Patent Application
20210171678
The present invention relates to poly(alpha-olefin) plasticizers and plasticized polymers comprising such poly(alpha-olefin) plasticizers.
Polyolefins are used for making a wide variety of products. However, one drawback of some polyolefins is their relatively high glass transition temperature (Tg). Polypropylene homopolymers and copolymers are particularly problematic in this respect. This high Tg may result in materials that are difficult to process and which may be brittle, especially at low temperatures. Also, for many products, high molecular weight polyolefins are required to provide the desired polymer properties. High molecular weight polyolefins can be even more difficult to process, due to their high melt viscosities.
As a result, there is a need to provide polymers with good processability that are also able to maintain their advantageous properties over time when exposed to a wide temperature range. One important property for such polymers is low-temperature toughness which should be improved while still providing a polymer that maintains its properties upon exposure to elevated temperatures over time.
Addition of a plasticizer to a polyolefin is known to improve properties such as impact strength and processability. Such plasticizers are often used to lower the Tg of the polymer. Lowering the Tg of the polymer can improve the processability and low temperature impact toughness of the polymer and reduce the tendency of the polymer to become brittle at low temperatures. In order to achieve this combination of advantages, the plasticizer should have the ability to maintain its viscosity at low temperature. Some plasticizers have a tendency to crystallize or form structure in the plasticizer at low temperatures leading to an undesirable increase in viscosity of the plasticizer. This may result in an adverse impact on the low temperature impact toughness of a polymer plasticized with this plasticizer by causing the polymer to become brittle.
Many plasticized polymers also suffer from problems such as blooming or diffusion of plasticizer to the surface of the polymer, or even volatilization of the plasticizer from the polymer, each resulting in long-term deterioration of polymer properties. As a result, plasticizers are sought which have a relatively low pour point and thus can impart the advantageous lowering of the Tg of the polymer discussed above while at the same time ensuring that the polymer retains its advantageous properties over time, particularly when exposed to high temperatures. In order to achieve this, the volatility or tendency of the plasticizer to diffuse to the surface of the polymer must be balanced with the lowering of the Tg of the polymer. One way to reduce the volatility of the plasticizer is to increase its number average molecular weight. However, increasing the number average molecular weight can have an adverse influence on the Tg of the plasticized polymer and the processability of the polymer.
Plasticizers having lower number-average molecular weights (Mn) tend to be better at lowering the Tg of the polymer since the Tg of the polymer tends to be inversely proportional to the Mg of the plasticizer. However, as the number-average molecular weight (Mn) of the plasticizer decreases, the plasticization durability of the properties imparted by the plasticizer to the polymer is adversely affected, especially when exposed to high temperatures. This is at least partially due to the increased tendency of the plasticizer to migrate to the surface of the polymer and/or volatilize. Thus, improved plasticizers are sought that have the ability to lower the Tg of a polymer without lowering the number average molecular weight of the plasticizer.
Another key aspect for selection of an appropriate plasticizer is the chemical compatibility of the plasticizer with the polymer. To achieve this goal, it is desirable to employ plasticizers that are chemically similar to the polymer that is being plasticized. This will enhance the chemical compatibility between the plasticizer and the polymer. For this purpose, polyalphaolefins (PAOs) have been proposed for use as polyolefin plasticizers.
Such PAOs are typically oligomers of olefins having five or more carbon atoms. In some cases, such oligomers with five or more carbon atoms may be copolymerized with ethylene to C4 olefins to reduce the pour point of the plasticizer. US 2004/054040 and WO 2004/014997 disclose PAO plasticizers having a weight average molecular weight (Mw) in the range of 100 to 20,000 g/mol. and a kinematic viscosity at 100° C. (KV100) of 0.1 to 3,000 cSt.
US 2004/106723 and WO 2004/014998 disclose plasticizers having a KV100 of 10 cSt or more and a viscosity index (VI) of 100 or more. These plasticizers include oligomers of C5 to C14 olefins. U.S. Pat. No. 4,536,537 discloses PAO plasticizers having a kinematic viscosity at 38° C. of about 2 to 6 cSt. WO 98/044041, WO 2002/018487 and WO 2003/048252 disclose PAO plasticizers having a KV100 of about 4 to 8 cSt.
WO 2009/020706 discloses plasticizers that are regularly branched PAO oligomers of one or more C2-C20 alpha-olefins having a KV100 of 3 to 3,000 cSt, a branching irregularity index (‘BII’) of 0.40 or less, and a molar-average carbon number (CLAO) of 6 to 14. Preferably, the regularly branched PAOs have a Mw/Mn of less than 2.3. Polyolefins plasticized with the regularly branched PAOs are said to have a reduced volatility as measured by thermogravimetric analysis, compared to comparable polyolefin compositions plasticized with conventional PAOs, or a reduced glass transition temperature (Tg) of the composition compared to comparable polyolefin compositions plasticized with conventional PAOs.
PAO plasticizers are typically prepared by olefin isomerization which results in oligomers having a variety of different structures caused by, for example, irregular branching. According to the present invention, it has now been found that PAOs having certain characteristics indicative of their structure can provide an improved combination of plasticization efficiency and plasticization durability of the properties imparted by the plasticizers when used in polyolefins.
The present invention generally relates to copolymers that include ethylene units and units of one or more C3-10 alpha-olefins, wherein the copolymer has a number average molecular weight of less than 5,000 g/mol as measured by GPC using polystyrene as a calibration reference; the ethylene unit content of the copolymer is less than 80 mol %, as measured by 1H-NMR spectroscopy; wherein the copolymer has a terminal unsaturation of 70 mol % or greater, as measured by 13C-NMR spectroscopy, and at least 70 mol % of the terminal unsaturation is terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene or any combination thereof, as measured by 1H-NMR spectroscopy, and wherein C2,Actual<
C2,Statistical.
The foregoing copolymer may have a crossover temperature of −20° C. or lower.
Each of the foregoing copolymers may have an average ethylene run length (C2,Actual) which is less than 2.8 or less than 2.6, as determined by 13C NMR spectroscopy, the average ethylene run length nc2,Actual is defined as the total number of ethylene-derived units in the copolymer divided by a number of runs of one or more sequential ethylene-derived units in the copolymer, and the average ethylene run length nc2 also satisfies the relationship shown by the expression below:
wherein C2,Actual<
C2,Statistical.
The present invention also generally relates to copolymers that include ethylene units and units of one or more C3-10 alpha-olefins, wherein the copolymer has a number average molecular weight of less than 5,000 g/mol as measured by GPC using polystyrene as a calibration reference; the ethylene unit content of the copolymer is less than 80 mol %, as measured by 1H-NMR spectroscopy; wherein the copolymer has a terminal unsaturation of 70 mol % or greater, as measured by 13C-NMR spectroscopy, and at least 70 mol % of the terminal unsaturation is terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene or any combination thereof, as measured by 1H-NMR spectroscopy, and wherein C2Actual<
C2,Statistical.
The foregoing copolymer may have an average ethylene run length (C2Actual) which is less than 2.8 or less than 2.6, as determined by 13C NMR spectroscopy, the average ethylene run length nc2Actual is defined as the total number of ethylene-derived units in the copolymer divided by a number of runs of one or more sequential ethylene-derived units in the copolymer, and wherein
C2Actual<
C2,Statistical. This copolymer may have a crossover temperature of −20° C. or lower.
In each of the foregoing embodiments, the ethylene unit content of the copolymer may be less than 70 mol %, or less than 65 mol %, or less than 60 mol %., or less than 55 mol %, or less than 50 mol %, or less than 45 mol %, or less than 40 mol %. In each of the foregoing embodiments, the ethylene unit content of the copolymer may be at least 10 mol % and less than 80 mol %, or at least 20 mol % and less than 70 mol %, or at least 30 mol % and less than 65 mol %, or at least 40 mol % and less than 60 mol %.
In each of the foregoing embodiments, the C3-C10 alpha-olefin unit content of the copolymer may be at least 20 mol %, or at least 30 mol %, or at least 35 mol %, or at least 40 mol %, or at least 45 mol %, or at least 50 mol %, or at least 55 mol %, or at least 60 mol %.
In each of the foregoing embodiments, at least 75 mol % of the copolymer may have terminal unsaturation selected from terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene and any combination thereof, or at least 80 mol % of the copolymer may have terminal unsaturation selected from terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene and any combination thereof, or at least 85 mol % of the copolymer may have terminal unsaturation selected from terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene and any combination thereof, or at least 90 mol % of the copolymer may have terminal unsaturation selected from terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene and any combination thereof, or at least 95 mol % of the copolymer may have terminal unsaturation selected from terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene and any combination thereof.
In each of the foregoing embodiments, the copolymer may have an average ethylene run length of less than 2.6, or less than 2.4, or less than 2.2, or less than 2.
In each of the foregoing embodiments, the crossover temperature of the copolymer may be −25° C. or lower, or −30° C. or lower, or −35° C. or lower, or −40° C. or lower.
In each of the foregoing embodiments, the copolymer may have a polydispersity index of less than or equal to 4, or less than or equal to 3, or less than or equal to 2.
In each of the foregoing embodiments, the C3-C10 alpha-olefin units may include propylene units.
In each of the foregoing embodiments, the number average molecular weight of the copolymer may be less than 4,000 g/mol, or less than 3,500 g/mol, as measured by GPC or less than 3,000 g/mol, or less than 2,500 g/mol, or less than 2,000 g/mol, or less than 1,500 g/mol, or less than 1,000 g/mol. In each of the foregoing embodiments, the number average molecular weight of the copolymer may be between 500 and 3,000 g/mol or 800 and 3,000 g/mol, as measured by GPC.
In each of the foregoing embodiments, less than 20% of unit triads in the copolymer are ethylene-ethylene-ethylene triads, or less than 10% of unit triads in the copolymer are ethylene-ethylene-ethylene triads, or less than 5% of unit triads in the copolymer are ethylene-ethylene-ethylene triads.
In each of the foregoing embodiments, the terminal vinylidene and the tri-substituted isomers of the terminal vinylidene of the copolymer have one or more of the following structural formulas (I)-(III):
wherein R represents a C1-C8 alkyl group and “
” indicates the bond is attached to the remaining portion of the copolymer.
In each of the foregoing embodiments, the copolymer may have a total Zr, Ti, Al, and B content of 25 ppmw or less, based on the total weight of the copolymer, wherein the Zr, Ti, Al, and B is derived from a single-site catalyst and an optional co-catalyst. In the foregoing embodiment, the copolymer may have a total Zr, Ti, Al and B content of 10 ppmw or less, or 5 ppmw or less, or 1 ppmw or less, based on the total weight of the copolymer, wherein the Zr, Ti, Al, and B is derived from a single-site catalyst and an optional co-catalyst.
In each of the foregoing embodiments, the copolymer may have a fluorine content of less than 10 ppmw, or less than 8 ppmw, or less than 5 ppmw, based on the total weight of the copolymer.
The present invention relates to ethylene-C3-C10 alpha-olefin copolymers and addition of such copolymers to one or more polyolefins in order to produce a blend with improved properties as compared to the unmodified polyolefin(s). Copolymers with certain characteristics may be employed to provide a better combination of properties in a plasticized polyolefin than conventional PAO plasticizers.
Various embodiments will now be described in greater detail below, including specific embodiments, versions and examples, but the inventions are not limited to these embodiments, versions or examples, which are included to enable a person having ordinary skill in the art to make and use the inventions, when the information in this patent is combined with available information and technology.
The following definitions are made for purposes of this invention and the claims thereto.
When a polymer or copolymer is referred to as comprising an ethylene unit or an olefin unit, the ethylene or olefin unit present in the polymer or copolymer is the polymerized or oligomerized form of the ethylene or olefin, respectively. The term, “polymer” is meant to encompass homopolymers and copolymers. The term, “copolymer” includes any polymer having two or more units from different monomers in the same chain, and encompasses random copolymers, statistical copolymers, interpolymers, and block copolymers. When a copolymer is said to comprise a certain percentage of an ethylene or olefin unit, that percentage is based on the total amount of units in the copolymer components.
