Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L27/00—Compositions of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Compositions of derivatives of such polymers
  • C08L27/02—Compositions of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Compositions of derivatives of such polymers not modified by chemical after-treatment
  • C08L27/04—Compositions of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Compositions of derivatives of such polymers not modified by chemical after-treatment containing chlorine atoms
  • C08L27/06—Homopolymers or copolymers of vinyl chloride
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F14/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
  • C08F14/02—Monomers containing chlorine
  • C08F14/04—Monomers containing two carbon atoms
  • C08F14/06—Vinyl chloride
• • 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
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
  • C08K3/00—Use of inorganic substances as compounding ingredients
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L23/00—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L73/00—Compositions of macromolecular compounds obtained by reactions forming a linkage containing oxygen or oxygen and carbon in the main chain, not provided for in groups C08L59/00 - C08L71/00; Compositions of derivatives of such polymers

Definitions

• the invention is directed towards novel carbon monoxide containing compositions effective as plasticizers for polyvinyl chloride resins.
• Polyvinyl chloride is a versatile polymer which is used in many applications such as water piping, floor tile, exterior vinyl siding, electrical wire insulation, shower curtains and synthetic leather.
• Plasticizers are added to PVC to improve flow, and therefore processability, as well as to reduce the brittleness of the product.
• a plasticizer is a material incorporated in a plastic to increase its workability and its flexibility or distensibility (i.e., elongation). This is achieved by lowering the glass transition temperature (“T g ”), thereby producing a change in properties from those of a hard, brittle, glasslike solid to those of a soft, flexible, tough material.
• T g glass transition temperature
• the vast majority of plasticizers used today are monomeric ester-types.
• Phthalates such as diisononyl phthalate, diisodecyl phthalate and di(2-ethylhexyl) phthalate (dioctyl phthalate, DOP) are well known and commonly used plasticizers. Further, plasticizers are usually added to PVC on hot rolls or in a hot mixer such as a Banbury. The plasticizer content varies widely depending on the end use of the material; however, typically plasticizer content will be approximately 5 to approximately 50% by weight.
• plasticizers When evaluating which plasticizers should be used for a particular application, the permanence of the plasticizer, in addition to miscibility with the PVC, is crucial. Permanence refers to the stability of plasticizer within the blend. More specifically, plasticizers, especially those with low molecular weights, tend to be migratory in that they tend to move to the surface of the blend where they subsequently evaporate and/or may be removed by soapy water, solvents, oils, etc. These problems are minimized by using high molecular weight polymers. Unfortunately, very high molecular weight polymers may present processing and compatibility problems, cause poor low temperature flexibility, and become costly.
• Copolymers of ethylene, carbon monoxide and a termonomer(s), such as vinyl acetate have been used as plasticizers in blends with PVC to produce flexible films, as well as, rigid and semi-rigid materials. These plasticizers are compatible with PVC, lower the T g and possess adequate permanence. However, while these plasticizers have proved to be effective, they are prepared using pure feeds of the individual monomers which can be costly. Hence, there is still a need to investigate other PVC plasticizers which are compatible with PVC and sufficiently lower the PVC resin's T g . Additionally, less expensive avenues to produce known plasticizers should also be pursued.
• the instant invention provides novel polyvinyl chloride compositions having CO-containing polymers which act as plasticizers.
• advantages of the instant invention include: lower plasticizer volatility and accompanying lower migration; lower cost than conventional monomeric plasticizers; improved processability and compatibility; and effective lowering of the PVC resin glass transition temperature (“T g ”).
• the invention is a PVC resin composition comprising polyvinyl chloride and a plasticizer wherein said plasticizer is selected from the group consisting of: i) a non-linear, paraffin-soluble olefin-CO copolymer; ii) a non-linear olefin-CO copolymer derived from non-pure feeds; iii) an olefin-CO-X terpolymer derived from non-pure feeds; and iv) a non-linear CO-X terpolymer; and mixtures thereof and wherein X is selected from the group consisting of free radically polymerizable vinyl monomers and mixtures thereof and wherein a non-pure feed comprises a first feed comprising olefins and a second feed comprising carbon monoxide and wherein when said polymer is (ii) and (iii) the amount of carbon monoxide and olefin combined in said non-pure feed
