| HS Code | |
| Productname | Hydrogen Peroxide |
| Chemicalformula | H2O2 |
| Casnumber | 7722-84-1 |
| Molecularweight | 34.0147 g/mol |
| Appearance | Colorless liquid |
| Odor | Slightly sharp, pungent |
| Density | 1.11 g/cm3 for 30% solution; 1.45 g/cm3 for 100% |
| Meltingpoint | -0.43 °C for 100% concentration |
| Boilingpoint | 150.2 °C for 100% concentration, decomposes |
| Solubility | Miscible with water |
| Ph | 4.5 to 6.0 for commercial aqueous solutions |
| Commonconcentrations | 3%, 6%, 30%, 35%, 50% |
| Decomposition | Decomposes into water and oxygen |
| Oxidizingproperties | Strong oxidizing agent |
| Storageconditions | Cool, dark, well-ventilated area away from incompatibles |
| Hazardclassification | Oxidizer; corrosive at high concentrations |
As an accredited Hydrogen Peroxide factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Hydrogen peroxide 35% solution in a 1 L opaque plastic bottle with vented cap, corrosive hazard labels, and safety warnings. |
| Container Loading (20′ FCL) | Loading Hydrogen Peroxide into 20′ FCL container under hazardous cargo rules, with vented packaging, compatible materials, and secure, stable stowage. |
| Shipping | Hydrogen peroxide is shipped as a hazardous oxidizing liquid under UN 2014 or UN 2015, depending on concentration. It requires compatible, vented containers and compliant packaging marked with oxidizer/corrosive labels. Transport must follow DOT, IMDG, and IATA rules; keep cool, segregate from combustibles, organics, and reducing agents, and document properly. |
| Storage | Store hydrogen peroxide in tightly closed, clearly labeled, vented containers made of compatible materials such as high-density polyethylene, glass, or PTFE. Keep in a cool, dry, dark, well-ventilated area away from heat, sunlight, and ignition sources. Separate from combustible, organic, reducing, alkaline, and metal-contaminated materials to prevent decomposition, pressure buildup, or violent reactions. Use secondary containment and follow the SDS. |
| Shelf Life | Hydrogen peroxide shelf life: typically 1–3 years if stored cool, dark, and sealed; heat, light, and contaminants accelerate decomposition. |
Hydrogen peroxide at 50% or 70% active content is metered into the post-refiner alkaline loop of thermomechanical pulp (TMP) and chemi-thermomechanical pulp (CTMP) lines where residual transition metals such as Fe, Mn, and Cu from wood chips would otherwise preferentially decompose the peroxide and generate chromophoric hydroxyl radicals. Sodium silicate at 1.5–3.0 kg/t dry fibre and diethylenetriaminepentaacetic acid (DTPA) at 0.2–0.5 kg/t dry fibre are dosed ahead of the peroxide injection point to establish a stabilised bleach liquor of pH 10.5–11.0. The peroxide charge itself typically ranges from 10–30 kg/t dry fibre, depending on initial chip brightness and the target ISO brightness increase of 10–18 points measured in accordance with ISO 2470-1:2016. Retention is carried out in high-consistency towers at 25–35% stock consistency for 60–120 minutes at 60–80 °C; insufficient stabilisation in this window raises bleach consumption by more than 30% because catalase and metal ions decompose peroxide before the chromophoric quinone groups in lignin are oxidised. Medium-consistency pumps fitted with vacuum de-aeration are standard on continuous lines because peroxide decomposition releases oxygen and can cause gas binding in centrifugal pump volutes. After bleaching, residual peroxide in the pulper feed is quenched with catalase before paper machine approach flow to prevent interference with wet-end retention aids. Brightness values above 80% ISO are rarely achieved on mechanical furnishes without sacrificing bulk and opacity. The bleached furnish then transfers to paper machines for newsprint, lightweight coated grades, and folding boxboard, where ISO brightness and yellowness index are the release parameters.
