| HS Code | 727843 |
| Chemical Formula | C4H6O2 |
| Cas Number | 108-05-4 |
| Molecular Weight | 86.09 g/mol |
| Appearance | Clear colorless liquid |
| Purity | >=99.9% |
| Boiling Point | 72.7°C |
| Melting Point | -93°C |
| Flash Point | -8°C (closed cup) |
| Specific Gravity | 0.934 at 20°C |
| Vapor Pressure | 120 mmHg at 20°C |
As an accredited Celanese Vinyl Acetate HQ 10-12 factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Supplied in 200 kg steel drums, 1,000 kg IBC totes, or bulk tankers for safe handling and storage. |
| Container Loading (20′ FCL) | 20′ FCL loaded with drums/pallets of Celanese Vinyl Acetate HQ 10-12, secured, labeled, and ventilated per hazardous chemical shipping regulations. |
| Shipping | Vinyl Acetate HQ 10-12 is a flammable, reactive liquid requiring stringent shipping controls. Transport in dedicated, properly grounded tank containers or drums under inert gas. Must comply with IMDG/ADR regulations, use UN-approved packaging, and avoid heat, ignition sources, and incompatible materials. Ensure clear hazard labeling and trained personnel for safe handling. |
| Storage | Store in a cool, dry, well-ventilated area away from heat, ignition sources, sunlight, oxidizers, and polymerization initiators. Keep containers tightly closed and grounded/bonded to prevent static discharge. Maintain temperature below recommended limits, ensure inhibitor effectiveness, and use explosion-proof equipment. Follow all local regulations and inspect regularly for leaks or degradation. |
| Shelf Life | Shelf life is typically 12 months when stored under nitrogen, in sealed containers, away from heat, light, and contaminants. |
Continuous methanolysis trains producing polyvinyl alcohol from Celanese Vinyl Acetate HQ 10-12 are typically fed with monomer polymerized in methanol to a controlled conversion of 50–67% in stirred stainless-steel or glass-lined reactors operating at 58–65°C, initiated with azobisisobutyronitrile or peroxyester initiators. The hydroquinone content of 10–12 ppm is carried directly into the polymerization section without a dedicated inhibitor-removal column; the inhibitor is consumed during radical initiation, and its influence appears as a short induction delay rather than a permanent chain-transfer modification. Methanol is used as both solvent and chain-transfer regulator, and the target polymerization solids are maintained between 50 and 70 wt%. The polyvinyl acetate solution is then transferred to an alcoholysis train where sodium methylate or sodium hydroxide in methanol converts the acetate groups to hydroxyl groups. The alkali ratio is adjusted to the desired residual acetyl content, producing polyvinyl alcohol with a degree of hydrolysis from 87 to 99 mol%; grades above 98 mol% are required for water-soluble film and polyvinyl butyral resin. A 4% aqueous solution viscosity is measured at 20°C using a Brookfield LVF viscometer per JIS K6726:2002, and degree of hydrolysis is checked by titration per ISO 15023-2:2019. Published kinetic data for the specific effect of 10–12 ppm hydroquinone on continuous PVOH trains is limited, but plant design generally treats the inhibitor as consumed before the first reactor discharge. Final products include textile warp sizes, paper coatings, water-soluble detergent films, and PVB resin after condensation with butyraldehyde.
In batch and semi-batch wood adhesive processes, the formulation is built around 85–100 parts vinyl acetate, 110–130 parts demineralized water, 3–6 parts polyvinyl alcohol protective colloid with a 4% solution viscosity of 13–25 mPa·s, and 1.0–3.0 parts nonionic surfactant. The aqueous phase is buffered to pH 4.0–5.2 with sodium acetate and acetic acid. Potassium persulfate at 0.08–0.30 parts per hundred monomer is used alone or with a reducing agent such as sodium formaldehyde sulfoxylate. The initial seed charge comprises 10–15 wt% of the total vinyl acetate and the full initial initiator charge; the remaining monomer is fed over 3.5–5 h at 72–78°C while the jacket is supplied with cooling water at 20–25°C. The hydroquinone in the initial charge produces a measurable induction period in redox and persulfate systems; the delayed monomer feed keeps the unreacted inhibitor concentration low and prevents quinone-derived discoloration. After the feed, residual vinyl acetate is stripped with live steam at 85–90°C and 200–300 mbar absolute pressure. The final dispersion is adjusted to 50–62% solids and a Brookfield viscosity of 3,000–8,000 mPa·s at 23°C. Wood bond strength is evaluated according to EN 204:2016 and EN 205:2016, with D2/D3 classifications requiring survival after cold-water immersion and hot-water exposure; film tensile properties are tested per ISO 527-3:2018. Finished goods include furniture assembly adhesives, packaging glues, and bookbinding formulations.
