Polymer Processing Aids for Polymer Extrusion

Abstract

The present invention relates to a thermoplastic polymer composition comprising a matrix polymer (A) and a polymer processing aid (B), wherein: - (δ polymer (B) – δ matrix polymer (A)) >=2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to Fedor method, and - the melt viscosity ratio of polymer (B) over matrix polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

Description

1 / 34 Polymer Processing Aids for Polymer Extrusion FIELD OF THE INVENTION

[001] The present invention relates to a thermoplastic polymer composition comprising a matrix polymer (A) and a polymer processing aid (B). The present invention also relates to a process for extruding a thermoplastic polymer composition in an extruder and an extruded article. BACKGROUND OF THE INVENTION

[002] In an extrusion process, typically a melt extrusion process, a solid polymer (referred to as a matrix polymer), usually in the form of microgranules or powder, is fed into an extruder and heated to a temperature above the melting point to produce a polymer mass. The polymer mass is then conveyed through an extrusion die located at the end of the extruder and shaped into a desired form, such as a tube, sheet, or film.

[003] During the extrusion process, the polymer mass is subjected to shear stresses which, in part, can cause quality defects on the product surface, the most common quality defect being “fusion fracture”. Fusion fracture appears as a surface haze, often described as a matte finish, and under magnification, visually appears as a rough surface with a sawtooth pattern.

[004] As a molten polymer exits the die, the slower-moving polymer in direct contact with the die accelerates rapidly. This rapid acceleration often causes cohesive fracture on the polymer surface, known as melt fracture. Melt fracture is typically considered an unacceptable quality problem that negatively affects the optical and visual characteristics of the Petition 870250073584, dated 08 / 20 / 2025, page 10 / 57 2 / 34 final product (an example would be a blown film). Fusion fracture can also negatively affect the physical and mechanical properties of the final product.

[005] Melt fracture formation is more prevalent when extruding, for example, high molecular weight polyolefinic polymers, such as those with Melt Index values ​​less than or equal to 1 g / 10 minutes. A high molecular weight polymer is often chosen to obtain better physical and mechanical properties of the produced film, such as higher tensile strength at break. Other times, higher molecular weight polymers are selected for necessary processing characteristics, such as higher strength of the molten polymer. Processes such as blown film extrusion and pipe extrusion are common examples of processes that benefit from polymers with higher melt viscosities.

[006] A quality problem sometimes attributed to melt fracture is the accumulation of polymer at the die exit, and this problem is often called die dripping. When melt fracture occurs, small particles of molten polymer can detach from the surface and accumulate on the tool surfaces near the die exit. Over time, the small particles of molten polymer accumulate and form die dripping. Because die dripping tends to remain in the die for long periods, it can burn and form solid particles that eventually detach from the die and cause quality defects (such as particles and drag marks) in the product. These problems, in addition to increasing scrap rates and labor costs, tend to limit overall production rates. Additives such as mineral fillers (contained in many polymer compounds) can further promote melt fracture and die dripping.

[007] Fusion fracture and matrix dripping formation Petition 870250073584, dated 08 / 20 / 2025, p. 11 / 57 3 / 34 frequently occur in association with another phenomenon called die expansion. Die expansion formation is associated with the rapid release of elastic stresses in the molten material as it exits the die. Excessive die expansion is known to contribute to quality problems.

[008] Extrusion of low-melting-index polymers often generates high melt pressures. Production speed is often limited by the maximum melt pressure of the system used.

[009] To address and solve these problems, polymer processing aids (PPAs) containing fluoropolymers are widely used. A polymer processing aid can act by depositing a “slippery” coating on the internal surfaces of the tool that are in direct contact with the molten polymer. This creates a “wall slide,” where the polymer at the interface with the die wall slides, thus reducing stress on the molten material as it exits the die. The molten polymer can then flow through the die with less shear stress formation, which eliminates melt fracture and reduces melt pressures.Polymer processing aids can provide multiple benefits, including, but not limited to, reducing or eliminating melt fracture (resulting in visually clearer products), less die expansion, less die dripping, lower melt pressures, faster line speeds, and improved product properties.

[010] For melt-processable thermoplastic polymers (and compounds), there is a shear rate that, if processed below, will produce only a smooth (and often glossy) surface and, if above, will produce a rough (and often dull) surface. The shear rate at which surface defects are first observed is called the Critical Shear Rate (CSR). Petition 870250073584, dated 08 / 20 / 2025, page 12 / 57 4 / 34 Below the shear stress test (SST), the polymer surface is typically smooth, and just above the SST, melt fracture begins to form. As a general rule, as the shear rate increases above the SST, the size or intensity of the melt fracture also increases. An example of a polymer with these characteristics would be a polyolefinic polymer, such as LLDPE (linear low-density polyethylene) resin, used in the manufacture of blown films. Other examples include LDPE (low-density polyethylene), MDPE (medium-density polyethylene), UHDPE (ultra-high-density polyethylene), or HDPE (high-density polyethylene).

[011] Low melt index LLDPE polymers typically exhibit low critical shear rates and are more prone to melt fracture formation. As a general rule, the lower the melt index of the polymer, the more prone the polymer will be to melt fracture formation. Since low melt index LLDPE polymers are typically used to produce blown films, as would be expected, melt fracture problems are a common concern in these processes.

[012] US patent 5986005 describes a composition comprising a fluoroelastomer and a thermoplastic polyamide diluted in a hydrocarbon polymer, to improve the conversion of hydrocarbon polymers. Thermoplastic polyamide is defined as a polymer containing polyamide blocks and polyether blocks.

[013] WO 02 / 066544 describes an extrudable composition comprising a non-fluorinated melt-processable polymer and a fluoropolymer processing aid.

[014] Document US2013 / 093118 describes a composition comprising a polyolefin and a polymer which may be a polyamide, copolyamide, a second polyolefin different from the first, ethylene vinyl acetate (EVA) copolymers, ethylene and Petition 870250073584, dated 08 / 20 / 2025, page 13 / 57 5 / 34 vinyl alcohol (EVOH), polystyrene, polycarbonate and polyvinyl chloride (PVC).

[015] WO 2023 / 017327 describes a polymer processing aid comprising a block copolymer having polyamide blocks and polyether blocks and significantly reducing melt defects in a thermoplastic polyolefin.

[016] However, it has been found that the PPAs mentioned above do not achieve a satisfactory result in reducing fusion defects.

[017] Therefore, there is a need for PPA additives that are more effective than the known fluorinated PPA or other type of PPA known in the art. SUMMARY OF THE INVENTION

[018] The present invention provides a thermoplastic polymer composition comprising a matrix polymer (A) and a PPA polymer processing aid (B), wherein:

[019] - (δ polymer (B) - δ matrix polymer (A)) >=2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to the Fedor method, and

[020] - the melt viscosity ratio of polymer (B) to the parent polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

[021] The solubility parameter is determined according to the Fedor method (RF Fedors, Polymer engineering and science 142, 147 to 154, 1974; RF Fedors, Polym. Eng. Science, vol.14, No.2, 147, 1974), according to the following formula: _ / Σ Ag / V / 2 (Σ>· ) δε corresponds to the cohesive energy and V to the molar volume.

[022] The method therefore consists of adding up the contributions Petition 870250073584, dated 08 / 20 / 2025, page 14 / 57 6 / 34 energy contributions of the various groups that make up the polymer. The energy contributions of the different groups are indicated in the following document: Eric A. Grulke, Solubility Parameter Values, Polymer Handbook, 4th edition, 1999, VII / 675-714.