• the composition may further comprise a compound selected from the group consisting of dialkyl phthalate, dialkyl isophthalate, dialkyl terephthalate, trialkyl trimellitate, tetraalkyl pyromellitate, monoalkhyl benzoate, dialkyl azelate, dialkyl sebacate, dialkyl adipate, and mixtures thereof.
• a stabilizer or filler selected from the group consisting of calcium, barium, cadmium, zinc, lead, calcium carbonate, clay, and mixtures thereof.
• the invention is a product prepared from the PVC resin as described above wherein said product is selected from the group consisting of a film, a sheet, an extruded item, a molded item a cast item and mixtures thereof.
• the invention is a method for a preparing a PVC resin comprising blending polyvinyl chloride with a plasticizer selected from the group consisting of: i) a non-linear, paraffin-soluble olefin-CO copolymer; ii) a non-linear olefin-CO copolymer derived from non-pure feeds; iii) an olefin-CO-X terpolymer derived from non-pure feeds; and iv) a non-linear CO-X terpolymer; and mixtures thereof and wherein X is selected from the group consisting of free radically polymerizable vinyl monomers and mixtures thereof and wherein a non-pure feed comprises a first feed comprising olefins and a second feed comprising carbon monoxide and wherein when said polymer is (ii) and (iii) the amount of carbon monoxide and olefin combined in said non
• a plasticizer selected from
• This method may further comprise the step of blending a compound selected from the group consisting of dialkyl phthalate, dialkyl isophthalate, dialkyl terephthalate, trialkyl trimellitate, tetraalkyl pyromellitate, monoalkyl benzoate, dialkyl azelate, dialkyl sebacate, dialkyl adipate, and mixtures thereof.
• a non-pure feedstream is a feedstream comprising a first feed comprising olefins and a second feed comprising carbon monoxide where the amount of olefins and carbon monoxide combined is less than or equal to 95 mole %.
• the non-pure feed can be either a combination of the first and second feed or a co-feed of the first and second feed.
• the non-pure feeds it is possible for either of the first olefinic feed or the second CO feed to be a pure feed so long as once the feeds are combined, the amount of olefin in combination with CO is less than or equal to 95 mole %. Additionally, when the feed comprising CO contains ⁇ 90 mole is % CO, the remaining 90% of the feed will preferably comprise at least 90 mole % hydrogen. It is also, therefore, possible for each of the first olefinic feed and second CO feed to contain other components.
• the first olefinic feed may be a pure feed of vinyl monomers, including olefins
• the CO feed may comprise synthesis gas (“syngas”) or multi-component synthesis gas (“MCS”).
• the CO may originate from MCS feeds which contain at least one olefin, carbon monoxide, hydrogen, carbon dioxide, methane and optionally acetylene or paraffins.
• MCS feeds which contain at least one olefin, carbon monoxide, hydrogen, carbon dioxide, methane and optionally acetylene or paraffins.
• the first feed comprising olefins will contain C 3 to C 6 olefins or dienes. If the CO feedstream is not pure and contains components other than CO, it will typically contain up to 90-mole % CO, preferably up to 95-mole % CO
• CO-containing polymers are low molecular weight (“MW”) copolymers.
• Low MW means less than 50,000, preferably less than 30,000 and most preferably between about 200 to 30,000.
• copolymers includes terpolymers and other polymers having various combinations of different monomer units.
• polyvinyl chloride or “PVC” means homopolymers of vinyl chloride, as well as, copolymers thereof containing up to about 20% of other monomers including, but not limited to, vinyl acetate, propylene, ethylene, butyl vinyl ether, diethyl maleate, dimethyl fumarate, etc.
• CO feeds utilizable herein are described in U.S. Pat. No. 6,049,011 to Kiss et al.
• the feedstream comprising CO will be syngas or multicomponent syngas.
• the non-pure feeds will typically contain at least about 10% CO, preferably at least about 15% and at least about 50% olefin, preferable at least about 60%.
• the plasticizers of this invention may be synthesized using well known free radical polymerization techniques.
• the CO containing polymers are formed in free radical polymerization processes using organic peroxides as a free radical initiator according to conventional methods.
• Representative initiators include, but are not limited to, dialkyl peroxides such as ditertiary-butyl peroxide, 2,5-dimethyl-2, 5-ditertiary-butyl-peroxyhexane, dicumyl peroxide; alkyl peroxides such as tertiary-butyl hydroperoxide, tertiary-octyl hydroperoxide, cumene hydroperoxide; aroyl peroxides such as benzoyl peroxide; peroxy esters such as tertiary-butyl peroxypivalate, tertiary-butyl-perbenzoate; and compounds such as azo-bis-isobutyronitrile.
• Free radical initiators with an appropriate half-life at reaction temperatures ranging from about 50° C. to about 230° C. can be used. Of these, t-butyl peroxypivalate, which has a half-life of about 10 hours at 66° C., is preferred.
• Such feeds and initiators are useful for forming CO-containing polymers under copolymerization conditions at temperatures ranging from about 50 to about 230° C., preferably from about 50 to about 100° C., pressures ranging from about 100 to about 30,000 psig, preferably from about 100 to about 3,000 psig, and in the presence of a free radical initiator.