Prepared and desized cotton fabric is impregnated with a pad liquor containing 20–40 mL/L of 50% hydrogen peroxide, 5–10 g/L sodium hydroxide, and 2–5 g/L sodium silicate or a polyacrylate-based organic stabiliser. The saturated pick-up is set at 80–100% on a two-roll padder with a nip pressure of 2–4 bar; lower pick-up values produce edge-drying and non-uniform whiteness after the steamer. The fabric then enters a U-box or roller-bed steam chamber at 100–102 °C for 15–20 minutes, during which the perhydroxyl anion concentration controls bleaching kinetics and the stabiliser suppresses catalytic decomposition caused by Fe, Cu, and Mn present in cotton and process water. Whiteness is assessed by AATCC 110-2015 or ISO 105-J02:2012, and the process is typically specified to deliver a CIE whiteness index above 140 without reducing the degree of polymerisation below 1800–2000 units. Tensile strength loss above 15% relative to grey fabric triggers a reduction in alkali addition rather than peroxide addition because the alkali swells cellulose and accelerates oxidative chain scission at fibre surfaces. In cold pad-batch operations, the same formulation is batched onto a roll at 20–25 °C for 16–24 hours, but the stabiliser system shifts toward magnesium sulfate at 1–2 g/L and organic chelates because sodium silicate deposits on padder rollers over long dwell times. Knitted cotton goods are preferably processed in rope form on overflow dyeing machines at 98 °C for 30–45 minutes with 2–4% owf hydrogen peroxide, and the exhaust liquor is then neutralised with catalase to remove residual oxidant before dyeing with reactive dyes. The stabiliser system is screened against ZDHC MRSL and EU REACH Annex XVII; nonylphenol ethoxylate stabilisers are excluded because they form endocrine-active degradation products. Finished fabric enters downstream optical brightening, dyeing, or printing.
Hydrogen peroxide at 30–50 wt% is fed with propylene and a methanol recycle stream into a fixed-bed or slurry epoxidation reactor containing titanium silicalite-1 (TS-1) catalyst. Methanol constitutes 50–90 wt% of the liquid phase and is not inert; it solvates the peroxide and permits simultaneous access of propylene and hydrogen peroxide to the isolated tetrahedral Ti(IV) sites that generate the peroxy intermediate. Reaction temperature is held at 40–60 °C and pressure at 2.0–4.0 MPa to maintain propylene in the liquid phase. Under these conditions, hydrogen peroxide conversion exceeds 95% and propylene oxide selectivity can exceed 95%; water is the main co-product, and trace oxygen from peroxide decomposition is removed in a vapour-liquid separator. Feed purity determines catalyst deactivation rate: carry-over of alkali, amines, or phosphate esters neutralises the Ti(IV) active sites, and organic acids accelerate TS-1 framework dissolution. The methanol recycle stream is therefore maintained below 0.1 mg/kg sodium and below 0.5 mg/kg total chloride, with continuous purge of the water formed by the reaction to avoid stripping titanium from the catalyst. The propylene-to-peroxide molar feed ratio is held between 1.05:1 and 1.50:1; higher propylene excess suppresses ring-opening to propylene glycol, but excessive propylene raises off-gas compression load. Propylene oxide product is purified in a multi-column distillation train, and the resulting oxide is used for polyether polyols, propylene glycol ethers, and polyurethane intermediates. Compliance is normally verified against REACH Annex XVII and ISO 9001:2015 process control, with methanol and propylene oxide inventories handled under the storage and pressure-equipment requirements of Seveso III Directive 2012/18/EU where applicable.