A “polyolefin” is a polymer comprising at least 50 mol % of one or more olefin monomers. Preferably, a polyolefin comprises at least 60 mol %, or at least 70 mol %, or at least 80 mol %, or at least 90 mol %, or at least 95 mol %, or 100 mol % of one or more olefin monomers. Preferably, the olefin monomers are selected from ethylene to ethylene olefins, or ethylene to C16 olefins, or ethylene to C10 olefins. More preferably the olefin monomers are selected from ethylene, propylene, 1-butene, 1-hexene, and 1-octene. Polyolefins may also comprise up to 50 mol % of one or more diene monomers.
The nomenclature “Cx” where x is an integer means there are “x carbons” in the compound; for example, a “C5 alpha-olefin” is an alpha-olefin with 5 carbon atoms.
For purpose of this invention and the claims thereto, unless otherwise noted, physical and chemical properties described herein are measured using the test methods described under the Experimental Methods section.
In one aspect, there is disclosed copolymers of ethylene and C3-C10 alpha-olefins that are suitable for use as plasticizers, particular for plasticizing polyolefins.
The copolymers described herein contain a plurality of ethylene units and a plurality of one or more C3-C10 alpha-olefin units. Exemplary alpha-olefin units include propylene, butane, pentene, hexene, heptane, octene, nonene and decene units. Thus, the carbon number of each alpha-olefin unit may be 3, 4, 5, 6, 7, 8, 9, or 10. The alpha-olefin units may be derived from monomers such as, for example, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene or 1-decene.
An ethylene unit generally refers to an —CH2CH2— unit within a copolymer chain. Ethylene units result from copolymerization of ethylene monomers. Alpha-olefin units generally refer to a unit such as the propylene unit —CH2CH2CH2— and similarly result from copolymerization of alpha-olefin monomers. The term “olefin” is given its ordinary meaning in the art, e.g., referring to a family of organic compounds which are alkenes having the chemical formula CxH2x, where x is the carbon number, and wherein the alkenes have a double bond within their structure. The term “alpha-olefin” is given its ordinary meaning in the art and refers to olefins having a double bond within their structure at the primary or alpha position.
One important characteristic of the copolymer described herein is the crossover temperature or onset temperature of the copolymer. The copolymer is generally viscoelastic; in other words, its mechanical properties are between those of a purely elastic solid and those of a purely viscous liquid. The viscoelastic behavior of the copolymer may be characterized as the combination of an elastic portion (referred to as either an elastic modulus or a storage modulus), and a viscous portion (referred to as either a viscous modulus or a loss modulus). The values of these moduli are used to characterize the viscoelastic properties of the copolymer at a given temperature. Both the storage modulus and the loss modulus are dependent on temperature, although each may change at a different rate as a function of temperature. Thus, the copolymer may exhibit more elasticity or more viscosity, depending on the temperature. The crossover temperature is defined herein as the temperature at which the storage modulus equals the loss modulus. The crossover temperature may also be referred to as the onset temperature.
Oscillatory rheology is a technique that may be used to determine values (generally expressed in units of pressure) for the storage modulus and loss modulus. The basic principle of an oscillatory rheometer is to induce a sinusoidal shear deformation in the sample (e.g., a sample of copolymer) and measure the resultant stress response. In a typical experiment, the sample is placed between two plates. While the top plate remains stationary, a motor rotates the bottom plate, thereby imposing a time dependent strain on the sample. Simultaneously, the time dependent stress is quantified by measuring the torque that the sample imposes on the top plate.
Measuring this time dependent stress response reveals characteristics about the behavior of the material. If the material is an ideal elastic solid, then the sample stress is proportional to the strain deformation, and the proportionality constant is the shear modulus of the material. In this case, the stress is always exactly in phase with the applied sinusoidal strain deformation. In contrast, if the material is a purely viscous fluid, the stress in the sample is proportional to the rate of strain deformation, where the proportionality constant is the viscosity of the fluid. In this case, the applied strain and the measured stress are out of phase.
Viscoelastic materials show a response that contains both in-phase and out-of-phase contributions. These contributions reveal the extents of solid-like and liquid-like behavior. A viscoelastic material will show a phase shift with respect to the applied strain deformation that lies between that of solids and liquids. These can be decoupled into an elastic component (the storage modulus) and a viscosity component (the loss modulus). The viscoelastic behavior of the system can thus be characterized by the storage modulus and the loss modulus, which respectively characterize the solid-like and fluid-like contributions to the measured stress response.
As mentioned above, the values of the storage modulus and loss modulus are temperature dependent. At warmer temperatures, the value of the loss modulus for the copolymer is greater than the value of the storage modulus. However, as the temperature decreases, the copolymer may behave more like an elastic solid, and the degree of contribution from the storage modulus approaches that from the loss modulus. As the temperature lowers, eventually, at a certain temperature the storage modulus of the copolymer crosses over the loss modulus and becomes the predominant contributor to the viscoelastic behavior of the copolymer. According to one or more embodiments, a lower crossover temperature of the copolymer correlates to better low temperature performance of oils into which the copolymer is incorporated.
According to one or more embodiments, the copolymer may have a crossover temperature of −20° C. or lower, −25° C. or lower, −30° C. or lower, −35° C. or lower, −40° C. or lower, −50° C. or lower, −60° C. or lower, or −70° C. or lower as determined by oscillatory rheometry. Other values are also possible. An advantageous crossover temperature for the copolymer may be achieved through controlling characteristics of the copolymer during its manufacture. One such characteristic is an average ethylene run length in the copolymer.
According to one or more embodiments, the sequence of the ethylene-derived units and C3-C10 alpha-olefin-derived units within the copolymer may be arranged in such a way as to provide good low temperature performance. One important characteristic of the arrangement of the ethylene and C3-C10 alpha-olefin units is the average ethylene run length. The sequential arrangement of the different units may be characterized by an “average ethylene run length” As used herein, “average ethylene run length” refers to the average ethylene-derived unit run length incorporated into the copolymer. The average ethylene-derived unit run length nc2 is defined as the total number of ethylene-derived units in the copolymer divided by a number of runs of one or more sequential ethylene-derived units in the copolymer. Thus, the average ethylene run length is an average of the number of ethylene units in each sequence of ethylene units in the copolymer. For example, in the sequence of units C3-C10 alpha-olefin-ethylene-ethylene-C3-C10 alpha-olefin the ethylene unit run length is two since there are two ethylene units in the run of ethylene units of this sequence. Thus, in a copolymer having the following two sequences (A) and (B), the ethylene unit run lengths are 2 and 3, respectively and the average ethylene run length is 2.5: (A) C3-C10 alpha-olefin-ethylene-ethylene-C3-C10 alpha-olefin, and (B) C3-C10 alpha-olefin-ethylene-ethylen-ethylene-C3-C10 alpha-olefin. In a copolymer molecule comprising a chain of ethylene and C3-C10 alpha-olefin units, the units are not distributed uniformly within the copolymer chain. The average ethylene run length may be determined by dividing the total number of ethylene-derived units by the number of ethylene unit runs in the copolymer. For example, a copolymer having a total of four ethylene units and three runs of ethylene units has an average ethylene run length of 4/3=1.33.
Methods for determining values of the average ethylene run length are known in the art and comprise established spectroscopic procedures using 13C nuclear magnetic resonance methods as described, for example, in “Carbon-13 NMR in Polymer Science,” ACS Symposium Series 103, American Chemical Society, Washington, D.C. 1978 at p. 97 and in “Polymer Sequence Determination Carbon-13 NMR Method,” J. C. Randall, Academic Press, New York, N.Y. at p. 53.
For example, the average ethylene run length (nC2,Actual) may be calculated by measuring the triad distribution in the copolymer. The “triad distribution” refers to the statistical distribution of the possible combinations of three subunits in a row in the copolymer chain. Taking as an example an ethylene-propylene copolymer, where “E” represents an ethylene unit and “P” represents a propylene-derived unit, the potential combinations of unit triads are: EEE, EEP, PEE, PEP, EPE, PPE, and PPP. According to one or more embodiments, the percentage of EEE units based on the total number of unit triads in the copolymer is preferably less than 20%, less than 10%, or less than 5%. The percentage of EEE units is indicative of a relatively short C2,Actual.
The method used for calculating the triad distribution of ethylene-propylene copolymers is described in J. C. Randall JMS-Review Macromolecules Chem Physics C29, 201 (1989) and E. W. Hansen, K. Redford Polymer Vol. 37, No. 1, 19-24 (1996). After collecting 13C(1H) NMR data under quantitative conditions, eight regions (A-H), shown in Table 1 are integrated. The equations of Table 2 are applied and the values normalized. For the examples described herein, the D, E, and F regions were combined due to peak overlap in the NMR spectra. The symbol “k” represents a normalization constant and T=the total intensity.
The calculated mole fractions of the EEE, EAE, AEE, EEA, and AEA triads are entered into Equation 5 in order to obtain c2,Actual. When measurements and calculations from an ethylene-propylene copolymer are used in Equation 5, AEE is PEE, EEA is EEP, and AEA is PEP.
The copolymers herein must have c2,Actual less than 2.8. However, not only must the copolymers herein have
C2,Actual less than 2.8, but the copolymers must also satisfy the relationship below:
z,44c2,Actual<C2,Statistical.
Where the arrangement of the units in the copolymer chains is purely random, each unit has a chance of appearing in a certain position proportional to the remaining molar percentage of the monomer corresponding to that unit that is present in the monomer mixture, regardless of whether the immediately preceding unit is the same or different. Thus, an expected average ethylene run length for a purely random unit distribution can be calculated as a function of the molar percentage of ethylene monomer. This value is referred to herein as the statistically-expected random average ethylene run-length (C2,Statistical).
According to one or more embodiments, the copolymer may be synthesized by a process through which the average run length of one of the copolymer units is less than the (C2,Statistical) for a given molar percentage of the monomer of that unit present in the reaction mixture. For example, considering a copolymer of ethylene and propylene units, one or more catalysts and/or co-catalysts may be chosen such that during copolymer chain formation, a propylene unit is favored to bond to a preceding ethylene unit, while an ethylene unit is favored to bond to a preceding propylene unit, as discussed further below. As a result of this choice, the (
C2,Actual) in the copolymer can be reduced to be less than the (
C2,Statistical) for the given molar percentage of ethylene monomers in the reaction mixture. Where the
C2,Actual) is less than the (
C2,Statistical), the copolymer is referred to as being between “statistical” and “alternating”, where “alternating” refers to a copolymer wherein the ethylene and propylene units always alternate. Alternatively, where the average unit run length is greater than the (
C2,Statistical), the copolymer is said to between “statistical” and “blocky.”
According to one or more embodiments, an (C2,Actual) in the copolymer is, at least in part, a function of the percentage of ethylene units in the copolymer, and the chosen catalyst(s) and co-catalyst(s). For example, a higher percentage of ethylene units in the copolymer will result in a higher (
C2,Actual). The choice of catalyst and co-catalyst may be used to affect the (
C2,Actual), in situations where the catalyst affects the relative insertion rate of insertion of the different units of the copolymer.
During polymer chain formation, the reaction rate at which an ethylene monomer bonds to a preceding ethylene unit at the end of the growing copolymer chain is referred to as the ethylene-ethylene reaction rate constant (“kpEE”). The reaction rate at which a propylene (or other alpha-olefin monomer) bonds to an ethylene unit at the end of the growing copolymer chain is referred to as the ethylene-propylene reaction rate constant (“kpEP”). The reactivity ratio of ethylene (“rE”) refers to the ratio of the ethylene-ethylene reaction rate constant to the ethylene-propylene reaction rate constant, kpEE/kpEP.