• co-polymer is used herein according to its broad meaning of a macromolecule formed from two or more momomer sources.
• polymer as used herein according to its broad meaning of a macromolecule formed from at least one monomer source.
• the reaction occurs in the presence of a solvent.
• suitable solvents include toluene, benzene, dioxane, pentane, heptane, hexane, propylene oxide, cyclohexane, etc. Hexane is preferred.
• the polymers and co-polymers utilized herein may be recovered using conventional methods, for example, filtration or evaporation of the diluent. They may be brought into the desired shape using standard forming techniques, such as cold or hot pressing. Alternatively, the polymerization is carried out in such a way that the copolymer is formed in the desired shape, such as by solution polymerization in a thin layer and subsequent removal of the diluent, which yields the co-polymer in the form of a film.
• the number average molecular weight (“Mn”) of the copolymers utilizable in accordance with the invention can range from about less than 50,000, preferably about 200 to about 30,000.
• Free radical polymerizable vinyl monomers include Vinyl monomers useful in the invention include styrene and styrene derivatives such as a-methylstyrene, p-methylstyrene, vinyl acetate, vinyl chloride, isobutyl vinyl ether, methyl vinyl ketone, 1-vinylpyrrolidone, acrylic acid, methacrylic acid, methylacrylate, methylmethacrylate, acrylonitrile, acrylamide, acrolein, allyl alcohol, allyl chloride, allyl acetate, mixtures thereof, and similar materials.
• Vinyl monomers useful in the invention include styrene and styrene derivatives such as a-methylstyrene, p-methylstyrene, vinyl acetate, vinyl chloride, isobutyl vinyl ether, methyl vinyl ketone, 1-vinylpyrrolidone, acrylic acid, methacrylic acid, methylacrylate, methylmethacryl
• the resulting non-linear copolymers may also be characterized as being non-alternating.
• the instant invention provides novel polyvinyl chloride compositions having CO-containing polymers which act as plasticizers. These CO-containing polymers are low molecular weight copolymers. Depending on the particular plasticizer(s) used and the type of PVC, percentage mix, etc., advantages of the instant invention include: lower plasticizer volatility; lower cost than conventional monomeric plasticizers; improved processability and compatibility; and effective lowering of the PVC resin glass transition temperature (“T g ”).
• composition of the invention is a PVC resin which contains a novel plasticizer. More specifically, the plasticizer is selected from the following:
• the composition may optionally contain, in addition to the plasticizers defined above, a dialkyl phthalate, or other suitable monomeric esters such as dialkyl isophthalates, dialkyl terephthalates, benzoates, trialkyl trimellitates, and the like.
• Preferred dialkyl phthalates are those having alkyl groups with approximately 4 to 20 carbons.
• the ratio of plasticizer to dialkyl phthalates will be in the range of 9:1 to 1:9 and the mix of these plasticizers will account for about 0.01 to 75 weight percent of the PVC resin composition.
• the polyvinyl chloride will make up approximately 25 to 99.99 weight percent of the PVC resin composition.
• the composition may also further comprise stabilizers, fillers, and/or other well-known additives that are commonly used in the art.
• Suitable stabilizers include, but are not limited to, calcium, barium, cadmium, zinc, lead and mixtures thereof.
• the stabilizers will make up approximately 0.01 to 7 weight percent of the PVC resin.
• Suitable fillers include, but are not limited to, calcium carbonate, clay and mixture thereof.
• fillers will be approximately 0.01 to 6 weight percent of the PVC resin.
• the invention is an article produced from the PVC resin composition described above.
• the PVC resin composition could be made into a film or a sheet. Articles can also be extruded, molded or cast from the PVC resin composition.
• a method for preparing a PVC resin comprising blending polyvinyl chloride with a plasticizer, as defined above.
• the method may further include the step of blending a dialkyl phthalate.
• stabilizers and/or fillers may also be blended.
• Standard PVC/plasticizer blending techniques well known to those skilled in the art, may be used such as adding the plasticizers to PVC on hot rolls or in a hot mixture such as a Banbury. Typical temperatures for such blending techniques are in the range of about 20 to 300° C. Preferred temperature ranges are from about 50 to 230° C. Typical pressures for these blending techniques can range widely from about 100 to 60000 psi.
• Preferred pressure ranges are in the range of about 100 to 30000 psi.
• Processing aids such as stearic acid, may optionally be used. Thus, small amounts of these processing aids may, or may not, become incorporated into the composition. Additionally, as illustrated in the examples below, the copolymer and terpolymers can be dissolved in organic solvents along with the PVC and then cast to form a film.
• CO containing polymers using a dilute MCS feed was synthesized according to free-radical polymerization techniques as follows:
• a 300 ml autoclave reactor was charged with 150 ml pure n-hexane and 0.6 g of a 75% solution of t-butyl peroxypivalate in mineral spirits.
