| HS Code | 154183 |
| Product Name | Caustic Soda 10KG Bucket |
| Chemical Name | Sodium Hydroxide |
| Chemical Formula | NaOH |
| Cas Number | 1310-73-2 |
| Molecular Weight | 40.00 g/mol |
| Physical State | Solid (pearls/flakes/prills) |
| Appearance | White translucent solid, hygroscopic |
| Odor | Odorless |
| Purity | >= 98% (typical industrial grade) |
| Net Weight Per Bucket | 10 kg |
| Packaging | Plastic bucket with lid |
| Solubility In Water | Soluble; exothermic reaction |
| Melting Point | 318 °C (604 °F) |
| Boiling Point | 1388 °C (2530 °F) |
| Density | 2.13 g/cm³ at 25 °C |
| Ph Of 1 Percent Solution | Approximately 13 |
| Storage Conditions | Keep in airtight container in cool, dry, ventilated area; away from acids and moisture |
| Hazard Classification | Corrosive; causes severe burns (UN 1823, Class 8) |
As an accredited Caustic Soda 10KG Bucket factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | One 10 kg bucket of caustic soda, securely sealed, with hazard labeling and moisture-resistant packaging for safe handling and storage. |
| Container Loading (20′ FCL) | 20′ FCL: Caustic soda 10kg buckets palletized, shrink-wrapped, securely stacked, moisture-proof, labeled corrosive, loaded in ventilated container. |
| Shipping | Caustic soda is a corrosive, hazardous chemical. Shipments require UN1823 classification, rigid HDPE drums with secure lids, and upright, palletized loading. Only licensed carriers handling dangerous goods may transport it. Ground transport is standard; air and sea options are restricted. Proper labeling and documentation are mandatory to ensure safe, compliant delivery. |
| Storage | Store the 10 kg caustic soda bucket in a cool, dry, well-ventilated area away from direct sunlight, moisture, and incompatible substances like acids. Keep the lid tightly sealed when not in use, and place the bucket on a sturdy, impermeable secondary containment pallet to prevent floor contact and contain any leaks. Avoid storing near aluminum or magnesium materials. |
| Shelf Life | Shelf life: 2 years from manufacture when stored unopened in a cool, dry place. Keep bucket sealed to prevent moisture absorption. |
Clean-in-place circuit charge tanks on dairy and brewery lines are charged with sodium hydroxide solution at 0.8–1.5 wt% prepared by metering a 10 kg high-density polyethylene pail into 1,000–1,250 L of softened water at 60–80 °C. Batch-to-batch variation in caustic strength is reduced by platform-scale weighing to ±0.05 kg and by free-alkalinity titration against phenolphthalein before circulation. For compliance, sodium hydroxide used in food contact operations is covered by 21 CFR 184.1763 as a GRAS direct food substance under good manufacturing practice, and the cleaning system is validated under ISO 22000:2018 prerequisite programmes. The caustic working solution is circulated through spray balls at 1.5–2.5 m/s for 15–30 min after a pre-rinse removes loose soil; the terminal process sequence includes intermediate rinse, acid wash with 0.5–1.0 wt% phosphoric or nitric acid, final potable-water rinse verified by conductivity, and sanitizer injection. Terminal finished product types include pasteurized milk, fermented dairy products, packaged beer, and carbonated soft drinks produced on the cleaned stainless steel lines. Caustic CIP is not applied to aluminum wetted parts because alkaline attack at 60 °C produces hydrogen and surface etching.
Neutralization of acidic industrial effluent in 1,000–5,000 L batch tanks is controlled by a 10 wt% sodium hydroxide solution dosed through a peristaltic or diaphragm metering pump and regulated by a glass combination pH electrode with automatic temperature compensation mounted downstream of a static mixer; the pH controller dead band is typically set at ±0.2 pH to prevent overshoot above the NPDES upper limit of 9.0. Oily or scaling effluent can foul the pH probe and delay response by 20–60 s, so insertion probes are fitted with jet-wash or ultrasonic cleaning heads on continuous discharge lines. Compliance monitoring uses ISO 10523:2008 and ASTM D1293-18 for pH determination, with discharge limits typically 6.0–9.0 for publicly owned treatment works acceptance. The formulation addition ratio is determined by titration of the raw effluent rather than by fixed weight; strong mineral acid wastes may require 0.15–0.30 g/L NaOH per pH unit of correction, while bicarbonate-buffered streams consume 0.05–0.10 g/L per pH unit because of the carbonic acid equilibrium breakpoint near pH 8.3. The downstream production process consists of waste collection, screening, batch neutralization with recirculation for 10–30 min, flocculation, settling, and decanting. Terminal finished output types are acceptable discharge water, reused scrubber water, and neutralized filter backwash. Exothermic dilution of solid caustic must be controlled by adding sodium hydroxide to water, not water to solid, and dilution beyond 25 wt% can raise local temperature above 80 °C if mixing is inadequate.