Likewise, the reaction rate at which a propylene (or other alpha-olefin) monomer bonds to a propylene unit at the end of the growing copolymer chain is referred to as the propylene-propylene reaction rate constant (“kpPP”). The reaction rate at which an ethylene monomer bonds to a propylene unit at the end of the growing copolymer chain is referred to as the ethylene-propylene reaction rate constant (“kpPE”). The reactivity ratio of propylene (“rP”) refers to the ratio of the propylene-propylene reaction rate constant to the propylene-ethylene reaction rate constant, kpPP/kpPE.
The lower each of the reactivity ratios (rE or rP) are, the more likely it is that a different unit will follow the preceding unit and the resulting copolymer chain will have an alternating character, with a lower C2,Actual than the (
C2,Statistical) According to one or more embodiments, selection of an appropriate catalyst, as well as control of other process parameters, may reduce one or more of the reactivity ratios for various units/monomers and may therefore also reduce the
c2,Actual.
A lower C2,Actual may provide certain advantages. For example, it may result in a lower crossover temperature for the copolymer, thereby improving one or more aspects of performance such as cold-weather performance of a polyolefin plasticized with the copolymer. In general, the shorter the
c2,Actual, the lower the crossover temperature of the copolymer, which ultimately results in a better low temperature performance for polyolefins plasticized with the copolymer.
According to one or more embodiments, a copolymer comprising ethylene and C3-C10 alpha-olefin units is selected to have an C2,Actual that is less than the
C2,Statistical for the given molar percentage of ethylene units in the copolymer. The formulae (2)-(5) below can be used to calculate the
C2,Statistical for the given molar percentage of ethylene units in the copolymer. For example, as shown in
C2,Statistical for a random distribution at the given molar percentage of ethylene units in the copolymer.
According to one or more embodiments, the copolymer may have an C2,Actual that is less than 3.0, less than 2.9, less than 2.8, less than 2.7, less than 2.6, less than 2.5, less than 2.4, less than 2.3, less than 2.1, or less than 2.0. In such embodiments, the
C2,Actual may also be selected to be is less than the
C2,Statistical for the given molar percentage of ethylene units in the copolymer.
Copolymers of ethylene and propylene produced with perfectly alternating microstructures do not have a distribution of ethylene unit run lengths, as every sequence of ethylene units is exactly the same length. The ethylene unit run length for a perfectly alternating microstructure is calculated from Equation (1).
Copolymers that do not have a perfectly alternating microstructure have a distribution of ethylene unit run lengths, and the prediction for a purely statistical microstructure of a copolymer represents the average ethylene run length for the distribution of ethylene unit run lengths in that copolymer. The average ethylene run length for copolymers produced with a purely statistical microstructure can be calculated using Bernoullian statistics. The mole fraction of ethylene incorporated in the copolymer, xethylene, as measured by 1H-NMR spectroscopy, is used to calculate the fraction of EEE, AEE, EEA, and AEA triads in the copolymer (there are also EAE, AAE and EAA and AAA triads) in a purely statistical polymer using Equations (2)-(5) given below.
E represents an ethylene unit and A represents an alpha-olefin unit and thus the triad “AEA” represents the three unit triad ethylene-alpha-olefin-ethylene.
The ethylene incorporation (xC2) in mol % was determined by 1H-NMR using a standard technique known to those of ordinary skill in the art.
A comparison of the C2,Actual and the calculations for the alternating and statistical results are shown in
C2,Actual to the calculated statistical and alternating results yields an indication of whether the copolymers have microstructures less than
C2,Statistical. It is believed that microstructures that are less than statistical have a broader distribution of ethylene unit run lengths about the average ethylene run length.
Increasing the ethylene unit content of the copolymer increases the plasticization efficiency, plasticization durability, and oxidative stability of the plasticizer but also decreases the amount of structure forming that may occur at lower temperatures. It is unexpected that the particular combination of properties and microstructure of the copolymer of the present invention provides adequate plasticization efficiency, plasticization durability, and oxidative stability while at the same time providing a good low temperature performance.
The results shown in
The copolymerization reaction can be controlled to provide the desired copolymers of the invention. Parameters such as the reaction temperature, pressure, mixing, reactor heat management, feed rates of one or more of the reactants, types, ratio, and concentration of catalyst and/or co-catalyst and/or scavenger as well as the phase of the feed components can be controlled to influence the structure of the copolymer obtained from the reaction. Thus, a combination of several different reaction conditions can be controlled to produce the desired copolymer.
For example, it is important to run the copolymerization reaction with appropriate heat management. Since the copolymerization reaction is exothermic, in order to maintain a desired set point temperature in the reactor heat must be removed. This can be accomplished by, for example, two different methods often practiced in combination. Heat can be removed by cooling the feed stream to the reactor to a temperature well below the reaction set point temperature (even sometimes cryogenically) and therefore allowing the feed stream to absorb some of the heat of reaction through a temperature rise. In addition, heat can be removed from the reactor by external cooling, such as a cooling coil and/or a cooling jacket. The lower the set point temperature in the reactor, the more demand there is for heat removal. The higher the reaction temperature, the less heat needs to be removed, or alternatively or in combination, the more concentrated the copolymer can be (higher productivity) and/or the shorter the residence time can be (smaller reactor). The results characterizing the deviation of the average ethylene run length from a purely statistical microstructure are shown in
As the reaction temperature was increased beyond 135° C., it appears that control of the microstructure may be lost and the copolymer typically becomes worse than statistical. As a result, the low temperature properties of the copolymer may be compromised. Without being bound by theory, the reduced control of the microstructure of copolymers produced at higher temperatures is believed to be due to a drop in the reaction kinetics of comonomer incorporation relative to ethylene incorporation. The more difficult it is for the comonomer to incorporate in the copolymer, the less regularly the comonomer breaks up the runs of ethylene units in the chain during copolymerization. Some strategies for improving the incorporation of comonomer at higher reaction temperatures include increasing the ratio of monomers of C3-C10 alpha-olefin/ethylene in the reactor, increasing the Al/Zr ratio in the catalyst or by making changes in the catalyst architecture.
Thus, in some embodiments of the invention, reaction temperatures of 60-135° C. are employed for the copolymerization reaction, or, more preferably, reaction temperatures of 62-130° C., or 65-125° C., or preferably 68-120° C. or 70-90° C., are employed for the copolymerization reaction.
A preferred Al/Zr ratio in the catalyst system may be less than 10,000:1, less than 1,000:1, less than 100:1, less than 10:1, less than 5:1, or less than 1:1. For boron-containing technology, a preferred Al/Zr ratio in the catalyst is less than 100:1, less than 50:1, less than 10:1, less than 5:1, less than 1:1, less than 0.1:1 and a preferred B/Zr ratio is less than 10:1, less than 5:1, less than 2:1, less than 1.5:1, less than 1.2:1, or less than 1:1.
Low temperature properties of the copolymer can be correlated to the microstructure of the copolymer. Low temperature performance of the pure copolymer is measured by Oscillatory Rheometry. The point at which storage modulus is equal to the loss modulus, the crossover or onset temperature, is an indication of the temperature at which the copolymer will begin to exhibit unfavorable structure forming. The crossover temperature is the point at which the structure formed in the polymer exceeds the liquid-like character of the polymer. This temperature has been shown to be predictive for determining the impact of the copolymer structure on low temperature performance as a polyolefin plasticizer.
The impact of C2,Actual on crossover temperature is shown in
C2,Actual The copolymers produced with the Cp2ZrMe2/FAB/TEAL catalyst system can be controlled to provide the desired combination crossover temperature and
C2,Actual. A particularly wide range of crossover temperatures is observed for the copolymers produced using the Cp2ZrMe2/FAB/TEAL catalyst system is shown in
C2,Actual of 2.6, the crossover temperature of these copolymers varies from almost −40° C. to about 5° C. This wide range in crossover temperature correlates with the wide variety of different microstructures that was also observed for these copolymers at the same average
C2,Actual.
The number average molecular weight of the copolymer can be determined by 1H-NMR or gel permeation chromatography (GPC) using polystyrene as a calibration reference, as described in U.S. Pat. No. 5,266,223, with the GPC method being preferred. The GPC method additionally provides molecular weight distribution information; see W. W. Yau, J. J. Kirkland and D. D. Bly, “Modern Size Exclusion Liquid Chromatography”, John Wiley and Sons, New York, 1979. According to some embodiments, the copolymer may have a number average molecular weight of less than 5,000 g/mol, of less than 4,500 g/mol, of less than 4,000 g/mol, of less than 3,500 g/mol, of less than 3,000 g/mol, of less than 2,800 g/mol, of less than 2,500 g/mol, of less than 2,000 g/mol, of less than 1,500 g/mol, or of less than 1,000 g/mol as determined by GPC. According to some embodiments, the copolymer may have a number average molecular weight of greater than 200 g/mol, 500 g/mol, of greater than 800 g/mol, of greater than 1,000 g/mol, as determined by GPC. Combinations of all of the above-referenced end points to form ranges are also possible and are disclosed herein. Other values are also possible.
The polydispersity index (PDI) of the copolymer is a measure of the variation in the length, in units, of the individual chains of the copolymer. The polydispersity index is determined by dividing the weight average molecular weight (Mw) of the copolymer by the number average molecular weight (Mn) of the copolymer. The term number average molecular weight (determined by, e.g., 1H-NMR or GPC) is given its ordinary meaning in the art and is defined as the sum of the products of the weight of each polymer chain and the number of polymer chains having that weight, divided by the total number of polymer chains. The weight average molecular weight of the copolymer is given its ordinary meaning in the art and is defined as the sum of the products of the weight squared of each polymer chain and the total number of polymer chains having that weight, divided by the sum of the products of the weight of each polymer chain and the number of polymer chains having that weight. According to one or more embodiments, the PDI of the copolymer (Ww/Mn) may be less than or equal to 4, less than or equal to 3, less than or equal to 2, or less than or equal to 1.
In some embodiments, it is desirable to provide copolymers that have a lower kinematic viscosity without reducing the molecular weight of the copolymer. This goal can be achieved in certain embodiments by controlling the microstructure of the copolymer as discussed above.
One goal of embodiments herein is the provision of a copolymer with a lower viscosity and higher molecular than a comparable copolymer. For example, referring to
The copolymer may comprise a certain mole percentage (mol %) of ethylene-derived units in some embodiments. According to some embodiments, the ethylene unit content of the copolymer, relative to the total amount of units within the copolymer, is at least 10 mol %, at least 20 mol %, at least 30 mol %, at least 40 mol %, at least 45 mol %, at least 50 mol %, at least 55 mol %, at least 60 mol %, at least 65 mol %, at least 70 mol %, or at least 75 mol %. According to some embodiments, the ethylene unit content of the copolymer is less than 80 mol %, less than 75 mol %, less than 70 mol %, less than 65 mol %, less than 60 mol %, less than 55 mol %, less than 50 mol %, less than 45 mol %, less than 40 mol %, less than 30 mol %, or less than 20 mol %, Combinations of each of the above-mentioned end points to form ranges are also possible and are disclosed herein. Other ranges are also possible.
The copolymer may comprise a certain mole percentage of C3-C10 alpha-olefin units. According to some embodiments, the molar percentage of the C3-C10 alpha-olefin units the copolymer, relative to the total units within the copolymer, is at least 20 mol %, at least 25 mol %, at least 30 mol %, at least 35 mol %, at least 40 mol %, at least 45 mol %, at least 50 mol %, at least 55 mol %, at least 60 mol %, at least 65 mol %, at least 70 mol %, or at least 80 mol %. According to some embodiments, the C3-C10 alpha-olefin unit content of the copolymer is less than 90 mol %, less than 80 mol %, less than 70 mol %, less than 65 mol %, less than 60 mol %, less than 55 mol %, less than 50 mol %, less than 45 mol %, less than 40 mol %, less than 35 mol %, less than 30 mol %, less than 25 mol %, or less than 20 mol %, less than 90 mol %. Combinations of any the above referenced limits can be made to form ranges and are possible and disclosed herein. Other ranges are also possible.
