| HS Code | 544140 |
| Resin Type | Linear Low Density Polyethylene (LLDPE) |
| Comonomer | Hexene-1 |
| Melt Flow Rate 190 C 2 16kg | 0.50 g/10min |
| Density | 0.918 g/cm³ |
| Melting Point | 124 °C |
| Vicat Softening Point | 102 °C |
| Tensile Strength At Yield Md | 13 MPa |
| Tensile Strength At Break Md | 35 MPa |
| Elongation At Break Md | 550% |
| Dart Drop Impact F50 | 650 g |
| Puncture Resistance | 35 J/cm |
| Haze | 10% |
| Gloss 45 | 60 |
As an accredited INEOS LLDPE LL6130AA factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Supplied as free-flowing pellets in 25 kg multi-layer paper bags, palletized and shrink-wrapped, with 40 bags per pallet. |
| Container Loading (20′ FCL) | 20′ FCL loaded with INEOS LLDPE LL6130AA pellets, safely stowed and secured with proper weight distribution for transport. |
| Shipping | INEOS LLDPE LL6130AA is a linear low-density polyethylene resin supplied as free-flowing pellets. Ship in clean, dry containers—bulk bags, hopper trucks, or railcars—to prevent contamination and moisture pickup. Avoid excessive heat and humidity during transit. Ensure proper ventilation and secure loading to prevent shifting. |
| Storage | Store INEOS LLDPE LL6130AA in a cool, dry, well-ventilated area, away from direct sunlight, heat, open flames, and strong oxidizing agents. Keep in original sealed packaging to prevent moisture pickup and contamination. Avoid generating dust and static charges; use proper grounding during handling. Follow all local regulations for polymer storage. |
| Shelf Life | Shelf life is indefinite if stored in original packaging in a cool, dry, well-ventilated area away from direct sunlight. |
On production-scale blown film lines converting 50 kg fertiliser sacks, LL6130AA is run as the primary film-forming resin at addition levels of 80–90 wt% with high-pressure LDPE at 10–20 wt%. The LDPE addition is not incidental: it raises melt strength for single-bubble stability at BUR 2.5–3.0, while the LLDPE phase contributes dart impact and tear resistance. The grade is a butene-comonomer linear low-density polyethylene with nominal density 0.934 g/cm³ and MFR 3.0 g/10 min at 190 °C/2.16 kg per ISO 1133-1:2022. The finished sack, when used for fertiliser or cement, is specified against ASTM D4976-12a for polyethylene film, and FIBC liners are assessed to ISO 21898:2018; food-contact variants fall under EU Regulation (EU) No 10/2011 with overall migration limit 10 mg/dm² and FDA 21 CFR 177.1520(c). Processing uses a single-screw extruder with 30:1 L/D barrier screw and Maddock mixing section, die diameter 250 mm, die gap 1.6–2.0 mm, melt temperature 200–230 °C, and frost line height 6–8 die diameters. Film gauges between 125 µm and 200 µm are drawn into heavy-duty shipping sacks, sand and cement bags, and inner liners for flexible intermediate bulk containers.
Bubble instability at BUR above 3.5 produces gauge variation exceeding ±8%, a known failure mode on lines without internal bubble cooling or on fluted black film. Raising LDPE above 20 wt% reduces tear propagation resistance and increases haze, so converters in tropical shipping environments maintain LL6130AA at the upper end of the 80–90 wt% range and adjust frost line height rather than blend ratio.
