| HS Code | 302156 |
| Cas Number | 10493-43-3 |
| Molecular Formula | C4F8O |
| Molecular Weight | 216.03 g/mol |
| Boiling Point | 10 °C at 760 mmHg |
| Melting Point | -135 °C |
| Liquid Density | 1.55 g/cm³ at boiling point |
| Refractive Index | 1.24 (liquid, 20 °C) |
| Vapor Density | 7.5 (air = 1) |
| Flash Point | None (non-flammable) |
| Solubility In Water | Insoluble |
As an accredited Perfluoroethylvinyl Ether factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Perfluoroethylvinyl Ether is packaged in 100 g glass bottles under inert nitrogen with PTFE-lined closures for stability. |
| Container Loading (20′ FCL) | Load 20′ FCL with properly sealed drums, secure and brace, segregate from incompatible materials, and label as per chemical safety regulations. |
| Shipping | Ship as **UN 3154 Perfluoro(ethyl vinyl ether)**, Hazard Class **2.1 (Flammable Gas)**, in approved cylinders. Keep away from heat, sparks, and open flames. Use secure pressure-relief equipment, proper placards, and hazmat documentation. Not permitted on passenger aircraft. Follow local transport regulations. |
| Storage | Store in a tightly sealed, original container in a cool, dry, well-ventilated area away from heat, open flames, and direct sunlight. Protect from moisture and incompatible oxidizers. Ensure proper grounding and bonding when handling. Keep containers upright and inspect regularly for leaks or damage. Follow all manufacturer and safety data sheet instructions. |
| Shelf Life | Store sealed under inert gas, away from light and heat. Typical shelf life is 12 months under recommended conditions. |
In semiconductor ultra-pure water and chemical distribution systems, TFE–PEVE copolymer tube stock is melt-extruded for wet-bench manifolds, chemical delivery lines, valve bodies, and high-purity transport carriers. The resin grade selected for this service contains 2–5 mol% PEVE, with a melt mass-flow rate of 2–10 g/10 min at 372 °C under 5 kg load following ISO 1133-1:2022 and ASTM D1238. Dimensional stability and low extractables are not achieved by post-treatment but by excluding metal stearates, slip agents, plasticisers, and halogenated processing aids entirely from the compound. Single-screw extrusion on a 25:1 to 30:1 L/D machine with hardened screw, corrosion-resistant barrel, and PTFE-free purge material reaches melt temperatures of 360–400 °C. Die-lip build-up and melt fracture appear when the shear rate exceeds 200 s⁻¹ in narrow die gaps, so land lengths are extended to 10–15 times the gap. The resin lot is pre-dried for 4 h at 150 °C when storage relative humidity has exceeded 60%, although equilibrium moisture uptake remains low. Final wall thickness is monitored by ultrasonic gauge, and finished tube is helium leak tested at 1×10⁻⁶ mbar·L/s or better. Compliance is verified against SEMI F57 for ultra-pure water system polymers, FDA 21 CFR 177.1550 for perfluorocarbon resins, and ASTM D3307 for PFA molding and extrusion materials.
The same stock is converted into flareless tube fittings and diaphragm valve bodies by injection molding. Mould temperatures of 180–220 °C are used with melt temperatures of 370–400 °C and clamp force sufficient to hold moulds closed under packing pressures of 60–100 MPa. Production failure modes include flash at the parting line from excessive screw recovery speed and surface pit formation when mould venting is below 0.02 mm channel depth. Final parts are double-bagged in cleanroom packaging after a deionised-water rinse, with no aqueous surfactant or anti-static spray permitted because ionic residues alter surface conductivity and can fail SEMI F57 extraction limits.
Rotolining of carbon steel pressure vessels and pipe spools with TFE–PEVE copolymer powder requires a narrow fusion window because pinhole density at the steel interface increases rapidly when peak metal temperature falls below 335 °C or when the powder carries moisture above 0.05 wt%. The steel shell is grit blasted to Sa 2.5 per ISO 8501-1, then heated in a biaxial rotational machine to 340–380 °C. The PFA powder charged into the rotating shell has a median particle diameter of 40–80 µm and an MFR of 12–30 g/10 min at 372 °C/5 kg by ASTM D1238. Under rotation, the powder densifies within the first 10–20 min; full void elimination requires maintaining the metal substrate above 340 °C for an additional 30–60 min depending on shell mass and lining thickness.