• t-Butyl peroxypivalate has a 10 hour half-life at 55° C. in a 0.2 M benzene solution, Swem, Organic Peroxides , John Wiley and Sons, 1970, Vol. 1, pp. 82, 87).
• the reactor was sealed and purged with purified nitrogen.
• the reactor was then pressurized with the MCS mixture (ethylene 5.4 mole %, carbon monoxide 1.3 mole %, carbon dioxide 7.4 mole %, hydrogen 4.6 mole % and methane 81.3 mole %) to 700 psig.
• the temperature was raised to 66° C. while stirring and the pressure was maintained for 24 hours.
• the reactor was allowed to cool to room temperature and was then depressurized.
• the hexane was removed on a rotary evaporator to obtain the product.
• the product was characterized by IR, NMR and GPC.
• the FTIR spectrum of the product showed a very strong peak at 1715 cm ⁇ 1 due to carbonyl group, indicating incorporation of carbon monoxide in the product.
• the 13 C NMR of the product indicated that the polymer had 5.1% CO incorporation and a non-linear (branched) polyethylene structure, as indicated by a broad multiplet in the 13 C NMR for the alkyl region at 9-48 ppm and a multiplet at 206-218 for the CO resonance.
• the GPC of the product indicated a Mn of 320 and a Mw of 420.
• CO containing polymers using a dilute MCS as co-feed with 1-octene was synthesized according to free-radical polymerization techniques as follows:
• Example 2 The polymerization conditions were similar to those set forth in Example 1.
• a 300 ml autoclave reactor was charged with 150 ml pure n-hexane and 0.6 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. 20 g 1-octene was added in the reactor.
• the reactor was sealed and purged with purified nitrogen.
• the reactor was then pressurized with the MCS mixture (ethylene 5.4 mole %, carbon monoxide 1.3 mole %, carbon dioxide 7.4 mole %, hydrogen 4.6 mole % and methane 81.3 mole %) to 700 psig.
• the temperature was raised to 66° C. while stirring and the pressure was maintained for 24 hours.
• the reactor was allowed to cool to room temperature and was then depressurized.
• the hexane and unreacted octene was removed on a rotary evaporator to obtain the 2.9 g of product.
• the product was characterized by IR, NMR and GPC.
• the FTIR spectrum of the product showed a very strong peak at 1715 cm ⁇ 1 due to carbonyl group, indicating incorporation of carbon monoxide in the product.
• the GPC of the product indicated a Mn of 860 and a Mw of 1010.
• CO containing polymers using a dilute MCS as co-feed with vinyl acetate was synthesized according to free-radical polymerization techniques as follows:
• Example 2 The polymerization conditions were similar to those set forth in Example 1.
• a 300 ml autoclave reactor was charged with 150 ml pure n-hexane and 0.6 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. 2 g vinyl acetate was added in the reactor. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with the MCS mixture (ethylene 5.4 mole %, carbon monoxide 1.3 mole %, carbon dioxide 7.4 mole %, hydrogen 4.6 mole % and methane 81.3 mole %) to 700 psig. The temperature was raised to 66° C. while stirring and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and was then depressurized. The hexane and unreacted octene was removed on a rotary evaporator to obtain the 2.5 g of product.
• MCS mixture ethylene 5.4 mole %, carbon monoxide 1.3 mole
• the product was characterized by IR, NMR and GPC.
• the 13 C NMR of the product indicated that the polymer had 9 mole % CO, 56 mole % ethylene and 35 mole % vinyl acetate.
• the GPC of the product indicated a Mn of 730 and a Mw of 1620.
• CO containing polymers using a dilute MCS as co-feed with neo vinyl ester was synthesized according to free-radical polymerization techniques as follows:
• Example 2 The polymerization conditions were similar to those set forth in Example 1.
• a 300 ml autoclave reactor was charged with 150 ml pure n-hexane and 0.6 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. 5 g neo vinyl ester (ExxarTM Neo-10) was added in the reactor. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with the MCS mixture (ethylene 5.4 mole %, carbon monoxide 1.3 mole %, carbon dioxide 7.4 mole %, hydrogen 4.6 mole % and methane 81.3 mole %) to 700 psig. The temperature was raised to 66° C. while stirring and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and was then depressurized. The hexane and unreacted neo vinyl ester was removed initially on a rotary evaporator and then on Kugelrohr apparatus to obtain the 1.9 g of product.
• the 13 C NMR of the product indicated that the polymer had 4.6 mole % CO, 48 mole % ethylene and 47.4 mole % neo vinyl ester (ExxarTM Neo-10).
• the GPC of the product indicated a Mn of 1450 and a Mw of 2100.
• CO containing polymers using a dilute MCS as co-feed with neo vinyl ester was synthesized according to free-radical polymerization techniques as follows:
• Example 2 The polymerization conditions were similar to those set forth in Example 1.
• a 300 ml autoclave reactor was charged with 150 ml pure n-hexane and 0.6 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. 2 g neo vinyl ester (ExxarTM Neo-10) was added in the reactor. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with the MCS mixture (ethylene 5.4 mole %, carbon monoxide 1.3 mole %, carbon dioxide 7.4 mole % hydrogen 4.6 mole % and methane 81.3 mole %) to 700 psig. The temperature was raised to 66° C. while stirring and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and was then depressurized. The hexane and unreacted neo vinyl ester was removed initially on a rotary evaporator and then on Kugelrohr apparatus to obtain the product.