On architectural aluminum anodizing lines, the etch bath is operated at 50–70 g/L free sodium hydroxide and 50–65 °C to produce a matte finish on 6063-T5 and 6060-T5 extrusions before anodizing. Dissolved aluminum concentration is the primary bath-life variable: below 30 g/L, etch rate is high but differential attack on grain boundaries may appear in 6060 alloys; above 60–75 g/L, etch rate declines and surface roughness decreases, requiring either bath decanting or caustic replenishment. The formulation addition ratio for make-up is 5–7 kg sodium hydroxide per 100 L deionized water to establish a 50–70 g/L free-alkali bath, with 10 kg bucket inventory used for weekly line replenishment. The downstream processing sequence includes alkaline degreasing, etching, double counterflow rinse, desmut in 20–30 vol% nitric acid or 10–20 wt% sulfuric acid, then anodizing in 180–200 g/L sulfuric acid at 15–20 °C and 1.4–1.6 A/dm². Agitated immersion racks with air sparging at 0.2–0.5 L/min/m² prevent gas boundary-layer etching variation in deep channels. Compliance is governed by ISO 7599:2018 for general specifications for anodic oxidation coatings and ASTM B137-95(2014) for coating mass measurement, with military or aerospace work commonly referencing MIL-A-8625F Type II. Terminal finished product types are anodized curtain-wall profiles, heat sinks, automotive trim, and electronic enclosures. The operational boundary is the accumulation of dissolved aluminum: once the aluminum-to-caustic ratio exceeds 1.0 by weight, matte uniformity in blind holes and deep channels deteriorates, and smut removal becomes incomplete in the subsequent desmut stage.
Cold-process soap production using 10 kg sodium hydroxide pails requires lye concentration to be calculated from the saponification value of each oil phase rather than a single fixed dosage; for coconut oil with a saponification value of 256 mg KOH/g, the stoichiometric sodium hydroxide demand is 0.183 g NaOH/g oil, and a 5% superfat discount reduces the actual addition to 0.174 g NaOH/g oil. Variable oil composition must be tracked because a shift in saponification value of 10 mg KOH/g changes the caustic charge by approximately 0.7% of oil mass. The saponification value is determined in accordance with ISO 3657:2020, and finished soap quality is assessed by total alkali and free caustic alkalinity methods under ISO 685:2020. In semi-boiled or cold-process production, the oil phase is warmed to 38–45 °C, the lye solution is cooled to 40–45 °C, and the two phases are combined under a high-shear stick blender at 3,000–5,000 rpm until stable trace is reached at 40–50 °C. The batch is then poured into wooden or silicone molds, allowed to pass through gel phase at 50–65 °C, and cured for 4–6 weeks to reduce free caustic and water content. Terminal finished product types are cold-process toilet soap bars, shaving soap pucks, and laundry bar soap bases. Limitations include the exothermic nature of alkoxide formation and the incompatibility of hot sodium hydroxide with aluminum equipment; mixing vessels and molds must be 304 or 316 stainless steel, high-density polyethylene, or silicone-lined wood.
In cold-process cosmetic manufacturing, a 10 kg bucket of sodium hydroxide is diluted to an 18 wt% stock solution and metered into aqueous carbomer dispersions to trigger neutralization and gel network formation. The addition ratio is formula-specific but commonly falls at 0.10–0.50 wt% of the diluted lye solution relative to total batch weight, targeting a final pH of 5.5–6.5 for skin-contact gels and 6.5–7.0 for hair-styling formulations. The downstream production process requires dispersing carbomer at 800–1,200 rpm with a Cowles-blade mixer to avoid aeration, then reducing shear to 300–500 rpm before slow lye addition; viscosity build is observed on a Brookfield RVT viscometer using spindle 7 at 20 rpm, with plateau values commonly in the range of 15,000–30,000 mPa·s. Air entrainment from high-speed dispersion creates microvoids that reduce yield stress and clarity in transparent gel systems. Compliance is anchored to ISO 22716:2007 Good Manufacturing Practices for cosmetics and EC 1223/2009 for finished product safety, with sodium hydroxide used as a pH adjuster within the limits established by the cosmetic product safety report. Terminal finished product types include hair-styling gels, moisturizing gels, pre-shave gels, and hydroalcoholic hand sanitizers. The operational boundary is pH overshoot: above pH 7.5, many carbomer grades undergo viscosity collapse, and re-acidification does not fully restore the original rheological profile.
