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| HS Code | 294200 |
| Chemical Name | Sodium formate |
| Chemical Formula | HCOONa |
| Molecular Weight | 68.007 g/mol |
| Cas Number | 141-53-7 |
| Appearance | White crystalline powder or granules |
| Odor | Slight odor of formic acid |
| Density | 1.92 g/cm³ at 20 °C |
| Melting Point | 253 °C |
| Boiling Point | Decomposes above 253 °C |
| Solubility In Water | 97.2 g/100 mL at 20 °C |
| Solubility In Ethanol | Slightly soluble |
| Ph Of Aqueous Solution | 7 to 8 for a 1% solution |
As an accredited Sodium Formate factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | 25 kg sealed polyethylene-lined woven bags, moisture-proof, labeled with chemical name, hazard information, and handling precautions. |
| Container Loading (20′ FCL) | 20′ FCL container loading of sodium formate: packed in sealed bags on pallets, secured to prevent shifting, ensuring safe, stable transport. |
| Shipping | Sodium formate ships as a non-dangerous dry chemical in sealed polyethylene-lined bags or fiber drums. Protect from moisture and incompatible acids. Pack on pallets, secure, and store in dry conditions. Transport is not typically regulated under IMDG/ADR/IATA when kept free of hazardous impurities. |
| Storage | Store sodium formate in a tightly sealed container in a cool, dry, well-ventilated area. Protect from moisture, humidity, and direct sunlight to prevent caking or degradation. Keep away from strong acids, oxidizers, and incompatible materials. Clearly label the container, and ensure storage conditions comply with local chemical safety regulations. |
| Shelf Life | Sodium formate typically has a shelf life of two years when stored in a cool, dry, tightly sealed container. |
Solid granular sodium formate is applied to runway and taxiway ice surfaces where chloride-free de-icing and anti-icing is required to limit corrosion on aircraft aluminium alloys and high-tensile steel undercarriage components. In qualification testing under SAE AMS 1431, the granular product is assessed for ice-melt capacity, particle size distribution, and corrosion mass loss on standard aerospace metals. Operational spread rates used on aerodrome pavements typically fall within 15–45 g/m² for frost and 60–120 g/m² for compacted ice, with final rates adjusted using runway friction data collected according to FAA AC 150/5200-30C. The production process for the terminal de-icing product consists of spray-drying or fluid-bed compaction of sodium formate liquor, screening to a nominal top size of 1.0–3.35 mm, and blending with anticaking additives at 0.2–0.5 wt%. Terminal product types include runway de-icing pellets, apron anti-icing powder, and packaged solid de-icer to be diluted on-site by mobile brine-making units. Published production-scale data on optimum spread rates for sodium formate at extremely low temperatures, specifically below −12°C, are limited because the melting rate becomes slower than acetate-based liquid systems under wind-chill conditions on exposed taxiway shoulders.
Reservoir drill-in and completion operations use sodium formate brine as a chloride-free monovalent base fluid for pay-zone exposure where formation clay stabilisation and solids-free behaviour are required. The brine is prepared by dissolving dry sodium formate in filtered fresh water at weight fractions between 25 wt% and 45 wt%, yielding specific gravities from 1.16 to 1.33 at 20°C. Density is measured with a pressurised mud balance in accordance with API RP 13J and ISO 13503-3:2005, while crystallisation temperature is determined on a thermostatically controlled test cell before the brine is transferred to bulk mixing tanks. The production sequence at a shore-based brine plant includes high-shear mixing, addition of an oxygen scavenger at 50–150 ppm, filtration through 1–5 µm cartridge elements, and final density trim using a second mud balance. Terminal uses include low-solids drill-in fluid for horizontal wellbores, completion brine for sand-screen placement, and packer fluid in monovalent-compatible reservoirs. The principal process conflict occurs when the operator requests a density above 1.30 g/cm³ while ambient storage temperature falls below 10°C; under those conditions, sodium formate brines can approach saturation, and published data on pipe-rheology stability after repeated cooling cycles are limited. Barium or calcium salts must not be introduced because precipitation of barium sulfate and calcium formate scaling at brine-mixing points has been observed in field batch records.