[023] According to the present invention, the amount of the matrix polymer (A) is at least 50%, typically from 55 to 99.9% by weight in the thermoplastic polymer composition.

[024] In some embodiments, the thermoplastic polymer composition comprises more than one polymer processing aid.

[025] The present invention makes it possible to meet the need expressed above. It provides, more particularly, enhanced PPA additives to improve the processability of extruded polymers. For example, it reduces or eliminates melt fractures, matrix buildup and / or surface defects in polymer compositions during the extrusion process. This is achieved through the use of a specific polymer processing aid, considering the matrix polymer used in the extrusion process.

[026] Compared to conventional fluorinated PPAs, it is even more advantageous because it is cheaper and halogen-free.

[027] The present invention, therefore, provides more effective PPA additives for improving the processability of extruded polymeric materials, in particular for reducing melt fracture.

[028] In some embodiments, the amount of polymer processing aid (B) in the thermoplastic polymer composition is 50 to 5000 ppm (parts per million), preferably 100 to 3000 ppm, more preferably 200 to 3000 ppm, based on the weight of the matrix polymer.

[029] In some embodiments, the matrix polymer is a polyolefin composition, preferably a polyolefin composition with Petition 870250073584, dated 08 / 20 / 2025, page 15 / 57 7 / 34 preende, consiste essencial em, ou consiste em poliolefin não funcionalizado.

[030] In some embodiments, the matrix polymer comprises, consists essentially of, or consists of linear low-density polyethylene (LLDPE), low-density polyethylene (LDPE), medium-density polyethylene (MDPE), high-density polyethylene (HDPE), ultra-high-density polyethylene (UHDPE) or polypropylene (PP), or combinations thereof.

[031] In some embodiments, the polymer processing aid is chosen from a polyamide, a PEBA or a mixture thereof.

[032] In some embodiments, the polymer processing aid is a polyamide.

[033] In some embodiments, the polymer processing aid is a polyamide being or comprising a homopolyamide including PA6, PA10, PA11 and / or PA12, and / or a copolyamide including PA66; PA610; PA612; PA1012; PA1212; and / or PA6, 10, 12, preferably PA11.

[034] In some embodiments, the polymer processing aid is a copolyamide.

[035] In some embodiments, the polymer processing aid is a PEBA.

[036] In some embodiments, the polymer processing aid (B) has a solubility parameter greater than 20.0, preferably greater than 21.0 (J1 / 2.cm-3 / 2), the solubility parameter being calculated according to the Fedor method, and a melt viscosity between 10 and 500 Pa.s, preferably between 20 and 400, more preferably between 20 and 350, measured by capillary rheometry at 210° C and at a shear rate of 100 s-1.

[037] In some embodiments, the thermo polymeric composition Petition 870250073584, dated 08 / 20 / 2025, p. 16 / 57 8 / 34 plastic comprises at least one adjuvant, preferably the adjuvant is or comprises one or more selected from a polyether, an aliphatic polyester, a poly(hydroxybutyrate), a silicone, a fatty acid ester and a fatty acid amide, preferably a polyether copolymer.

[038] According to another aspect, the present invention relates to a process for extruding a thermoplastic polymer composition comprising a matrix polymer (A) in an extruder, comprising a step of feeding a polymer processing aid into the extruder, wherein:

[039] - (δ polymer (B) - δ matrix polymer (A)) >=2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to the Fedor method, and

[040] - the melt viscosity ratio of polymer (B) to the parent polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

[041] In some embodiments, the process also includes a step of feeding at least one adjuvant into the extruder.

[042] In some embodiments, the polymer processing aid and the adjuvant, if present, are fed in the form of a master composition containing a carrier polymer (C).

[043] In some embodiments, the polymer processing aid and the adjuvant, if present, are fed directly into the extruder, separately, simultaneously or as a blend.

[044] In some embodiments, the matrix polymer is a polyolefin, preferably, the polyolefin composition comprises, consists essentially of, or consists of non-functionalized polyolefin.

[045] In some embodiments, the matrix polymer comprises, consists essentially of, or consists of a linear polyethylene of Petition 870250073584, dated 08 / 20 / 2025, p. 17 / 57 9 / 34 low-density polyethylene (LLDPE), low-density polyethylene (LDPE), medium-density polyethylene (MDPE), high-density polyethylene (HDPE), ultra-high-density polyethylene (UHDPE) or polypropylene (PP), or combinations thereof.

[046] In some embodiments, the amount of polymer processing aid (B) varies from 50 to 5000 ppm, preferably from 100 to 3000 ppm, more preferably from 200 to 3000 ppm, based on the weight of the matrix polymer.

[047] In some embodiments, the polymer processing aid is chosen from a polyamide, a PEBA or a mixture thereof.

[048] In some embodiments, the polymer processing aid (B) has a solubility parameter greater than 20 (J1 / 2.cm3 / 2), the solubility parameter being calculated according to the Fedor method, and a melt viscosity between 10 and 500 Pa.s, preferably between 20 and 500, more preferably between 20 and 400, more preferably between 30 and 100, measured by capillary rheometry at 210° C and at a shear rate of 100 s-1.

[049] In some embodiments, the polymer processing aid is a polyamide, a PEBA, or a mixture thereof.

[050] Preferably, polyamide is chosen from PA66, PA 610, PA612, PA1010, PA1012, PA 1212 or a copolyamide PA 6 / 12, PA 6 / 11, PA 6 / 1010, PA 6 / 66, PA 6 / 66 / 12, PA 6 / 66 / 11, PA 6 / 66 / 610, PA 6 / 612 / 11 or a mixture of these polymers.

[051] Preferably, the PEBA block polyamide is chosen from PA66, PA 610, PA612, PA1010, PA1012, PA 1212 or a copolyamide PA 6 / 12, PA 6 / 11, PA 6 / 1010, PA 6 / 66, PA 6 / 66 / 12, PA 6 / 66 / 11, PA 6 / 66 / 610, PA 6 / 612 / 11, or a mixture of these polymers.

[052] In some embodiments, one or more polymer processing aids are mixed (e.g., premixed) or Petition 870250073584, dated 08 / 20 / 2025, page 18 / 57 10 / 34 pre-blended (e.g., dry blended or melt blended) with the matrix polymer, followed by extrusion of the matrix polymer.

[053] In some embodiments, one or more polymer processing aids are co-fed with the matrix polymer into the extruder.

[054] In some embodiments, one or more polymer processing aids are added to the matrix polymer to prepare a masterbatch. The resulting masterbatch can then be used to introduce one or more polymer processing aids into the matrix polymer in any conventional manner before extrusion of the matrix polymer (e.g., dry blending or melt blending) or during extrusion of the matrix polymer (e.g., co-feeding with the matrix polymer in an extruder).

[055] According to another aspect, the present invention relates to an extruded article comprising a polymeric composition as defined above, preferably the article being a film, a sheet, a tube, a pipe, a yarn, a fiber, a cable, a yarn coating or a cable jacket.

[056] According to another aspect, the present invention relates to the use of a polymer (B) as a processing aid for the extrusion of a thermoplastic polymeric composition comprising a matrix polymer (A), wherein:

[057] - (δ polymer (B) - δ matrix polymer (A)) >=2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to the Fedor method, and

[058] - the melt viscosity ratio of polymer (B) to the parent polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1. Petition 870250073584, dated 08 / 20 / 2025, page 19 / 57 11 / 34 DETAILED DESCRIPTION

[059] The invention will now be described in more detail, without limitation, in the following description.