Small drinking-water and wastewater treatment plants producing sodium hypochlorite on-site from chlorine gas and sodium hydroxide from 10 kg pails operate under a vacuum eductor so that chlorine gas pressure remains below atmospheric; the caustic feed is prepared at 25–30 wt% NaOH and reacted in a packed absorption column to produce sodium hypochlorite with an available chlorine content of 120–150 g/L. The formulation addition ratio is fixed by stoichiometry, with 2 mol NaOH consumed per 1 mol Cl2; a residual excess of 5–10 g/L free sodium hydroxide is maintained to hold product pH at 12.5–13.0 and suppress hypochlorous acid decomposition. Compliance is specified by AWWA B300-18 for hypochlorites and NSF/ANSI/CAN 60 for drinking-water treatment chemicals, with analytical control by iodometric titration for available chlorine. The downstream production process includes gas diffusion, cooling to 15–25 °C, product storage in high-density polyethylene tanks, and metering into treatment streams; chlorate formation is controlled by avoiding temperatures above 30 °C and by maintaining pH above 12 during storage. Vacuum eductor failure can allow chlorine gas breakthrough, so gas detectors with a 0.5 ppm alarm setpoint are interlocked with caustic feed shutoff and ventilation. Terminal finished product types are potable-water disinfection chemical, cooling-tower biocide, and municipal wastewater chlorination product. The process is not suitable for use with ammonia-containing streams without breakpoint chlorination control, and sodium hypochlorite must never be mixed with acid cleaners due to rapid chlorine gas release.
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Caustic Soda 10KG Bucket is a packaged solid sodium hydroxide product in which the active species, NaOH, is furnished as white pearls, granules, or flakes with a net fill of 10 kg. The material is identified by CAS 1310-73-2 and EC 215-185-5, with transport classification UN 1823, Class 8, Packing Group II. The pail is typically an HDPE open-head container marked to UN 1H2 for removable-head plastics drums or pails used in solid corrosive service. Model or catalog designation is supplier-specific; when a formal part number is not printed, the pail label must at minimum identify the grade as solid sodium hydroxide, 10 kg net, UN 1823, and the fill-lot number. A lot-specific certificate of analysis is required to confirm assay, carbonate content, chloride content, and trace-metal profile for the intended application.
| Parameter | Typical value or limit | Test method or standard |
|---|---|---|
| Sodium hydroxide as NaOH | 98.5–99.5% by mass | ISO 979 |
| Sodium carbonate as Na₂CO₃ | ≤0.5% by mass | ISO 3196 |
| Sodium chloride as NaCl | ≤0.03% by mass | ISO 3194 |
The remaining mass balance consists principally of water, sulfate, and trace metal oxides. Carbonate and chloride are reported separately because they govern precipitation behavior and corrosion risk in closed-loop alkaline baths. Product supplied as membrane-grade solid may show lower carbonate and chloride values on the certificate of analysis. Industrial pail stock is not automatically food-grade; use in food-contact applications requires explicit certification under 21 CFR 184.1763 or the applicable regional food-additive regulation.
Solid sodium hydroxide is both hygroscopic and carbon dioxide-sensitive. The carbonation reaction proceeds as 2 NaOH + CO₂ → Na₂CO₃ + H₂O; surface crusting after opening is therefore not merely moisture uptake but chemical conversion that reduces free causticity per unit mass. When product is withdrawn repeatedly with a scoop, the geometric surface area available for CO₂ exchange is determined by the opening diameter and the remaining solids depth. A resealable 10 kg bucket controls this exchange more effectively than a 25 kg multi-wall paper or woven sack, which often cannot be closed hermetically after sampling. In production areas exceeding 70% RH, open transfer should be limited to a single shift unless dry-air purge or nitrogen blanketing is available.
| Form and package | Active NaOH per unit | Post-opening moisture and CO₂ control | Minimum handling equipment | Cold-storage boundary |
|---|---|---|---|---|
| 10 kg HDPE bucket solid | 10 kg | gasketed lid, resealable | scoop, eductor, or dedicated dissolving tank | solid does not freeze down to 0°C |
| 25 kg sack solid | 25 kg | limited after opening | hoist or manual charge; charge mass may exceed single-shift use | solid does not freeze down to 0°C |
| 50% liquid membrane-grade solution | 0.5 kg NaOH per kg solution | closed coupling, minimal carbonation | pump, storage tank, heat tracing if ambient is below freezing point | crystallizes near 12°C for 50% grade |
The choice between solid bucket, sack, and liquid is controlled by consumption rate, water availability for dilution, and plant utility support. A 10 kg bucket is frequently selected for pilot-scale pH neutralization, small wastewater batch treatment, and compact CIP skids where the thermal load of dissolution can be managed by controlled addition or external cooling. Bulk liquid supply eliminates the dissolution step but introduces freeze protection and pump maintenance requirements.