Cattle hide processing introduces sodium formate after acidification with sulfuric acid and formic acid in the pickle stage, where it functions as a buffering and masking adjunct before chrome tanning. A typical dose is 0.3–0.8 wt% based on wet pelt weight, added before chromium sulfate powder at 0.25–0.40 wt% chrome oxide equivalent. The production step takes place in a stainless steel drum rotating at 12–16 rpm for 45–90 min; the liquor pH is controlled between 2.8 and 3.2 before basification begins. Sodium formate forms formate-chromium complexes that moderate the rate of chromium uptake during basification, allowing final pH in the 3.8–4.0 range without precipitation of chromium hydroxide on grain surfaces. Process liquor pH is verified by ISO 4045:2018, and chromic oxide content in the resulting wet-blue is determined by ISO 5398-1:2018. Terminal product types include shoe-upper wet-blue, automotive upholstery leather, and split leather for low-fogging interior panels. At doses above 1.0 wt% of pelt weight, the buffering action may slow basification excessively, and published production guidance warns against combination with bicarbonate-based basifying agents in a single addition because the local pH shift at the drum surface can trigger grain-pipe abrasion on thin belly areas.
Sodium formate is incorporated into concrete as a chloride-free hardening accelerator, particularly where calcium chloride is prohibited due to reinforcement corrosion risk or where galvanised steel embedments are present. The addition ratio is typically 0.5–2.0% by mass of cement; workability-adjusted plant trials are conducted in accordance with ASTM C494/C494M Type C and EN 934-2:2009 Table 2, with setting-time verification by ASTM C191 and compressive strength development by ASTM C39. The production process for precast concrete involves dry blending sodium formate with cement or adding it as a pre-dissolved solution at the batching plant, followed by mould filling, vibration compaction at 0.1–0.3 mm displacement amplitude, and steam curing at 50–60°C for 6–10 h. Terminal product types include reinforced manholes, hollow-core slabs, concrete pipes, and precast tunnel segments. The critical limit is the dosage band: addition above 3.0% by cement mass can increase the heat of early hydration and may lead to later-age strength inversion in certain ordinary portland cement blends. Published data for sodium formate-modified calcium sulfoaluminate cement systems are limited, and plant trials with sulfate-resistant cement are mandatory before use in hot-weather precast operations where formwork stripping is scheduled at 12–16 h after casting.
Dry sodium formate is fed into a heated acidulation reactor with concentrated sulfuric acid at a molar ratio of 0.50–0.55 mol H₂SO₄ per mol HCOONa. The reaction mass is held under vacuum at 80–110°C while formic acid vapour is condensed in a glass-lined heat exchanger; the residual sodium sulfate cake is discharged from the reactor bottom and dried as a co-product. Compliance for the synthesis plant is handled under REACH (EC) No 1907/2006, and the 85–95 wt% formic acid stream is tested for purity by oxidation-reduction titration and total sulfate residue before transfer to storage. Terminal products include formic acid solutions for leather pickling, descaler formulations, silage preservatives, and rubber coagulation latex auxiliaries. The critical operational boundary is reactor material selection: sodium formate acidulation generates formic acid vapour and sulfuric acid mist, so stainless steel 316L evaporator internals without a glass lining are not recommended where moisture content in the sodium formate feed exceeds 1.0 wt% because accelerated pitting has been recorded in maintenance logs. Published heat-load data for continuous acidulation of moist sodium formate are limited, and batch reactor suppliers typically size heating surfaces based on a heat-transfer coefficient of 250–350 W/m²·K under vacuum.
Textile and paper reducing-agent manufacture consumes sodium formate as the reducing feedstock in alkaline sulfur dioxide absorption to produce sodium dithionite. The theoretical stoichiometric consumption is 0.390 kg sodium formate per kg of sodium dithionite; industrial liquid-phase processes run with excess sulfur dioxide and caustic soda, and the exact excess is plant-confidential but the crude reaction mixture is maintained at pH 9.0–10.5 to prevent sulfoxylate decomposition. The production process involves contacting sodium formate with sulfur dioxide gas in a cooled, agitated reactor at 35–45°C, followed by crystallisation, centrifugal separation, and vacuum drying of the sodium dithionite cake. Terminal product types include vat-dye reducing agents for indigo continuous dyeing, bleach-stage reducing agents for deinked pulp, and reducing agents for mineral flotation. Compliance is validated through the stabilised sodium dithionite specification under REACH (EC) No 1907/2006 and, where the product is used in textile chemical applications, residual heavy-metal content is checked against OEKO-TEX Standard 100 limit values. The main processing hazard is the exothermic decomposition of sodium dithionite in contact with humid air; accordingly, the dried product is packed in moisture-tight drums or bags with residual oxygen below 0.5 vol% in the headspace. Published data on continuous sulfonate-formate reactor selectivity under variable sulfur dioxide feed pressure are limited, and pilot studies often report yield losses of 5–15% when the sulfur dioxide absorption rate exceeds the cooling capacity of the reactor jacket.