[060] According to the invention, a PPA is used to improve the processability of an extruded thermoplastic composition comprising a matrix polymer. Preferably, a PPA is used as a polymer processing aid in the extrusion of a polyolefin composition.

[061] The term “polymer processing aid” or PPA, also known as “extrusion agent”, refers to an additive used to improve the conversion of polymeric materials, improve the extrusion processability of polymeric materials and / or reduce quality defects, such as melt fracture and die buildup, that may arise during the extrusion process, and may also improve the mechanical and / or optical properties of polymeric materials.

[062] Examples of improvements provided by the use of PPA according to the invention include, among others, elimination or reduction of melt fracture (shark skin); improved film transparency; improved smoothness and surface appearance; improved product appearance; improved mechanical properties; reduced gels; gauge control; reduced maintenance time; reduced die buildup; production consistency; smoother extrusion conditions; lower energy consumption; reduced cycle times and faster transition; reduced potential negative interaction with other film additives, such as antiblocking light stabilizers and hindered amine (HALS); reduced extruder torque; reduced critical polymer shear rate.

[063] A common way of evaluating PPA performance is to measure the time required to eliminate fusion fracture after introduction. Petition 870250073584, dated 08 / 20 / 2025, page 20 / 57 12 / 34 of the PPA. A typical test involves establishing extrusion conditions favorable to melt fracture formation, which include the appropriate selection of tools, polymers, and process conditions. Once the correct conditions for melt fracture formation are obtained and the process stabilized, PPA can be added, and the time required to eliminate melt fracture recorded. A better-performing PPA is one that requires less time to eliminate melt fracture. The time elapsed after extruder startup, during which the extruded articles exhibit a high degree of melt fracture before obtaining an extrudate with a smooth, melt fracture-free surface, is also called the conditioning time.

[064] In general, PPAs capable of eliminating fusion fracture quickly also exhibit greater efficiency. As an example, when producing a blown film, if one PPA can eliminate fusion fracture in 30 minutes and another PPA in 40 minutes, the PPA capable of eliminating fusion fracture in 30 minutes is considered more efficient in eliminating fusion fracture.

[065] The present invention relates to a thermoplastic polymer composition comprising a matrix polymer (A) and a PPA polymer processing aid (B), wherein:

[066] - (δ polymer (B) - δ matrix polymer (A)) >=2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to the Fedor method, and

[067] - the melt viscosity ratio of polymer (B) to the parent polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

[068] In some embodiments, the difference between the polymer solubility parameter (B) and the polymer solubility parameter Petition 870250073584, dated 08 / 20 / 2025, p. 21 / 57 13 / 34 matrix (A) (polymer δ (B) - polymer matrix δ (A)) is greater than 3.2, preferably greater than 3.5, more preferably greater than 4.0 and even more preferably greater than 5.0 (J1 / 2.cm-3 / 2).

[069] In some embodiments, the melt viscosity ratio of the polymer (B) to the matrix polymer (A) is less than 0.15, preferably less than 0.10 and more preferably less than 0.05.

[070] In some embodiments, the thermoplastic polymer composition comprises a matrix polymer (A) and a PPA polymer processing aid (B), wherein:

[071] - (δ polymer (B) - δ matrix polymer (A)) > 3.2 (J1 / 2.cm-3 / 2), preferably > 3.5 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to the Fedor method, and

[072] - the melt viscosity ratio of polymer (B) to the parent polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

[073] In some embodiments, the thermoplastic polymer composition has a ratio of (δ polymer (B) - δ matrix polymer (A)) to (ratio of melt viscosity of polymer (B) to matrix polymer (A)) that is greater than 13.1, preferably greater than 20.0, more preferably greater than 30.0.

[074] According to the present invention, the polymer processing aid is typically chosen from a polyamide, copolyether block amides (PEBA) or a mixture thereof. Polyamide

[075] According to the present invention, the polymer processing aid is typically a homopolyamide, i.e., a polyamide obtained from a single type of monomer, or a copolyamide, i.e., a polyamide obtained from several types of monomers. Petition 870250073584, dated 20 / 08 / 2025, page 22 / 57 14 / 34 different numbers.

[076] In some embodiments, the polymer processing aid is homopolyamide.

[077] In some embodiments, the polymer processing aid is copolyamide.

[078] The monomer (repeating unit) that constitutes the polyamide can be chosen from units derived from an amino acid, a lactam and a unit corresponding to the formula (Ca diamine) (Cb diacid), with a representing the number of carbon atoms of the diamine and b representing the number of carbon atoms of the diacid, with a and b varying from 4 to 36.

[079] When the unit represents a unit derived from an amino acid, it may be chosen from 9-aminononanoic acid (A = 9), 10-aminodecanoic acid (A = 10), 12-aminododecanoic acid (A = 12) and 11-aminoundecanoic acid (A = 11), and their derivatives, in particular N-heptyl-11-aminoundecanoic acid.

[080] When the unit represents a unit derived from a lactam, it can be chosen from pyrrolidinone, 2-piperidinone, caprolactam (A = 6), enantholactam, caprylolactam, pelargolactam, decanolactam, undecanolactam and laurilactam (A = 12).

[081] When the unit represents a unit derived from a unit corresponding to the formula (Ca diamine).(Cb diacid), the unit (Ca diamine) is chosen from linear or branched aliphatic diamines, cycloaliphatic diamines and alkylaromatic diamines.

[082] When the diamine is aliphatic and linear, with the formula H2N(CH2)a-NH2, the monomer (Ca diamine) is preferably chosen from butanediamine (a = 4), pentanediamine (a = 5), hexanediamine (a = 6), heptanediamine (a = 7), octanediamine (a = 8), nonanediamine (a = 9), decanediamine (a = 10), undecanediamine (a = 11), dodecanediamine (a = 12), tridecanediamine (a = 13), tetradecanediamine (a = Petition 870250073584, dated 08 / 20 / 2025, page 23 / 57 15 / 34 14), hexadecanediamine (a = 16), octadecanediamine (a = 18), octadecenodiamine (a = 18), eicosanediamine (a = 20), docosanediamine (a = 22) and diamines obtained from fatty acids.

[083] When the diamine is aliphatic and branched, it may contain one or more methyl or ethyl substituents on the main chain. For example, the monomer (Ca diamine) may be advantageously selected from 2,2,4-trimethyl-1,6-hexanediamine, 2,4,4-trimethyl-1,6-hexanediamine, 1,3-diaminopentane, 2-methyl-1,5-pentanediamine and 2-methyl-1,8-octanediamine.

[084] When the monomer (Ca diamine) is cycloaliphatic, it is preferably chosen from bis(3,5-dialkyl-4-aminocyclohexyl)methane, bis(3,5-dialkyl-4-aminocyclohexyl)ethane, bis(3,5-dialkyl-4-aminocyclohexyl)propane, bis(3,5-dialkyl-4-aminocyclohexyl)butane, bis(3-methyl-4-aminocyclohexyl)methane (BMACM or MACM), p-bis(aminocyclohexyl)methane (PACM) and isopropylidene di(cyclohexylamine) (PACP). It may also comprise the following carbon-based structural chains: norbornylmethane, cyclohexylmethane, dicyclohexylpropane, di(methylcyclohexyl) and di(methylcyclohexyl)propane. A non-exhaustive list of these cycloaliphatic diamines is presented in the publication “Cycloaliphatic Amines” (Encyclopedia of Chemical Technology, Kirk-Othmer, 4th edition (1992), pp. 386-405). When the monomer (Ca diamine) is alkylaromatic, it is preferably chosen from among 1,3-xylylenediamine and 1,4-xylylenediamine.

