methoxyphenyl)phosphine, tris(2,6-dimethoxyphenyl)phosphine, tris (p- methoxyphenyl)phosphine, tris(p-methylphenyl)phosphine and tris(2,6- dimethylphenyl)phosphine, and mixtures of at least two thereof.
• Suitable bidentate ligands are of the formula
• R 1 and R 2 are the radicals previously defined.
• organic radicals are phenyl, p-methylphenyl, o-methoxyphenyl, p- methoxyphenyl, o-dimethoxyphenyl and 2,6-dimethylphenyl.
• the R 4 group is a divalent aryl or alkaryl organic group of from 2 to 20 carbon atoms with preferably two or three carbon atoms separating Z. Suitable atoms for Z include nitrogen, phosphorus, arsenic and antimony, preferably nitrogen or phosphorus. Examples of bidentate ligands include:
• Suitable tridentate ligands are preferably of the formula
• R 1 and R 2 are the radicals previously defined. Examples of such organic radicals are phenyl, p-methylphenyl, o-methoxyphenyl, p- methoxyphenyl, o-dimethoxyphenyl and 2,6-dimethylphenyl.
• the R 5 group is a divalent radical with preferably one or two carbon atoms
• M is any trivalent group such as nitrogen, phosphorus, arsenic, or antimony.
• Y is nitrogen, phosphorus, arsenic and R 6 is not present or if Y is carbon, then R 6 is any organic radical of from 1 to 20 carbon atoms or hydrogen.
• tridentate ligands examples include: 1,1,1-tris (dimethylphosphinomethyl)ethane, tris(dimethylphosphinomethyl)methane, 1,1,1-tris (dimethylphosphinomethyl)propane, tris (diphenylphosphinomethyl)methane, 1,1,1-tris(diphenylphosphinomethyl)ethane, 1,1,1-tris(diphenylphosphinomethyl)propane, tris(diphenylphosphinoethyl)methane, N,N,N-[tris(diphenylphosphinomethyl) ]amine, N,N,N-[tris(diphenylphosphinoethyl) ]amine, 1,1,1-tris[bis(2,6-dimethoxyphenyl)phosphinomethyl]ethane, 1,1,1-tris[bis(2,6-dimethylphenyl)phosphinomethyl]ethane
• the palladium tetrafluoroborate compositions can be prepared by contacting metallic palladium with a slight excess of nitrosonium tetrafluoroborate in a suitable synthesis solvent which is compatible with the oxidizing agent followed by partial or complete displacement of this solvent with a coordinating ligand.
• suitable synthesis solvents include, for example, acetonitrile, benzonitrile, propionitrile, dimethoxyethane, 1,4-dioxane, and mixtures of at least two thereof.
• the reaction is preferably conducted using a slight stoichiometric excess of nitrosonium tetrafluoroborate by contacting the reactants at any temperature which doesn't decompose the reactants or products. Preferably the reaction is conducted at room temperature under an inert atmosphere.
• Another method for generating the palladium metal complex involves the direct reaction of palladium metal with an oxidizing acid, for example, trifluoromethanesulfonic acid, tetrafluoroboric acid or more preferably perchloric acid in the appropriate synthesis solvent followed by partial or complete displacement of the solvent with a coordinating ligand.
• the oxidizing acid must be capable of oxidizing the palladium metal from Pd(0) to Pd(II) .
• the synthesis solvents include, for example, but are not limited to dimethylsulfoxide, hexamethylphosphoramide, dimethyl ormamide, acetonitrile, propionitrile, benzonitrile, 1-piperidinecarbonitirle, pyridine, aniline, dimethoxyethane, diethyl ether, tetrahydrofuran, 1,4-dioxane, or any compatible mixture of at least two thereof.
• the reaction is preferably conducted with palladium in the presence of a slight excess of the acid component.
• the palladium metal complex may also be generated by the reaction of a palladium dihalide with a metal containing salt in the appropriate solvent using salt elimination as the driving force followed by partial displacement of the solvent with a coordinating ligand.
• the palladium dihalide may be comprised of either Cl, Br or I.
• the metal salt may consist for example of lithium, sodium, potassium or silver and the anion of an acid such as tetraphenylborate, perchlorate, nitrate or hexafluorophosphate.
• metal containing salts include sodium tetraphenylborate, silver tetraphenylborate, silver perchlorate, sodium nitrate, silver nitrate, sodium hexafluorophosphate, silver trifluoromethanesulfonate and potassium hexafluorophosphate.
• the synthesis solvents include for example, but are not limited to dimethylformamide, hexamethylphosphoramide, pyridine, acetonitrile, benzonitrile, propionitrile, 1-piperidinecarbonitrile, 1,2- dimethoxyethane, tetrahydrofuran, aniline, dimethylsulfoxide, 1,4- dioxane, or any compatible mixture of at least two thereof.