In front-end semiconductor wafer processing, hydrogen peroxide serves as the oxidising component in both Standard Clean 1 (SC-1) and Standard Clean 2 (SC-2) chemistries. The SC-1 bath, used for particle removal and organic oxidation, is prepared from 29% ammonium hydroxide, 30% hydrogen peroxide, and ultrapure water in a volume ratio of 1:1:5, although ratios down to 1:4:20 are used for low-etch-budget processes on sensitive SiGe or strained-silicon surfaces. Temperature is controlled at 75–80 °C, and megasonic transducers operate at 0.8–1.2 MHz to avoid cavitation damage to sub-10 nm gate oxides. The SC-2 bath, typically 37% hydrochloric acid, 30% hydrogen peroxide, and ultrapure water at 1:1:6 by volume, removes metal cations by forming soluble chloro complexes. Electronic-grade hydrogen peroxide used in these baths is specified under SEMI C30 and is subject to lot-by-lot trace metal and particle certification. The liquid must be transferred through fluoropolymer-lined distribution systems because even stainless steel extractables introduce Fe, Ni, and Cr above the 0.001–0.01 mg/kg threshold required for front-of-line cleaning. Table 1 summarises a typical control window for a sub-7 nm logic fabrication facility against a general industrial 50% peroxide grade.
| Parameter | General industrial 50% | SEMI C30 electronic grade |
|---|---|---|
| H2O2 content | 49.0–51.0 wt% | 30.0–32.0 wt% |
| Residue after ignition | ≤ 50 mg/kg | ≤ 1 mg/kg |
| Iron (Fe) | ≤ 1 mg/kg | ≤ 0.005 mg/kg |
| Copper (Cu) | ≤ 0.1 mg/kg | ≤ 0.001 mg/kg |
| Particles ≥ 0.5 µm | ≤ 100 mL⁻¹ | ≤ 10 mL⁻¹ |
Metal contamination from an improper peroxide grade manifests as surface roughening and minority-carrier lifetime degradation, and lot acceptance is normally tied to total organic carbon below 5 mg/L and anionic impurities below 0.1 mg/kg because organic residues decompose under subsequent plasma etch and create micromasking defects. Equipment for SC-1/SC-2 recirculation is fabricated from quartz or perfluoroalkoxy alkane (PFA) and is fitted with point-of-use filtration at 0.1 µm; bath replacement frequency is calculated from particle counts and peroxide half-life, which falls sharply above 80 °C due to thermal decomposition. Terminal use includes pre-gate oxide cleans, post-etch residue removal, and wafer reclaim processes.
Fenton oxidation is applied to non-biodegradable COD in chemical, pharmaceutical, and textile effluents where the initial COD concentration lies between 1,000 mg/L and 10,000 mg/L. Hydrogen peroxide is dosed at 0.5–5.0 g/L, and ferrous sulfate heptahydrate is added at a molar Fe2+:H2O2 ratio of 1:2 to 1:5; lower ratios leave unused peroxide in the effluent, while higher ratios generate excessive Fe3+ sludge and consume hydroxyl radicals through the radical-scavenging side reaction. The pH is maintained at 2.8–3.5 by sulfuric acid before the reaction tank because Fe2+ precipitates above pH 4 and hydroxyl radical formation is suppressed. Reaction time in a continuous stirred-tank reactor is 30–120 minutes, with ORP maintained between 400 mV and 600 mV versus Ag/AgCl to avoid overdosing. After oxidation, the pH is raised to 8–9 with lime or sodium hydroxide to precipitate Fe(OH)3 and settle the resulting sludge. COD removal in this configuration typically reaches 60–85% as measured by ISO 6060:1989, but the exact endpoint depends on the proportion of recalcitrant organohalogen compounds and the H2O2:COD mass ratio. Table 2 gives process windows for three effluent classes.