[085] When the unit is a unit corresponding to the formula (Ca diamine).(Cb diacid), the unit (Cb diacid) is chosen from linear or branched aliphatic diacids, cycloaliphatic diacids and aromatic diacids.

[086] When the monomer (Cb diacid) is aliphatic and linear, it is chosen from succinic acid (b = 4), pentanedioic acid (b = 5), adipic acid (b = 6), heptanedioic acid (b = 7), octanedioic acid (b Petition 870250073584, dated 08 / 20 / 2025, page 24 / 57 16 / 34 = 8), azelaic acid (b = 9), sebacic acid (b = 10), undecanedioic acid (b = 11), dodecanedioic acid (b = 12), brassylic acid (b = 13), tetradecanedioic acid (b = 14), hexadecanedioic acid (b = 16), octadecanedioic acid (b = 18), octadecenedioic acid (b = 18), eicosanedioic acid (b = 20), docosanedioic acid (b = 22) and fatty acid dimers containing 36 carbons.

[087] The fatty acid dimers mentioned above are dimerized fatty acids obtained by oligomerization or polymerization of long-chain unsaturated monobasic fatty acids based on hydrocarbons (such as linoleic acid and oleic acid), as described in particular in document EP 0 471 566.

[088] When the diacid is cycloaliphatic, it may comprise the following carbon-based main chains: norbornylmethane, cyclohexylmethane, dicyclohexylmethane, dicyclohexylpropane, di(methylcyclohexyl) and di(methylcyclohexyl)propane. When the diacid is aromatic, it is preferably chosen from terephthalic acid (denoted T), isophthalic acid (denoted I) and naphthalenic diacids.

[089] Polyamides can be crystalline or amorphous and transparent.

[090] Preferably, the polyamides according to the invention are selected from aliphatic polyamides, more particularly those whose chain length of the units ranges from 4 to 18, more particularly from 4 to 12.

[091] More preferably, the polyamides according to the invention are selected from polyamides such as PA6, PA10, PA11, PA12, PA66, PA610, PA612, PA1010, PA1012, PA1212.

[092] More preferably, the polyamides according to the invention are selected from a copolyamide PA 6 / 12, PA 6 / 11, PA 6 / 1010, PA 6 / 66, PA 6 / 66 / 12, PA 6 / 66 / 11, PA 6 / 66 / 610, PA 6 / 612 / 11 or a mixture of these polymers. Petition 870250073584, dated 08 / 20 / 2025, p. 25 / 57 17 / 34

[093] The number molecular weight of polyamide can vary considerably, as those skilled in the art will understand. In some embodiments, the number average molecular weight Mn of polyamide is between 300 and 50,000 g / mol, preferably between 500 and 30,000 g / mol, more preferably between 1,000 and 25,000 g / mol.

[094] The number average molecular weight, or number average molar mass Mn, is expressed in PMMA equivalents (used as a calibration standard) and can be measured by size exclusion chromatography (SEC), according to ISO 16014-1:2019, with the polymer dissolved in hexafluoroisopropanol stabilized with 0.05 M potassium trifluoroacetate for 24 h at room temperature at a concentration of 1 g / L before being passed through the columns, for example, at a flow rate of 1 ml / min, the molar mass being measured by the refractive index.Size exclusion chromatography can be performed using modified silica columns, for example, in a set of two columns and a modified silica pre-column (such as PGF columns and Polymer Standards Service pre-columns) comprising a 1000 A column with dimensions of 300 x 8 mm and a particle size of 7 μm, a 100 A column with dimensions of 300 x 8 mm and a particle size of 7 μm, and a pre-column with dimensions of 50 x 8 mm, for example, at a temperature of 40° C.

[095] Polyamide or copolyamide can be obtained by condensation / fusion of a single type of monomer or two different types of monomers, as described above.

[096] Some suitable polyamides or copolyamides are commercially available from ARKEMA under the registered trademarks RILSAN® and Platamid®, or from EVONIK under the registered trademarks VESTAMID® and VESTAMELT®, or from EMS under the registered trademarks GRILAMID® and GRILTEX®.

[097] A polyamide, such as PA 12, or a copolyamide ade Petition 870250073584, dated 08 / 20 / 2025, p. 26 / 57 18 / 34 Quada according to the present invention can also be obtained by anionic polymerization of lactam(s) in solvent or in solution. Some suitable ones are commercially available under the ORGASOL® brand name from Arkema. PEBA

[098] According to the present invention, the polymer processing aid can be a copolyether block amide (PEBA), resulting from the polycondensation of reactive-ended polyamide blocks with reactive-ended polyether blocks, such as, among others:

[099] 1) polyamide blocks with diamine chain ends with polyoxyalkylene blocks with dicarboxylic chain ends;

[100] 2) polyamide blocks with dicarboxylic chain ends with polyoxyalkylene blocks with diamine chain ends, obtained by cyanoethylation and hydrogenation of aliphatic α,ω-dihydroxylated polyoxyalkylene blocks, known as polyetherdiols;

[101] 3) polyamide blocks containing dicarboxylic chain ends with polyetherdiols, the products obtained being, in this specific case, polyetheresteramides.

[102] The number average molecular weight (Mn) of PEBA can vary between 500 and 30,000 g / mol, preferably between 1,000 and 25,000 g / mol, more preferably between 1,000 and 20,000 g / mol, even more preferably between 1,000 and 15,000 g / mol. The number average molar weight of PEBA can be measured before copolymerization of the blocks by gel permeation chromatography (GPC).

[103] Polyamide blocks containing dicarboxylic chain ends originate, for example, from the condensation of polyamide precursors in the presence of a chain-limiting dicarboxylic acid (also called a chain limiter). Polyamide blocks with Petition 870250073584, dated 08 / 20 / 2025, page 27 / 57 19 / 34 diamine chain ends originate, for example, from the condensation of polyamide precursors in the presence of a chain-limiting diamine (also called a chain-limiting molecule).

[104] Polymers containing polyamide blocks and polyether blocks may also comprise randomly distributed units.

[105] Types of polyamide blocks can be used as described above for polyamide. Typically, the polyamides that constitute the polyamide blocks are selected from aliphatic polyamides, more particularly those whose chain length of the units ranges from 4 to 18, more particularly from 4 to 12.

[106] More preferably, the polyamides that constitute the polyamide blocks are selected from PA6, PA10, PA11, PA12, PA66, PA 610, PA612, PA1010, PA1012, PA1212 or a copolyamide PA 6 / 12, PA 6 / 11, PA 6 / 1010, PA 6 / 66, PA 6 / 66 / 12, PA 6 / 66 / 11, PA 6 / 66 / 610, PA 6 / 612 / 11 or a blend of these polymers.

[107] PE polyether blocks are formed from alkylene oxide units. These units can be, for example, ethylene oxide units, propylene oxide units or tetrahydrofuran (which leads to polytetrahydrofuran sequences). Therefore, PEG (polyethylene glycol) blocks are used, i.e., blocks formed from ethylene oxide units, PPG (propylene glycol) blocks, i.e., blocks formed from propylene oxide units, PO3G (polytrimethylene glycol) blocks, i.e., blocks formed from polytrimethylene glycol ether units (such copolymers with polytrimethylene glycol ether blocks are described in US6590065), and PTMG blocks, i.e., blocks formed from tetramethylene glycol units, also known as polytetrahydrofuran. PEBA copolymers can comprise various types of polyethers in their chain, with the copolymers possibly being in block form. Petition 870250073584, dated 08 / 20 / 2025, p. 28 / 57 20 / 34 or statistics.