• the polymerization reaction is preferably carried out by contacting the monomers and catalyst in a liquid phase or in a gas phase using methods commonly employed by industry.
• the quantity of catalyst used can vary within wide limits.
• the quantity of catalyst used will contain from lxlO -1 mol of palladium to lxlO -6 mol of palladium per liter of polymerization solvent.
• carbon monoxide is polymerized with at least one ethylenically unsaturated hydrocarbon (i.e., alpha olefins) using the novel catalyst composition described herein.
• hydrocarbons having from 2 to 20 carbon atoms are preferred, with those having from 2 to 10 being more preferable.
• These hydrocarbons include oc-olefins such as ethylene, propylene, butene, 4- methyl-1-pentene, hexene, octene, decene, styrene or p-methylstyrene.
• the preferred alpha-olefins are ethylene and/or propylene.
• An activator can be employed along with the catalyst composition in the polymerization process.
• Activators are generally alkanols such as methanol.
• the alcohol serves as a telogen in the reaction mixture. Enhanced reaction rates are observed when an alcohol is present which further suggests it may serve to initiate and/or terminate polymerization.
• the alcohol can also serve as the polymerization solvent, however, decreased reaction rates are observed for catalysts containing weakly coordinating anions such as BF ⁇ .
• the preferred molar ratio of alcohol: palladium ranges from 1:1 to 1,000,000:1 with the most preferred range being from 100:1 to 100,000:1.
• Suitable alcohols include, for example, lower alkanols of 1-4 carbon atoms, such as methanol, ethanol, n-propanol, isopropanol, n-butanol, s-butanol and t-butanol.
• Suitable reaction pressures for the polymerization range from 1 atmosphere to 700 atmospheres with the preferred range being from 7 atmospheres to 300 atmospheres.
• the partial pressure ratio of the olefins:carbon monoxide ranges from 1:2 to 1:20 and preferably from 1:4 to 1:10.
• inert solvent is meant one which dissolves the catalyst composition without decomposition or displacement of the ligands at elevated temperature and pressure.
• the inert solvent may, however, comprise a component, e.g., a lower alkanol, which may affect the rate of initiation, chain termination, or chain transfer reactions in the polymerization process.
• a solvent with low vapor pressure at reaction temperatures is desirable to eliminate the need for higher reactor pressures.
• Suitable solvents include ethers, diethers, cyclic ethers, ketones, diketones, alkanols, aromatic hydrocarbons, halogenated hydrocarbons, aromatic amines and nitriles.
• solvents examples include diethyl ether, dimethoxyethane, 1,4-dioxane, tetrahydrofuran, acetone, methylethylketone, dimethylsulfoxide, methanol, ethanol, n-propanol, isopropanol, n-butanol, s-butanol, t-butanol, toluene, xylene, carbon tetrachloride, chloroform, methylene chloride, 1,2-dichloroethane, acetonitrile, propionitrile, piperidinecarbonitrile, benzonitrile, aniline, pyridine, and mixtures of at least two thereof.
• Solvent selection and reaction temperature have an effect on polymer tacticity when the olefin group contains more than two carbon atoms, particularly when the anion is non-coordinating, such as BF4 ⁇ .
• acetone as a solvent at a temperature of 30°C or less gives a more tactic polymer than 1,2-dichloroethane under similar reaction conditions.
• Increasing the reaction temperature to at least 65°C gives essentially an atactic copolymer independant of the solvent.
• the polymerization rate is affected by the counterion present in the catalyst.
• the anion is non-coordinating, such as BF4
• the polymerization reaction rate is lower in polar solvents than in non- polar solvents.
• the anion is strongly coordinating, such as perchlorate
• the reaction rate is generally higher in polar solvents than in less polar solvents.
• Reactors may include those employed in the industry for the particular method of polymerization being used. Suitable reaction temperatures preferably include those which give significant reaction rates without decomposition of the catalyst. Furthermore, temperature can affect the molecular weight and tacticity of the polymers depending on the reaction mixture employed. The reactants, carbon monoxide and alpha-olefins, are highly reducing to Pd(II) and the reduction rate increases with increasing temperature. In general, all catalysts are more easily reduced at elevated temperatures. Polymerization can occur over a range of -78°C to 200°C with the most preferred range being 25°C to 150°C. Increasing reaction temperature also increases the rate of polymerization provided that catalyst deactivation is not significant.
• catalysts having BF4- as the anion are less stable at reactor temperatures above 100°C than those having perchlorate which shows virtually no loss in reaction rate after more than 7 hours at 80°C.
• Deactivation of the catalyst may occur by decomposition or any other mechanism which destroys the ability of the catalyst to promote the desired reaction.