| Effluent class | H2O2:COD mass ratio | Fe2+:H2O2 molar ratio | pH | COD reduction |
|---|---|---|---|---|
| Textile dyehouse mixed stream | 0.5–1.5 | 1:2–1:3 | 3.0–3.5 | 50–70% |
| Pharmaceutical process effluent | 1.0–2.5 | 1:3–1:5 | 2.8–3.2 | 60–80% |
| Landfill leachate membrane concentrate | 2.0–5.0 | 1:3–1:5 | 3.0–4.0 | 50–75% |
For weak-acid dissociable (WAD) cyanide destruction in gold leach tailings, hydrogen peroxide is dosed into agitated thickener overflow streams at pH 9.5–10.5 following copper sulfate addition at 10–30 mg/L Cu2+. The stoichiometric mass requirement for oxidation of cyanide to cyanate is 1.31 kg H2O2 per kg CN⁻, but plant dosing typically exceeds this by 20–100% because sulfides, thiocyanate, and transition metals in tailings compete for the peroxide. Retention time in a baffled reactor is 15–60 minutes; residual WAD cyanide is measured by ISO 14403-1:2012 and is usually specified below 10 mg/L before discharge to a tailings storage facility. Lime slurry is used to hold pH within the alkaline band, because below pH 9.0 hydrogen cyanide volatilisation risk increases sharply. Hydrogen peroxide also finds use in uranium ore leaching as an oxidant in acid circuits, but the reaction with pyrite-bearing ores can generate excessive sulfate and heat, so the feed rate is trimmed against redox potential and pulp temperature. In silver and gold cyanidation, low-level peroxide dosing at 0.1–0.5 kg/t ore can supplement dissolved oxygen in oxygen-limited thickener pulps; published data for this specific configuration is limited, and site-specific jar leach tests are required before full-scale adoption. Terminal outputs are tailings compliant with local cyanide discharge limits and, in the uranium case, clarified uranyl sulfate pregnant leach solution.
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Hydrogen peroxide (H2O2, CAS 7722-84-1, molecular weight 34.014 g/mol) is supplied as a clear, odourless aqueous solution with oxidising capacity determined by concentration. Commercial liquid product ranges from 3% topical solution to 70% high-test peroxide for propellant and aerospace use. A 35% solution has a density of 1.13 g/cm³ at 20°C and approximately 16.5% active oxygen, while a 50% solution carries 23.5% active oxygen. The decomposition reaction is exothermic with an enthalpy change of about -98.2 kJ/mol and is accelerated by pH above 4–5, temperatures above 50°C, transition-metal contamination, catalase, and rough surfaces. Technical grades are stabilised to limit annual absolute decomposition to less than 1% under ambient storage; electronic grades are often unstabilised or stabilised with volatile agents so that no involuntary residue remains on device surfaces. Commercial designations are not defined by a single model number but by concentration, stabiliser chemistry, and residue class: 35% technical, 50% high-strength, 60% chemical/intermediate, and 70% high-test peroxide. Specification sheets report concentration by permanganate titration, residue on evaporation, acidity as sulfuric acid, and trace-metal content by inductively coupled plasma mass spectrometry.
Stabiliser chemistry governs downstream compatibility. Technical and food-contact grades commonly use sodium stannate, phosphonate, or colloidal stannate packages at concentrations below 50 mg/L as tin, maintaining pH between 2.5 and 4.0 to slow autodecomposition. The stabiliser functions by sequestering trace iron and copper and by coating suspended particles. However, stannate residues can foul cation-exchange columns and reverse-osmosis membranes; cleaning cycles with mineral acid are then required. For semiconductor cleaning, stabilised solutions are generally avoided because tin or sodium residues remain on wafer surfaces after drying. High-purity grades conforming to SEMI C30 are therefore supplied at 30–32% with total trace-metal reporting at ppb levels and negligible residue on evaporation, but they require dedicated stainless-steel or passivated aluminum storage and cooling to avoid pressure build-up. In pharmaceutical topical solution, the concentration window is 2.5–3.5 g/100 mL and residue on evaporation is controlled by the relevant pharmacopoeial monograph. Published data for specific stabiliser-blend effects on membrane fouling in high-purity water systems is limited; therefore compatibility tests are required before switching grades.