Cast stretch film operations that position LL6130AA in the core layer use addition levels of 30–50 wt% with a higher-alpha-olefin mLLDPE being co-extruded as the cling skin; the skin layer typically receives 2–4 wt% polyisobutylene tackifier or 0.5–1.5 wt% erucamide to set the required cling force. The grade's density of 0.934 g/cm³ provides a measurable increase in modulus compared with lower-density mLLDPE, but its butene branching requires tight control of the air gap. Compliance for pallet wrap is anchored to ASTM D5748 for puncture resistance, ASTM D882 and ISO 527-3 for film tensile, EU Regulation (EU) No 10/2011, FDA 21 CFR 177.1520(c), and REACH. The production line uses a 90 mm single-screw extruder with 30:1 L/D, a slot die of 2000 mm width, die gap 0.4–0.7 mm, melt temperature 245–270 °C, air gap 40–80 mm, chill roll temperature 18–25 °C, and line speed 250–400 m/min. Edge trim is held at 5–8%; at air gaps above 80 mm neck-in reaches 45–60 mm per side, while chill roll temperatures above 30 °C drive tackifier migration and blocking after 72 h. Terminal outputs include machine-grade pallet wrap at 23–25 µm, hand stretch film at 12–18 µm, and agricultural silage stretch film.
Thin-wall distribution packaging uses LL6130AA either as a 100 wt% base resin or compounded into homopolymer PP at 10–25 wt% to raise notched Izod impact. The 3.0 g/10 min melt flow rate measured to ISO 1133-1:2022 permits filling of multi-cavity hot-runner tooling without excessive injection pressure, while the 0.934 g/cm³ density avoids the sink marking associated with higher-density ethylene copolymers. Compliance for stack-and-nest totes and returnable transit packaging includes ISO 527-1:2019 and ISO 527-2:2012 for tensile, ISO 178:2019 for flexural, ISO 180:2023 for notched Izod, FDA 21 CFR 177.1520(c), EU Regulation (EU) No 10/2011, and REACH. Moulding on a hydraulic injection machine of 150–300 t clamp force uses melt temperature 200–230 °C, mould temperature 10–25 °C, injection pressure 700–1000 bar, holding pressure 60–80% of peak, and cooling times of 10–18 s for a 1.2 mm nominal wall. The moulded output includes thin-wall pails, caps, closures, and returnable totes. Differential shrinkage in flat areas is a recognised defect source; hot-runner manifolds must be balanced to ±2 °C and gate freeze time mapped against packing pressure decay to avoid warpage outside dimensional tolerance.
When LL6130AA is blended into an extrusion coating melt at 15–40 wt% with LDPE, the resulting haul-off window is controlled by melt curtain stability rather than polymer output capacity. The coating weight on PP woven fabric is typically 20–35 g/m²; the LDPE fraction provides neck-in control, while the LLDPE fraction improves dart impact and seal initiation. Compliance for the coated fabric is set by ASTM D882 and ISO 527-3 for film tensile, ASTM F88 for seal strength, ASTM D792 for density, EU Regulation (EU) No 10/2011, and FDA 21 CFR 177.1520(c). The coating line uses a 90–120 mm single-screw extruder with 30:1 L/D, melt temperature 280–320 °C, die gap 0.5 mm, air gap 150–250 mm, chill roll temperature 12–20 °C, and line speed 80–150 m/min. Substrate pre-treatment to surface energy above 42 mN/m is required on polypropylene woven. Terminal downstream products include PP woven cement bags, FIBC outer laminates, paper-based pet food bags, and aluminium foil laminates. Air gaps above 250 mm or melt temperatures below 280 °C produce melt curtain sag and edge tear; published data for this specific blend configuration is limited, so line trials must establish the exact LDPE dilution at the edge of the curtain stability envelope.
Injection moulding compounds based on homopolymer PP intended for appliance and battery-box applications use LL6130AA as a discrete impact modifier at addition levels of 10–25 wt%. The selection of the exact loading depends on the ductile-brittle transition target and notched Izod requirement under ISO 180:2023, with tensile properties measured to ISO 527-1:2019 and flexural modulus to ISO 178:2019. The compounding process is carried out on a co-rotating twin-screw extruder with 40:1 L/D, barrel temperatures 190–210 °C, screw speed 300–400 rpm, and strand pelletizing; the pellets are subsequently injection moulded into finished parts. End-use components include appliance housings, automotive interior trims, and material-handling totes where notched impact and gloss are specified together. A recognised limitation is that published data for this specific configuration is limited; the morphology of the PP/LLDPE blend after twin-screw mixing, especially the dispersed phase particle size distribution, controls impact performance and must be validated by scanning electron microscopy before production release. For food-contact appliance components, FDA 21 CFR 177.1520(c) and EU Regulation (EU) No 10/2011 apply to the final compound.