• All catalyst complexes were prepared under dry nitrogen which was passed through a column of reduced chromium on PA-400 Davidson refrigeration grade silica to remove the last traces of water and oxygen.
• Acetonitrile, propionitrile, benzonitrile, dimethylforamide and hexamethylphosphoramide were purchased as anhydrous when available or high purity from Aldrich Chemical Company and used without further purification.
• Palladium powder, nitrosonium tetrafluoroborate, silver perchlorate, palladium dichloride, sodium hexaphophate, silver trifluoromethanesulfonate and sodium tetraphenylborate were purchased from Aldrich Chemical Company and were used without further purification.
• N,N,N' ,N'-tetramethyl-l,3-propanediamine was purchased from Aldrich Chemical Company and refluxed over calcium hydride under dry nitrogen followed by distillation from calcium hydride.
• Tris (o- methoxyphenyl)phosphine and 1,3-bis(diphenylphosphino)propane were purchased from Strem Chemical Company and used without further purification with the exception of some impure batches of 1,3- bis(diphenylphosphino)propane purchased from Aldrich which required crystallization from hot methanol.
• the 1,1,1- tris(dimethylphosphinomethyl)-ethane and 1,1,1- tris(diphenylphosphinomethyl)ethane ligands were prepared by adapted literature methods (Maier, . J. Inorcr. Nucl. Chem. 24, (1962) 275 and Whitesides, G.M. J. Am. Chem. Soc. 93, 6, (1971) 1379 - 1389). All complexes were stored and weighed in a Vacuum Atmospheres dry box equipped with an oxygen and water removal train.
• a 250 mli vessel was charged in a dry box with palladium powder, 0.5 g (4.70 mmole) , then transferred to a vacuum line. Acetonitrile was added, 50 rtiL, to form a slurry of finely divided metal which was stirred magnetically.
• a 100 rtiL vessel was charged in a dry box with nitrosonium tetrafluoroborate, 1.21 g (10.34 mmole), then transferred to a vacuum line. Acetonitrile was added, (2 X 50 m ) in order to dissolve the nitrosonium tetrafluoroborate which was transferred (2 X 50 mL) to the vesselcontaining the palladium metal slurry.
• the mixture was stirred at least four hours at room temperature resulting in the formation of a yellow solution of the palladium complex in acetonitrile with trace amounts of suspended metal.
• the yellow solution was filtered to remove any excess metal residue from the palladium complex prior to use.
• This complex will be referred to as the cation, I, in the following preparations.
• the cation, I was prepared as described above on a 4.70 mmole scale.
• 1,3- bis(diphenylphosphino)propane 2.13 g (5.12 mmole).
• the vessel was transferred to a vacuum line and acetonitrile was added, 100 mL.
• the solution was stirred magnetically during the course of the reaction.
• I was filtered directly into the vessel containing the phosphine resulting in precipitation of a blood red product. The color faded slowly upon stirring at room temperature resulting in a soluble product which became almost colorless after stirring overnight. All volatiles were removed under vacuum leaving an off-white solid which was washed with hexane (2 X 100 mL) . Hexane was filtered from the solid which was dried completely under vacuum at room temperature for several hours.
• the cation, I was prepared as described on a 4.70 mmole scale. To a 500 mL vessel in a dry box was added tris(o- methoxyphenyl)phosphine, 3.64 g (10.34 mmole), then transferred to a vacuum line. Acetonitrile, 75 mL, was added which partially dissolved the phosphine. The mixture was stirred magnetically at room temperature during the course of the reaction. I was filtered directly into the vessel containing the phosphine causing the solution to darken. The color lightened to a pale yellow after stirring overnight at room temperature. All volatiles were removed under vacuum leaving a solid which was washed with hexane (2 X 100 mL) . The residue was vacuum dried leaving an off-white solid.
• the cation, I was prepared as described on a 4.70 mmole scale. To a 500 mL vessel in a dry box was added 3.23 g, 5.17 mmole, of
• 1,1,1-tris(diphenylphosphinomethyl)ethane The vessel was transferred to a vacuum line and acetonitrile, 100 mL, was added which dissolved the ligand. The mixture was stirred magnetically during the course of the reaction. I was filtered into the vessel containing the phosphine resulting in formation of an orange solution. The mixture was stirred overnight at room temperature. All volatiles were removed under vacuum leaving a powdery residue. The residue was washed with hexane (1 X 200 mL) then vacuum dry several hours leaving a yellow-orange solid.
• the cation, I was prepared as described on a 1.88 mmole scale in acetonitrile.
• a 500 mL vessel was charged with N,N,N',N'- tetramethyl-l,3-propanediamine, 0.48 g (4.14 mmole), and acetonitrile, 75 mL.