A production failure mode is residual porosity at welded seams, where heat sinking lowers local wall temperature by 10–20 °C; the corrective sequence is to increase heat input in the seam zone and reduce rotation speed. The liner wall is built to 2–5 mm in two to three successive powder additions because single-shot thicknesses above 6 mm develop internal shrinkage voids at the melt-to-powder interface. After cooling, the lining is inspected with a spark tester at 5–15 kV DC; any pinhole triggers a local repair patch that must be fusion bonded over the failed area. Final components are supplied to ASTM F1545 for plastic-lined ferrous metal pipe and fittings, with hydrostatic test pressure held at 1.5 times the design pressure. The end products are lined reactors, acid storage vessels, and chlorine dioxide mixing tanks in chemical processing plants.
In downhole sensor cable and aerospace wiring harnesses, TFE–PEVE insulation replaces PTFE tape-wrap construction because it permits continuous melt extrusion directly over silver-plated or nickel-plated copper conductors. The insulation grade is selected with an MFR of 10–30 g/10 min at 372 °C/5 kg and is extruded on a 30:1 L/D single-screw wire line with a 24 AWG to 8 AWG conductor preheating stage. Melt temperature is held at 370–410 °C, and the pressure drop through a 1 mm die with a 10 mm land is monitored to keep draw-down ratio below 100:1; violations produce eccentric insulation and reduced dielectric strength. A typical wall thickness of 0.15–0.50 mm is measured continuously with an X-ray or laser diameter gauge.
The insulated single-core construction is evaluated for spark test at 2.5 kV a.c. and for flammability mark acceptance under UL 1581 VW-1. Continuous conductor temperature rating of 260 °C is supported by long-term aging data generated under SAE AS22759-type protocols for fluoropolymer aerospace wire. Process instability appears as cone breaks at the wire tip when conductor preheat is below 120 °C or when screw speed fluctuates more than ±2%; this yields intermittent bare sections that are rejected in the in-line spark test. Terminal products include downhole heater cable, aerospace sensor harness, and motor lead wire for high-temperature pumps.
| Application segment | Property checked | Standard/method | Typical acceptance window |
|---|---|---|---|
| Semiconductor PFA tube | Melt mass-flow rate | ISO 1133-1:2022 / ASTM D1238 | 2–10 g/10 min at 372 °C/5 kg |
| Semiconductor PFA tube | Extractables for UPW contact | SEMI F57 | pass |
| Rotolined steel vessel | Surface preparation | ISO 8501-1 | Sa 2.5 |
| Rotolined steel vessel | Lining pinhole integrity | ASTM F1545 | spark test 5–15 kV DC |
| High-temperature wire | Flammability mark | UL 1581 VW-1 | pass |
| Thermoformed sheet | Flexural modulus | ISO 178 | 550–650 MPa at 23 °C |
| Powder coating | Solvent resistance | ASTM D5402 | no delamination after 100 double rubs |
| FKM evaluation | Mooney viscosity | ASTM D1646 | ML 1+10 30–80 at 121 °C |
Thermoformed PFA sheet for pharmaceutical process trays and vessel liners uses a TFE–PEVE resin with PEVE content toward the upper practical window, typically 3–5 mol%, to lower zero-shear viscosity and improve replication of plug-assist details. The sheet is extruded from a 40 mm single-screw extruder with L/D 30:1 through a flat die onto a calendering stack held at 180–220 °C. A high PEVE level reduces flexural modulus; values measured by ISO 178 are commonly 550–650 MPa at 23 °C, whereas lower comonomer grades may exceed 650 MPa. Thermoforming is carried out with sheet temperatures of 260–290 °C, plug temperature 180–220 °C, and mould temperature 150–200 °C.
If the sheet temperature exceeds 295 °C, sagging and wall-thinning beyond 0.5 mm occur in the sidewall; if it drops below 255 °C, the part shows stress whitening and incomplete corner filling. The finished article meets USP <87> and USP <88> extraction protocols and is accepted for contact with pharmaceutical process water after steam-in-place cycles at 121 °C. End products are reusable containment trays, lyophilisation tray liners, and vessel scuff liners used in active pharmaceutical ingredient handling.