• MCS mixture
• the 13 C NMR of the product indicated that the polymer had 7.9 mole % CO, 55.6 mole % ethylene and 36.4 mole % neo vinyl ester (ExxarTM Neo-10).
• the GPC of the product indicated a Mn of 970 and a Mw of 1300.
• a 300 ml autoclave reactor was charged with 150 ml pure n-hexane and 0.6 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. 10 g 1-octene was added in the reactor. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with CO to 700 psig. The temperature was raised to 66° C. while stirring and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and was then depressurized. The hexane and unreacted octene was removed on a rotary evaporator to obtain the 1.38 g of product.
• the FTIR spectrum of the product showed a very strong peak at 1711 cm ⁇ 1 due to carbonyl group, indicating incorporation of carbon monoxide in the product.
• the 13 C NMR of the product indicated that the polymer had 27 mole % CO and 73 mole % 1-octene.
• the GPC of the product indicated a Mn of 965 and a Mw of 1175.
• films of the PVC resin were prepared as follows: 10 g PVC polymer (Aldrich, 233,000) was dissolved in 150 ml THF and the solution was stirred at room temperature for 24 hrs to obtain a stock solution. 2.5 ml of PVC solution was mixed with appropriate concentration of plasticizer (as THF solution) to give plasticizer content from 10 to 50%. The mixer was stirred for 12 hours at room temperature and the resultant solution poured on to horizontal aluminum or glass container. The solvent was allowed to evaporate slowly under nitrogen. After 12 hours the films were peeled away from the container. They were dried in a vacuum over at 50° C. for 12 hours. The flexibility of the films was compared by bending back and forth between the fingers; also their glass transition temperatures (“T g ”) were evaluated using a differential scanning calorimeter (“DSC”).
• T g glass transition temperatures
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with an ethylene and syngas mixture (ethylene:carbon monoxide:hydrogen 50:25:25, respectively). The temperature was raised to 66° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and then depressurized. The hexane was removed on a rotary evaporator, leaving 7.8 g of product.
• the IR spectrum of the product shows a very strong peak at 1705 cm ⁇ 1 due to the carbonyl group. Thus, CO has been incorporated in the product.
• the NMR of the product suggests that the polymer has 39.5% CO incorporation.
• the GPC of the product indicates a Mn of 1100 and Mw of 2300 (polystyrene standards, THF solvent).
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with an ethylene and syngas mixture (ethylene:carbon monoxide:hydrogen 70:15:15, respectively). The temperature was raised to 66° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and then depressurized. The hexane was removed on a rotary evaporator leaving 9.3 g of product.
• the IR spectrum of the product shows a very strong peak at 1709 cm ⁇ 1 due to the carbonyl group. Thus, CO has been incorporated in the product.
• the NMR of the product suggests that the polymer has 33.9% CO incorporation.
• the GPC of the product indicates a Mn of 1600 and Mw of 3200 (polystyrene standards, THF solvent).
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of t-butyl peroxide in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with an ethylene and syngas mixture (ethylene:carbon monoxide:hydrogen 70:15:15, respectively). The temperature was raised to 120° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and then depressurized. The hexane was removed on a rotary evaporator leaving 4.3 g of product.
• the IR spectrum of the product shows a very strong peak at 1711 cm ⁇ 1 due to the carbonyl group. Thus, CO has been incorporated in the product.
• the NMR of the product suggests that polymer had 19.3% CO incorporation.
• the GPC of the product indicates a Mn of 590 and Mw of 1100 (polystyrene standards, THF solvent).
• films of the polymers were prepared as follows: 10 g PVC polymer (Aldrich, 233,000) were dissolved in 150 ml THF and the solution was stirred at room temperature for 24 hours to obtain a stock solution. Then 2.5 ml of PVC solution were mixed with an appropriate concentration of plasticizer (as THF solution, sometimes hot THF solution) to give plasticizer content from 10 to 50%. The solvent was allowed to evaporate under nitrogen. After 12 hours the films were peeled away from the container. They were dried in a vacuum oven at 50° C. for 12 hours. Film flexibility was compared by bending the films back and forth between the fingers; also, their T g was evaluated.
• plasticizer as THF solution, sometimes hot THF solution
• Table 2 shows the decrease in the T g of PVC upon addition of various levels of ethylene-CO copolymers.
• the commercial plasticizer ditridecyl phthalate (DTDP) is also plotted as a reference.
• TABLE 2 Effect of ethylene-CO plasticizers on the Tg of PVC Plasticizer Tg of Tg of PVC + Tg of PVC + Tg of PVC + Concentra- PVC + ECO polymer ECO polymer ECO polymer tion (wt %) DTDP of Example 8 of Example 9 of Example 10 0 82 82 82 82 10 60 63 61 52 20 43 47 46 34 30 27 29 33 21 40 — — 27 13 50 10 — — 4