Acid neutralization consumes this product in direct stoichiometric proportion to acidic species. For hydrochloric acid, 40.00 g NaOH neutralizes 36.46 g HCl; for sulfuric acid, 80.00 g NaOH neutralizes 98.08 g H₂SO₄. In a 1,000 L rinse-water tank containing 0.5 mol L⁻¹ HCl, the theoretical NaOH charge is 20.0 kg, or two full buckets. Actual dosing is undertaken as a dilute 10–20% solution, with final pH controlled by a pH controller operating within a neutralization band of pH 6.5–8.5 depending on discharge permits. A 0.1 mol L⁻¹ NaOH solution has a pH of approximately 13 at 25°C.
The principal processing conflict arises from the heat of solution. The enthalpy of solution at infinite dilution is approximately −44.5 kJ mol⁻¹. A 10 kg charge added to 100 L of water at 20°C produces a nominal 10 wt% solution and an adiabatic temperature rise of roughly 25–30°C; actual temperature is lower because of tank-wall losses and ambient convection. In water volumes below 50 L per bucket, the same charge can approach the atmospheric boiling point at the solid-liquid interface. Therefore, partial bucket charges or active cooling are required for small dissolution vessels. The product must be added to water, never water to the solid charge, because localized hydration can form a concentrated alkaline film that may boil and splash.
Immersion stripping of organic coatings and cleaned-in-place processing of stainless steel tanks often maintain NaOH concentrations between 0.5 and 2.0 wt% at 60–85°C. A 10 kg bucket added to a 500 L bath provides a nominal 2.0 wt% caustic concentration; the same bath requires only 2.5 kg for a 0.5 wt% working solution, so partial bucket use is usually unavoidable. In these operations, a bucket format is easier to reseal and store than a partially used sack, reducing the formation of carbonate crust at the top of the solids. Aluminum and zinc components are not compatible with these solutions; aluminum dissolution is exothermic and generates hydrogen at a ratio of 3 mol H₂ per 2 mol Al. Hydrogen evolution must be controlled by ventilation to maintain concentration below the lower flammable limit of 4 vol%.
Dissolution equipment should be constructed of carbon steel, stainless steel, or compatible polymer-lined vessels. For repeat small-batch preparation, a dedicated dissolution tank with a bottom drain and top-mounted eductor is used; the eductor return line should remain submerged to reduce aerosol formation. Low-speed agitation sufficient to disengage solids from the eductor loop is preferable to high-shear mixing, which increases mist release. Transfer lines and centrifugal pumps should be fitted with mechanical seals compatible with strong bases; EPDM and PTFE are generally selected for seal components in caustic service.
Compared with potassium hydroxide, sodium hydroxide has a lower molar mass of 40.00 g mol⁻¹ versus 56.11 g mol⁻¹, giving higher acid-neutralizing capacity per unit mass. Sodium hydroxide is therefore preferred for large-volume neutralization and general alkaline cleaning, while potassium hydroxide may be selected when higher solution solubility or potassium-based reaction products are required. This distinction is material when a formulated salt is desired from the neutralization reaction.
Unopened pails should be stored indoors at 5–35°C and below 60% RH, with the lid closure tight and the pail upright. Although the solid does not crystallize or freeze, the pail gasket and closure may lose flexibility at low temperatures, and condensation inside the headspace increases when a cold pail is moved into a warm, humid loading area. The headspace should be flushed with dry air or nitrogen after each opening when storage extends beyond 24 h. Moisture uptake is not a simple shelf-life endpoint; it increases carbonate formation and decreases free NaOH assay. Published long-term moisture-ingress data for partially used HDPE pails under cyclic warehouse humidity are limited; conservative stock rotation is therefore applied. Material held more than 24 months in an opened pail should be re-qualified by the same quality-control method referenced on the certificate of analysis.
Do not store or handle the bucket near concentrated acids, halogenated solvents, chlorinating agents, ammonium salts, or amphoteric metals. Mixing with acids is strongly exothermic and may produce violent boiling. Contact with aluminum, zinc, tin, or galvanized surfaces generates hydrogen gas. The NFPA 704 rating commonly assigned to solid sodium hydroxide is Health 3, Flammability 0, Instability 1, with an ALK corrosive note. Personnel handling the product should use corrosion-resistant gloves, face shielding, and protective clothing selected under the site PPE risk assessment.
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