| Grade | Concentration | Stabiliser system | Critical specification | Typical use |
|---|---|---|---|---|
| Topical solution | 2.5–3.5% w/v | Sodium stannate or nitrate | Residue on evaporation ≤ 0.05% | Antisepsis |
| Technical | 35%, 50% | Stannate, phosphonate, colloidal tin | Annual decomposition < 1% absolute | Bleaching, wastewater oxidation |
| Food chemical codex | 30–50% | Stannate or pyrophosphate | Heavy metals per FCC monograph | Aseptic packaging |
| Semiconductor | 30–32% | Unstabilised or volatile | Trace metals per SEMI C30 | RCA clean |
In cotton knitted-fabric preparation, hydrogen peroxide is applied in alkaline pad-steam and cold pad-batch processes. Pad-steam bleaching runs at 90–98°C for 15–20 min with 20–35 mL/kg of 35% solution and sodium silicate or peroxide stabiliser at pH 10.5–11.5; cold pad-batch bleaching uses 20–30°C dwell for 12–24 h at higher alkali concentration. The peroxide bath is not a direct model-numbered formulation but is dosed by fabric weight and desired whiteness index, measured as CIE WI per AATCC 110. Replacement of sodium hypochlorite with hydrogen peroxide removes chlorinated organic by-products that are monitored as adsorbable organic halogen under ISO 9562, and it avoids the pH shock and fabric yellowing associated with chlorine residual. In denim applications, the same product can be used for oxidative sulphur removal after sulphur dyeing, but published data for specific garment processing lines is limited and trials are required to set the bath concentration.
In front-end semiconductor cleaning, aqueous H₂O₂ is combined with ammonium hydroxide or hydrochloric acid in SC1 and SC2 baths. The SC1 bath, typically a mixture of 1 part 30% H₂O₂ to 1 part NH₄OH to 5 parts deionised water, operates at 65–80°C and removes organic residues and particles by simultaneous oxidation and undercutting; SC2 uses HCl/H₂O₂/water at 65–80°C to complex metal contamination. Bath life is governed by peroxide concentration decay and by dissolved silica and metal accumulation. Unstabilised SEMI C30 peroxide is preferred because tin or sodium residues from technical grades create defects after drying. Metallic contamination is verified by vapor phase decomposition inductively coupled plasma mass spectrometry, with target metal surface concentrations often specified at or below 1×10¹⁰ atoms/cm² for critical front-end surfaces. Bath replacement is required when peroxide concentration falls below 50% of initial value or when particle counts exceed tool threshold. The SC1 bath is volatile and requires exhaust of ammonia; its cleaning window narrows as bath age increases because the peroxide concentration and pH drift simultaneously.
Aseptic packaging lines use 30–35% hydrogen peroxide in bath or spray form to sterilise laminate surfaces. The rate-determining factor is not only concentration but also temperature and contact time; a reference temperature of 70°C with contact of 6–10 s is typical for carton sterilisation, but microbial reduction data must be collected for each packaging material. The process relies on removal of peroxide residual by hot air because residual levels are regulated under food-contact sanitising provisions. Compliance is documented under 21 CFR 178.1005 for the sanitising solution and aseptic filling machine validation under ISO 13408-1. Catalase contamination from dairy or fruit residues shortens bath life; stainless-steel surfaces above 70°C can promote decomposition, and storage tanks must be vented. Substitution of peracetic acid with hydrogen peroxide changes the residue profile to water and oxygen but may require higher temperature or longer contact to reach the same sporicidal log reduction, depending on the packaging material.
Vaporized hydrogen peroxide is used for room biodecontamination at 30–35% liquid feed concentration, with vapor injection controlled by dew-point margin rather than fixed concentration. Cycle development typically targets 250–500 ppm vapour concentration, relative humidity below 80%, and a dew-point margin of 2–5°C to prevent condensation. Dwell time is chosen to achieve 6-log sporicidal reduction using biological indicators of Geobacillus stearothermophilus with a population of 10⁶ spores per carrier. Cycle validation is performed per ISO 14937 or relevant national biodecontamination standards. The vapour is not interchangeable with liquid peracetic acid because it decomposes to water and oxygen, leaving no measurable residue if aeration is complete. Enclosure compatibility requires evaluation of polycarbonate, acrylic, and electronic components because vapour condensation at the dew point can accelerate oxidative degradation of polymers.