PEVE-containing PFA powder coatings are applied to carbon steel mixer blades, centrifuge components, and rack fixtures where chemical exposure demands a pinhole-free fluoropolymer layer without a vacuum lining process. The powder is fluidised and sprayed electrostatically at 60–90 kV with gun-to-part distance 150–250 mm, giving initial film thickness 300–800 µm. The substrate is prepared to Sa 2.5 and preheated to 180–220 °C before powder application to improve first-pass adhesion. The bake cycle uses a peak metal temperature of 370–400 °C for 15–30 min; if the peak metal temperature remains below 360 °C, the coating shows low solvent rub resistance and intercoat delamination under ISO 2409 cross-cut tape pull.
The final coating is spark tested at 5–10 kV. Adhesion is further qualified by ISO 2409 cross-cut tape test, solvent resistance by ASTM D5402, and corrosion resistance in ISO 9227 neutral salt spray for 1000 h. The end products are coated pharmaceutical drying trays, chemical mixer blades, and centrifuge liners for corrosive solid-liquid separation.
Perfluoroethyl vinyl ether is screened in specialty fluoroelastomer formulations when a lower-molecular-weight perfluoroalkoxy vinyl ether is required to plasticise a vinylidene fluoride-rich backbone without introducing hydrocarbon flexibiliser. In such evaluations, PEVE is introduced as a comonomer in the terpolymerisation with VDF and hexafluoropropylene or TFE, with PEVE feed typically 1–5 mol% of the monomer mix. The resulting polymer is a gum of Mooney viscosity ML 1+10 at 121 °C in the range 30–80, determined by ASTM D1646. Compounding on a two-roll mill at 30–50 °C incorporates bisphenol-A cure systems or peroxide cure systems. The vulcanizate then undergoes press cure at 177 °C for 10–15 min and post cure at 200–230 °C for 4–24 h. The intended effect is a lower gel-point elastic modulus and better retention of sealing force at low temperature, tested by ISO 815-1 compression set after 70 h at 150 °C. Published compounding data for this specific PEVE architecture is limited; screening is therefore confined to material-qualification batches rather than commercial part print substitution. End products under evaluation are O-rings, gaskets, and oilfield packer elements.
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Perfluoroethyl vinyl ether (PEVE), also written perfluoroethylvinyl ether, is introduced as a low-boiling perfluorinated vinyl ether with the molecular formula CF2=CF–O–CF2CF3, CAS registry number 10493-43-3, and molar mass 216.03 g mol⁻¹. At ambient pressure, the monomer boils near 8 °C; it is therefore handled as a pressurized liquefied gas rather than as a conventional liquid solvent. The material is supplied in carbon steel or stainless steel cylinders and is used almost exclusively as a comonomer in radical-initiated copolymerization with tetrafluoroethylene (TFE) and vinylidene fluoride (VDF) to produce melt-processable fluoroplastics and peroxide-curable fluoroelastomers. Unlike hydrocarbon vinyl ethers, the fully fluorinated ethyl side chain contains no abstractable C–H bond, which reduces chain-transfer susceptibility during aqueous emulsion polymerization and alters the thermal oxidation profile of the resulting copolymer. Commercial grade designations are supplier-specific; a universal model code for PEVE does not exist under ISO or ASTM nomenclature. A purchaser must therefore specify the grade by purity, water content, acidity, inhibitor identity, and cylinder size rather than by a generic product number.
Because no single ISO or ASTM monograph defines a universal PEVE grade, procurement specifications are negotiated between the monomer supplier and the polymerization unit. Gas chromatographic assay with flame ionization detection is used to quantify PEVE purity; many fluoropolymer producers require an assay above 99.0 area%, but the exact acceptance limit depends on the boiling point distribution of the supplied lot. Water content is measured by Karl Fischer titration, and material intended for low-temperature fluoroelastomer synthesis is often controlled below 50 mg kg⁻¹ because protonic impurities consume initiator or terminate active chain ends in the aqueous emulsion recipe. Acidity expressed as hydrogen fluoride is typically limited to 10 mg kg⁻¹ or lower; higher free HF concentrations corrode carbon steel cylinders and generate metal fluoride fines that later appear as filter plugging in polymer finishing lines. Vapor-space oxygen is reduced by nitrogen padding, commonly to below 1000 ppmv, to preserve inhibitor activity and prevent accumulation of low-molecular-weight peroxy compounds. Inhibitor content is not always normalized in the certificate of analysis; instead, the reactor recipe compensates by pre-distillation or by adjusting the initiator charge. The inhibitor chemistry is supplier-specific and may be a hindered phenolic or other non-amine radical scavenger, but the exact identity and concentration must be disclosed through the safety data sheet before the monomer enters a production reactor.