Inside a 20 m³ pressure-rated stirred reactor with an ethylene sparge ring below the lower impeller, a low-VOC VAE dispersion is produced by charging water, polyvinyl alcohol protective colloid, nonionic emulsifier, and buffer, then pressurizing the reactor with ethylene to a constant partial pressure of 30–85 bar. Vinyl acetate monomer containing 10–12 ppm hydroquinone is metered over 3–5 h under monomer-starved conditions, so the inhibitor is consumed without a dedicated removal step. The final polymer contains 75–90 wt% vinyl acetate and 10–25 wt% ethylene; across this range the Fox-equation glass transition temperature moves from approximately −12°C to +8°C, and the actual matrix glass transition is measured by DSC per ISO 11357-2:2020. Ethylene mass transfer and pressure control are the dominant variables for molecular weight and branching, while the residual HQ has no controlling role. After letdown, residual vinyl acetate is stripped to below 0.1 wt%, and the dispersion pH is adjusted to 4.5–5.5. Interior architectural paints formulated with VAE are tested for VOC content according to ISO 11890-2:2020 and must comply with EU Directive 2004/42/EC phase II limits; ceramic tile adhesives are evaluated according to ISO 13007-1:2014 for tensile adhesion after water immersion, heat ageing, and freeze-thaw conditioning. Downstream goods include low-VOC indoor paints, carpet and nonwoven binders, tile adhesives, and sprayable insulation.
| Downstream process | Reference method | Property evaluated |
|---|---|---|
| PVOH from continuous alcoholysis | ISO 15023-2:2019 / JIS K6726:2002 | Degree of hydrolysis, 4% solution viscosity |
| PVAc wood adhesive | EN 204:2016 / EN 205:2016 | Bond strength classification D1–D4 |
| VAE dispersion for construction | ISO 13007-1:2014 / ISO 11890-2:2020 | Tensile adhesion after water immersion, VOC content |
| High-pressure EVA copolymer | ISO 1133-1:2022 / ASTM D5594:2018 | Melt flow rate, vinyl acetate content |
| PVB interlayer | ISO 14782:2021 / ISO 527-3:2018 | Haze, tensile properties |
| VC–VAC solution resin | ISO 1628-3:2010 / ISO 3219:2021 | K-value, solution viscosity |
High-pressure EVA reactors operate at 1,400–2,500 bar and 150–280°C in continuous autoclave or tubular configurations. The vinyl acetate comonomer is normally injected downstream of the primary ethylene compressor because of its lower thermal stability; the hydroquinone inhibitor in the 10–12 ppm grade is either removed by vacuum distillation or activated alumina in plants producing ultra-low-gel encapsulation film, or left untreated in less restrictive hot-melt and footwear grades. When direct injection is used, the preheater temperature above 150°C and dilution in the ethylene feed reduce the inhibitor to a level below the radical flux; however, published kinetic data for direct injection of this specific HQ concentration in high-pressure EVA reactors is limited, and licensor evaluations determine whether an inhibitor-removal unit is included. The final resin contains 18–40 wt% vinyl acetate, measured by ASTM D5594:2018; melt flow rate is determined at 190°C with a 2.16 kg load per ISO 1133-1:2022. Hot-melt adhesives typically use EVA grades with 18–28 wt% vinyl acetate and MFR from 3 to 400 g/10 min, while photovoltaic encapsulant grades use 28–35 wt% vinyl acetate and MFR below 40 g/10 min. Film and encapsulant producers check gel content by melt filtration through a 20 μm screen at 190°C.
For laminated glass interlayer resin, the critical monomer-related defects are carbonyl-bearing impurities and colour bodies rather than residual hydroquinone, because the polyvinyl alcohol intermediate is the direct feedstock. PVOH with a degree of hydrolysis of 98–99 mol% and a 4% solution viscosity of 20–70 mPa·s is reacted with butyraldehyde under acidic catalysis to an acetalization degree of 75–82%. The residual PVOH content in the PVB resin is controlled between 18 and 23 wt%, and the resin is washed and dried to reduce ash below 0.2 wt%. The hydroquinone in the original vinyl acetate is consumed upstream; colour formation in PVB is controlled by avoiding oxygen contact and excessive temperature rather than by post-removal of HQ. The final PVB sheet is compounded with triethylene glycol bis(2-ethylhexanoate) or similar low-volatility plasticizer at 20–30 phr and extruded through a polished-roll stack at 170–210°C to a thickness of 0.38–1.52 mm. Haze is measured according to ISO 14782:2021, tensile properties according to ISO 527-3:2018, and the laminated glass construction is validated under EN ISO 12543-2:2021. The application covers architectural safety glass and automotive laminated windscreens.