• the contents of the vessel were stirred magnetically during the course of the reaction.
• I was filtered directly into the vessel containing the bidentate amine. The mixture was stirred overnight at room temperature. All volatiles were removed under vacuum. The remaining red-orange solid was washed with hexane (2 X 100 mL) . The solid was vacuum dried for several hours.
• a 100 mL vessel was charged with palladium dichloride, 0.25 g (1.41 mmole) in a dry box then transferred to a vacuum line.
• a 250 mL vessel was charged with silver perchlorate, 0.64 g (2.82 mmole), in a dry box and transferred to a vacuum line.
• To the vessel containing PdCl 2 was added acetonitrile, 50 mL and the slurry was stirred magnetically.
• Acetonitrile, 50 mL was added to the 250 mL vessel containing silver perchlorate. The contents of the vessel were stirred magnetically throughout the procedure.
• the palladium dichloride slurry was added via canula to the silver perchlorate solution resulting in a gradual formation of a yellow solution over white salts.
• the mixture was stirred approximately 15 hours at room temperature.
• a 250 mL vessel was charged with 1,3- bis (diphenylphosphino)propane (DPPP) , 0.64 g (1.41 mmole), in a dry box then transferred to a vacuum line.
• Acetonitrile, 30 mL was added to the vessel containing DPPP which was stirred for the duration of the following reaction. Stirring was halted of the vessel containing the reaction product of palladium dichloride with silver perchlorate and the salts were allowed to settle from the solution.
• DPPP 1,3- bis (diphenylphosphino)propane
• the solvent phase containing the soluble dication [Pd(CH3C ) ] +2 [C10 4 ] ⁇ 2 was filtered from the mixture directly into the solution of DPPP in acetonitrile. Additional precipitate formed which became dark blue which is believed to be primarily oxidation products of DPPP with excess AgC10 4 and precipitated AgCl. The mixture was stirred 12 hours then allowed to settle in order to separate the precipitate from the solution phase. The yellow solution was filtered from the precipitate and solvent was removed under vacuum. A light yellow-green solid was obtained which appeared crystalline. The solid was washed with hexane (2 X 30 mL) then vacuum dried (room temperature at 3 X 10 "3 Torr (0.4 Pa) guage) .
• the silver perchlorate solution was transferred via canula to the stirred slurry containing palladium dichloride resulting in immediate formation of a dark yellow solution over a white-gray precipitate.
• the mixture was stirred at room temperature approximately 15 hours. Stirring was terminated and the solution was allowed to separate from the salts.
• a 250 mL vessel equipped with a magnetic stir bar was charged, in a dry box, with 1,3- bis(diphenylphosphino)propane (DPPP), 1.28 g (2.82 mmole), then transferred to a vacuum line. Dimethylformamaide, 30 mL, was added to the DPPP while stirring partially dissolving the sample.
• DPPP 1,3- bis(diphenylphosphino)propane
• the reaction product of silver perchlorate with palladium dichloride was filtered from the precipitate in to the vessel containing DPPP.
• the remaining DPPP rapidly dissolved and a bright yellow solution immediately formed.
• the solution was stirred approximately 2 hours then placed under vacuum at 40°C to remove excess solvent.
• a gummy yellow brown product was obtained which was washed with hexane (2 X 50 mL) then vacuum dried.
• the final product was a fine beige powder.
• a 100 mL vessel was charged in a dry box with palladium powder, 0.25g (2.35 mmole), then transferred to a vacuum line.
• Benzonitrile, 20 mL was added to the vessel to form a slurry of finely divided metal which was stirred magnetically.
• a 100 mL vessel was charged in a dry box with nitrosonium tetrafluoroborate, 0.60 g (5.17 mmole), then transferred to a vacuum line.
• Benzonitrile, 20 mL was added to form a solution which was stirred magnetically.
• the nitrosonium tetrafluoroborate was added via canula to the Pd slurry and the mixture was allowed to react for three days.
• the mixture was filtered from the solid and hexane, 50 mL, was added to the filtered solution resulting in precipitation of a beige powder.
• the powder was washed with hexane (3 X 20 mL) then dried under vacuum several hours at room temperature prior to use.
• a 100 mL vessel was charged in a dry box with palladium powder, 0.25g (2.35 mmole), then transferred to a vacuum line.
• Propionitrile, 25 mL was added to the vessel to form a slurry of finely divided metal which was stirred magnetically.
• a 100 mL vessel was charged in a dry box with nitrosonium tetrafluoroborate, 0.60 g (5.17 mmole), then transferred to a vacuum line.
• Propionitrile, 25 mL was added to form a solution which was stirred magnetically.