[108] Blocks obtained by oxyethylation of bisphenols, for example, bisphenol A, can also be used. These latter products are described in patent EP613919.

[109] Polyether blocks can also be formed from ethoxylated primary amines. As examples of ethoxylated primary amines, the following formula products can be mentioned: H--(OCH2CH2)m—N--(CH2CH2Ü)n—H (CH2)xch3em where men are between 1 and 20 and ex is between 8 and 18. These products are commercially available under the brand name Noramox® from the company CECA and under the brand name Genamin® from the company Clariant.

[110] Flexible polyether blocks can be composed of polyoxyalkylene blocks with NH2 chain ends, such blocks being obtainable by cyanoacetylation of aliphatic α,ω-dihydroxylated polyoxyalkylene blocks, called polyetherdiols. More specifically, Jeffamine products can be used (for example, Jeffamine® D400, D2000, ED 2003, XTJ 542, which are commercial products of the Huntsman company, also described in patents JP2004346274, JP2004352794 and EP1482011).

[111] Polyetherdiol blocks are used in unmodified form and copolycondensed with polyamide blocks containing carboxylic end groups, or are aminated to be converted into polyetherdiamines and condensed with polyamide blocks containing carboxylic end groups. The general method for the two-step preparation of PEBA copolymers containing ester linkages between PA blocks and PE blocks is known and described, for example, in French patent FR2846332. The general method for the preparation of Petition 870250073584, dated 08 / 20 / 2025, page 29 / 57 21 / 34 PEBA copolymers of the invention containing amide linkages between PA blocks and PE blocks are known and described, for example, in European patent EP1482011. The polyether blocks can also be blended with polyamide precursors and a chain-limiting diacid to form polymers containing polyamide blocks and polyether blocks with randomly distributed units (one-step process).

[112] It goes without saying that the name PEBA in the present description of the invention refers not only to Pebax® products sold by Arkema, Vestamid® products sold by Evonik® and Grilamid® products sold by EMS, but also to Kellaflex® products sold by DSM or to any other PEBA from other suppliers.

[113] The number-average molar mass Mn of the polyamide blocks in PEBA can typically range from 400 to 20,000 g / mol, preferably from 500 to 10,000 g / mol, and more preferably from 600 to 5,000 g / mol.

[114] The number average molar mass of the polyether blocks can typically be from 100 to 6,000 g / mol, preferably from 200 to 3,000 g / mol, more preferably from 600 to 2,500 g / mol.

[115] The number-average molar mass is defined by the chain-limiting content. It can be calculated according to the equation:

[116] Mn = n monomer x MW repeating unit / C chain limiter + MW chain limiter

[117] In this formula, nmonomer represents the number of moles of monomer, nchain limiter represents the number of moles of excess diacid limiter, MWrepeating unit represents the molar mass of the repeating unit, and MWchain limiter represents the molar mass of the excess diacid. Adjuvant

[118] In some embodiments, the polymer processing aid is used in combination with at least one adjuvant. In other words, the polymer processing aid and at least Petition 870250073584, dated 08 / 20 / 2025, p. 30 / 57 22 / 34 an adjuvant is used together with a PPA in the extrusion of the polymer composition. The adjuvant can be selected to further improve the stability and / or effectiveness of that PPA. Examples of adjuvants include, but are not limited to:

[119] i) Aliphatic polyesters, such as poly(caprolactone), poly(lactic acid) and poly(butylene adipate);

[120] ii) Poly(hydroxybutyrate);

[121] iii) Silicones;

[122] iv) Fatty acid esters, such as sorbitan monolaurate;

[123] v) Fatty acid amides, such as stearamide and erucamide.

[124] The polymer processing aid and adjuvant may be supplied as a blend before being included in a masterbatch or before being added directly to the polymer composition, as described below. The blend may be formed by a process comprising dry blending, melt blending or compounding. It may be in the form of microgranules or powder, for example.

[125] Matrix polymer (A)

[126] In some embodiments of the invention, the matrix polymer (A) is a polyolefin composition, preferably, the polyolefin composition comprises, consists essentially of, or consists of non-functionalized polyolefin.

[127] Examples of polyolefin composition include, among others, linear low-density polyethylene (LLDPE), low-density polyethylene (LDPE), medium-density polyethylene (MDPE), high-density polyethylene (HDPE), ultra-high-density polyethylene (ULDPE), polypropylene (PP) or combinations thereof. Preferably, the polyolefin composition comprises, consists essentially of, or consists of an LDPE or an LLDPE. Petition 870250073584, dated 08 / 20 / 2025, page 31 / 57 23 / 34

[128] The melt index of the matrix polymer can vary from 0.01 g / 10 min to 100 g / 10 min, preferably from 0.06 g / 10 min to 60 g / 10 min and, more preferably, from 0.06 to 10 g / 10 min (melt index measured with a weight of 2.16 kg, with a collection shear rate of 300 s-1e at a melt temperature of 190° C).

[129] In one embodiment, these bands apply to the matrix composition without / before the addition of PPA. In another embodiment, these bands apply to the resulting thermoplastic composition after the addition of PPA.

[130] The polydispersity of the matrix polymer composition can vary from 1.1 to 9.0, preferably from 1.1 to 4.0 and, more preferably, from 1.1 to 2.5. These ranges apply to the matrix composition without / before the addition of PPA.

[131] The Polydispersity Index (PDI) is a measure of chain length homogeneity, calculated by the ratio between the weight-average molecular weight (Mw) and the number-average molecular weight (Mn). These values ​​are defined by the following formulas. Mn EN^ EN Mw ΣNM2 ΣN^ P Dl MwM

[132] Where Ni is the number of molecules and Mi is the molar mass of the molecules.

[133] The polydispersity of the matrix polymer can typically be determined by gel permeation chromatography (GPC)-viscometry. The GPC-viscometry technique was based on the ASTM D6474-99 standard method and uses a dual refractometer / viscometer detector system to analyze polymer samples.

[134] In some embodiments, polyolefin in the composition Petition 870250073584, dated 08 / 20 / 2025, page 32 / 57 24 / 34 polyolefin is or comprises non-functionalized polyolefin.

[135] The polyolefin composition may also include one or more additives, such as fillers, pigments, dyes, antioxidants, UV absorbers and light stabilizers, nucleating agents and reinforcing agents.

[136] The filler may comprise dispersed organic or inorganic particles. An inorganic filler may be, for example, silica, alumina, zeolite, titanium oxide, carbonate (e.g., sodium carbonate or potassium carbonate), hydrotalcite, talc, zinc oxide, magnesium oxide or calcium oxide, diatomaceous earth, carbon black and the like. Pigments may be inorganic or organic.

[137] In some embodiments, the polyolefin composition is extruded as a film, tube or sheet, for example, as a blown film.

[138] PPA and at least one adjuvant, if present, are added to the thermoplastic polymer composition to be extruded in such a way that the total amount of PPA and at least one adjuvant (if present) is between 10 and 200,000 ppm by weight, preferably between 25 and 100,000 ppm by weight, more preferably between 50 and 2,000 ppm by weight, based on the total weight of the resulting thermoplastic composition after extrusion.