In many applications for plasticizers known in the art, it may be desirable to provide a polymerizable plasticizer, a functionalizable plasticizer or a reactive plasticizer. For one or more of these purposes, it is desirable to include unsaturation in the copolymers of the present invention.
In the embodiments of the invention, the copolymer comprises a plurality of copolymer molecules, 70 mol % or greater of the copolymer has a carbon-carbon double bond in a terminal monomer unit. For the avoidance of doubt, it is to be understood that the term “terminal unsaturation” means at least one of the carbons of the carbon-carbon double bond is derived from the terminal monomer unit. According to some embodiments, more than 75 mol %, more than 80 mol %, more than 85 mol %, more than 90 mol %, more than 95 mol %, or more than 97 mol %, of the copolymer molecules each possess terminal unsaturation. The percentage of polymeric chains exhibiting terminal unsaturation may be determined by FTIR spectroscopic analysis, titration, or 13C NMR. See, e.g., U.S. Pat. No. 5,128,056.
In the embodiments of the invention, the copolymer may terminate, at one end, with either an ethylene unit or a C3-C10 alpha-olefin unit. The unsaturation can be derived from the ethylene monomer or from the C3-C10 alpha olefin monomer. If the terminal unsaturation is derived from the ethylene monomer, the terminal unsaturation it may be vinyl or a di-substituted isomer of vinyl. As shown below, if the terminal unsaturation is derived from a C3-C10 alpha-olefin unit, it may be a terminal vinylidene, one or more a tri-substituted isomers of the terminal vinylidene or any combination thereof.
In some embodiments, more than 70 mol %, more than 75 mol %, more than 80 mol %, more than 85 mol %, more than 90 mol %, or more than 95 mol % of the terminal unsaturation is derived from C3-C10 alpha-olefin monomer. In such case, the terminal unsaturation has one or more of the following structural formulas (I)-(III):
For each of Formulas (I)-(III), R represents the appropriate alkyl group for that particular C3-C10 alpha-olefin unit, e.g., a methyl group if the alpha olefin is propylene, an ethyl group if the alpha olefin is 1-butene, etc., and “
” indicates me Dona mat is me point of attachment of the group (I), (II) or (III) to the remaining portion of the copolymer molecule.
As used herein, the terms “terminal vinylidene” and “terminal vinylidene group” refer to the structure represented by Formula (I). As used herein, the terms “tri-substituted isomer of terminal vinylidene” and “tri-substituted isomer of terminal vinylidene group” refer to one of the structures represented by the Formulas (II) and (III).
Terminal vinylidene, tri-substituted isomers of terminal vinylidene, as well as other types of terminal unsaturation in the copolymers can be detected by 1H-NMR. From the integrated intensity of each signal, the amount of each terminal unsaturation can be determined as discussed in US 2016/0257862. For the avoidance of doubt, one of skill in the art will understand that each of the first carbon atoms to the right of the “
” in Formulas (II) and (III) are from the penultimate monomer unit.
There are many tests that can be used to evaluate the chemical compatibility of thermoplastic materials. Three major groups of tests for chemical compatibility include retention of physical/mechanical properties, visual evaluations and creep and creep rupture. Physical properties such as change in volume, weight, dimensions, or hardness are particularly useful when evaluating chemical compatibility. Tests monitoring the change in weight or hardness would be a good indication of chemical compatibility. Plasticization allows movement of the individual molecular chains causing the polymer to become increasingly flexible as more plasticizer is absorbed. As in the case with solvation, change in weight, hardness, and in addition, dimension and volume are good indicators of chemical compatibility.
Mechanical properties such as tensile strength and elongation, impact, and flexural strength can be very good indicators of chemical compatibility. In this type of testing the properties are performed initially and again after time has elapsed. Plasticization tends to soften polymers, increasing the ductility and thus causing an increase in the tensile elongation while at the same time lowering tensile strength. The changes that occur are dependent on the amount of plasticizer present and thus results can be affected by other factors. Chemical compatibility effects that can be difficult to determine by other methods such as Environmental Stress Cracking (ESC) can be established by testing retention of tensile properties.
Visual evaluations can be used in conjunction with almost any test method when determining chemical compatibility. One such test method is ASTM D543, which combines visual evaluations with other tests. There are, however, test methods where visual evaluations and ratings are the primary result. ASTM D1693, is designed for use with ethylene type plastics and involves bending test specimens in a fixture, nicking the specimens to initiate a controlled imperfection, and optionally applying chemical agents. The specimens are then evaluated for crack growth and results determined based on the number and severity of the cracks. ASTM D1 693 is limited to flexible materials, primarily opaque, and to the observance of cracking.
Polymers can exhibit elastic deformation and reduction in strength when solvation/plasticization occurs. Creep measurements are therefore useful in determining compatibility with solvents or plasticizers. ASTM D2990 is a suitable test for creep measurements.
Estimation of the solubility parameter is another suitable way to determine chemical compatibility. The solubility parameter and molar volume of each monomer can be estimated from the structure of the monomer. Specifically, the estimation method of Fedors, R. F., “A Method for Estimating Both the Solubility Parameters and Molar Volumes of Liquids,”Pol. Eng. Sci., 14, 147-154 (1974) is employed for the copolymers of the present application. This method employs the formula:
wherein the group contributions are as given in Table 3 below.
The group contributions shown in Table 3 are added for each monomer unit to obtain the total for each copolymer. For copolymers, the following equation of Schneier. B., “An Equation for Calculating the Solubility Parameter of Random Copolymers,”Pol. Lett., 10, 245-251 (1972) can be used.
wherein 1, 2, and x are monomer 1, monomer 2, and the mixture, respectively, V is the molar volume, δ is the solubility parameter, and X is the mole weight fraction. The mole weight fraction is:
where M is the monomer molecular weight and n is the number of moles of each monomer. Vx is taken as the molar average of the two monomer molar volumes:
wherein the total solubility parameters are as given in Table 4 below.
In some embodiments the plasticizer has a difference of no more than 2 (cal cm−3)1/2 in the solubility parameter as compared to the solubility parameter of the polyolefin or other polymer into which the plasticizer is to be incorporated. Another way to calculate the solubility parameter for homopolymers is described in Small, P.A., “Some Factors Affecting the Solubility of Polymers,” J. Appl. Chem., 3, 71-79 (1953).
Various properties of the plasticizers of the present invention can be determined and/or evaluated based on the information given in, “Principles of Plasticization,” Immergut, E. H. and Mark, H. P., (1965), doi: 10.1021/ba-1965-0048.ch001, the disclosure of which is incorporated by reference herein in its entirety for providing information for determining and evaluating properties of plasticizers.
A suitable method for the production of the copolymers of the invention includes a step of reacting ethylene and at least one C3-C10 alpha-olefin using a coordination polymerization catalyst and a co-catalyst at a temperature of from 60° C. to 135° C. for a time sufficient to produce a copolymer comprising ethylene units and C3-C10 alpha-olefin units. The reaction conditions are preferably controlled such that copolymer has a number average molecular weight of less than 5,000 g/mol; 70 mol % of the copolymer has terminal unsaturation that is terminal vinylidene, one or more tri-substituted isomers of the terminal vinylidene or any combination thereof; the copolymer has an average ethylene run length of less than 4, as determined through NMR spectroscopy; the copolymer has an ethylene unit content of less than 80 mol %; and the copolymer has a crossover temperature of −20° C. or lower.
A metallocene comprises cyclopentadienyl anions (“Cp”) bound to a metal center. The C3-C10 alpha-olefin unit content can be controlled through the selection of the metallocene catalyst component and by controlling the partial pressure or relative feed rates of the various monomers.
The metallocene catalysts employed in the production of the reactant polymers are organometallic coordination compounds which are cyclopentadienyl derivatives of a Group 4b metal of the Periodic Table of the Elements (56th Edition of Handbook of Chemistry and Physics, CRC Press [1975]) and include mono, di and tricyclopentadienyls and their derivatives of the transition metals. Particularly desirable are the metallocene of a Group 4b metal such as titanium, zirconium, and hafnium. The aluminoxanes employed in forming the reaction product with the metallocenes are themselves the reaction products of an aluminum trialkyl with water.
In certain embodiments, the coordinated metallocene may comprise a zirconium. For example, the coordinated metallocene may comprise Cp2ZrCl2. In addition, a co-catalyst may optionally be employed. The co-catalyst may comprise an aluminoxane such as methylaluminoxane.
The copolymer may be produced in a reactor. Parameters that may be controlled during the copolymerization reaction include at least pressure and temperature. The reaction may be operated continuously, semi-continuously, or batchwise. The ethylene may be delivered to the reactor as ethylene gas through a metered feed. The C3-C10 alpha-olefin may be delivered to the reactor through a separate metered feed. The catalyst and optional co-catalyst may be delivered to the reactor in solution. The weight percentage of either the catalyst or the co-catalyst in the solution delivered to the reactor may be less than 20 wt. %, less than 15 wt. %, less than 10 wt. %, less than 8 wt. %, less than 6 wt. %, less than 5 wt. %, less than 4 wt. %, less than 3 wt. %, less than 2 wt. %, or less than 1 wt. %, according to different embodiments. The ethylene, C3-C10 alpha-olefin, solvent and catalyst and optional co-catalyst may then be mixed in the reactor. Skilled persons are familiar with many suitable reactions, reactors and reaction conditions for copolymerization of ethylene and C3-C10 alpha-olefins. Examples of several processes for forming the copolymer are described in the examples below.
The catalyst may comprise a granular support based especially on a refractory oxide such as, for example, silica and/or alumina. Such a catalyst can be prepared by a method comprising bringing the granular support into contact with (a) a dialkylmagnesium and optionally a trialkylaluminium, (b) a halogenated hydrocarbon e.g. a monohalogenated hydrocarbon, (c) and a tetravalent titanium compound. Such a method is described in European Patent Application EP-A-453,088.
The catalyst may also contain a magnesium chloride support and in particular a preactived support such as that described in European Patent Application EP-A-336,545. A catalyst of this type can be prepared by a method comprising bringing a magnesium chloride support into contact with (a) an organometallic compound which is a reducing agent for titanium, (b) a tetravalent titanium compound and c) optionally one or more electron-donor compounds. Such a method is described in French Patent Application FR-A-2,669,640.
The catalyst may be used in the form of a solid as it is or in the form of a prepolymer, especially when it is used in a gas phase polymerization. The prepolymer is obtained by bringing the catalyst into contact with one or more of olefins e.g. containing from 2 to 8 carbon atoms such as, for example, ethylene or a mixture of ethylene with C3-C8 olefin(s) in the presence of an organometallic cocatalyst. In general, the prepolymer obtained contains from 0.1 to 200 g preferably from 10 to 100 g of polymer per millimole of titanium.
The catalyst may be employed with an organometallic cocatalyst which may be chosen from organoaluminium, organomagnesium and organozinc compounds. In most cases the organometallic cocatalyst is an alkylaluminium such as, for example, trimethylaluminium, triethylaluminium, tri-n-octylaluminium or else a mixture of these compounds.
The copolymers can alternatively be polymerized using catalysts prepared by the admixture of certain boron compounds with a salt of a metal selected from Groups 4a, 5a, 6a and 8, of the Mendeleeff Periodic Table. These compounds of boron are the hydrides and hydrocarbon derivatives of boron. The boron hydride used in preparing such catalytic compositions is usually diborane (B H although other hydrides of boron can also be used including, for example, pentaborane, hexaborane, and decaborane.