In production-scale aqueous emulsion copolymerization, PEVE is introduced into a stirred jacketed autoclave either as a pre-charged liquid or as a continuously metered feed through a Coriolis mass-flow controller sized for low-viscosity liquefied fluorinated monomers. The reactor is typically operated at pressures between 0.8 MPa and 2.5 MPa and temperatures from 60 °C to 90 °C for TFE-based systems, although published data for PEVE-specific polymerization kinetics are limited compared with perfluoro(propyl vinyl ether) systems. Monomer uptake is monitored by differential pressure drop and near-infrared or gas-phase FTIR analysis of the reactor headspace because the comonomer concentration in the polymer cannot be inferred from the feed ratio alone. When PEVE is incorporated as the modifying comonomer, the perfluoroethoxy side chain interrupts fluoropolymer crystallinity; however, because the side chain is one difluoromethylene unit shorter than that of perfluoro(propyl vinyl ether), a higher molar incorporation level may be required to achieve a given reduction in the crystalline melt endotherm. Melt flow rate data according to ISO 1133-1:2022 and differential scanning calorimetry according to ISO 11357-3:2018 are used to tune the comonomer feed. On a twin-screw extruder with an L/D ratio of 40:1, PEVE-modified resin may display a narrower melt fracture window than PPVE-modified resin at equivalent melt flow rate; the effect is observed as surface roughness on tubing or cable insulation at elevated draw speeds. Published data for this specific production configuration are limited, and pilot-scale extrusion trials are required to establish the draw-speed boundary for a given resin grade.
The incorporation level of PEVE in the isolated copolymer is determined by solid-state ¹⁹F NMR or by infrared spectroscopy calibrated against ¹⁹F NMR. In PEVE-modified resin, the signal associated with the −O–CF2CF3 side chain is integrated against the −CF2− backbone resonances to calculate the comonomer mole fraction. This measurement is preferred over elemental analysis because the carbon-fluorine ratio does not change as sharply across the comonomer range as it does with hydrocarbon comonomers. In production campaigns, the target comonomer mole fraction is usually held within a narrow band because the melt flow rate is highly sensitive to side-chain concentration. A drift of the comonomer feed by even a few percent relative to TFE can shift the melt flow rate beyond the specification window and create off-spec resin that cannot be reworked by simple blending.
The selection of PEVE over perfluoro(methyl vinyl ether) (PMVE) or perfluoro(propyl vinyl ether) (PPVE) shifts both monomer handling and polymer architecture. Table 1 compares supplier-reported molecular weights and normal boiling points; the boiling point values vary with inhibitor content and pressure calibration and should not be used for critical relief-valve sizing without lot-specific physical property data.
| Parameter | PMVE | PEVE | PPVE |
|---|---|---|---|
| CAS registry number | 1187-93-5 | 10493-43-3 | 1623-05-8 |
| Molar mass | 166.02 g mol⁻¹ | 216.03 g mol⁻¹ | 266.03 g mol⁻¹ |
| Normal boiling point at 101.3 kPa | −22 °C | 8 °C | 36 °C |
| Perfluoroalkoxy side chain | −O–CF3 | −O–CF2CF3 | −O–CF2CF2CF3 |
Compared with PMVE, PEVE has a higher boiling point and lower room-temperature vapor pressure, which simplifies cylinder handling but reduces vapor-phase monomer availability in semi-batch reactors. Compared with PPVE, PEVE introduces one fewer difluoromethylene unit in the side chain; this can increase the minimum comonomer weight fraction needed to suppress the primary melt endotherm and can reduce the low-temperature flex life of the final perfluoroalkoxy resin. The shorter PEVE side chain may, however, lower melt viscosity at a given comonomer mole fraction and may improve optical clarity in thin-wall tubing because the smaller side group reduces light-scattering domain size. These trade-offs are not captured by a single polymer standard; resin qualification therefore requires a test matrix including ASTM D1238-23, ISO 11357-3:2018, ASTM D790-17 for flexural modulus, and ASTM D638-14 for tensile properties. Published data on PEVE-based perfluoroalkoxy resin are less extensive than PPVE-based data, so formulators generally validate each grade on pilot-scale extrusion and injection molding lines before transfer to production.
