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| HS Code | 917126 |
| Chemical Name | Allyl Chloride |
| Chemical Formula | C3H5Cl |
| Cas Number | 107-05-1 |
| Molecular Weight | 76.52 g/mol |
| Appearance | Colorless to light yellow liquid |
| Odor | Unpleasant, pungent, garlic-like odor |
| Density | 0.938 g/cm³ at 20°C |
| Boiling Point | 45 °C (113 °F) |
| Melting Point | -134.5 °C (-210.1 °F) |
| Flash Point | -32 °C (-25.6 °F) closed cup |
| Solubility In Water | Slightly soluble (2.5 g/L at 20°C) |
| Vapor Pressure | 340 mmHg at 20°C |
| Refractive Index | 1.415 at 20°C |
| Autoignition Temperature | 392 °C (737 °F) |
As an accredited Allyl Chloride factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Available in 200 kg steel drums and bulk ISO tanks, with nitrogen blanketing for safe, stable containment. |
| Container Loading (20′ FCL) | Load 20’ FCL with UN-listed drums/ISO tanks of Allyl Chloride; secure, ventilate, label hazardous, segregate from oxidizers and foodstuffs. |
| Shipping | Allyl Chloride (UN 1100, Class 3, Packing Group I) ships as a flammable, toxic liquid. Use approved steel drums or ISO tanks, grounded and ventilated. Segregate from foodstuffs and oxidizers. Label as “Allyl Chloride,” include hazard placards, and follow IATA/IMDG/ADR regulations for safe transport. |
| Storage | Store Allyl Chloride in a cool, dry, well-ventilated area away from heat, sparks, open flames, and direct sunlight. Use approved, tightly sealed containers and bond/ground equipment to prevent static discharge. Keep separate from oxidizers, acids, and moisture. Employ explosion-proof refrigeration if needed and ensure secondary containment to manage spills safely. |
| Shelf Life | Store cool, dry, under inert gas, away from light. Shelf life is typically 12 months when unopened and properly handled. |
The dominant industrial route to epichlorohydrin consumes allyl chloride through a chlorohydrination sequence in which chlorine is dissolved into process water to generate hypochlorous acid, followed by addition across the terminal double bond of allyl chloride to form 1,3-dichloro-2-propanol. Temperature is controlled at 40–50 °C under gauge pressure 0.1–0.3 MPa, and pH is held at pH 4–5 to minimize hydrolysis of the dichloropropanol. Industrial chlorohydrination plants typically feed chlorine-to-allyl chloride at a molar ratio of 1.05:1–1.15:1; unconverted allyl chloride is recovered by fractional distillation and returned to the reactor. The intermediate dichloropropanol stream is subsequently contacted with a calcium hydroxide slurry or sodium hydroxide solution at 60–90 °C in steam-stripped reaction columns, yielding epichlorohydrin. Because epichlorohydrin forms an azeotrope with water, the downstream purification train relies on decantation and twin-column distillation rather than simple fractional distillation. Primary equipment consists of glass-lined carbon-steel chlorohydrination reactors, titanium plate-and-frame exchangers for chlorine water cooling, and vacuum distillation columns with structured packing. Downstream liquid epoxy resin producers convert epichlorohydrin with bisphenol A under alkaline conditions; the controlling formulation parameter is the epichlorohydrin-to-bisphenol A molar ratio, which is maintained at 8:1–10:1 for standard DGEBA resins and reduced to 2:1–3:1 for semi-solid or solid epoxy resins. Sodium hydroxide is added at 1.1–1.3 equivalents per phenolic hydroxyl group to drive dehydrochlorination. Quality verification of the resulting epoxy resins uses ASTM D1652-11e1 or ISO 3001:1999 for epoxide equivalent weight, with liquid DGEBA resins falling between 182 g/eq and 192 g/eq. Food-contact can coatings formulated from these resins are evaluated under FDA 21 CFR 175.300; REACH registration for epichlorohydrin includes its CLP Carcinogen Category 1B classification, which imposes closed-loop handling and emission monitoring on conversion lines. Terminal finished product types include bisphenol A liquid epoxy resins for solvent-free floor coatings, high-solids anticorrosion marine primers, wind turbine blade laminates, and electrical potting compounds; epoxy novolac resins derived from the same epichlorohydrin stream are used in high-temperature adhesives and printed circuit laminate prepregs.