Hydrocarbon derivatives of boron which may be used include alkyl borons, cycloalkyl borons, aryl borons and the like. Examples of alkyl borons which can be used include, trimethyl boron, triethylboron, tripropyl boron, tributyl boron, tridecyl boron and the like. Examples of aryl borons include triphenyl boron, tritolyl boron, tri-p-xylyl boron, trinaphthyl boron and the like. Mixed hydride-hydrocarbon derivatives of boron can also be used, e. g. symmetrical or asymmetrical dimethyldiborane, methyldiborane and the like. Also the hydrocarbon-halogen derivatives of boron, e. g. dimethylboron bromide, dimethylboron iodide, diphenylboron bromide or chloride, etc can be used. Exemplary boron catalysts can be found in, for example, U.S. Pat. Nos. 3,166,536; 3,160,672 and 2,840,551.
In some embodiments, the microstructure of the copolymer may be desirably influenced by spatially distributing the composition uniformly within the reactor. Methods of ensuring uniformity of the spatial distribution include, but are not limited to, agitation, selection of particular feed locations for feeding the monomers, solvent and catalyst components and particular methods of introducing one or more of the various components. Additional factors that may impact compositional uniformity in the reactor include operation within a particular temperature and/or pressure range that provides a single fluid phase within the reactor. In some embodiments this may involve ensuring that the reactor temperature and pressure conditions remain above the entire vapor-liquid phase behavior envelope of the feed composition. It is also envisioned that premixing of two or more of the feed components may be employed and the premixing time and mixing intensity of the feed components may be useful for control of spatial uniformity within the reactor, at least in some cases. In certain embodiments it may also be desirable to ensure that no pockets of vapor exist within the reactor that would create a composition gradient either at a vapor-liquid interface or within the liquid.
Some strategies for improving the incorporation of comonomer at higher reaction temperatures include increasing the ratio of monomers of C3-C10 alpha-olefin/ethylene in the reactor, increasing the Al/Zr ratio in a zirconium-containing coordination metallocene catalyst or by making changes in the catalyst architecture.
Temperature control may be used to influence the reactivity ratios in a manner that leads to microstructures with better than statistical microstructures and/or to microstructures tending toward alternating microstructures. Typically, lower temperature are advantageous for achieving a better than statistical microstructure and/or a microstructure that tends toward alternation of the ethylene and C3-C10 alpha-olefin units. Some or all of the above may be important for controlling the microstructure within the copolymer chains as well as controlling variations of the C3-C10 alpha-olefin unit composition from chain to chain.
Low Metal and/or Fluorine Content
Low metal content copolymers are desirable for many uses due to the harmful effects of metals in various environments. For example, metals or ash can have an adverse impact on after-treatment devices employed in various types of engines. It is also desirable to ensure that the copolymers have a low fluorine content since fluorine is ecologically undesirable in many environments.
There are several methods to achieve a low metal content in the copolymer as described herein. The present invention incorporates methods known by those skilled in the art to purify and remove impurities. For example, in Giuseppe Forte and Sara Ronca, “Synthesis of Disentangled Ultra-High Molecular Weight Polyethylene: Influence of Reaction Medium on Material Properties,” International Journal of Polymer Science, vol. 2017, Article ID 7431419, 8 pages, 2017. doi:10.1155/2017/7431419, methods for purifying a polyethylene compound are disclosed. The method of purifying the copolymer comprises dissolving the copolymer in acidified methanol (CH3OH/HCl) to a DCM (dichloromethane) solution of the polymer/catalyst mixture. This results in precipitation of the “purified” polymer, while the catalyst and other byproducts remain in solution. The copolymer may then be filtered and washed out with additional methanol, and oven dried under vacuum at 40° C.
According to one or more embodiments, the copolymer may be purified to achieve a low metal content by passing the polymer/catalyst mixture through an adsorption column. The adsorption column contains an adsorber, preferably, activated alumina.
In a more preferred embodiment, the copolymer may be purified to achieve a low metal content by stripping the polymer compositions using toluene and a rotavap with a temperature-controlled oil bath.
In an alternative embodiment, the copolymer does not require a purification step. In this embodiment, the copolymer of the present invention is preferably copolymerized using a catalyst having a catalyst productivity of from 200-1500 kg copolymer/gram of single-site catalyst, or from 350-1500 kg copolymer/gram of single-site catalyst, or from 500-1200 kg copolymer/gram of single-site catalyst, or from 500-800 kg copolymer/gram of single-site catalyst. Suitable single-site catalyst systems having these productivities may be selected from those known in the art. The catalysts may be selected for the production of copolymers having Mn's in the range of 700-1400 g/mol. or from 550-650 g/mol. Selection of a suitable single-site catalyst may eliminate the need for a wash step to achieve the low metal content of the copolymer.
Catalyst productivity, expressed as the kg polymer produced per gram of catalyst, may be improved by efficient catalyst systems. The present invention incorporates the use of catalyst systems known by those skilled in the art which are capable of achieving high catalyst productivities. For example, U.S. Pat. No. 9,441,063 relates to catalyst compositions containing activator-supports and half-metallocene titanium phosphinimide complexes or half-metallocene titanium iminoimidazolidides capable of producing polyolefins with high catalyst productivities of at least up to 202 kg polymer/g catalyst (551 kg polymer/g cat/hr with a 22 min residence time, See Example 5 and Table 1, Columns 47 and 48.) Also, U.S. Pat. No. 8,614,277 relates to methods for preparing isotactic polypropylene and ethylene-propylene copolymers. U.S. Pat. No. 8,614,277 provides catalyst systems suitable for preparing copolymers at catalyst productivity levels greater than 200 kg polymer/g catalyst. The catalysts provided therein are metallocenes comprising zirconium as their central atom. (See the examples in Tables 1a-1c).
The copolymer may comprise a metal or ash content of 25 ppmw or less, based on the total weight of the copolymer. Preferably, the metal or ash content of the copolymer is 10 ppmw or less, or more preferably 5 ppmw or less, or even more preferably 1 ppmw or less, based on the total weight of the copolymer. Typically, the metal or ash content of the copolymer is derived from the single-site catalyst and optional co-catalyst(s) employed in the copolymerization reactor.
These single-site catalysts may include metallocene catalysts. Zr and Ti metals are typically derived from such metallocene catalysts. Various co-catalysts may be employed in combination with the single-site catalyst. Such co-catalysts may include boron and aluminum metals, as well as ecologically undesirable fluorine atoms or compounds. Thus, the metal or ash content of the copolymers of the present invention is the total metal or ash including Zr. Ti, Al and/or B. Various suitable catalyst systems are described elsewhere herein.
The copolymers may have a fluorine content of less than 10 ppmw, or less than 8 ppmw, or less than 5 ppmw, based on the total weight of the copolymer. Typically, the fluorine will come from co-catalyst systems based on boron compounds such as pefluoroaryl boranes.
According to one or more embodiments, the copolymer described herein may be functionalized. The invention provides functionalized derivatives of the copolymers described above, and provides for compositions comprising the same. The functionalized copolymers of this invention may exhibit lower viscosities for better melt flows and lower operating temperatures in various processing applications. The invention also relates to methods of using these functionalized copolymers in applications requiring particular processing elements and/or specific physical properties in the final product. In still another aspect, the invention relates to the articles prepared from these functionalized copolymers. These functionalized copolymers and polymeric blends containing the same, may be employed in the preparation of solid articles, such as moldings, films, sheets, and foamed objects. These articles may be prepared by molding, extruding, or other processes. The functionalized copolymers are useful in adhesives, tie layers, laminates, polymeric blends, and other end uses. The resulting products may be used in the manufacture of components for automobiles, such as profiles, bumpers and trim parts, or may be used in the manufacture of packaging materials, electric cable insulation, coatings and other applications.
The ethylene/C3-C10 alpha-olefin copolymers can be functionalized by incorporating at least one functional group in the copolymer structure. Exemplary functional groups may include, for example, ethylenically unsaturated mono- and di-functional carboxylic acids, ethylenically unsaturated mono- and di-functional carboxylic acid anhydrides, salts thereof and esters thereof and epoxy-group containing esters of unsaturated carboxylic acids. Such functional groups may be incorporated into the copolymer by reaction with some or all of the unsaturation in the copolymer
Examples of the unsaturated carboxylic acids, dicarboxylic acids which may be present in the functionalized copolymer are those having about 3 to about 20 carbon atoms per molecule such as acrylic acid, methacrylic acid, maleic acid, fumaric acid and itaconic acid. Unsaturated dicarboxylic acids having about 4 to about 10 carbon atoms per molecule and anhydrides thereof are especially preferred. Compounds that can be reacted with the unsaturation in the copolymer include for example, maleic acid, fumaric acid, itaconic acid, citraconic acid, cyclohex-4-ene-1,2-di-carboxylic acid, bicyclo[2.21]hept-5-ene-2,3-dicarboxylic acid, maleic anhydride, itaconic anhydride, citraconic anhydride, allylsuccinic anhydride, 4-methylcyclohex-4-ene-1,2-dicarboxylic anhydride and bicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic anhydride. One particularly useful functional group may be introduced using maleic anhydride.
The ethylene/C3-C10 alpha-olefin copolymers can be functionalized by an ene reaction of the alkenyl group of the copolymer and an enophile containing a multiple bond.
The amount of the functional group present in the functionalized copolymer can vary. The functional group can typically be present in an amount of at least about 0.3 weight percent, or at least 1.0 weight percent, preferably at least about 5 weight percent, and more preferably at least about 7 weight percent. The functional group will typically be present in an amount less than about 40 weight percent, preferably less than about 30 weight percent, and more preferably less than about 25 weight percent, or less than about 10 weight percent and more preferably less than about 5 weight percent. A desirable range can be any combination of any lower wt. % limit with any upper wt. % limit described herein provided the lower limit is less than the upper limit, each of which combinations of upper and lower limits are disclosed herein.
Polymers Plasticized with the Copolymers
The ethylene/C3-C10 alpha olefin copolymers described herein are blended with at least one polyolefin to prepare the plasticized compositions of this invention.
Suitable polyolefins include homopolymers or copolymers of one or more olefins selected from C2 to C20 linear, branched, cyclic, and aromatic-containing monomers, specifically including ethylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1-dodecene, 4-methyl-1-pentene, 3-methyl-1-pentene, 3,5,5-trimethyl-1-hexene, 5-ethyl-1-nonene, vinylcyclohexane, vinylcyclohexene, vinylnorbornene, ethylidene norbornene, cyclopentadiene, cyclopentene, cyclohexene, cyclobutene, vinyladamantane, styrene, alpha-methylstyrene, para-alkylstyrenes such as paramethyl styrene, 4-phenyl-1-butene, allyl benzene, vinyltoluenes, vinylnaphthalene, allyl benzene, and indene. For example, the polyolefin may be poly(4-methyl-pentene-1) homopolymer, or a copolymer of 4-methyl-penten-1 and another olefin.
Preferred polyolefins include polyethylene homopolymers, polypropylene homopolymers, polybutene homopolymers, ethylene-propylene copolymers, ethylene-butene copolymers, ethylene-hexene copolymers, ethylene-octene copolymers, propylene-butene copolymers, propylene-hexene copolymers, propylene-octene copolymers, and copolymers of one or more olefins selected from C2 to C4 olefins with one or more comonomers selected from diolefins and oxygen-containing olefins (examples being ethylene-propylene-diene and ethylene-vinyl acetate copolymers). The polyolefin component may be a blend of one or more polyolefins, or a blend of polymers comprising at least 50 wt. % of one or more polyolefins.
In certain embodiments, the polyolefin is selected from the general class of polyolefins known as “polyethylene” (i.e., ethylene homopolymers, ethylene copolymers, and blends thereof). These include plastomers having a density of less than 0.91 g/cm; low density polyethylene having a density of more than 0.91 g/cm3 to less than 0.94 g/cm3; and high density polyethylene (HDPE) having a density of 0.94 g/cm3 or more. A polyethylene material comprises at least 50 mole %, or 60 mol %, or at least 70 mol %, or at least 80 mol %, or at least 90 mol %, or at least 95 mol %, or 100 mole % ethylene units. Polyethylene copolymers may be random copolymers, statistical copolymers, block copolymers, and blends thereof. Comonomers are preferably selected from C3 to C20 alpha-olefins, or from C3 to C10 alpha-olefins, or from 1-butene, 1-hexene, and 1-octene; and preferably are present from 0.1 to 20 wt. %, or from 0.5 to 10 wt. %, or from 1 to 5 wt. %, or from 2 to 35 wt. %, or from 5 to 30 wt. %, or from 15 to 25 wt. %. Polyethylene copolymers may comprise up to 50 mol % diene.