[139] In the case where PPA is used in conjunction with at least one adjuvant, the weight ratio of PPA and at least one adjuvant in the resulting polymer composition may be in the range of 90:10 to 20:80, preferably 70:30 to 30:70, more preferably 60:40 to 40:60 and, for example, approximately 50:50. Master

[140] In some embodiments, PPA (B) and the adjuvant, if present, are added together in the form of a masterbatch to the thermoplastic polymer composition comprising the matrix polymer (A). Petition 870250073584, dated 08 / 20 / 2025, p. 33 / 57 25 / 34

[141] In the present application, the term “master” refers to a composition consisting of a polymer processing aid predispersed in a carrier polymer. The term “carrier polymer” or “diluent polymer” describes a primary component of a master used to contain a composition of polymer processing aids. The carrier polymer may be or comprise the same polymer composition to be extruded. Alternatively, the carrier polymer may be or comprise a different polymer composition that does not adversely affect the extrusion behavior of the polymer composition to be extruded. In the present application, the polymer composition to be extruded, i.e., the host resin or matrix polymer, is the polyolefin composition.

[142] The masterbatch may be supplied in powder, granule or microgranule form. Preparation of the masterbatch may utilize any method or process known in the art, such as the method described in US8501862.

[143] The masterbatch is normally produced by compound extrusion to produce a product in the form of microgranules, but other embodiments besides microgranules may also be included.

[144] The carrier polymer may be a polyolefin, which may be functionalized, non-functionalized or a mixture thereof. For example, it may be a polyethylene, such as low-density polyethylene (LDPE), high-density polyethylene (HDPE), linear low-density polyethylene (LLDPE), medium-density polyethylene (MDPE) or ultra-high-density polyethylene (ULDPE), or combinations thereof. It may be a polyethylene obtained using a metallocene-type catalyst or, more generally, a 'single-site' catalyst, a Phillips-type catalyst or a Ziegler-Natta-type catalyst; a polypropylene, in particular an iso- or syndiotactic polypropylene; a biaxially oriented polypropylene; a polybutene (obtained from Petition 870250073584, dated 08 / 20 / 2025, p. 34 / 57 26 / 34 from 1-butene); a poly(3-methylbutene) or a poly(4-methylpentene); blends of two or more polyolefins, for example, a blend of an LLDPE with an LDPE, can be used as the carrier.

[145] The carrier polymer can be a copolymer, for example, ethylene acrylate (which can be found under the trademark Lotryl® from SK Functional Polymer) or ethylene vinyl acetate.

[146] The selection of a suitable polyolefin carrier polymer for the masterbatch typically addresses several issues, including miscibility in the polyolefin polymer to be used and the ability to disperse well without gel formation. A masterbatch prepared with a low Melting Index (high melt viscosity) carrier polymer would be expected to generate gels or have the potential to generate gels if introduced into a higher Melting Index polyolefin polymer. The gel formed would specifically consist of a large, undispersed agglomerate of the masterbatch. Typically, the carrier polymer is selected to have a Melting Index equal to or greater than that of the parent polymer to be used. A typical Melting Index range for a carrier polymer is between 0.06 and 20, and a masterbatch produced with this polyethylene carrier polymer would be most suitable in polyolefin polymers with a Melting Index less than or equal to 2.

[147] In some embodiments, PPA and adjuvant, if present, are added to the thermoplastic polymer composition comprising the matrix polymer in the form of a polyolefin-containing masterbatch.

[148] In some embodiments, the masterbatch comprises PPA and adjuvant, if present, at levels in the range of 1 to 30% by weight, preferably between 2 and 15% by weight, more preferably between 5 and 10% by weight, based on the total weight of the masterbatch. For example, the amount of PPA and adjuvant, if present in the masterbatch, is approximately 7.5% by weight.

[149] The master can be used in any known way Petition 870250073584, dated 08 / 20 / 2025, p. 35 / 57 27 / 34 in the art and is typically premixed with a thermoplastic polymer composition comprising the matrix polymer in the form of microgranules or powder, or individually fed using suitable equipment such as loss-in-weight feeders, or pre-composed to produce an extrudable compound. For example, the masterbatch can be added in a dry blend during the extrusion processing of a polymer composition.

[150] The masterbatch is particularly advantageous when used as a PPA for thermoplastic polymers, such as high molecular weight polyethylenes and / or those exhibiting a narrow molecular weight distribution (typically so that the polydispersity index is less than 3, preferably less than 2.5 and, even better, less than 2.2). The masterbatch is particularly useful for the extrusion of a polyolefin, in particular a polyethylene, in the form of a film.

[151] In addition to the form of a master, in some modalities, the PPA and adjuvant, if present, are added directly to the polymer composition. PPA and adjuvant, if present, may be added separately, simultaneously, or as a blend (in particular, a dry blend) to the thermoplastic polymer composition to be extruded.

[152] PPA and adjuvant, if present, may be added to the thermoplastic polymer composition by dry blending in powder form, or by blending or composition by melting. Melting blending may be carried out in an extruder or co-mixer, more preferably a twin-screw extruder or a co-mixer. Process

[153] The invention also relates to a process for extruding a thermoplastic polymer composition comprising a polymer matrix in an extruder, comprising a step of feeding a polymer processing aid into the extruder. Petition 870250073584, dated 08 / 20 / 2025, p. 36 / 57 28 / 34

[154] The extrusion process of the present invention is typically a melt extrusion process.

[155] In some embodiments, the process also includes a step of feeding at least one adjuvant into the extruder. PPA, at least one adjuvant and the thermoplastic polymer composition are those defined above.

[156] In some embodiments, the polymer processing aid and the adjuvant, if present, are fed in the form of a masterbatch containing a carrier polymer (C). In some embodiments, the polymer processing aid and the adjuvant, if present, are fed directly into the extruder, separately, simultaneously or as a blend.

[157] The process may include an additional step of feeding one or more additives into the extruder, such as fillers, pigments, dyes and antioxidants.

[158] In some embodiments, the process is carried out at a shear rate that would produce a thermoplastic composition extrudate with melt fracture defects, if carried out using a thermoplastic composition consisting essentially of a matrix polymer. Article

[159] The invention also relates to an article comprising or made from the thermoplastic polymer composition extruded by the process according to the invention.

[160] In some embodiments, the article is selected from a film, a tube, a pipe, a wire, a fiber, a cable, a wire coating and a cable jacket. EXAMPLES

[161] The following examples illustrate the invention, without limiting it. Petition 870250073584, dated 08 / 20 / 2025, p. 37 / 57 29 / 34 Polyamide Synthesis Example 1:

[162] In a 4 L autoclave, 308 g of caprolactam, 111.6 g of hexamethylenediamine, 140.6 g of adipic acid, 840 g of laurillactam and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 280°C, with stirring and autogenous pressure. The mixture is maintained at 280°C for 4 hours and then expanded for 2 hours at atmospheric pressure to reach 230°C. A nitrogen sweep is installed, a torque meter allows monitoring of the viscosity of the reaction medium, and polymerization is stopped at the desired torque. The reactor is drained into a water bath and the polymer forms a cooled rod that is granulated. Example 2:

[163] In a 4 L autoclave, 630 g of caprolactam, 217 g of hexamethylenediamine, 273 g of adipic acid, 280 g of laurillactam and 7 g of water are introduced. The synthesis proceeds as in Example 1, except that the temperature of the material to be reached is 260° C and the holding time is 3 hours. Example 3:

[164] In a 4 L autoclave, 343 g of caprolactam, 98.1 g of hexamethylenediamine, 289.6 g of dodecanedioic acid, 421.4 g of amino-11-undecanoic acid, and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 260°C under stirring and autogenous pressure. The mixture is maintained at 260°C for 1 hour and then expanded for 2 hours until atmospheric pressure reaches 230°C. A nitrogen sweep is established for 30 minutes and then placed under vacuum (< 20 mbar). 247.9 g of PEG with a molar mass of 600 and then 2.8 g of zirconium acetate are introduced into the reactor. The reactor is again placed under vacuum and the polymerization is stopped at the desired torque. The reactor is Petition 870250073584, dated 08 / 20 / 2025, page 38 / 57 30 / 34 drained into a water bath and the polymer forms a cooled rod that is granulated. Example 4:

[165] In a 4 L autoclave, 655.1 g of ca-prolactam, 73.4 g of adipic acid, and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 230°C with stirring and autogenous pressure. The mixture is held at 260°C for 1 hour and then expanded for 2 hours until atmospheric pressure reaches 230°C. A nitrogen sweep is established for 10 min, and then 671.5 g of PEG1500 are introduced into the reactor. The reactor is placed under vacuum (< 10 mbar) for 1 hour, and then 4.2 g of zirconium butoxide are added. Polymerization continues under vacuum until the desired torque is reached. The reactor is drained into a water bath, and the polymer forms a cooled rod that is granulated. Example 5:

[166] In a 4 L autoclave, 659.9 g of lauryl lactam, 70.6 g of adipic acid, and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 280°C with stirring and autogenous pressure. The mixture is maintained at 280°C for 4 hours and then expanded for 2 hours to atmospheric pressure to reach 230°C. A nitrogen sweep is established for 10 min, and then 669.5 g of PEG1500 are introduced into the reactor. The reactor is placed under vacuum (< 10 mbar) for 1 hour, and then 3 g of zirconium butoxide are added. Polymerization continues under vacuum until the desired torque is reached. The reactor is drained into a water bath, and the polymer forms a cooled rod that is granulated. Example 6 (Comparative Example):

[167] The synthesis proceeds as in Example 5, except that are Petition 870250073584, dated 08 / 20 / 2025, page 39 / 57 31 / 34 consisted of 235.2 g of laurillactam, 37.3 g of adipic acid, 7 g of water, 576.7 g of PEG1500, and 1.7 g of zirconium butoxide. Example 7:

[168] In a 4 L autoclave, 259.8 g of lauryl lactam, 78.8 g of adipic acid, and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 280°C with stirring and autogenous pressure. The mixture is maintained at 280°C for 4 hours and then expanded for 2 hours at atmospheric pressure to reach 230°C. A nitrogen sweep is established for 10 min, and then 1061.3 g of PTMG2000 are introduced into the reactor. The reactor is placed under vacuum (< 10 mbar) for 1 hour, and then 4.2 g of zirconium butoxide are added. Polymerization continues under vacuum until the desired torque is reached. The reactor is drained into a water bath, and the polymer forms a cooled rod that is granulated. Example 8:

[169] In a 4 L autoclave, 648.1 g of 11-amino-undecanoic acid, 72.0 g of adipic acid, and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 250°C with stirring and autogenous pressure. The mixture is held at 250°C for 1 hour and then expanded for 2 hours at atmospheric pressure to reach 230°C. A nitrogen sweep is established for 10 min, and then 679.8 g of PTMG1000 are introduced into the reactor. The reactor is placed under vacuum (< 10 mbar) for 1 hour, and then 2 g of zirconium butoxide are added. Polymerization continues under vacuum until the desired torque is reached. The reactor is drained into a water bath, and the polymer forms a cooled rod that is granulated. Example 9:

[170] The synthesis proceeds as in Example 5, except that 652 g of laurillactam, 56.5 g of adipic acid, 7 g of water, 691.5 g of PTMG2000 and 2.2 g of zirconium butoxide are used. Petition 870250073584, dated 08 / 20 / 2025, pp. 40 / 57 32 / 34 Example 10:

[171] In a 4 L autoclave, 7.4 g of adipic acid, 1392.6 g of laurillactam and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 280°C, with stirring and autogenous pressure. The mixture is maintained at 280°C for 4 hours and then expanded for 2 hours at atmospheric pressure to reach 230°C. A nitrogen sweep is established, a torque meter allows monitoring of the viscosity of the reaction medium, and polymerization is stopped at the desired torque. The reactor is drained into a water bath, the polymer then forms a cooled rod which is granulated. Example 11:

[172] In a 4 L autoclave, 9.3 g of adipic acid, 1,390.7 g of amino-11-undecanoic acid, and 7 g of water are introduced. After inertization under nitrogen, the mixture is heated to 250°C with stirring and autogenous pressure. The mixture is maintained at 250°C for 1 hour and then expanded for 2 hours at atmospheric pressure to reach 230°C. A nitrogen sweep is established, a torque meter allows monitoring of the viscosity of the reaction medium, and polymerization is stopped at the desired torque. The reactor is drained into a water bath, and the polymer forms a cooled rod that is granulated. Solubility Parameter

[173] As an example, the calculation of the solubility parameter of Example 1 (Table 1) is explained below. This is a random copolymer of PA6, PA66 and PA12.

[174] PA6 consists of 5 CH2 groups and 1 amide, PA66 consists of CH2 groups and 2 amides, PA12 consists of 11 CH2 groups and 1 amide.

[175] The cohesive energy E is the sum of the squares of the energies of each group.

[176] The molar volume V is the sum of the squares of the molar volumes of each group. Petition 870250073584, dated 08 / 20 / 2025, pp. 41 / 57 33 / 34

[177] The solubility parameter is the square root of the sum of the mole fractions of E over the sum of the mole fractions of V. [Table 1] Ex 1 Groups CH2 CONH EJ / mol V cm3 / mol d (J1 / 2.cm-3 / 2) E (J / mol) 4940 33490 V (cm3 / mol) 16.1 9.5 mol% 6 34.28% 5 1 58190 90 23.1 66 12.10% 10 2 116380 180 12 53.62% 11 1 87830 186.6 Fusion Fracture Test

[178] Considering the degree of fusion fracture of LLDPE without additives as 100%, the time required to reduce fusion fracture by 100% was obtained for examples 1 to 14.

[179] The results are presented in Table 2 below.

[180] The term “fusion fracture” is well known to those skilled in the art and can generally refer to a film having evident signs of surface imperfections, which manifest as matrix lines, haze bands, or small bands of soft fusion fracture (orange peel) or hard fusion fracture (shark skin). The expression “clean fusion fracture” means that a film has a clean, defect-free surface.

[181] The polymers of examples 1 to 14 (2000 ppm) were added to an LLDPE (PE) base polymer during extrusion. The LLDPE has a melt volumetric flow rate (MVR) of 8 g / 10 min for a weight of 2.16 kg, under the condition of a collection shear rate of 300 s-1 at a melt temperature of 190° C. Petition 870250073584, dated 08 / 20 / 2025, pp. 42 / 57 [Table 2] Ex PPA Molar Ratios d (J1 / 2.cm-3 / 2) Melting Viscosity 100 s-1 210° C Δd (PPA-PE) Melting Viscosity Ratio PPA / PE Time to Clear MF (min) 1 PA6 / 66 / 12 34 / 12 / 54 23.1 50 5.6 0.023 29 2 PA6 / 66 / 12 62 / 21 / 16 24.6 315 7.1 0.144 41 3 PA6 / 612 / 11-PEG12 22.6 60 5.1 0.028 27 4 PA6-PEG 50 / 50 22.5 250 5 0.115 31 5 PA12 (1500)-PEG (1500) 50 / 50 20.7 250 3.2 0.115 48 6 (CE) PA12 (4500)-PEG (1500) 50 / 50 20.1 750 2.6 0.344 Does not clean 7 (CE) PA12 (600)-PTMG (2000) 50 / 50 19.3 300 1.8 0.138 Does not clean 8 PA 11 (1000)-PTMG (1000) 50 / 50 20.4 470 2.9 0.216 59 9 PA 12 (2000)-PTMG(2000) 50 / 50 20.2 430 2.9 0.197 56 10 PA12 21.7 350 4.2 0.161 48 11 PA11 22.1 350 4.6 0.161 44 12 PA12 Orgasol® 2002 EXD NAT 1 21.7 463 4.2 0.212 59 13 PA12 Orgasol® 2001 UD NAT 2 21.7 117 4.2 0.054 35 14(CE) Polystyrene 21.6 680 4.1 0.312 Does not clean PE 17.5 2180 0 1.000 / 34 / 34

[182] As observed in the results of the examples in Table 2, the melt fracture of LLDPE during extrusion was effectively reduced by using polymers from examples 1 to 5 and 8 to 13 as an additive.