Diallyl phthalate molding compounds represent a thermoset branch in which allyl chloride is first hydrolyzed to allyl alcohol and then esterified with phthalic anhydride; the resulting diallyl phthalate monomer undergoes partial polymerization to a storage-stable prepolymer before being compounded with fillers. Compound formulation records typically place the diallyl phthalate prepolymer binder at 25–40 wt% of total compound, with mineral or fibrous fillers at 40–60 wt%, dicumyl peroxide initiator at 1.0–2.0 phr based on resin, and hydroquinone inhibitor at 0.05–0.1 wt% to control shelf life. Prepolymerization is carried out in jacketed reactors at 80–120 °C until the Brookfield viscosity reaches 300–1,500 mPa·s; the prepolymer is then transferred to heated two-roll mills at 80–110 °C for filler dispersion. Molding is performed on compression presses with 100–300 t clamping force at 150–175 °C and 10–35 MPa cavity pressure for 2–5 min, followed by post-cure at 150 °C for 4 h. Compliance is anchored to ASTM D5948-05(2020) for diallyl phthalate molding compound classification and to UL 94 V-0 flammability performance at 0.8 mm thickness for high-temperature electrical grades. Terminal parts sold into EU electrical applications are evaluated under IEC 60112 for comparative tracking index and under 2011/65/EU RoHS restrictions. Finished product types include automotive alternator rectifier brush holders, circuit breaker arc chambers, aerospace connectors, and encapsulated ignition components where dimensional stability at 180 °C is required. The prepolymer must not be overheated above 120 °C during compounding because gelation can occur in the two-roll mill.
In the production of coagulation-grade polyDADMAC, the initial alkylation of dimethylamine with allyl chloride is rarely the capacity-limiting step; the bottleneck occurs during residual monomer stripping and molecular-weight control. The monomer synthesis uses a two-fold molar excess of allyl chloride over dimethylamine, with recorded feed ratios of 1:2.05–1:2.20 dimethylamine to allyl chloride, and sodium hydroxide solution is used to maintain pH at 9–11 while liberating dimethylamine base from its hydrochloride salt. Alkylation takes place in glass-lined stirred reactors at 40–60 °C with residence times of 6–12 h; unreacted allyl chloride is then removed by vacuum distillation at 80–120 °C to a residual concentration of ≤1 ppm before polymerization. The polymerisation step uses ammonium persulfate initiator at 0.1–0.5 wt% based on monomer and is conducted at 60–80 °C in aqueous solution. Chain-transfer agents are adjusted batch-wise to control final viscosity between 500 mPa·s and 2,000 mPa·s at 40% solids. Finished coagulant dosing in drinking water clarification is typically 0.1–5.0 mg/L as active polymer; sludge dewatering at municipal plants adds 2.0–8.0 kg active polyDADMAC per 1,000 kg dry solids. Compliance for potable water exposure is governed by NSF/ANSI/CAN 60 and AWWA B451, which require product-specific toxicology review and residual monomer limits. Equipment used for final processing includes wiped-film evaporators for concentration, static mixers for viscosity adjustment, and stainless steel storage tanks with recirculation pumps. Terminal finished product types include liquid polyDADMAC coagulants at 20–40% solids, dry cationic polymer granules for sludge dewatering, and formulated dual-polymer retention aids for paper manufacturing. Operational boundaries include maintaining pH below 11 during alkylation and avoiding temperatures above 70 °C in the absence of adequate vacuum stripping, because alkaline hydrolysis of allyl chloride to allyl alcohol accelerates under those conditions and reduces DADMAC monomer purity.
When optical lens casting requires a crosslinked allylic network with high Abbe number and low chromatic aberration, diethylene glycol bis(allyl carbonate) monomer is synthesized from allyl alcohol that originates from alkaline hydrolysis of allyl chloride. The hydrolysis step is run at pH 12–13 and 80–120 °C with steam stripping; recovered allyl alcohol is then converted to diethylene glycol bis(allyl carbonate) monomer through carbonate ester synthesis. In lens casting, the monomer is used as the reactive liquid without a comonomer diluent; the initiator, diisopropyl peroxydicarbonate, is added at 2.0–4.0 wt% based on monomer, and UV absorbers are added at 0.05–0.1 wt% when specified for sunwear. The casting mixture is vacuum-degassed at 20–30 °C under 2–5 kPa, filtered through 0.22 μm membranes, and injected into glass mold assemblies with EVA gaskets. The thermal cure sequence is staged at 60 °C for 4 h, 80 °C for 8 h, and 100 °C for 4 h to avoid stress cracking; demolding is followed by annealing before edge polishing. Compliance for finished lenses is referenced to ISO 8980-1:2017 for ophthalmic optics and ANSI Z87.1-2020 for protective eyewear, with U.S. dress-lens impact requirements under FDA 21 CFR 801.410. The monomer is thermally unstable in bulk storage and must be maintained below 25 °C with inhibitor monitoring. Terminal finished product types include prescription ophthalmic lenses, plano sun lenses, motorcycle visor blanks, and high-impact security eyewear.