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with ethylene and syngas mixture (ethylene:carbon monoxide:hyrdrogen 70:15:15, respectively). Then 10.8 g of 1-butene was added, the temperature was raised to 66° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and then depressurized. The hexane was removed on a rotary evaporator, leaving 4.9 g of the product.
• the IR spectrum of the product shows a very strong peak at 1711 cm ⁇ 1 due to the carbonyl group.
• CO has been incorporated in the product.
• the NMR of the product suggests that the polymer has 25.8% CO incorporation.
• the NMR spectrum of the terpolymer suggested that it has 134.9 branches per 1000 carbons versus 65.5 branches per 1000 carbons for a control experiment without 1-butene termonomer. This observation indicates that increased in branching may result from alpha-olefin incorporation in the polymer.
• the GPC of the product indicates a Mn of 1000 and Mw of 2000 (polystyrene standards, THF solvent).
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with an ethylene and syngas mixture (ethylene:carbon monoxide:hydrogen 70:15:15, respectively). Then 5.9 g of 1-butene was added, the temperature was raised to 66° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and then depressurized. The hexane was removed on a rotary evaporator leaving 7.0 g of the product.
• the IR spectrum of the product showed a very strong peak at 1711 cm ⁇ 1 due to the carbonyl group. Thus, CO has been incorporated in the product.
• the NMR of the product suggested that the polymer had 29.6% CO incorporation.
• the NMR spectrum of the terpolymer suggested that it has 101 branches per 1000 carbons versus 65.5 branches per 1000 carbons obtained in a control experiment without the 1-butene termonomer. This observation indicates that increased branching may result from alpha-olefin incorporation in the polymer.
• the GPC of the product indicates a Mn of 500 and Mw of 1000 (polystyrene standards, THF solvent).
• a 300-mL autoclave engineer's reactor was charged with 150-mL pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with an ethylene and syngas mixture (ethylene:carbon monoxide:hydrogen 70:15:15, respectively). Then 5.9 g of propylene was added, the temperature was raised to 66° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and was then depressurized. The hexane was removed on a rotary evaporator, leaving 7.6 g of the product.
• the IR spectrum of the product showed a very strong peak at 1711 cm ⁇ 1 due to the carbonyl group. Thus, CO has been incorporated in the product.
• the NMR of the product suggested that the polymer had 17.5% CO incorporation.
• the NMR spectrum of the terpolymer suggested that it has 72.8 branches per 1000 carbons versus 65.5 branches per 1000 carbons obtained in a control experiment without the propylene termonomer. This observation indicates that increased branching may result from alpha-olefin incorporation in the polymer.
• the GPC of the product indicated a Mn of 500 and Mw of 1000 (polystyrene standards, THF solvent).
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with an ethylene and syngas (ethylene:carbon monoxide:hydrogen 70:15:15, respectively) mixture. Then 10.8 g of 2-butene was added, the temperature was raised to 66° C. while stirring, and the pressure was maintained for 24 hours. The reactor was allowed to cool to room temperature and then depressurized. The hexane was removed on a rotary evaporator, leaving 6.7 g of the product.
• ethylene and syngas ethylene:carbon monoxide:hydrogen 70:15:15, respectively
• the IR spectrum of the product showed a very strong peak at 1711 cm ⁇ 1 due to the carbonyl group. Thus, CO has been incorporated in the product.
• the NMR of the product suggested that the polymer had 18.2% CO incorporation.
• the NMR spectrum of the terpolymer suggested that it has 93.2 branches per 1000 carbons versus 65.5 branches per 1000 carbons obtained in a control experiment without 2-butene termonomer. This observation indicates that increased branching may result from alpha-olefin incorporation in the polymer.
• the GPC of the product indicated a Mn of 590 and Mw of 1120 (polystyrene standards, THF solvent).
• films of the polymers were prepared as follows: 10 g PVC polymer (Aldrich, 233,000) were dissolved in 150 ml THF and the solution was stirred at room temperature for 24 hours to obtain a stock solution. Then 2.5 ml of PVC solution was mixed with an appropriate concentration of plasticizer (as THF solution, sometimes hot THF solution) to give a plasticizer content from 10 to 50%. The solvent was allowed to evaporate under nitrogen. After 12 hours the films were peeled away from the container. They were dried in a vacuum oven at 50° C. for 12 hours. Film flexibility was compared by bending the films back and forth between the fingers; also, their T g was evaluated.
• plasticizer as THF solution, sometimes hot THF solution
• Table 3 shows the decrease in the T g of PVC upon addition of various levels of these terpolymers.
• the commercial plasticizer, di-tridecyl phthalate (DTDP) is also plotted as a reference.