| Parameter | Hydrogen peroxide | Sodium hypochlorite | Peracetic acid | Chlorine dioxide |
|---|---|---|---|---|
| Oxidation potential | 1.78 V | 1.49 V | 1.81 V | 1.57 V |
| Common liquid concentration | 35%, 50% | 10–15% available chlorine | 5%, 15% equilibrium mixture | 0.3–0.8% generated on-site |
| Principal residue | Water, oxygen | Chloride, chlorate, chlorinated organics | Acetic acid, oxygen | Chlorite, chlorate |
| Typical pH efficacy window | 2–11 | 6–9 | 5–7 | 2–10 |
| Storage stability | Annual loss < 1% stabilised | Degrades with temperature and light | Equilibrium mixture shifts with dilution | Generated on demand |
In municipal wastewater collection, hydrogen peroxide is injected upstream of sulfide-generating zones to oxidise dissolved sulfide and maintain aerobic biofilm conditions. The stoichiometric requirement for elemental sulfur formation is 1 mol H₂O₂ per mol sulfide; full oxidation to sulfate consumes 4 mol H₂O₂ per mol sulfide. Field dosing in force mains typically begins at 1.5–3.0 kg of 35% solution per kg of dissolved sulfide, adjusted by oxidation-reduction potential and downstream sulfide residual. The product differs from sodium hypochlorite in that it does not raise total dissolved chloride or introduce chlorate, but it is less effective when catalase activity is high because biological degradation consumes the peroxide before it reaches the sulfide. Published data for specific force-main sulfide loads is limited; consequently, dose confirmation is performed with temporary metering and in-line sulfide analysers.
For drinking-water treatment, product conforming to EN 902 is used at doses typically below 10 mg/L as H₂O₂ for oxidation of iron, manganese, or taste-and-odour compounds before sand filtration. The peroxide is then removed by residual breakdown or catalytic granular activated carbon; residual must be below detection at the point of distribution. This application is incompatible with raw water containing high peroxide demand from organic matter because oxidation competition can exhaust the dose before target compounds are removed.
In chemical pulp brightening, hydrogen peroxide is added to alkaline extraction stages or final bleaching towers at 50–90°C and pH 10.5–11.5. The product is usually charged at 5–20 kg/t of 100% peroxide depending on kappa factor and brightness target, often in combination with oxygen or chlorine dioxide. Peroxide bleaching is most effective on mechanical pulp and recycled fibre where chlorine dioxide is not required; the oxidant acts on carbonyl and quinoid chromophores without generating chlorinated phenols. High residual stabiliser in technical-grade product can contribute to scale in downstream evaporators, so pulp mills frequently specify low-residue grades or use stabiliser-free product with short on-site storage.
Hydrogen peroxide is used as the terminal oxidant in the hydrogen peroxide to propylene oxide process, where propylene is epoxidised over a titanium silicalite-1 catalyst in methanol solvent. The reaction operates at relatively low temperature, typically 40–60°C, and moderate pressure, with peroxide conversion above 95% to limit by-product propane diol and oxygen. The process consumes 0.62–0.65 kg of 100% hydrogen peroxide equivalent per kg of propylene oxide produced, depending on catalyst selectivity and methanol recycle quality. The main operational boundaries are the presence of residual stabiliser metals, which can reduce TS-1 catalyst life, and the concentration of water in the recycle loop, which must be controlled to prevent catalyst deactivation. The same chemistry is distinct from chlorohydrin or co-product propylene oxide routes because no chlorinated intermediate is formed and no co-product styrene monomer is required.
Storage of 50% and 70% hydrogen peroxide requires pressure-relief devices sized for the maximum oxygen evolution rate at decomposition onset. Tanks and piping are usually passivated 316L stainless steel or high-density polyethylene; carbon steel is unsuitable unless specifically lined and passivated. Decomposition onset may occur at solution temperatures above 60–70°C in unvented tanks. Published data for long-term high-test peroxide storage in partially passivated carbon steel is limited; each installation requires vent sizing based on supplier adiabatic calorimetry data. The product must be kept away from reducing agents, alkalis, and transition-metal salts because rapid decomposition can generate pressure and heat.