Carbon black masterbatch made with LL6130AA as carrier resin is formulated with 40–60 wt% carrier, 40–50 wt% carbon black, 2–5 wt% dispersant wax, and 0.1–0.5 wt% antioxidant; the let-down ratio in downstream blown film is typically 2–5%. The carrier's 3.0 g/10 min MFR measured to ISO 1133-1:2022 and density of 0.934 g/cm³ per ISO 1183-1:2019 provide a consistent melt phase for pigment dispersion; its tensile properties are measured to ISO 527-2:2012. Compliance for the masterbatch and finished film includes FDA 21 CFR 177.1520(c), EU Regulation (EU) No 10/2011, and REACH. Production uses a high-shear twin-screw extruder with 25:1 L/D side-fed carbon black, melt temperature 180–220 °C, screw speed 250–500 rpm, and a 200 µm screen pack before underwater pelletizing. Terminal applications include black agricultural mulch film, refuse sacks, and industrial pipe extrusion. If the screen pack pressure rises above 120 bar during the run, carbon black dispersion is failing and the let-down ratio must be checked for agglomerates; surface moisture from storage above 60% RH should be removed by warm-air drying at 60–70 °C for 1–2 h before compounding to avoid pellet porosity.
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INEOS LLDPE LL6130AA is a linear low-density polyethylene grade based on an ethylene-1-hexene copolymer. The resin is positioned in the medium-melt-flow range for cast film, thin-gauge oriented film, and high-speed extrusion coating. Nominal melt mass-flow rate is 3.5 g/10 min at 190°C with a 2.16 kg load, determined by ISO 1133-1:2022 or ASTM D1238; nominal density is 0.918 g/cm³ at 23°C, determined by ISO 1183-1:2019 or ASTM D1505. The 1-hexene comonomer differentiates the product from butene-based LLDPE because the longer branch shifts the amorphous tie-chain distribution governing dart impact and tear resistance in thin film. Additive loadings are lot-specific and must be checked against the supplier certificate of analysis.
| Property | Test method | Typical value |
| Melt mass-flow rate | ISO 1133-1:2022 / ASTM D1238 | 3.5 g/10 min |
| Density | ISO 1183-1:2019 / ASTM D1505 | 0.918 g/cm³ |
| Comonomer | Manufacturer documentation | 1-hexene |
| DSC peak melting region | ISO 11357-3:2018 | 123–125°C |
| Tensile stress at yield | ISO 527-2:2012 | 11 MPa |
Values are nominal rounded figures and are not batch specifications. The manufacturer’s certificate of analysis controls lot-specific release limits.
On a cast film line using a 90 mm single-screw extruder with a 30:1 L/D barrier screw, die melt temperature is normally controlled between 245°C and 275°C. The lower boundary is imposed by incomplete melting and poor die-lip wetting at high throughput; the upper boundary is governed by gel formation and fuming from oxidative degradation, with melt-temperature fluctuation greater than ±5°C typically appearing as transverse gauge bands. Die gap is held between 0.6 mm and 1.0 mm for film thicknesses of 12–50 µm, with air gap at 15–30 mm and polished chill roll temperature at 15–30°C. Above 300 m/min, edge bead stability depends on vacuum-box air distribution and die lip cleanliness; edge webbing, melt banks behind the nip, and gauge bands are observed when the melt curtain is not pinned uniformly. Since the grade has little long-chain branching, extensional viscosity does not rise sharply with Hencky strain, so draw resonance is controlled by narrowing the air gap and increasing the chill roll speed ratio rather than by raising melt temperature.