• TABLE 3 Effect of ethylene-CO-alpha-olefin plasticizers on the Tg of PVC Tg of PVC + Tg of PVC + Tg of PVC + Tg of PVC + Plasticizer Tg of terpolymer terpolymer terpolymer terpolymer terpolymer terpolymer terpolymer terpolymer terpolymer terpolymer Concentra- PVC + of Example of Example of Example of Example tion (wt %) DTDP 12 13 14 15 0 82 82 82 82 82 10 60 55 63.66 63.25 64.16 20 43 42 50.79 48.07 51.12 30 27 31 40.91 41.1 39.9 40 — 25 31.7 29.7 50 10 20 28
• the instant invention provides compatible CO-containing platsticizers for use with PVC. More specifically, the PVC resins of the instant invention have decreased T g . Additionally, the compositions produced in the non-limiting examples showed no evidence of phase separation which suggests adequate compatibility. Finally, the instant invention can be synthesized using relatively inexpensive non-pure fees such as syngas and MCS. Hence, the desirable characteristics (e.g., low Tg, compatibility and lower cost) discussed in the background section are satisfied by the instant invention.
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.5 g of t-butyl peroxide. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with ethylene and carbon monoxide (80:20) mixture. The temperature was raised to 120° C. while stirring, and the pressure was maintained at 700 psig for 24 hours. The reactor was allowed to cool to room temperature and depressurized. Hexane was removed using a rotary evaporator, leaving 6.91 g of the product.
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.5 g of t-butyl peroxide. The reactor was sealed and purged with purified nitrogen. The reactor was then pressurized with ethylene and syngas (ethylene:carbon monoxide:hydrogen 70:15:15, respectively) mixture. The temperature was raised to 120° C. while stirring, and the pressure was maintained at 700 psig for 24 hours. The reactor was allowed to cool to room temperature and depressurized. Hexane was removed using a rotary evaporator, leaving 4.3 g of the product.
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.5 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. 4.89 g of 1-butene was added into stainless steel addition vessel and attached to the reactor. The reactor was then pressurized with syngas (carbon monoxide:hydrogen 50:50) mixture to 700 psig. The temperature was raised to 66° C. while stirring. The butene was then introduced into the reactor from the addition vessel and the pressure was maintained at 700 psig for 24 hours. The reactor was allowed to cool to room temperature and depressurized.
• syngas carbon monoxide:hydrogen 50:50
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. 5.93 g of 1-butene was added into stainless steel addition vessel and attached to the reactor. The reactor was then pressurized with ethylene and syngas (ethylene:carbon monoxide:hydrogen 70:15:15, respectively) mixture. The temperature was raised to 66° C. while stirring. The butene was then introduced into the reactor from the addition vessel and the pressure was maintained at 700 psig for 24 hours. The reactor was allowed to cool to room temperature and depressurized. Hexane was removed using a rotary evaporator, leaving 7.01 g of the product.
• NMR of the product suggested that the polymer had 29.6% CO incorporation.
• the NMR also suggested that there are 101 branches/1000C.
• GPC of the product indicated a Mn of 500 and Mw of 1000 (polystyrene standards, THF solvent).
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. 10.172 g of 1-butene was added into stainless steel addition vessel and attached to the reactor. The reactor was then pressurized with carbon monoxide to 350 psig and the temperature was raised to 66° C. while stirring. The butene was then introduced into the reactor from the addition vessel and the pressure was increased with carbon monoxide to 700 pisg and maintained at 700 psig for 24 hours. The reactor was allowed to cool to room temperature and depressurized. Hexane was removed using a rotary evaporator, leaving 1.4 g of the product.
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. 10.682 g of propylene was added into stainless steel addition vessel and attached to the reactor. The reactor was then pressurized with carbon monoxide to 350 psig and the temperature was raised to 66° C. while stirring. The propylene was then introduced into the reactor from the addition vessel and the pressure was increased with carbon monoxide to 700 pisg and maintained at 700 psig for 24 hours. The reactor was allowed to cool to room temperature and depressurized. Hexane was removed using a rotary evaporator, leaving 1.5 g of the product.
• a 300-mL autoclave engineer's reactor was charged with 150 ml pure n-hexane and 0.64 g of a 75% solution of t-butyl peroxypivalate in mineral spirits. The reactor was sealed and purged with purified nitrogen. 10.475 g of RAF II mixture (mole % cis 2-butene: 17%, trans 2-butene 17%, Isobutylene 5.51%, 1,3-butadiene 5237 ppm and remaining 1-butene) was added into stainless steel addition vessel and attached to the reactor. The reactor was then pressurized with carbon monoxide to 350 psig and the temperature was raised to 66° C. while stirring.
• the RAF II was then introduced into the reactor from the addition vessel and the pressure was increased with carbon monoxide to 700 pisg and maintained at 700 psig for 24 hours.
• the reactor was allowed to cool to room temperature and depressurized. Hexane was removed using a rotary evaporator, leaving 1.33 g of the product.