Sodium allyl sulfonate enters nickel electroplating as an auxiliary brightener intermediate whose sulfonic acid group stabilizes the brightener film and suppresses edge overplating at high current density. It is not used alone; it is blended with saccharin or proprietary Class II brighteners in the final bath formulation. The working addition range for sodium allyl sulfonate in a Watts nickel bath is 0.02–0.10 g/L, with stock solutions prepared at 5–10 g/L in deionized water. The base bath composition consists of nickel sulfate at 240–300 g/L, nickel chloride at 30–60 g/L, and boric acid at 35–45 g/L; operating parameters are maintained at pH 4.0–4.8, 50–60 °C, and cathode current density of 2–8 A/dm². Continuous filtration through activated carbon at 2–4 bath volumes per hour is used to remove organic decomposition products, while air agitation or eductor mixing maintains uniform additive distribution. Deposition times are set to produce 8–20 μm nickel underplate before subsequent chromium flash. Compliance for plated plastic components is referenced to ISO 4525:2003 for electrodeposited nickel plus chromium coatings on plastics, and discharge limits for process wastewater are governed by 40 CFR Part 413 metal finishing effluent guidelines. Equipment on production lines consists of polypropylene plating tanks, titanium anode baskets with bagged nickel rounds, PTFE immersion heaters, and rectifiers with ripple below 5%. Terminal finished product types include automotive ABS grilles, headlamp bezels, plumbing fixtures, motorcycle trim, and appliance control panels requiring bright nickel-chromium appearance. Operational boundaries include maintaining total brightener concentration below 0.15 g/L because excess sodium allyl sulfonate increases nickel deposit tensile stress and can induce microcracking during thermal cycling.
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Allyl chloride (3-chloro-1-propene, CAS 107-05-1, EC 203-457-6), formula CH2=CHCH2Cl, molecular mass 76.52 g/mol, is a low-boiling chlorinated alkene supplied as a clear, volatile liquid with a sharp, chlorinated odor. Industrial production is carried out by gas-phase free-radical chlorination of propylene in a flow reactor, followed by quench, HCl recovery, caustic or water scrubbing, drying, and fractional distillation. The commercial synthesis-grade product is specified at minimum purity 98.0 wt% by gas chromatography, with a typical distillation range of 44.0–46.0 °C, water content not exceeding 0.05 wt% by ASTM E203, and APHA color not exceeding 20 by ASTM D1209. Density is 0.938 g/cm³ at 20 °C, vapor pressure is 39.3 kPa at 20 °C, closed-cup flash point is −32 °C, autoignition temperature is 392 °C, and explosive limits in air range from 2.9 vol% to 11.1 vol%. In neutral water the compound hydrolyses slowly to allyl alcohol and hydrogen chloride; the rate increases sharply with acid or base addition, elevated temperature, and in the presence of dissolved metal salts. The product is supplied in bulk as a stabilised or unstabilised grade, with the inhibitor identity and concentration being producer-specific and usually confirmed before downstream qualification.
| Parameter | Value | Method |
|---|---|---|
| Purity, wt% | 98.0 minimum | in-house GC-FID |
| Water, wt% | 0.05 maximum | ASTM E203 |
| Color, APHA | 20 maximum | ASTM D1209 |
| Distillation range, °C | 44.0–46.0 | ASTM D1078 |
| Density at 20 °C, g/cm³ | 0.938 | ASTM D4052 |
| Acidity as HCl, wt% | 0.005 maximum | ASTM D1613 |
Compared with saturated propyl chlorides, allyl chloride differs in both physical hazard profile and reaction chemistry. 1-Chloropropane boils at 46.7 °C and has a higher flash point than allyl chloride, while 2-chloropropane boils at 35.7 °C; both lack the vinylic bond required for silane hydrosilylation or free-radical addition. In nucleophilic substitution, the allylic chloromethyl group ionizes through a resonance-stabilized allyl cation pathway, so alkaline hydrolysis to allyl alcohol proceeds under milder conditions than with saturated propyl chlorides. The same resonance stabilization increases the potential for exothermic oligomerization when local caustic concentration is not controlled. Production-scale alkaline hydrolysis vessels are therefore specified with high-efficiency agitation, external jacket cooling, and caustic dosing distributed across the liquid surface rather than at a single location. Published data for this specific configuration is limited; however, process design typically treats reaction enthalpy removal as the limiting scale-up factor, not mass transfer.