Solution-grade vinyl chloride–vinyl acetate copolymers are manufactured by suspension or emulsion polymerization at 40–70°C and 8–15 bar, with 10–20 wt% vinyl acetate as the internal plasticizing comonomer. The vinyl acetate is charged with the vinyl chloride; the hydroquinone inhibitor at 10–12 ppm is diluted into the organic phase and does not require a separate removal column in suspension polymerization, because oil-soluble peroxide initiators and chain-transfer agents control the radical balance. The resulting resins are amorphous, with glass transition temperatures from 65 to 75°C, and are soluble in methyl ethyl ketone, toluene, esters, and glycol ethers. K-value is determined per ISO 1628-3:2010 and usually falls between 40 and 60. In coil coating primers, the resin is combined with epoxy or melamine crosslinkers, applied by reverse roller coater at 5–15 μm dry film thickness, and cured at 200–240°C peak metal temperature. In gravure inks, the resin is used as a 20–35% solids solution and provides pigment wetting and adhesion to treated polyester and PVC; solution viscosity is measured by rotational viscometer per ISO 3219:2021. Adhesion of the cured system is evaluated by cross-cut according to ISO 2409:2020. Manufacturers typically specify residual vinyl chloride below 1 ppm and residual vinyl acetate below 0.1 wt% in the dried resin. Downstream products include coil coating primers, gravure inks, and heat-seal lacquers.
After spray drying, redispersible polymer powders derived from VAE and vinyl acetate–VeoVa10–butyl acrylate dispersions are incorporated into dry-mix mortars at 1.5–4.0 wt%, where the main monomer-related requirements are low residual vinyl acetate and stable protective-colloid stabilization. The dispersion is synthesized with polyvinyl alcohol as the main stabilizer and dried in a co-current spray tower at an inlet temperature of 120–180°C and an outlet temperature of 60–80°C. The resulting powder is treated with anticaking clay or silica to produce free-flowing particles in the 100–250 μm size range, with bulk density of 400–600 g/L, residual moisture below 1.5 wt%, and ash content of 5–15 wt%. Redispersibility is checked by optical microscopy or laser diffraction after controlled shear mixing in water, and the powder must re-form a dispersion with a particle size close to the original latex. The hydroquinone level of the original vinyl acetate is not a direct powder specification; the more relevant VAM-derived quality parameters are residual monomer, acetaldehyde, and buffering salt residues. Tile adhesives are evaluated under ISO 13007-1:2014 for tensile adhesion after water immersion, heat ageing, and freeze-thaw cycling; external thermal insulation systems are assessed under EAD 040083-00-0404 for adhesion and impact resistance after climatic cycling. Finished goods include C2-class tile adhesives, self-leveling compounds, and façade basecoats.
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Celanese Vinyl Acetate HQ 10-12 is a polymer-grade vinyl acetate monomer (CAS 108-05-4; EINECS 203-545-4) stabilized with hydroquinone at a weight concentration of 10–12 ppm. The designation refers to the inhibitor loading envelope, not to a structural modification of the monomer; the underlying vinyl acetate molecule is identical to other polymer-grade forms within the same purity band. The material is released within the framework of ASTM D2190, with typical boundaries of ≥99.9 wt% vinyl acetate purity by gas chromatography, ≤0.02 wt% water by Karl Fischer titration, ≤0.005 wt% acidity as acetic acid, and a distillation range of 72–73 °C at 101.3 kPa. Hydroquinone content is controlled between 10 ppm and 12 ppm and is verified by ultraviolet-visible spectrophotometry or high-performance liquid chromatography. The monomer is a flammable liquid with a Tag closed-cup flash point of −8 °C, a vapor pressure of approximately 115 hPa at 20 °C, and an autoignition temperature of 402 °C. The primary downstream routes are free-radical polymerization to polyvinyl acetate, ethylene-vinyl acetate copolymerization, alcoholysis to polyvinyl alcohol, and vinyl acetate-acrylic or vinyl acetate-ethylene-vinyl chloride dispersion polymers. The grade is intended for bulk storage under an air-containing headspace because hydroquinone requires dissolved oxygen to maintain its radical-scavenging function.