• the nitrosonium tetrafluoroborate was added via canula to the Pd slurry resulting in rapid formation of an olive colored solution.
• the mixture was allowed to react for four hours with some precipitate formation noted.
• a 250 mL vessel was charged with 1,3-bis(diphenylphosphino)propane (DPPP), 1.07g (2.58 mmole) in a dry box then transferred to a vacuum line.
• Propionitrile 25 mL, was added to the vessel containing DPPP which was stirred magnetically.
• the vessel containing the reaction product of palladium with NOBF4 was added via canula to the vessel containing DPPP.
• the mixture was stirred 4 hours and additional precipitate formation was noted.
• the solution was filtered into a 100 mL vessel and precipitated with hexane, 35 mL, after volume reduction under vacuum.
• a 250 mL vessel was charged in a dry box with palladium dichloride, 0.25g (1.42 mmole), then transferred to a vacuum line. Acetonitrile, 30 mL, was added to the vessel to form a slurry which was stirred magnetically.
• a 100 mL vessel was charged in a dry box with sodium hexafluorophosphate, 0.52 g (3.10 mmole), then transferred to a vacuum line. Acetonitrile, 30 mL, was added to form a solution/slurry which was stirred magnetically.
• a 250 mL vessel was charged in a dry box with palladium powder, 0.25g (2.35 mmole), then transferred to a vacuum line. Dimethoxyethane, 25 mL, was added to the vessel to form a slurry of finely divided metal which was stirred magnetically.
• a 100 mL vessel was charged in a dry box with nitrosonium tetrafluoroborate, 0.60 g
• the vessel containing the reaction product of palladium with NOBF4 was added via canula to the vessel containing DPPP.
• the mixture was stirred 4 hours with formation of a bright yellow solution over white precipitate.
• the solution was filtered from the solids and volatiles were removed under vacuum.
• the sticky solid was washed with hexane (2 X 50 mL) followed by dissolution in 1,2-dimethoxyethane, 50 mL, then addition of hexane, 100 mL, resulting in formation of a yellow precipitate which was washed with hexane (3 X 50 mL) followed by vacuum drying prior to use.
• POLYMERIZATION A 450 mL stainless steel (316-SS) reactor purchased from Parr Instrument Company was used for the copolymerization of carbon monoxide with olefins. The reactor was fitted with an internal cooling loop for heat removal and a double stacked arrangement of four blade stirrers. Temperature was controlled, unless otherwise noted, by a PID (proportional-integral-derivative) controller which predicts cooling and heating as a function of the rate and trend of temperature changes during the polymerization and the temperature setpoint. Moisture and oxygen were removed, unless otherwise noted, from the reactor surfaces by heating the cylinder and stirrer assemblies at least 12 hours at 120°C in a convection oven, followed by assembly of these components under a high purity nitrogen purge.
• PID proportional-integral-derivative
• Catalyst was transferred and weighed in a dry box into a four ounce bottle fitted with a rubber septum. Solvent, generally 50 - 100 mL, was transferred to the catalyst bottle in order to dissolve the solid under dry nitrogen using standard airless transfer. Catalyst was transferred to the reactor, as well as promoter and solvent, through a 100 mL capacity pressure addition vessel. The vessel was maintained under an inert atmosphere during the transfer and the liquid contents were forced into the reactor under high (750 - 1000 psig (5,170 - 6,895 kPa guage) ) nitrogen pressure.
• each component was added to the reactor in the following order unless otherwise noted; 1) promoter (methanol), 2) solvent and 3) catalyst in solvent.
• the reactor was vented to atmospheric pressure after each addition.
• Propylene and/or ethylene was next added to the reactor to give the desired partial pressure followed by carbon monoxide at which time the reaction commenced. All reaction times are based on the time at which the last component, carbon monoxide, was added to the reactor.
• the reactor was charged at room temperature by adding in air to the reactor cylinder catalyst dissolved in the run solvent, methanol and solvent. The cylinder was then attached to the reactor head and briefly purged with nitrogen or gaseous olefin prior to charging.
• Propylene and/or ethylene was next added to the reactor to give the desired partial pressure of each component.
• the reactor was heated to or within a few degrees of the desired setpoint and carbon monoxide was added to give the desired total pressure. All reaction time are based on the time at which carbon monoxide was added to the reactor.
• the mixture was stirred at 1000 rpm for the duration of the run.
• pressure was released from the reactor to terminate the reaction and product was removed by disassembling the cylinder from the reactor head and pouring-off the product.
• Solvent was devolatilized from the polymer overnight in a fume hood then further dried in a vacuum oven for at least 48 hours at 60 - 90°C. No stabilizers or antioxidants were added to the products.