Extruder barrel zone temperatures are typically set from 160°C at the feed throat to 240°C at the metering section, with adapter and die zones held at 245–260°C. In cast film operations using a resin of this melt-flow class, backpressure on a 90 mm / 30:1 L/D barrier screw can range from 180 bar to 260 bar at throughputs of 250–350 kg/h, depending on die width and lip setting. Pressure fluctuation greater than ±10 bar over a 10 min interval indicates feed instability, screw wear, or nonuniform melt temperature and should be corrected before high-speed gauge scanning. Chill roll release is influenced by the resin’s additive package and the absence of an external lubricant; on polished chrome rolls, clean release is maintained when the chill roll temperature is kept below 30°C and roll surface roughness is controlled at 0.05–0.15 µm Ra for gloss film. Edge sticking can occur if roll roughness falls below 0.05 µm Ra or if the air gap is too short for the melt curtain to develop a stable pinned edge.
Molecular architecture differences generated by the 1-hexene comonomer alter the film-fracture hierarchy compared with butene LLDPE. The longer pendant branch in hexene-based linear low-density polyethylene increases the probability of interlamellar tie-chain formation, which improves Elmendorf tear and dart drop impact at equivalent density and melt mass-flow rate. This benefit is most visible in film below 25 µm; at thicker gauges, quench rate and crystallinity differences begin to dominate. The same linear architecture reduces shear thinning relative to high-pressure LDPE, and capillary rheometry of polyolefins in this melt-flow class typically shows a power-law index of 0.55–0.70. Because the molecular weight distribution is narrow relative to LDPE, the grade generates less melt-pressure sensitivity at low screw speeds but exhibits a higher onset of melt fracture at high screw speeds. Pellets do not require predrying unless surface condensation is present; after outdoor storage or ambient relative humidity above 80%, a desiccant hopper set at 70°C for 2 h removes surface moisture without increasing oxidation risk.
The principal difference between LL6130AA and a high-pressure LDPE of equivalent melt mass-flow rate is the absence of significant long-chain branching. High-pressure LDPE builds extensional viscosity with increasing draw, which supports a broader stable draw ratio and lower neck-in in extrusion coating; LL6130AA does not, so die width and air gap must be adjusted as separate variables. Against butene LLDPE, the 1-hexene branch length in LL6130AA improves dart impact and tear resistance at the same density and gauge, but the melt-strength contribution remains lower than that of LDPE. When a converter blends LDPE into LL6130AA to recover melt strength, haze can increase nonlinearly above 10 wt% LDPE in some hexene LLDPE systems; published data for the specific blend configuration is limited, and pilot-line verification is required. At equal density and melt mass-flow rate, a butene LLDPE typically shows lower dart drop impact and lower Elmendorf tear but can display a wider processing window in thick-gauge blown film because the lower melting temperature of the butene chain can reduce the required frost line height. A plant that replaces a butene grade with LL6130AA may need to lower melt temperature by 5–10°C to maintain equivalent haze in cast film because the hexene resin can generate slightly higher shear heating in a high-compression screw. Although the grade is intended primarily for cast film, it can be run on a 55 mm groove-fed extruder at 30:1 L/D with a die gap of 1.5 mm and a blow-up ratio of 2.0:1 to 3.0:1 for limited blown film validation.
Within the INEOS LLDPE series, the 3.5 g/10 min melt mass-flow rate of LL6130AA places it above blown-film-oriented grades that are typically below 2.0 g/10 min. The higher flow reduces melt pressure at a given cast film throughput, allowing shorter residence time in the die and lower melt-temperature rise due to shear heating. This is valuable when the downstream process requires a narrow residence-time distribution; however, it also means the grade is less suitable for thick-gauge blown film where bubble stability is dominated by melt tenacity. Lower-melt-flow grades in the same density band show higher melt pressure and better bubble stability at a blow-up ratio of 2.5:1, but they can require higher drive load and generate more frictional heat in a shallow screw designed for LLDPE.