In continuous epichlorohydrin manufacture, allyl chloride is contacted with chlorine and water in a gas-liquid chlorohydrination system to form a mixture of dichloropropanols. The reactor is operated with excess allyl chloride to limit chlorine accumulation, and the liquid recycle loop is cooled to prevent hydrolysis of allyl chloride and to control the evolution of hydrogen chloride. The chlorohydrin-containing organic layer is then dehydrochlorinated with milk of lime or sodium hydroxide in a stripping column, where 1,3-dichloropropan-2-ol and 2,3-dichloropropan-1-ol are converted to epichlorohydrin. The reboiler and overhead condenser are specified for the low-boiling chlorinated feed; flameproof electrical classification follows flammable liquid category 2. The process is sensitive to both pH and temperature in the dehydrochlorination step. Temperature is maintained within a narrow band, typically a set point with ±5 °C alarm limits, because lower temperatures reduce conversion while higher temperatures increase byproduct formation and fouling in the reboiler. Aqueous phase recycle is controlled to avoid accumulation of chloride salts and glycol ethers that depress phase separation.
Downstream separation uses a combination of steam stripping, decantation, and fractional distillation. Crude epichlorohydrin is purified to meet downstream resin specifications, while excess allyl chloride is recovered overhead and returned to the chlorohydrination reactor. The choice of allyl chloride rather than allyl alcohol as the starting intermediate for epichlorohydrin reflects the established integration with chlor-alkali operations; however, the route demands rigorous moisture control because water accelerates hydrolysis of allyl chloride to allyl alcohol and can form azeotropic mixtures that affect column mass balance.
Allyl alcohol is produced from allyl chloride in a continuously stirred alkaline hydrolysis reactor, with pH and temperature adjusted to favour alcohol formation while suppressing diallyl ether byproduct. Water content in the hydrolysis feed is maintained high enough to act as thermal ballast and to minimize ether formation. The crude allyl alcohol is recovered by extractive distillation, and the aqueous phase is steam-stripped before biological treatment. In allylamine synthesis, allyl chloride is reacted with anhydrous ammonia in a high-pressure continuous reactor using a large molar excess of ammonia to reduce secondary and tertiary amine byproducts. The reaction is performed in a two-stage system: a primary amination loop with ammonia recovery, followed by neutralisation and product drying. These downstream processes rely on the same structural feature that distinguishes allyl chloride from saturated propyl chlorides—substitution at the chloromethyl group occurs without loss of the terminal alkene, allowing the resulting products to retain polymerisable unsaturation.
Batch-to-batch variance in commercial allyl chloride is concentrated mainly in water, acidity, color, and low-level chlorinated impurities. Incoming raw-material specifications at polymer production sites often add individual impurity limits for 1,2-dichloropropane, 1,3-dichloropropene, and trichloropropanes, because heavy chlorinates can persist through hydrolysis and influence final resin color and molecular weight distribution. Closed-loop samplers with chilled receivers are used for quality control sampling because the liquid boils at 45 °C and can flash during open sampling. Analytical methods include ASTM D4052 for density, ASTM D1209 for color, ASTM E203 for water, ASTM D1078 for distillation range, and ASTM D1613 for acidity as hydrogen chloride. The presence of a stabiliser does not remove the need for temperature-controlled storage but extends the safe shelf life under a nitrogen blanket.
The terminal alkene function permits allyl chloride to be converted into allyl-functional silane coupling agents and allyl ether monomers. Reaction with trimethoxysilane under hydrosilylation yields allyltrimethoxysilane, a moisture-reactive adhesion promoter used in mineral-filled thermoplastics, crosslinkable polyolefins, and moisture-cure coatings. In compounded polypropylene or polyethylene, the silane is fed into a co-rotating twin-screw extruder with L/D ratio from 40:1 to 48:1, with the feed point selected after the polymer melting zone to reduce premature vapor loss. The methoxysilane groups hydrolyze at the filler interface, while the allyl terminus can participate in free-radical grafting or hydrosilylation cure. Unlike chloropropyltrimethoxysilane, allyltrimethoxysilane retains an unsaturated site that can be consumed in the polymer matrix, which can increase crosslink density in moisture-cure formulations but also demands tighter temperature control during compounding to prevent scorch. Lap-shear adhesion is validated by ASTM D1002 or ISO 4587 using the production substrate and adhesive.