• Tetrahydrofuran, diethyl ether and 1,2-dimethoxyethane were purchased from Aldrich in Kilo-Lab cylinders then dried by refluxing over Na/K alloy in the presence of benzophenone to produce the Na/K benzophenone ketal radical anion.
• Solvent was distilled from the above mixture.
• Toluene was obtained from Fisher and dried over 4A molecular sieves followed by reflux and distillation from molten Na.
• Chloroform, methylene chloride, 1,2-dichloroethane and acetonitrile were purchased as anhydrous form Aldrich in Sure Seal Bottles and used without further purification.
• Acetone was obtained as reagent grade in 55 gallon drums from Delta Distributors and used without further purification.
• Absolute methanol was obtained from Fisher and purged with nitrogen followed by the addition of Mg turnings to produce magnesium methoxide. Anhydrous methanol was distilled from the mixture under dry nitrogen followed by the addition of more Mg turnings then distillation of the product under dry nitrogen. All anhydrous solvents were stored under dry nitrogen.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of III, 1,2-dichloroethane, 150 mL, methanol, 10 mL, octene, 50 mL and carbon monoxide, 821 psig (5,660 kPa, guage) at 20°C. The mixture was stirred 25 hours with no heating. Approximately 1 g of polymer was recovered from the reactor. The polymerization rate was 2g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of IV, 1,2-dichloroethane, 150 mL, methanol, 10 mL, octene, 50 mL and carbon monoxide, 820 psig (5,654 kPa, guage) at 23°C. The mixture was stirred 24 hours with no heating. A trace amount of polymer was recovered from the reactor.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of V, 1,2-dichloroethane, 135 mL, methanol, 10 mL, propylene, 80 psig (552 kPa, guage) at 19°C and enough carbon monoxide to give a total reactor pressure of 906 psig (6,247 kPa, guage) at 17°C.
• the mixture was stirred 24 hours and 50 minutes with no heating. A total of 13.68 g of polymer was recovered from the reactor.
• the polymerization rate was 26g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of VI, 1,2-dichloroethane, 150 mL, methanol, 10 mL, ethylene, 275 psig (1,896 kPa, guage) at 24°C and enough carbon monoxide to give a total reactor pressure of 1012 psig (6,977 kPa, guage) at 24°C.
• the mixture was stirred 29 hours and 26 minutes with no heating. A total of 0.30 g of polymer was recovered from the reactor.
• the polymerization rate was 0.5g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.12 mmole of VII, 1,2-dichloroethane, 150 mL, methanol, 5mL, ethylene 214 psig (1,475 kPa, guage) at 18°C and enough carbon monoxide was added to give a total reactor pressure of 914 psig (6,302 kPa, guage) at 32°C. Initially, the reactor setpoint was 45°C. The final setpoint was 100°C with a maximum temperature of 102°C observed during the run. The mixture was allowed to stir 51 minutes prior to termination. Two additional carbon monoxide charges were made during the course of the reaction. A total of 25.87 g of polymer was collected. The polymerization rate was 2,384g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.12 mmole of VII, acetone, 150 mL, methanol, 10 mL, ethylene, 229 psig (1,579 kPa, guage) at 24°C and enough carbon monoxide was added to give a total reactor pressure of 920 psig (6,343 kPa, guage) at 25°C.
• the reactor setpoint was 45°C.
• the final setpoint was 80°C with a maximum temperature of 83°C observed during the run.
• the mixture was allowed to stir for 1 hour prior to termination. Two additional carbon monoxide charges were made during the course of the reaction. A total of 35.98 g of polymer was collected.
• the polymerization rate was 2,818g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.12 mmole of VII, methanol, 150 mL ethylene, 119 psig (820 kPa, guage) at 20°C and enough carbon monoxide was added to give a total reactor pressure of 900 psig (6,205 kPa, guage) at 25°C.
• the reactor setpoint was 45°C.
• the final setpoint was 80°C, however, the reaction was terminated prior to reaching setpoint and the maximum temperature observed was 77°C.
• the mixture was allowed to stir 40 minutes prior to termination.
• One additional carbon monoxide charge was made during the course of the reaction. A total of 13.17 g of polymer was collected.
• the polymerization rate was l,547g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.012 mmole of VIII, acetone, 150 mL methanol, 1 mL, ethylene, 211 psig (1,455 kPa, guage) at 12°C and enough carbon monoxide was added to give a total reactor pressure of 985 psig (6,791 kPa, guage) at 47°C.
• the reactor setpoint was 80°C, carbon monoxide was added during heating when the reactor reached 45°C. A maximum reactor temperature of 82°C was observed during the polymerization run.
• the mixture was allowed to stir 7 hours and 20 minutes prior to termination.
• the catalyst was still active as indicated by the continued drop in total pressure. Two additional carbon monoxide charges were made during the course of the reaction. A total of 28.84 g of polymer was collected.