[183] ​​The improvement in fusion fracture reduction was particularly noticeable in examples 1 to 5, 10 and 11. Petition 870250073584, dated 08 / 20 / 2025, pp. 43 / 57

Claims

1 / 5 CLAIMS 1. Thermoplastic polymer composition comprising a matrix polymer (A) and a polymer processing aid (B), characterized in that: - (δ polymer (B) - δ matrix polymer (A)) >= 2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), δ being the solubility parameter calculated according to the Fedor method, and - the melt viscosity ratio of polymer (B) to matrix polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

2. Thermoplastic polymer composition, according to claim 1, characterized in that the amount of polymer processing aid (B) is from 50 to 5000 ppm, preferably from 100 to 3000 ppm, more preferably from 200 to 3000 ppm, based on the weight of the matrix polymer (A).

3. Thermoplastic polymer composition, according to claim 1 or 2, characterized in that the matrix polymer is a polyolefin composition, preferably, the polyolefin composition comprises, consists essentially of, or consists of non-functionalized polyolefin.

4. Thermoplastic polymer composition, according to any one of claims 1 to 3, characterized in that the matrix polymer comprises, consists essentially of, or consists of linear low-density polyethylene (LLDPE), low-density polyethylene (LDPE), medium-density polyethylene (MDPE), high-density polyethylene (HDPE), ultra-high-density polyethylene (UHDPE), or polypropylene (PP), or combinations thereof.

5. Thermoplastic polymer composition, according to any one of claims 1 to 4, characterized in that the processing aid polymer is selected from a polyamide, a PEBA or a mixture thereof.

6. Thermoplastic polymeric composition, according to claim 5, characterized in that the polyamide or PEBA block polyamide is PA6, PA10, PA11, PA12, PA66, PA610, PA612, PA1010, PA1012, PA1212 or a copolyamide PA6 / 12, PA6 / 11, PA6 / 1010, PA6 / 66, PA6 / 66 / 12, PA6 / 66 / 11, PA6 / 66 / 610, PA6 / 612 / 11 or a mixture of these polymers.

7. Thermoplastic polymeric composition, according to any one of claims 1 to 6, characterized in that the polymer processing aid (B) has a solubility parameter greater than 20.0, preferably greater than 21.0 (J1 / 2.cm3 / 2), the solubility parameter being calculated according to the Fedor method, and a melt viscosity between 10 and 500 Pa.s, preferably between 20 and 400, more preferably between 20 and 350, measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

8. Thermoplastic polymeric composition, according to any one of claims 1 to 7, characterized in that it comprises at least one adjuvant, preferably the adjuvant is or comprises one or more selected from a polyether, an aliphatic polyester, a poly(hydroxybutyrate), a silicone, a fatty acid ester and a fatty acid amide, preferably a polyether copolymer.

9. Process for melt extrusion of a thermoplastic polymeric composition comprising a matrix polymer (A), characterized in that it comprises a step of feeding a matrix polymer (A) and a polymer processing aid (B) into the extruder, together or separately, wherein: - (δ polymer (B) - δ matrix polymer (A)) >= 2.0 (J1 / 2.cm-3 / 2), Petition 870250073584, dated 20 / 08 / 2025, p. 45 / 57 3 / 5 preferably > 3.0 (J1 / 2.cm-3 / 2), where δ is the solubility parameter calculated according to the Fedor method, and - the melt viscosity ratio of the polymer (B) to the matrix polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1.

10. Process according to claim 9, characterized in that it further comprises a step of feeding at least one adjuvant into the extruder.

11. Process according to claim 9 or 10, characterized in that the polymer processing aid and the adjuvant, if present, are fed in the form of a master composition containing a carrier polymer (C).

12. Process, according to any one of claims 9 to 11, characterized in that the polymer processing aid and the adjuvant, if present, are fed directly into the extruder, separately, simultaneously or as a blend.

13. Process, according to any one of claims 9 to 12, characterized in that the matrix polymer is a polyolefin, preferably, the polyolefin composition comprises, consists essentially of, or consists of non-functionalized polyolefin.

14. A process according to any one of claims 9 to 13, characterized in that the matrix polymer comprises, consists essentially of, or is composed of, linear low-density polyethylene (LLDPE), low-density polyethylene (LDPE), medium-density polyethylene (MDPE), high-density polyethylene (HDPE), ultra-high-density polyethylene (UHDPE), or polypropylene (PP), or combinations thereof.

15. Process, according to any of the claims in Petition 870250073584, dated 08 / 20 / 2025, page 46 / 57 4 / 5, characterized in that the quantity of polymer processing aid (B) is from 50 to 5000 ppm, preferably from 100 to 3000 ppm, more preferably from 200 to 3000 ppm, based on the weight of the matrix polymer (A).

16. Process, according to any one of claims 9 to 15, characterized in that the polymer processing aid (B) has a solubility parameter greater than 20.0, preferably greater than 21.0 (J1 / 2.cm-3 / 2), the solubility parameter being calculated according to the Fedor method, and a melt viscosity between 10 and 500 Pa.s, preferably between 20 and 400, more preferably between 20 and 350, measured by capillary rheometry at 210°C and a shear rate of 100 s-1 17. Process, according to any one of claims 9 to 16, characterized in that the processing auxiliary polymer is selected from a polyamide, a PEBA or a mixture thereof.

18. Process according to claim 17, characterized in that the polyamide or PEBA block polyamide is PA6, PA10, PA11, PA12, PA66, PA610, PA612, PA1010, PA1012, PA1212 or a copolyamide PA6 / 12, PA6 / 11, PA6 / 1010, PA6 / 66, PA6 / 66 / 12, PA6 / 66 / 11, PA6 / 66 / 610, PA6 / 612 / 11 or a mixture of these polymers.

19. Extruded article, characterized in that it comprises a polymeric composition as defined in any one of claims 1 to 8, preferably the article being a film, a sheet, a tube, a pipe, a wire, a fiber, a cable, a wire coating or a cable jacket.

20. Use of a polymer (B) as a processing aid for the extrusion of a thermoplastic polymeric composition comprising a matrix polymer (A), characterized in that: Petition 870250073584, dated 20 / 08 / 2025, page 47 / 57 5 / 5 - (δ polymer (B) - δ matrix polymer (A)) >= 2.0 (J1 / 2.cm-3 / 2), preferably > 3.0 (J1 / 2.cm-3 / 2), where δ is the solubility parameter calculated according to the Fedor method, and - the melt viscosity ratio of polymer (B) to matrix polymer (A) is less than 0.30, preferably less than 0.20, the melt viscosity being measured by capillary rheometry at 210°C and a shear rate of 100 s-1. Petition 870250073584, dated 08 / 20 / 2025, pp. 48 / 57