In other embodiments, the polyolefin is selected from the general class of polyolefins known as “polypropylene” (i.e., propylene homopolymers, copolymers, and blends thereof). These include isotactic polypropylene (iPP), highly isotactic polypropylene, syndiotactic polypropylene (sPP), homopolymer polypropylene (hPP, also called propylene homopolymer or homopolypropylene), so-called random copolymer polypropylene. A polypropylene material comprises at least 50 mol %, or 60 mol %, or at least 70 mol %, or at least 80 mol %, or at least 90 mol %, or at least 95 mol %, or 100 mol % propylene units. Polypropylene copolymers may be random copolymers, statistical copolymers, block copolymers, impact copolymers, and blends thereof. Comonomers are preferably selected from ethylene and C4 to C20 alpha-olefins, or from ethylene and C4 to C10 alpha-olefins, or from ethylene, 1-butene, 1-hexene, and 1-octene; and preferably are present from 0.1 to 20 wt. %, or from 1 to 10 wt. %, or from 2 to 5 wt. %, or from 2 to 35 wt. %, or from 5 to 30 wt. %, or from 15 to 25 wt. %. Polypropylene copolymers may also comprise up to 50 mol % diene.
In other embodiments, the polyolefin is selected from the general class of polyolefins known as “polybutene” (i.e., butene-1 homopolymers, copolymers, and blends thereof). The homopolymer may be atactic, isotactic, or syndiotactic polybutene, and blends thereof. The copolymer can be a random copolymer, a statistical copolymer, a block copolymer, and blends thereof. Random copolymers include those where the comonomer is selected from ethylene, propylene, 1-hexene, and 1-octene. Blends include impact copolymers, elastomers and plastomers, any of which may be physical blends or in situ blends with the polybutene. Poly(I-butene) homopolymers and 1-butene/ethylene copolymers are commercially available from Basell Polyolefins.
In other embodiments, the polyolefin is selected from the general class of polyolefins known as “ethylene-propylene (EP) elastomers” which are copolymers of ethylene and propylene and optionally one or more diene monomer(s), and also known in the art as EPM or EPDM elastomers. EP elastomers have little to no crystallinity with a heat of fusion of 20 J/g or less, a density of 0.86 g/cm3 or less, an ethylene unit content from 35 to 85 mol %, a diene content of 0 to 5 mol %, a minimum propylene unit content of 15 mol %, and a molecular weight of at least 50 kg/mol.
Suitable polyolefins may comprise up to 20 wt. %, or up to 10%, or up to 1 wt. % diene (i.e., diolefin) monomers. Examples include alpha-omega diene (i.e., di-vinyl) monomers such as 1,6-heptadiene, 1,7-octadiene, 1,8-nonadiene, 1,9-decadiene, 1,10-undecadiene, 1,11-dodecadiene, 1,12-tridecadiene, and 1,13-tetradecadiene, as well as cyclic dienes such as cyclopentadiene, vinylnorbornene, norbornadiene, ethylidene norbornene, divinylbenzene, and dicyclopentadiene.
Other suitable polyolefins are described in WO 03/040201, WO 03/040095, WO 03/040202, WO 03/040233, WO 2009/020706, and WO 03/040442.
The method of making the polyolefin is not critical, as it can be made by slurry, solution, gas phase, high pressure or other suitable processes, and by using catalyst systems appropriate for the polymerization of polyethylenes, such as chromium catalysts, metallocene-type catalysts, other appropriate catalyst systems or combinations thereof, or by free-radical polymerization. Catalyst systems suitable to make polyethylene are well known in the art; see, for example Metallocene-Based Polyolefins (Wiley & Sons, 2000).
In one or more embodiments, one or more of the ethylene/C3-C10 alpha olefin plasticizer components of the invention is present in an amount of from a low of 0.5 wt. %, or 1 wt. %, or 2 wt. %, or 3 wt. %, or 4 wt. %, or 5 wt. %, to a high of 50 wt. %, or 45 wt. %, or 40 wt. %, or 35 wt. %, or 30 wt. %, or 25 wt. %, or 20 wt. %, or 15 wt. %, or 10 wt. %, or 5 wt. %, based on total weight of plasticizer component(s) and polyolefin(s), wherein a desirable range can be any combination of any lower wt. % limit with any upper wt. % limit described herein provided the lower limit is less than the upper limit. In other embodiments, the composition includes the at least one ethylene/C3-C10 alpha olefin plasticizer in an amount of about 1 to 40 wt. %, or 2 to 30 wt. %, or 4 to 20 wt. %, based on the total weight of the composition.
In one or more embodiments, one or more polyolefin component is present in an amount of from a low of 50 wt. %, or 55 wt. %, or 60 wt. %, or 65 wt. %, or 70 wt. %, or 75 wt. %, or 80 wt. %, or 85 wt. %, or 90 wt. %, or 95 wt. % to a high of 99 wt. %, or 95 wt. %, or 90 wt. %, or 85 wt. %, or 80 wt. %, or 75 wt. %, or 70 wt. %, or 65 wt. %, or 60 wt. %, based on total weight of ethylene/C3-C10 alpha olefin plasticizer component(s) and polyolefin(s), wherein a desirable range can be any combination of any lower wt. % limit with any upper wt. % limit described herein provided the lower limit is less than the upper limit. In other embodiments, the composition includes at least one polyolefin in an amount of about 60 to 99 wt. %, or 70 to 98 wt. %, or 80 to 96 wt. %, based on the total weight of the composition.
Additives commonly used in the polyolefin industry to impart certain desirable properties may be present in the polyolefin compositions of the present invention. Such additives are described in Plastics Additive Handbook, 5th Ed.; H. Zweifel, Ed. (Hamer-Gardner, 2001) and include antioxidants (including organic phosphites, hindered amines, and phenolics), stabilizers (including UV stabilizers and other UV absorbers), nucleating agents (including clarifying agents, metal salts such as sodium benzoate, sorbitol derivatives, and metal phosphates), pigments, dyes, color masterbatches, processing aids, waxes, oils, lubricants, surfactants, slip agents (including metal salts of fatty acids such as zinc stearate and fatty acid amides such erucamide), tackifiers, block, antiblock, neutralizers (such as hydro talcite), acid scavengers, anticorrosion agents, cavitating agents, blowing agents, quenchers, antistatic agents, fire retardants, cure or cross linking agents or systems (such as elemental sulfur, organo-sulfur compounds, organic peroxides, and di- or tri-amines), coupling agents (such as silane), and combinations thereof. The additives may be present in amounts known in the art to be effective, preferably at 0.01 to 10 wt. % (100 to 100,000 ppm), or 0.02 to 1 wt. % (200 to 10,000 ppm), or 0.025 to 0.5 wt. % (250 to 5,000 ppm), or 0.05 to 0.25 wt. % (500 to 2,500 ppm), or 0.1 to 5 wt. % (1,000 to 50,000 ppm), based upon the weight of the composition (where ppm is parts-per-million by weight).
Fillers may be present in the polyolefin compositions of the present invention. Desirable fillers include but not limited to: natural or synthetic mineral aggregates (including talc, wollastonite, and calcium carbonate), fibers (including glass fibers, carbon fibers, or polymeric fibers), carbon black, graphite, natural and synthetic clays (including nanoclays and organoclays), sand, glass beads, and any other porous or nonporous fillers and supports known in the art, utilized alone or admixed to obtain desired properties. The filler may be present at 0.1 to 50 wt. %, or 1 to 40 wt. %, or 2 to 30 wt. %, or 5 to 20 wt. %, based on the weight of the total composition. Filler content is equated with the wt. % ash content as determined by the ISO 3451-1 (A) test method. Blending
The ethylene/C3-C10 alpha olefin plasticizer(s), polyolefin(s), and optional additives can be combined using any suitable means. Those skilled in the art will be able to determine the appropriate procedure to balance the need for intimate mixing with the desire for process economy. For example, one or more polyolefin component can be in the form of pellets or reactor granules, which are combined with the copolymer plasticizer(s) and optional additives by simple physical blending of constituent pellets and/or granules, since the forming of articles includes a (re)melting and mixing of the raw material(s). The polyolefin components may be in any physical form when blended with the ethylene/C3-C10 alpha olefin plasticizer(s) and optional additives. For example, they may be in the form of reactor granules (i.e., granules of polymer that are isolated from the polymerization reactor prior to any processing procedures), or in the form of pellets that are formed from melt extrusion of the reactor granules. The polyolefin(s), ethylene/C3-C10 alpha olefin plasticizer, and optional additives can be blended by any suitable means known to those skilled in the art such as, for example, the blending processes described in WO 2009/020706.
The compositions of the present invention can be useful for the fabrication of shaped articles made or formed by any useful discrete molding or continuous extrusion means for forming and shaping polyolefins known in the art, including: compression molding, injection molding, co-injection molding, gas-assisted injection molding, blow molding, multi-layer blow molding, injection blow molding, stretch blow molding, extrusion blow molding, transfer molding; cast molding, rotational molding, foam molding, slush molding, transfer molding, wet lay-up or contact molding, cast molding, cold forming matched-die molding, thermoforming, vacuum forming, film blowing, film or sheet casting, sheet extrusion, profile extrusion or co-extrusion, fiber spinning, fiber spunbonding, fiber melt blowing, lamination, calendering, coating, pultrusion, protrusion, draw reduction, foaming, or other forms of processing such as described in, for example, Plastics Processing (Radian Corporation, Noyes Data Corp. 1986), or combinations thereof.
The plasticized compositions of the present invention can be useful for consumer goods, industrial goods, construction materials, packaging materials, appliance components, electrical components, and automotive components. Non-limiting examples of desirable articles of manufacture made from compositions of the invention include films, tapes, sheets, fibers, tubing, pipes, hoses, belts, coatings, fabrics (woven and nonwoven), tarps, agricultural barriers, packaging (durable and disposable), kitchen devices and household appliances (washing machines, refrigerators, blenders, air conditioners, etc.), furniture (indoor and outdoor, such as tables, chairs, benches, shelving, etc.), sporting equipment (skis, surfboards, skateboards, skates, boots, sleds, scooters, kayaks, paddles, etc.), solid wheels, stadium seating, amusement park rides, personal protective equipment (safety helmets, shin guards, etc.), emergency response equipment, cookware, utensils, trays, pallets, carts, tanks, tubs, pond liners, storage containers (crates, pails, jars, bottles, etc.), toys, child car seats and booster chairs, medical devices and components (including syringe parts and catheters), luggage, tool housings (for drills, saws, etc.), wire and cable jackets, electronics housings and components (for televisions, computers, phones, hand-held devices, media players, stereos, radios, clocks, etc.), building construction materials (flooring, siding, roofing, counter tops, seals, joints, isolators, etc.), lighting, gardening equipment (handles on shovels, wheelbarrows, etc.), playground equipment, motor housings, pump housings, battery housings, instrument housings, switches, knobs, buttons, handles, pet supplies, laboratory supplies, personal hygiene devices (razors, brushes, hairdryers, etc.), cleaning supplies (brooms, dust pans, etc.), musical instrument cases, statues, trophies, artwork, costume jewelry, picture frames, eyeglass frames, plant pots, and firearm components.