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Industrial sodium formate is supplied as solid and liquid product models. Solid models include technical grade, refined grade, and synthesis grade; liquid product is commonly a 40 wt% aqueous solution with a crystallisation point near -20°C. The solid is a white crystalline solid with empirical formula HCOONa, CAS 141-53-7, EC 205-488-0, and molar mass 68.007 g/mol. Commercial production typically reacts carbon monoxide with aqueous sodium hydroxide in a bubble column reactor at 160–200°C and 1.5–2.0 MPa; the crude liquor is clarified through a plate-and-frame filter press, concentrated in a falling-film evaporator, and dried in a spray dryer. Batch-to-batch variation in bulk density is most often traced to spray-dryer inlet-air temperature and atomizer wheel speed. Because the solid is hygroscopic, storage should use sealed silos or moisture-barrier sacks at relative humidity below 60%; product exposed above this threshold may require drying at 80–90°C in a fluid-bed dryer before pneumatic conveying. Standard packaging includes 25 kg multi-wall bags, 1000 kg supersacks, and bulk tanker delivery. Representative specification bands for technical, refined, and synthesis grades are given in Table 1.
| Parameter | Technical grade | Refined grade | Synthesis grade |
|---|---|---|---|
| Assay as HCOONa (wt%) | ≥ 97.0 | ≥ 98.0 | ≥ 99.0 |
| Moisture by Karl Fischer titration (wt%) | ≤ 0.5 | ≤ 0.3 | ≤ 0.2 |
| Sodium chloride (wt%) | ≤ 0.3 | ≤ 0.1 | ≤ 0.05 |
| Sodium carbonate (wt%) | ≤ 1.0 | ≤ 0.5 | ≤ 0.1 |
| Water-insoluble matter (wt%) | ≤ 0.1 | ≤ 0.05 | ≤ 0.01 |
| Bulk density (g/cm³) | 0.80–1.10 | 0.85–1.05 | 0.90–1.00 |
The solid has a density of 1.92 g/cm³ at 20°C and a melting point of 253°C. Solubility in water is 97 g/100 mL at 20°C and 160 g/100 mL at 100°C; dissolution is endothermic, and large batching tanks therefore require jacket heating to avoid localized crystallization. A 1% aqueous solution has pH 7.5–8.5. Thermal decomposition under oxygen-limited conditions proceeds through sodium oxalate and hydrogen and becomes significant above 290°C, which restricts the material in high-temperature melt processing. Under EU CLP Regulation (EC) No 1272/2008, sodium formate is not listed in the harmonised classification for acute toxicity, specific target organ toxicity, or reproductive toxicity; dust control and local occupational exposure limits still apply during bulk handling. REACH registration is established under EC 205-488-0.
In runway and taxiway winter maintenance, solid sodium formate is applied as a non-chloride de-icing agent where chloride-induced corrosion is unacceptable. Mechanical spreaders are calibrated to deliver 10–40 g/m² for anti-icing before snowfall and 50–100 g/m² for de-icing compacted snow and ice; actual rates are adjusted using pavement temperature sensors and precipitation-rate data. Corrosion performance is tested under SAE AMS 1431 using standardised weight-loss coupons including aluminum alloy, cadmium-plated steel, and magnesium alloy. Sodium formate produces lower metal loss than sodium chloride, but it is not non-corrosive to cadmium or magnesium coatings at high concentration. Brine ice-melting activity is limited by a eutectic temperature near -20°C; this is adequate for moderate winter climates but below the performance of potassium formate or potassium acetate brines, which remain liquid below -40°C. Spreadability is controlled by sieve analysis after spray drying; oversize granules above 2.0 mm can bridge in auger-driven spreaders and generate uneven application on high-speed runway surfaces. Brine make-down for pre-wetting uses agitated tanks with heating coils because dissolution is endothermic. A 40 wt% sodium formate brine is transferred through insulated pipework to pre-wetting stations; at temperatures below -15°C, brine viscosity increases and pump selection must account for higher shear stress. Runoff from formate de-icing operations exerts chemical oxygen demand because formate is biodegradable. Airport stormwater permits often require COD monitoring; published data for specific catchment configurations is limited, but retention ponds or aerated lagoons are used to attenuate oxygen demand before discharge.