Allyl chloride derivative chains extend to allyl alcohol-derived allyl glycidyl ether, allyl methacrylate, diallyl phthalate, and pharmaceutical alkylation products. In each case, process selection is determined by the leaving-group chemistry of the chloromethyl group and the need to preserve the double bond for later reaction. Allyl methacrylate produced from allyl alcohol is used as a crosslinker in acrylic and coating resins, where the allyl unsaturation reacts more slowly than the methacrylate double bond and permits staged cure. When used for pharmaceutical alkylation, residual allyl chloride in the final active pharmaceutical ingredient is controlled by gas chromatography and purge-factor studies because the compound is classified as an acutely toxic alkylating agent. Published data for this specific configuration is limited; process validation includes spiking studies and mass balance calculations matched to the production batch size.
Unloading and storage systems for allyl chloride require exclusion of atmospheric oxygen and moisture. Exposure to oxygen leads to slow peroxide formation and can initiate free-radical oligomerization, producing high-boiling residues that foul storage tanks and downstream vaporiser tubes. Exposure to water liberates hydrogen chloride and raises acidity, which accelerates hydrolysis and corrodes carbon steel surfaces. Storage tanks are therefore blanketed with nitrogen, fitted with conservation vents and flame arrestors, and maintained with top-space oxygen concentration below the lower explosive limit. The material is typically stored at temperatures below 35 °C to reduce vapor pressure and autoxidation rate; for prolonged storage, the product is kept under a nitrogen pressure pad and monitored for peroxide content and acidity trends. Piping and tankage are commonly constructed of 316L stainless steel or lined carbon steel, with fluoropolymer or graphite gaskets selected for chlorinated organic service. Transfer is performed with seal-less canned-motor or magnetic-drive pumps to reduce fugitive emission risk from a liquid with a closed-cup flash point below 0 °C.
In plant-scale unloading, nitrogen displacement rather than air displacement is used for tank cars, and the vapor return line is routed to a scrubber or thermal oxidizer. Liquid line size and pump speed are set to avoid static discharge; maximum flow velocity is limited in accordance with IEC TS 60079-32 or equivalent electrostatic control guidance. Because allyl chloride vapor is heavier than air, drains and sumps are ventilated at low level and monitored with fixed photoionization detectors. The material is incompatible with strong bases, aluminium chloride, and some metal oxides; contact with caustic or amines inside a confined tank can generate heat and hydrogen chloride, increasing pressure. Published data for every material combination is limited, so compatibility testing is performed before introducing new linings or gaskets.
Allyl chloride is classified under CLP Regulation (EC) No 1272/2008 as flammable liquid category 2, acute toxicity category 3 by oral and inhalation routes, skin irritant category 2, eye irritant category 2, and chronic aquatic toxicity category 3. The corresponding hazard statements include H225, H301, H331, H315, H319, and H412. The OSHA permissible exposure limit is 1 ppm as an 8-hour time-weighted average; the NIOSH short-term exposure limit is 2 ppm. Transport is governed by UN 1100, Class 3. In handling areas, fixed photoionization detectors, local exhaust ventilation, and flameproof electrical classification are specified because vapors can accumulate in low areas and travel to ignition sources. Emergency relief sizing for storage and reactor systems uses the boiling point and vapor pressure profile of the liquid; relief discharges are routed to a scrubbed flare or thermal oxidizer rather than directly to atmosphere. Wastewater from drainage and scrubber blowdown is collected and treated as chlorinated organic waste because allyl chloride and its hydrolysis products are toxic to aquatic organisms.
Compared with allyl alcohol, allyl chloride offers a lower boiling point and higher vapour hazard but avoids the high aqueous solubility and hydrogen-bonding of the alcohol in downstream separation. Compared with epichlorohydrin, allyl chloride is more volatile, lacks the oxirane ring, and is less reactive with carboxyl and amine nucleophiles at ambient temperature; epichlorohydrin is selected when terminal epoxide functionality is required for resin crosslinking, while allyl chloride is selected when a chloromethyl group and terminal alkene must be present in the same intermediate. Compared with allyl bromide, allyl chloride is less reactive as an allylating agent and lower in cost, and it does not introduce bromide into waste incineration or biological treatment streams. The product therefore occupies a narrow but persistent position in chlor-alkali derivative chains, feeding allyl alcohol, allylamine, epichlorohydrin, allyl-functional silanes, and pharmaceutical intermediates from a single low-molecular-weight olefinic chloride.