The molecular weight of vinyl acetate is 86.09 g/mol, the liquid density at 20 °C is approximately 0.933 g/cm³, and water solubility at 20 °C is approximately 20 g/L. The monomer is miscible with common organic solvents including methanol, toluene, and acetone. Its lower explosion limit in air is 2.6 vol% and the upper explosion limit is 13.4 vol%; the vapor is denser than air and can form flammable mixtures in closed tanks or process vessels. These physical boundaries require electrically grounded storage and transfer equipment, vapor routing to thermal oxidizer or flare, and elimination of direct discharge near drains or ignition sources.
Hydroquinone is a phenolic chain-transfer inhibitor that removes propagating radicals by hydrogen-atom donation. In oxygenated vinyl acetate, trace radicals formed by light, heat, or residual peroxide first convert to peroxy radicals. Hydroquinone donates a phenolic hydrogen to the peroxy radical, producing hydroperoxide and a semiquinone radical; the semiquinone radical then terminates a second radical. This sequence interrupts the radical chain and creates an induction period that delays the onset of observable polymerization. Hydroquinone is not a complete thermal stabilizer in the absence of oxygen. Under nitrogen or carbon dioxide blanketing, the dissolved oxygen concentration falls, the peroxy-radical pathway diminishes, and carbon-centered radicals propagate more readily because hydroquinone traps them at a lower rate. The 10–12 ppm loading therefore sets a defined induction buffer for downstream initiation systems without imposing the higher inhibitor burden of long-distance stability grades. The concentration is measured as 10–12 ppm by weight in the liquid monomer using ASTM D2190 spectrophotometric procedures. At this loading, the oxygen-coupled inhibitor system can maintain monomer stability in closed storage at ≤30 °C for periods determined by site-specific hydroquinone depletion monitoring. Published data for precise consumption kinetics of 10–12 ppm hydroquinone in full-scale field tanks is limited; tank inventory should be evaluated by periodic top, middle, and bottom sampling rather than by a fixed universal shelf-life date.
The release envelope in Table 1 is assembled from the ASTM D2190 standard framework and regional distributor product notes. It is not a single certificate of analysis; actual lot values may be tighter but must remain within the stated boundaries for transfer as polymer-grade vinyl acetate. The hydroquinone loading is the sole compositional driver separating HQ 10-12 from low-inhibitor and high-inhibitor commercial forms.
| Parameter | Typical release boundary | Method or standard designation |
|---|---|---|
| Vinyl acetate purity | ≥99.9 wt% | ASTM D2190 gas chromatography |
| Water | ≤0.02 wt% | ASTM E203 Karl Fischer coulometry |
| Acidity as acetic acid | ≤0.005 wt% | ASTM D1613 titration |
| Hydroquinone | 10–12 ppm | ASTM D2190 UV-Vis spectrophotometry |
| Color, Pt-Co | ≤5 | ASTM D1209 |
| Distillation range at 101.3 kPa | 72–73 °C | ASTM D1078 |
| Methyl acetate | ≤0.02 wt% | Internal gas chromatography |
Field tanks between 50 m³ and 500 m³ should retain an air headspace, not a nitrogen blanket, because hydroquinone inhibition is oxygen-dependent. If the vapor space is inerted, the protective peroxy-radical pathway is suppressed and the system shifts toward slower carbon-centered radical termination. The temperature boundary for continuous storage is ≤30 °C; temperatures above 40 °C raise the radical generation rate and consume hydroquinone more rapidly. Light exposure also accelerates inhibitor loss. Storage vessels are typically fabricated from 304L or 316L stainless steel or lined carbon steel; brass pressure instruments and copper alloy components should be avoided because trace metal ions can promote oxidation and reduce inhibitor efficiency. If the material is held for more than 30 days, top, middle, and bottom samples should be analyzed for hydroquinone content and peroxide value. A drop below 3 ppm hydroquinone indicates the protection margin is nearly exhausted; the material should be consumed within 30 days, re-inhibited under plant protocol, or sampled at short intervals before each transfer. Tanks should be equipped with relief devices sized for vapor pressure at ambient temperature and with earthing for the flammable liquid, closed-cup flash point −8 °C. Avoid contact with free-radical initiators, strong acids, and strong bases. Vinyl acetate hydrolyzes in water to acetic acid and acetaldehyde; the reaction is slow at neutral pH but accelerates in acidic or alkaline service, so transfer lines and tank boots should be drained of accumulated aqueous phase after steam-out operations.