• the polymerization rate was 3,080g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.17 mmole of IX, 1,2-dichloroethane, 100 mL, methanol, 10 mL, ethylene, 215 psig (1,482 kPa, guage) at 24°C and enough carbon monoxide was added to give a total reactor pressure of 1002 psig (6,909 kPa, guage) at 52°C.
• the reactor setpoint was 65°C, carbon monoxide was added during heating when the reactor reached 45°C. A maximum temperature of 70°C was observed during the run.
• the mixture was allowed to stir 1 hour and 35 minutes prior to termination.
• the catalyst was still active at the end of the run. Two additional carbon monoxide charges were made during the course of the reaction. A total of 28.35 g of polymer was collected.
• the polymerization rated was l,008g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.19 mmole of X, 1,2-dichloroethane, 150 mL, methanol, 10 mL, ethylene, 216 psig (1,489 kPa, guage) at 21°C and enough carbon monoxide was added to give a total reactor pressure of 1001 psig (6,902 kPa, guage) at 49°C.
• the reactor setpoint was 65°C, carbon monoxide was added during heating when the reactor reached 45°C. A maximum temperature of 66°C was observed during the run.
• the mixture was allowed to stir 1 hour and 11 minutes prior to termination.
• the catalyst was still active at the end of the run.
• One additional carbon monoxide charge was made during the course of the reaction.
• a total of 18.14 g of polymer was collected.
• the polymerization rated was 771g of polymer/g-Pd/hr.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.17 mmole of XI, 1,2-dichloroethane, 150 mL, methanol, 10 mL, ethylene, 224 psig (1,544 kPa, guage) at 28°C and enough carbon monoxide was added to give a total reactor pressure of 1023 psig (7,053 kPa, guage) at 49°C.
• the reactor setpoint was 65°C, carbon monoxide was added during heating when the reactor reached 45°C.
• the reactor temperature was increased to 75°C after 24 minutes then to 90°C after a total run time of 38 minutes. The mixture was allowed to stir 47 minutes prior to termination. A trace of polymer was obtained .
• TTiTiUST A TVE EXAMPLE 1 The reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.17 mmole of XI, acetonitrile, 150 mL, methanol, 10 mL, ethylene, 222 psig (1,531 kPa, guage)at 26°C and enough carbon monoxide was added to give a total reactor pressure of 1001 psig (6,902 kPa, guage) at 50°C.
• the reactor setpoint was 65°C, carbon monoxide was added during heating when the reactor reached 45°C.
• the mixture was allowed to stir 43 minutes prior to termination. No polymer was obtained, however, some oligomeric product was evident from a sticky coating on the reactor surfaces.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.19 mmole of XII, 1,2-dichloroethane, 150 mL, methanol, 10 mL, ethylene, 226 psig (1,558 kPa, guage) at 31°C and enough carbon monoxide was added to give a total reactor pressure of 1004 psig (6,922 kPa, guage) at 49°C.
• the reactor setpoint was 65°C, carbon monoxide was added during heating when the reactor reached 45°C. The mixture was allowed to stir 2 hours and 6 minutes prior to termination. A trace of polymer was obtained.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously descrived with 0.12 mmole of VIII, acetone, 150 mL, methanol, 10 mL, propylene, 76 psig (524 kPa, guage) at 25°C, enough ethylene to give a combined propylene + ethylene pressure of 224 psig (1,544 kPa, guage) at 26°C and enough carbon monoxide to give a combined propylene + ethylene + carbon monoxide pressure of 1026 psig (7,074 kPa, guage) at 72°C.
• the reactor setpoint was 100°C with a maximum temperature of 101°C observed during the run.
• the mixture was allowed to stir 2 hours and 18 minutes prior to termination. Two additional carbon monxide charges were made to the reactor during the course of the reaction. A total of 31.48g of polymer was collected. The polymerization rate was l,072g of polymer/g-Pd/hr. Analysis showed 9.31 mole percent of the polymer consisted of incorporated propylene.
• the reactor was charged under atmospheric conditions with no consideration against air or moisture exposure as previously described with 0.11 mmole of XIII, acetone, 150 mL, methanol, 10 mL, ethylene
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, 1,2,-dichloroethane, 150 mL, methanol, 10 mL, octene, 50 mL and carbon monoxide 810 psig (5,585 kPa, guage) at 26°C. The mixture was stirred 22 hours and 15 minutes at with no heating. A total of 11.40 g of polymer was recovered from the reactor. The polymerization rate was 24g of polymer/g-Pd/hr. COMPARA TVE E AMPT.E 7
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, 1,2-dichloroethane, 150 mL, methanol, 10 mL, propylene, 80 psig at 17°C and enough carbon monoxide to give a total reactor pressure of 1001 psig (6,902 kPa, guage) at 17°C.