Landscapes

• Chemical & Material Sciences (AREA)
• Health & Medical Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Medicinal Chemistry (AREA)
• Polymers & Plastics (AREA)
• Organic Chemistry (AREA)
• Compositions Of Macromolecular Compounds (AREA)
• Polyethers (AREA)
• Processes Of Treating Macromolecular Substances (AREA)
• Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
• Manufacture Of Macromolecular Shaped Articles (AREA)

Priority Applications (4)

Applications Claiming Priority (2)

Related Parent Applications (1)

Related Child Applications (1)

Publications (1)

Family

ID=24476667

Family Applications (2)

Family Applications After (1)

Country Status (12)

Cited By (2)

Families Citing this family (15)

Family Cites Families (5)

• 2001
  • 2001-06-15 US US09/882,414 patent/US20020042475A1/en not_active Abandoned
  • 2001-06-26 AU AU2001271471A patent/AU2001271471A1/en not_active Abandoned
  • 2001-06-26 BR BR0112549-4A patent/BR0112549A/pt not_active Application Discontinuation
  • 2001-06-26 KR KR10-2003-7000671A patent/KR20030066584A/ko not_active Application Discontinuation
  • 2001-06-26 EP EP01950484A patent/EP1355983A2/en not_active Withdrawn
  • 2001-06-26 JP JP2002512294A patent/JP2004508429A/ja active Pending
  • 2001-06-26 WO PCT/US2001/020288 patent/WO2002006395A2/en active Application Filing
  • 2001-06-26 MX MXPA03000234A patent/MXPA03000234A/es not_active Application Discontinuation
  • 2001-06-26 CA CA002416514A patent/CA2416514A1/en not_active Abandoned
  • 2001-07-16 TW TW090117372A patent/TW555806B/zh not_active IP Right Cessation
  • 2001-07-17 AR ARP010103423A patent/AR030568A1/es unknown
• 2002
  • 2002-09-10 US US10/238,172 patent/US6750278B2/en not_active Expired - Fee Related
• 2003
  • 2003-01-17 NO NO20030242A patent/NO20030242L/no not_active Application Discontinuation

Also Published As

Similar Documents

Legal Events