For batch and semi-batch polyvinyl acetate dispersion synthesis, Celanese Vinyl Acetate HQ 10-12 is metered into a glass-lined or 316L stainless steel reactor containing deionized water, protective colloid such as polyvinyl alcohol or hydroxyethylcellulose, and buffer. The formulation pH is ordinarily maintained between 4.0 and 5.0; above 6.0, alkaline hydrolysis of vinyl acetate generates acetic acid and acetaldehyde, which consumes the bicarbonate buffer and may destabilize the colloid. The hydroquinone in the monomer contributes to an induction period before the polymerization exotherm is detected. Reactor operators compensate by adjusting the persulfate or redox initiator dose on a heat-flow basis; published data for this specific configuration is limited, but the induction delay is typically measured in minutes rather than hours at 70–80 °C. A standard semi-batch schedule charges 60–80% of the monomer after nucleation, with the remaining monomer fed during the initiator feed. The final dispersion is characterized by solids content, Brookfield viscosity, particle size, and residual monomer content. Residual vinyl acetate is commonly reduced to below 0.5 wt% by vacuum or steam stripping.
High-solids polyvinyl acetate dispersions at 55–65 wt% solids are produced by seeded semi-continuous emulsion polymerization. The hydroquinone loading of 10–12 ppm in the monomer feed affects the radical balance at the start of the feed interval, particularly when redox initiation is used. In persulfate-initiated systems at 70–80 °C, the initial reactor charge may show an exotherm onset delay of 10–20 min relative to uninhibited monomer; the exact value depends on reactor heat-transfer geometry, agitation, and initiator concentration. Compensating for inhibitor content by a simple stoichiometric oxidizer addition is not reliable because hydroquinone does not scavenge radicals on a fixed one-to-one molar basis under all oxygen concentrations. Production-scale control is usually maintained by automating initiator feed based on reactor temperature and jacket inlet-outlet temperature difference. High-solids dispersions are also sensitive to localized shear; anchor impellers or dual axial-flow impellers operating at 60–120 rpm limit coagulum formation. Particle size in these products is typically bimodal or broad, with mean diameters from 1 µm to 3 µm, and Brookfield viscosity at 25 °C may range from 2,000 mPa·s to 8,000 mPa·s. The hydroquinone-derived quinone by-products can contribute to slight yellowing in the wet latex but are usually below visible thresholds once the polymer is dried.
The selection of hydroquinone loading is a storage-stability and polymerization-induction trade-off. A comparative series of commercial vinyl acetate monomer forms is presented in Table 2. These values represent typical inhibitor-strength landscape ranges, not a single Celanese certificate of analysis. Downstream polymerization plants may segregate storage tanks and feed lines by inhibitor level to avoid cross-contaminating low-inhibitor monomer with 10–12 ppm material and thereby shifting initiator demand.
| Grade form | Hydroquinone loading | Typical use context | Processing impact | Storage boundary |
|---|---|---|---|---|
| HQ 10-12 | 10–12 ppm | General polymer-grade storage; PVAc, EVA, PVOH | Moderate induction; adjust initiator or reduce inhibitor before use | ≤30 °C, air headspace, monitor HQ above 3 ppm |
| Low-inhibitor HQ 3–5 | 3–5 ppm | Accelerated polymerization; high-pressure EVA; low-temperature redox | Shorter induction; narrower storage window | ≤25 °C, use within 1–3 months |
| High-inhibitor HQ 14–17 | 14–17 ppm | Long-distance transport; hot-climate storage | Longer induction; may require higher initiator dose or pre-stripping | ≤35 °C, extended storage |
| Uninhibited | <1 ppm | Specialty controlled synthesis; catalyst-sensitive systems | No inhibitor delay; immediate radical initiation; high autopolymerization risk | Refrigerated, inert gas, use within 1 week |
Ethylene-vinyl acetate copolymerization in high-pressure autoclave or tubular trains operates at 1,400–2,500 bar and 150–220 °C. In these continuous systems, the hydroquinone burden of the vinyl acetate feed must be accounted for in the peroxide initiator balance because an induction delay at the reactor front can shift the hot-spot temperature profile. Producers with high-pressure facilities often specify low-inhibitor or uninhibited vinyl acetate to avoid this disturbance, but 10–12 ppm hydroquinone material can be used if the initiator package is adjusted and the feed is scheduled into a dedicated monomer buffer tank. In polyvinyl alcohol production, vinyl acetate is first polymerized to polyvinyl acetate, then alcoholized in methanol with sodium hydroxide or sodium methoxide. The hydroquinone inhibitor is not a structural comonomer; it remains in the methanol-rich process stream or is removed during washing and drying. The resulting polyvinyl alcohol degree of hydrolysis, typically 87–99 mol%, is controlled by alcoholysis stoichiometry and residence time rather than by the original HQ loading in the vinyl acetate monomer. Polyvinyl alcohol resin derived from this monomer is hygroscopic; when relative humidity exceeds 60%, pre-drying in a dehumidified hopper dryer at 80–100 °C for 4–6 h is required before melt extrusion or cast film processing.