Plasticized polyolefin compositions of the present invention provide for improved plasticization durability of the plasticizer relative to comparable compositions made using conventional plasticizers. Improved plasticization durability is advantageous for successful long-term property retention. In certain embodiments, useful plasticized polyolefin compositions may exhibit a reduced TGA Volatility. Plasticized polyolefin compositions of the present invention provide for lower glass transition temperatures relative to comparable compositions made using a conventional plasticizer. A lower Tg is advantageous for improved low temperature flexibility and toughness. Plasticized polyolefin compositions of the present invention may also provide for lower melt viscosity relative to comparable compositions made using a conventional plasticizer. A lower melt viscosity (e.g., MI or MFR) is advantageous for improved low temperature flexibility and toughness.
The following examples are illustrative, but not limiting, of the methods and compositions of the present disclosure. Examples 1-16 exemplify different copolymers comprising ethylene units and propylene units and processes for producing them. As shown, changes in the conditions and parameters of the process, such as the feed rate of various reactants, may be employed to achieve different characteristics of the resulting copolymer such as changing the crossover temperature of the copolymer.
Examples F1-F12 exemplify different functionalized copolymers and processes for producing the same.
Table 5 below summarizes the characteristics of the copolymer from select examples from below.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.127 wt. % Cp2ZrCl2 in toluene), co-catalyst (5.0 wt. % MMAO in toluene), solvent (toluene), and ethylene and propylene monomers. The reactor was operated liquid-full at 70 psig and agitated with a four-blade pitched-turbine impeller operating at 220 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 0.90 g/min and 0.90 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.71 g/min, 15.22 g/min and 11.71 g/min, respectively. The reactor temperature was maintained at 65° C. as measured by a ⅛″ thermocouple located in the reactor. The production rate of polymer was measured gravimetrically as 2.78 g/min.
The copolymer was found to contain 49 mol % of ethylene units using 1H-NMR. The relative number average molecular weight (MO and PDI of the copolymer were measured by GPC and found to be 1159 g/mol and 3.73, respectively. The weight average molecular weight (MW) of the copolymer was measured by 1H-NMR and found to be 1038 g/mol and the olefin distribution in the copolymer as measured by 1H-NMR was 96.5% methyl-vinylidene, 1.6% beta-vinylidene, 1.3% di-substituted (i.e. 2 olefins in a single copolymer molecule) and 0.6% vinyl/allyl. The average ethylene run length as measured by 13C-NMR was 1.68. The crossover temperature measured by oscillatory rheometry was determined to be −73.5° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reactor was operated continuously; with a continuous feed of catalyst (0.127 wt. % Cp2ZrCl2 in toluene), co-catalyst (5.0 wt. % MMAO in toluene), solvent (toluene), ethylene and propylene. The reactor was operated liquid-full at 70 psig and agitated with a four-blade pitched-turbine impeller operating at 220 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 0.87 g/min and 0.87 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.78 g/min, 15.51 g/min and 10.65 g/min, respectively. The reactor temperature was maintained at 68° C. as measured by a ⅛″ thermocouple located in the reactor. The production rate of polymer was measured gravimetrically as 3.22 g/min.
The copolymer was found to contain 46 mol % ethylene units as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 1466 g/mol and 2.22, respectively. The weight average molecular weight (MW) of the copolymer as measured by 1H-NMR was 780 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 96.0% methyl-vinylidene, 1.8% beta-vinylidene, 1.3% di-substituted and 0.9% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 1.54. The crossover temperature measured by oscillatory rheometry was determined to be −77.6° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.077 wt. % Cp2ZrCl2 in toluene), co-catalyst (1.248 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 763 psig and agitated with a four-blade pitched-turbine impeller operating at 900 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 1.02 g/min and 0.82 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.23 g/min, 3.30 g/min and 9.31 g/min, respectively. The reactor temperature was maintained at 76° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.57 g/min.
The copolymer was found to contain 65 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2085 g/mol and 3.42, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1645 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 95.1% methyl-vinylidene, 1.8% beta-vinylidene, 1.3% di-substituted and 1.8% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.60. The crossover temperature measured by oscillatory rheometry was −24.5° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.075 wt. % Cp2ZrCl2 in toluene), co-catalyst (1.0 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 708 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 0.89 g/min and 0.91 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.23 g/min, 3.59 g/min and 9.36 g/min, respectively. The reactor temperature was maintained at 75° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.47 g/min.
The copolymer was found to contain 65 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2326 g/mol and 3.35, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1824 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 95.6% methyl-vinylidene, 1.7% beta-vinylidene, 1.1% di-substituted and 1.6% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.52. The crossover temperature measured by oscillatory rheometry was −27.0° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.150 wt. % Cp2ZrCl2 in toluene), co-catalyst (2.0 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 715 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 1.28 g/min and 1.26 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.23 g/min, 2.60 g/min and 9.38 g/min, respectively. The reactor temperature was maintained at 75° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.4 g/min.
The copolymer was found to contain 64 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 1241 g/mol and 3.00, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1114 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 95.5% methyl-vinylidene, 1.9% beta-vinylidene, 1.3% di-substituted and 1.4% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.39. The crossover temperature measured by oscillatory rheometry was −35.8° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.167 wt. % Cp2ZrCl2 in toluene), co-catalyst (2.222 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 696 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 0.66 g/min and 0.65 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 3.09 g/min, 8.11 g/min and 3.10 g/min, respectively. The reactor temperature was maintained at 80° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 6.63 g/min.
The copolymer was found to contain 58 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 3202 g/mol and 2.03, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1310 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 95.7% methyl-vinylidene, 1.5% beta-vinylidene, 1.6% di-substituted and 1.2% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.02. The crossover temperature measured by oscillatory rheometry was approximately −72.7° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.165 wt. % Cp2ZrCl2 in toluene), co-catalyst (2.2 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 703 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 1.21 g/min and 1.20 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.23 g/min, 2.51 g/min and 8.50 g/min, respectively. The reactor temperature was maintained at 75° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.48 g/min.
The copolymer was found to contain 68 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2838 g/mol and 1.87, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1203 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 94.6% methyl-vinylidene, 2.1% beta-vinylidene, 1.3% di-substituted and 2.0% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.72. The crossover temperature measured by oscillatory rheometry was approximately −13.7° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.182 wt. % Cp2ZrCl2 in toluene), co-catalyst (2.42 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 704 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 1.15 g/min and 1.14 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 2.20 g/min, 2.40 g/min and 7.97 g/min, respectively. The reactor temperature was maintained at 75° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.53 g/min.
The copolymer was found to contain 67 mol % ethylene as measured by 1H-NMR.
The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2269 g/mol and 2.17, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1167 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 94.6% methyl-vinylidene, 2.2% beta-vinylidene, 1.3% di-substituted and 1.9% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.65. The crossover temperature measured by oscillatory rheometry was approximately −18.5° C.
A 300 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst and co-catalyst. The reaction was operated continuously; with continuous feed of catalyst (0.167 wt. % Cp2ZrCl2 in toluene), co-catalyst (2.222 wt. % MMAO in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 701 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst and co-catalyst solutions were mixed immediately before introduction to the reactor at feed rates of 0.78 g/min and 0.89 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst and co-catalyst solutions at feed rates of 3.34 g/min, 7.77 g/min and 3.20 g/min, respectively. The reactor temperature was maintained at 89° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 7.98 g/min.
The copolymer was found to contain 56 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 3173 g/mol and 6948, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1281 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 94.9% methyl-vinylidene, 2.0% beta-vinylidene, 1.8% di-substituted and 1.3% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.05. The crossover temperature measured by oscillatory rheometry was lower than −37° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.011 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.023 wt. % FAB in toluene), scavenger (0.0080 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1520 psig and agitated with a four-blade pitched-turbine impeller operating at 1041 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.31, 0.32 and 0.52 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 0.60, 2.98 and 6.31 g/min, respectively. The reactor temperature was maintained at 134° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 0.96 g/min.
The copolymer was found to contain 55 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2883 g/mol and 2.05, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1411 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 76.6% methyl-vinylidene, 14.1% beta-vinylidene, 7.2% di-substituted and 2.1% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.60. The crossover temperature measured by oscillatory rheometry was approximately −22.4° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.141 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.144 wt. % FAB in toluene), scavenger (0.032 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1553 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.22 g/min, 0.49 g/min and 0.25 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 1.75 g/min, 2.55 g/min and 7.04 g/min, respectively. The reactor temperature was maintained at 120° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 2.53 g/min.
The copolymer was found to contain 62 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2318 g/mol and 1.98, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1199 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 75.6% methyl-vinylidene, 16.8% beta-vinylidene, 6.3% di-substituted and 1.4% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.22. The crossover temperature measured by oscillatory rheometry was lower than −37° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.04 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.083 wt. % FAB in toluene), scavenger (0.005 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1533 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.32 g/min, 0.34 g/min and 0.33 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 1.60 g/min, 3.05 g/min and 3.68 g/min, respectively. The reactor temperature was maintained at 98° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.69 g/min.
The copolymer was found to contain 45 mol % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2628 g/mol and 2.00, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1410 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 81.2% methyl-vinylidene, 13.0% beta-vinylidene, 5.2% di-substituted and 0.6% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 1.62. The crossover temperature measured by oscillatory rheometry was lower than −37° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.04 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.082 wt. % FAB in toluene), scavenger (0.01 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1533 psig and agitated with a four-blade pitched-turbine impeller operating at 1019 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.52 g/min, 0.52 g/min and 0.37 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 1.78 g/min, 2.76 g/min and 3.98 g/min, respectively. The reactor temperature was maintained at 119° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 3.5 g/min.
The copolymer was found to contain 54 mol. % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 1673 g/mol and 1.97, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 913 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 79.2% methyl-vinylidene, 14.7% beta-vinylidene, 5.0% di-substituted and 1.1% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 1.99. The crossover temperature measured by oscillatory rheometry was lower than −37° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.093 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.191 wt. % FAB in toluene), scavenger (0.011 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1462 psig and agitated with a four-blade pitched-turbine impeller operating at 1,000 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.65 g/min, 0.68 g/min and 0.63 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 1.70 g/min, 2.20 g/min and 6.85 g/min, respectively. The reactor temperature was maintained at 105° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 2.63 g/min.
The copolymer was found to contain 67 mol. % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 3004 g/mol and 2.04, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1504 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 83.0% methyl-vinylidene, 11.0% beta-vinylidene, 5.0% di-substituted and 2.0% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.64. The crossover temperature measured by oscillatory rheometry was approximately −20.0° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.008 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.015 wt. % FAB in toluene), scavenger (0.011 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1549 psig and agitated with a four-blade pitched-turbine impeller operating at 1008 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.37 g/min, 0.40 g/min and 0.27 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 0.48 g/min, 3.0 g/min and 6.98 g/min, respectively. The reactor temperature was maintained at 140° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 0.61 g/min.
The copolymer was found to contain 57 mol. % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 3,000 g/mol and 2.23, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1505 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 76.6% methyl-vinylidene, 13.7% beta-vinylidene, 7.6% di-substituted and 2.1% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.59. The crossover temperature measured by oscillatory rheometry was approximately 0.7° C.
A 100 mL Parr reactor was equipped with a water jacket for temperature control, a nitrogen-purged receiver for pressure control, a metered feed of ethylene gas and high-pressure metering pumps for separate feeds of propylene, toluene, catalyst, co-catalyst and scavenger. The reaction was operated continuously; with continuous feed of catalyst (0.015 wt. % Cp2ZrMe2 in toluene), co-catalyst (0.031 wt. % FAB in toluene), scavenger (0.009 wt. % TEAL in toluene), solvent (toluene), ethylene, and propylene. The reactor was operated liquid-full at 1539 psig and agitated with a four-blade pitched-turbine impeller operating at 1001 rpm. The catalyst, co-catalyst and scavenger solutions were mixed immediately before introduction to the reactor at feed rates of 0.26 g/min, 0.26 g/min and 0.46 g/min, respectively. The ethylene, propylene and toluene were also mixed together and fed to the reactor separately from the catalyst, co-catalyst and scavenger solutions at feed rates of 0.52 g/min, 3.04 g/min and 6.62 g/min, respectively. The reactor temperature was maintained at 140° C. as measured by a ⅛″ thermocouple in the reactor. The production rate of copolymer was measured gravimetrically as 0.64 g/min.