PEVE is not interchangeable with partially fluorinated vinyl ethers such as 2,2,2-trifluoroethyl vinyl ether because the absence of a hydrocarbon ethyl group changes the solubility parameter and the reactivity ratio in fluoroolefin copolymerization. Partially fluorinated monomers introduce C–H bonds that participate in chain transfer and reduce thermal stability; PEVE avoids this pathway at the cost of higher monomer volatility and more demanding distillation control. The fully fluorinated side chain also means that PEVE does not introduce a proton source into the polymerization, which is advantageous in peroxide-cured fluoroelastomer recipes where water and acid impurities must be kept low.
PEVE is stored under its own vapor pressure in cylinders fitted with pressure-relief devices and stainless steel or nickel-wetted components. The maximum allowable storage temperature is set by the supplier and by the inhibitor package; storing cylinders above 52 °C is generally avoided because inhibitor consumption accelerates and the monomer vapor pressure rises beyond standard cylinder service limits. Cylinders returned partially empty may contain vapor-space oxygen if not padded with nitrogen; oxygen ingress can generate low-concentration perfluoroether peroxides that concentrate during distillation or cylinder recycling. To prevent unsafe peroxide accumulation, PEVE transfer lines are designed for continuous flow rather than stagnant hold-up, and dead legs are minimized. The material should not be contacted with copper, aluminum, or their alloys because these metals can initiate oligomerization or degrade the inhibitor; fluoropolymer-lined or stainless steel components are preferred. Avoid combination with amine-based additives in the same feed system because amines can neutralize acidic stabilizers and accelerate exothermic oligomerization of the vinyl ether group. Cylinder changeover procedures on a fluoropolymer production line are scheduled around inhibitor lot number rather than calendar age alone; a new lot with a different inhibitor concentration is quarantined until the reactor feed mass-flow controller is recalibrated and residual oxygen is verified below the target limit.
Regulatory compliance for PEVE is handled at the monomer and polymer levels. The monomer is not a food-contact substance in itself; food-contact status is evaluated on the finished fluoropolymer under the relevant jurisdiction. For U.S. applications, finished resins may be assessed under 21 CFR 177.1550 for perfluorocarbon resins, but the monomer must be fully reacted and residual PEVE must be controlled below the levels established in the Food Contact Notification or threshold-of-regulation submission. In the European Union, PEVE is subject to REACH registration obligations, and industrial users must apply the exposure scenarios in the supplier safety data sheet; local exhaust ventilation and closed-loop transfer are standard because the material is a volatile fluorinated monomer. The polymer producer is responsible for demonstrating that residual monomer and oligomers do not violate specific migration limits under Regulation (EU) No 10/2011 when the final article is intended for food contact. Under industrial hygiene monitoring, fluoropolymer plants often use photoionization detection or thermal desorption gas chromatography to verify PEVE concentration against supplier-derived internal exposure limits; published regulatory occupational exposure limits specific to this substance are limited, so many sites do not rely on a single universal 8-hour time-weighted average.
Recovery of unreacted PEVE from the polymerization off-gas is performed in a refrigerated vent condenser followed by fractional distillation at reduced pressure. The off-gas stream may contain TFE, vinylidene fluoride, and carbon dioxide; the distillation column is therefore designed with a low-temperature reflux loop and a reboiler temperature controlled to avoid thermal homopolymerization in the column bottoms. Inhibitor is replenished in the recovered monomer before it is re-introduced to the reactor because the original inhibitor is partially consumed in the condenser and column. Unconverted PEVE collected from multiple batches can vary in assay by measurable gas chromatographic differences; this batch-to-batch variance is managed by blending recovered monomer into a dedicated feed tank and verifying purity before the blended lot is released for a production campaign. Transfer of the blended lot to the reactor feed system is conducted only after the mass-flow controller calibration and oxygen content have been verified, and after the recovered monomer has passed the same acidity and moisture limits applied to fresh material.