For extrusion coating and laminating lines, the melt curtain is run at a die melt temperature of 285–300°C with a die gap of 0.5–0.8 mm and a coat-weight range of 10–20 g/m². The lower melt strength of LL6130AA relative to LDPE requires a smaller die-to-laminator gap and, in many cases, a blending ratio of 10–20 wt% LDPE to control neck-in. Published data for the specific configuration of LL6130AA in extrusion coating is limited; pilot trials are necessary because substrate adhesion and heat-seal initiation are affected by cooling drum temperature and surface oxidation at the air gap. The grade’s density of 0.918 g/cm³ gives a lower heat-seal initiation temperature than higher-density polyethylene resins, but the exact seal strength must be measured by ASTM F88/F88M-21 on the converted laminate.
In machine-direction orientation, the cast web is reheated and stretched at draw ratios between 4:1 and 6:1; LL6130AA can be used as the core or skin layer if the formulation is adjusted with a lower-melt-index component. The hexene comonomer reduces low-temperature brittleness relative to butene LLDPE, but the film must be quenched rapidly to limit post-extrusion crystallization before stretching. Gel rating and film appearance are influenced by extrusion temperature history and screw design rather than by the base resin alone. When a high-shear barrier screw is run at low throughput, melt residence time increases and may generate oxidized gel specks, even if the melt temperature reading remains within the nominal window. The gel count should be measured by a laser scanner or camera system after a 1 h conditioning run at the target rate, not during startup. Film haze is recorded per ASTM D1003 and gloss at 60° per ASTM D2457; these values are line-dependent and must be tracked against the specific chill roll finish and air gap.
Food-contact suitability for LL6130AA must be confirmed against the lot-specific supplier certificate. Under FDA 21 CFR 177.1520(c), olefin polymers may be used in contact with food provided the resin density and condition-of-use limits satisfy the clause; migration testing for packaging is conducted under conditions described in 21 CFR 176.170(c). For European Union compliance, overall migration into food simulants is assessed under Regulation (EU) No 10/2011, Annex II, using ISO 1186-1:2002 or EN 1186-1:2002. Converters adding antistatic or color masterbatch must re-evaluate organoleptic and migration performance because the additive package in the masterbatch can change the final film’s compliance status. The resin’s stabilization package is not a substitute for an antistatic surface treatment; surface resistivity measurements should follow IEC 61340-2-3:2016 if the film is used for electronics packaging. Supply-chain documentation should include the REACH registration under EC No 1907/2006 and a RoHS 2011/65/EU statement where electronic packaging is involved.
| Regulatory area | Reference | Verification |
| FDA food contact | 21 CFR 177.1520(c) | Lot-specific CoC |
| EU food contact | Regulation (EU) No 10/2011 | Overall migration data |
| REACH | EC No 1907/2006 | SDS and registration |
| RoHS | 2011/65/EU Annex II | Supplier declaration |
Operational boundaries include a maximum practical film winding speed set by blocking tendency rather than by melt temperature. Because the base grade is not formulated with a high loading of slip agent, high-speed wound rolls may develop blocking if stored above 40°C. If high slip is required, the converter must add a slip masterbatch at the hopper; the addition level should be determined from coefficient-of-friction measurements per ISO 8295:1995 rather than from supplier generic recommendations. Incompatibility with certain antistatic masterbatches containing low-molecular-weight polar additives can lead to die-lip build-up and periodic haze lines; purge protocols should be established before the grade is introduced to a line previously running polar copolymers.
Conveying and feeding behavior differs from high-pressure LDPE because LL6130AA pellets have a narrower softening interval and are more prone to fines generation at high dilute-phase conveying velocities. In polyolefin pellet conveying, line velocities above 35 m/s are known to increase pellet attrition and dust accumulation in hopper vents; gravimetric feeder accuracy is then affected by fines bridging in the hopper throat. The resin is not inherently antistatic, and high-speed film converters should determine film-to-metal coefficient of friction per ISO 8295:1995 before slitting and pallet-wrapping operations to avoid rewind telescoping. If the film is to be printed or metallized, corona treatment levels should be verified immediately before conversion because surface energy decays with time and storage temperature. A dyne level of 38–42 mN/m is commonly used for solvent-based lamination, but the exact value depends on ink and adhesive chemistry; published data for LL6130AA-specific surface-energy decay is limited.