The copolymer was found to contain 57 mol. % ethylene as measured by 1H-NMR. The relative number average molecular weight (Mn) and PDI of the copolymer, as measured by GPC were 2331 g/mol and 2.38, respectively. The weight average molecular weight (Mw) of the copolymer as measured by 1H-NMR was 1197 g/mol and the olefin distribution in the copolymer measured by 1H-NMR was 76.9% methyl-vinylidene, 14.4% beta-vinylidene, 6.9% di-substituted and 1.8% vinyl/allyl. The average ethylene run length measured by 13C-NMR was 2.57. The crossover temperature measured by oscillatory rheometry was approximately −17.8° C.
Ethylene propylene copolymer (Example 1) 168.5 g (0.16 mol) and maleic anhydride 23.5 g (0.24 mol) were charged to a 350 mL PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 500 mL round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo. Analytical analysis: acid number: 0.966 and 91.0% functionalized copolymer.
Ethylene propylene copolymer (Example 2) 150 g (0.19 mol) and maleic anhydride 28.3 g (0.29 mol) were charged to a 350 mL PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 500 mL round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo. Analytical analysis: acid number: 1.24 and 91.6% functionalized copolymer.
Ethylene propylene copolymer (Example 3) 822.5 g (0.5 mol) and maleic anhydride 73.55 g (0.75 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 2 L round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 827.5 g of product. Analytical analysis: acid number: 0.577 and 85.4% functionalized copolymer.
Ethylene propylene copolymer (Example 4) 900 g (0.49 mol) and maleic anhydride 72.65 g (0.74 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 2 L round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 901.4 g of product. Analytical analysis: acid number: 0.571 and 84.8% functionalized copolymer.
Ethylene propylene copolymer (Example 5) 781 g (0.7 mol) and maleic anhydride 103.1 g (1.05 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 1 L round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 846.5 g of product. Analytical analysis: acid number: 0.986, and 88.6% functionalized copolymer.
Ethylene propylene copolymer (Example 6 1,000 g (0.76 mol) and maleic anhydride 112.3 g (1.15 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 2 L round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 1076.8 g of product. Analytical analysis: acid number: 0.76, and 78% functionalized copolymer.
Ethylene propylene copolymer (Example 7) 450 g (0.374 mol), ethylene propylene copolymer (Example 8) 450 g (0.386 mol) and maleic anhydride 111.79 g (1.14 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 2 L round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 960.2 g of product. Analytical analysis: acid number: 0.923, and 87.0% functionalized copolymer.
Ethylene propylene copolymer (Example 9) 845.2 g (0.66 mol) and maleic anhydride 97.0 g (0.99 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 2 L 3N-round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 904.2 g of product. Analytical analysis: acid number: 0.858, and 82.2% functionalized copolymer.
Ethylene propylene copolymer (Example 10) 150.0 g (0.11 mol) and maleic anhydride 15.7 g (0.159 mol) were charged to a 35 0 mL PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 500 mL 3N-round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 155.3 g of product. Analytical analysis: acid number: 0.72, and 85.6% functionalized copolymer.
Ethylene propylene copolymer (Example 11) 150.0 g (0.125 mol) and maleic anhydride 18.4 g (0.19 mol) were charged to a 350 mL PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 500 mL 3N-round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 159.5 g of product. Analytical analysis: acid number: 0.78, and 81.3% functionalized copolymer
Ethylene propylene copolymer (Example 12) 150.0 g (0.11 mol) and maleic anhydride 15.7 g (0.160 mol) were charged to a 350 mL PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50° C., purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 500 mL 3N-round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 155.6 g of product. Analytical analysis: acid number: 0.685, and 85.3% functionalized copolymer.
Ethylene propylene copolymer (Example 13) 1,000 g (1.1 mol) and maleic anhydride 161.2 g (1.64 mol) were charged to a 2 L PARR pressure reactor equipped with a stirrer and a thermocouple. The reaction mixture was heated to 50 C, purged with nitrogen for 15 min with stirring. The reactor temperature was raised to 235° C. and maintained at that temperature for 6 h while stirring. The reaction mixture was then cooled to 90° C. and transferred to a 500 mL 3N-round bottom flask. The reaction mixture was then heated and the unreacted maleic anhydride was removed in vacuo affording 1108.5 g of product. Analytical analysis: acid number: 1.057, and 83.8% functionalized copolymer
A 300 mL stirred autoclave was used to prepare a sample which comprised at least 1 kg of ethylene-propylene copolymer. The number average weight of the copolymer was 2085 g/mol, and an ethylene unit content of 65%. The reaction conditions for preparing the copolymer are shown in Table 8 below:
“Slpm” is standard liters per minute at 25° C. and 101.325 kPa. The test was run for 50 minutes and the initial sample was discarded. The reaction was then operated continuously for 6½ hours and the reactor effluent was collected and sampled every 30 to 45 minutes. A total of ten samples were collected, water-washed and rotavaped as discussed below. The samples were each weighed and the polymer content was determined.
The polymer samples were washed in a 4-liter glass separation kettle, which was equipped with an overhead stirrer and an electric heating mantle. Toluene was used to strip the samples in a 2-liter Buchi RR III Rotavap, and the temperature was maintained using a temperature-controlled oil bath.
The separation kettle was charged with one liter of distilled water, and then samples 1-4 were charged to the kettle. The kettle was heated to 50° C. and stirred for 25 minutes. After, the stirring was stopped and the phases were allowed to separate, a total of 1664 grams of toluene-polymer phase was removed without disrupting the aqueous layer.
Following this step, a total of 1479 grams of polymer from samples 5-6 were charged to the kettle. Once again the composition was stirred for 25 minutes at 50° C. and then allowed to separate. An additional 1286 grams of toluene layer was then decanted off the aqueous layer.
Next, samples 7-8 were treated as above and a total of 1341 grams were decanted from the aqueous layer.
Sample 9 was then charged to the kettle, stirred for 25 minutes at 50° C. and allowed to separate overnight. The next morning 615 grams were removed from the aqueous layer and the last sample 10 was added. After charging, stirring the composition at 50° C., and separation of the phases, 746 grams of toluene-polymer composition was decanted off. Then, an additional 214 grams of toluene was added to the kettle to dilute the polymer/toluene layer near the aqueous interface. 172 grams of toluene was then removed and a total of 1134 grams of the aqueous layer was drained from the kettle. The layer contained a visible amount of aluminum oxide along with toluene.
A Rotavap was heated to 120° C. and 10 mm Hg vacuum. The toluene-polymer solution recovered from the kettle was charged in a semi-batch manner to the rotavap over the span of nine hour while the toluene was recovered overhead. The polymer remained in the rotavap during operation and the vacuum was incrementally increased to 24 mm Hg as the polymer concentration increased in order to main the necessary boil-up rate. After all the charge was fed, the rotavap temperature was increased to 140° C. and the vacuum was increased to 29 mm Hg. The rotavap was maintained at these conditions for approximately 90 minutes.
Lastly, the rotavap was cooled and then drained and a total of 1310 grams of polymer was recovered.
While several embodiments of the present invention have been described and illustrated herein, those of ordinary skill in the art will readily envision a variety of other means and/or structures for performing the functions and/or obtaining the results and/or one or more of the advantages described herein, and each of such variations and/or modifications is deemed to be within the scope of the present invention. More generally, those skilled in the art will readily appreciate that all parameters, dimensions, materials, and configurations described herein are meant to be exemplary and that the actual parameters, dimensions, materials, and/or configurations will depend upon the specific application or applications for which the teachings of the present invention is/are used. Those skilled in the art will recognize, or be able to ascertain using no more than routine experimentation, many equivalents to the specific embodiments of the invention described herein. It is, therefore, to be understood that the foregoing embodiments are presented by way of example only and that, within the scope of the appended claims and equivalents thereto the invention may be practiced otherwise than as specifically described and claimed. The present invention is directed to each individual feature, system, article, material, kit, and/or method described herein. In addition, any combination of two or more such features, systems, articles, materials, kits, and/or methods, if such features, systems, articles, materials, kits, and/or methods are not mutually inconsistent, is included within the scope of the present invention.
All definitions, as defined and used herein, should be understood to control over dictionary definitions, definitions in documents incorporated by reference, and/or ordinary meanings of the defined terms.
The indefinite articles “a” and “an,” as used herein in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.”
The phrase “and/or,” as used herein in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.
As used herein in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used herein shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of” “only one of,” or “exactly one of” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.
As used herein in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.
When the word “about” is used herein in reference to a number, it should be understood that still another embodiment of the invention includes that number not modified by the presence of the word “about.”
It should also be understood that, unless clearly indicated to the contrary, in any methods claimed herein that include more than one step or act, the order of the steps or acts of the method is not necessarily limited to the order in which the steps or acts of the method are recited.
In the claims, as well as in the specification above, all transitional phrases such as “comprising,” “including,” “carrying,” “having,” “containing,” “involving,” “holding,” “composed of,” and the like are to be understood to be open-ended, i.e., to mean including but not limited to. Only the transitional phrases “consisting of” and “consisting essentially of” shall be closed or semi-closed transitional phrases, respectively, as set forth in the United States Patent Office Manual of Patent Examining Procedures, Section 2111.03.
Each numerical parameter should at least be construed in light of the number of reported significant digits and by applying ordinary rounding techniques. Notwithstanding that the numerical ranges and parameters setting forth the broad scope of the disclosure are approximations, the numerical values set forth in the specific examples are reported as precisely as possible. Any numerical value, however, inherently contains certain errors necessarily resulting from the standard deviation found in their respective testing measurements. It is intended that the specification and examples be considered as exemplary only, with a true scope and spirit of the disclosure being indicated by the following claims.
The patentees do not intend to dedicate any disclosed embodiments to the public, and to the extent any disclosed modifications or alterations may not literally fall within the scope of the claims, they are considered to be part hereof under the doctrine of equivalents. It is to be understood that each component, compound, substituent or parameter disclosed herein is to be interpreted as being disclosed for use alone or in combination with one or more of each and every other component, compound, substituent or parameter disclosed herein.
It is also to be understood that each amount/value or range of amounts/values for each component, compound, substituent or parameter disclosed herein is to be interpreted as also being disclosed in combination with each amount/value or range of amounts/values disclosed for any other component(s), compounds(s), substituent(s) or parameter(s) disclosed herein and that any combination of amounts/values or ranges of amounts/values for two or more component(s), compounds(s), substituent(s) or parameters disclosed herein are thus also disclosed in combination with each other for the purposes of this description.
It is further understood that each range disclosed herein is to be interpreted as a disclosure of each specific value within the disclosed range that has the same number of significant digits. Thus, a range of from 1-4 is to be interpreted as an express disclosure of the values 1, 2, 3 and 4.
It is further understood that each lower limit of each range disclosed herein is to be interpreted as disclosed in combination with each upper limit of each range and each specific value within each range disclosed herein for the same component, compounds, substituent or parameter. Thus, this disclosure to be interpreted as a disclosure of all ranges derived by combining each lower limit of each range with each upper limit of each range or with each specific value within each range, or by combining each upper limit of each range with each specific value within each range.
Furthermore, specific amounts/values of a component, compound, substituent or parameter disclosed in the description or an example is to be interpreted as a disclosure of either a lower or an upper limit of a range and thus can be combined with any other lower or upper limit of a range or specific amount/value for the same component, compound, substituent or parameter disclosed elsewhere in the application to form a range for that component, compound, substituent or parameter.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US2018/037116 | 6/12/2018 | WO | 00 |
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/US2017/065773 | Dec 2017 | US |
| Child | 16772039 | US |