• An additional carbon monoxide charge was made during the course of the polymerization due to consumption by polymerization.
• the mixture was stirred 27 hours and 30 minutes with no heating. A total of 51.05 g of polymer was recovered from the reactor.
• the polymerization rate was 87g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, acetonitrile, 150 mL, methanol, 10 mL, propylene, 90 psig (620 kPa, guage) at 15°C and enough carbon monoxide to give a total reactor pressure of 907 psig (6,254 kPa, guage) at 15°C.
• the reaction was allowed to stir for 33 hours and 55 minutes prior to termination with no heating. A total of 0.80 g of polymer was recovered from the reactor.
• the polymerization rate was lg of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, chloroform, 150 mL, methanol, 10 mL, propylene, 76 psig (524 kPa, guage) at 19°C and enough carbon monoxide to give a total reactor pressure of 929 psig (6,405 kPa, guage) at 18°C.
• the reaction was allowed to stir for 24 hours and 5 minutes prior to termination with no heating. A total of 25.412 g of polymer was recovered from the reactor.
• the polymerization rate was 24g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, methylene chloride, 150 mL, methanol, 10 mL, propylene, 76 psig (524 kPa, guage) at 20°C and enough carbon monoxide to give a total reactor pressure of 931 psig (6,419 kPa, guage) at 17°C.
• the reaction was allowed to stir for 24 hours prior to termination with no heating. A total of 27.172 g of polymer was recovered from the reactor.
• the polymerization rate was 53 g of copolymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, tetrahydrofuran, 150 mL, methanol, 10 mL, propylene, 78 psig (538 kPa, guage) at 18°C and enough carbon monoxide to give a total reactor pressure of 909 psig (6,267 kPa, guage) at 18°C.
• the reaction was allowed to stir 19 hours and 30 minutes prior to termination with no heating. A total of 10.41 g of polymer was recovered from the reactor.
• the polymerization rate was 25 g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, 1,2-dimethoxyethane, 150 mL, methanol, 10 mL, propylene, 86 psig (593 kPa, guage) at 22°C and enough carbon monoxide to give a total reactor pressure of 945 psig (6,516 kPa, guage) at 18°C.
• the reaction was allowed to stir 24 hours and 15 minutes prior to termination with no heating. A total of 6.08 g of polymer was recovered from the reactor.
• the polymerization rate was 12 g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole ofII, methanol, 150 mL, propylene, 94 psig (648 kPa, guage) at 18°C and enough carbon monoxide to give a total reactor pressure of 905 psig (6,240 kPa, guage) at 17°C.
• the reaction was allowed to stir 24 hours and 5 minutes prior to termination with no heating. A total of 3.25 g of polymer was recovered from the reactor. The polymerization rate was 6 g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, 1,2-dichloroethane, 150 mL, propylene, 80 psig (552 kPa, guage) at 18°C and enough carbon monoxide to give a total reactor pressure of 1002 psig (6,909 kPa, guage) at 16°C.
• the reaction was allowed to stir 24 hours and 25 minutes prior to termination with no heating. A total of 3.49 g of polymer was recovered from the reactor.
• the polymerization rate was 24 g of polymer/g-Pd/hr.
• COMPARATIVE EXAMPLE 10 The reactor was charged under inert conditions as previously described with 0.2 mmole of II, 1,2-dichloroethane, 150 mL, methanol, 10 mL, propylene, 77 psig (531 kPa, guage) at 19°C and enough carbon monoxide to give a total reactor pressure of 902 psig (6,219 kPa, guage) at 125°C. A total of 15 minutes was required to reach the reactor setpoint of 125°C after charging carbon monoxide to the reactor. The reaction was allowed to stir 2 hours and 30 minutes prior to termination, the catalyst showed no significant activity at the end of the run. A total of 9.05 g of polymer was recovered from the reactor. The polymerization rate was 170 g of polymer/g-Pd/hr.
• the reactor was charged under inert conditions as previously described with 0.2 mmole of II, 1,2-dichloroethane, 150 mL, methanol, 10 mL, ethylene, 271 psig (1868 kPa, guage) at 39°C and enough carbon monoxide to give a reactor pressure of 1150 psig (7,929 kPa, guage) at 54°C.
• the reactor was heated to 45°C prior to carbon monoxide addition.
• the setpoint for the reaction was 65°C. An exotherm of 8°C above the setpoint was observed after 3 minutes.
• the reaction was allowed to stir 2 hours and 51 minutes prior to termination. A total of 30.71 g of polymer was recovered from the reactor.
• the polymerization rate was 506 g of polymer/g-Pd/hr.

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