Chrome tanning baths use sodium formate after the initial chromium penetration step. The formate ion enters the chromium(III) coordination sphere as a masking ligand, slowing basification and preventing the formation of large, less-reactive chromium hydroxide clusters. In a stainless-steel tanning drum at 6–8 rpm and 35–40°C, sodium formate is dosed at 0.5–1.5 wt% of limed pelt weight, followed by gradual addition of sodium bicarbonate or magnesium oxide to raise float pH from 2.8–3.2 to 3.8–4.2. The masked chrome complex increases chromium uptake; wet-blue analyses typically show higher leather chromium content when formate is present than in formate-free basification. Overdosing beyond 2.0 wt% can produce drawn grain and a slippery handle. Sodium formate differs from sodium acetate in ligand size: formate is smaller and penetrates the chrome complex more rapidly, whereas acetate moderates basification more slowly in the same pH window.
For reservoir drilling-fluid formulations, sodium formate serves as soluble brine component and water-based mud additive. Saturated sodium formate brine density is near 1.33 g/cm³, sufficient for low-overbalance drilling but below potassium formate brine at approximately 1.57 g/cm³; this density ceiling excludes sodium formate from high-pressure well control where higher-density formate systems are needed. Rheology and filtration properties are measured under API RP 13B-1. Sodium formate lowers water activity and provides monovalent cation inhibition, but potassium formate is preferred where smectite-rich shale stability is the primary design objective because the potassium cation has an ionic diameter suitable for interlayer fixation. In completion operations, sodium formate brines are filtered through diatomaceous earth or cartridge units to 2–5 µm clarity before downhole placement to reduce formation damage. Field reports note that formate brines become corrosive to carbon steel when oxygen is not excluded at temperatures above 120°C; oxygen scavengers and pH buffers are required in surface tanks.
Concrete admixtures formulated with sodium formate accelerate Portland cement hydration without introducing chloride ions. The raw salt is dissolved in mixing water at 0.5–2.0% by mass of cement. Final admixture performance is assessed under ASTM C494/C494M Type C or EN 934-2:2019 Table 2, not on the raw salt alone. Compared with calcium chloride, sodium formate produces a less aggressive set acceleration and does not initiate chloride-induced corrosion of embedded steel; however, it contributes 0.456 kg of Na₂O equivalent per kilogram of active substance. This alkali loading is relevant for aggregate alkali-silica reactivity control. Calcium formate does not add alkali but has lower water solubility. Batching systems must handle the hygroscopic powder in closed auger conveyors; at relative humidity above 60%, caking can alter the calibrated feed rate from the powder dosing hopper. Initial setting time is measured with a Vicat apparatus according to ASTM C191; sodium formate at 2.0% can reduce initial set in ordinary Portland cement pastes, but published data for this specific configuration is limited. Trial batching with the actual cement lot is required because tricalcium aluminate content shifts the acceleration response.
Downstream chemical conversion consumes sodium formate in formic acid production by acidulation with sulfuric acid in a continuous distillation reactor; the sodium sulfate byproduct is removed by filtration. Sodium dithionite production also uses sodium formate as a feedstock. Technical-grade material is acceptable for many conversions, but formic acid destined for pharmaceutical intermediates may require the 99.0% assay grade to limit sulfate carryover.
Textile exhaust dyeing of wool and nylon with acid dyestuffs uses sodium formate as a buffer salt in stainless-steel dyeing machines. Combined with formic acid, it maintains dye-bath pH in the range 3.5–4.5, which is lower than the acetic acid/sodium acetate buffer range. The lower pH promotes exhaustion of acid dyes on nylon, but it can increase fiber surface damage if temperature exceeds 98°C for extended cycles. Compared with sodium acetate, sodium formate has a lower molar mass and therefore a different molar buffer capacity per kilogram; dosing is based on measured bath pH rather than mass equivalence.
Table 2 compares the properties that most often determine substitution decisions among sodium formate, potassium formate, and calcium formate. The selection is not based on chemical similarity alone; brine density, solubility, alkali contribution, and application temperature determine the operable window.
| Property | Sodium formate | Potassium formate | Calcium formate |
|---|---|---|---|
| Molar mass (g/mol) | 68.007 | 84.12 | 130.11 |
| Water solubility at 20°C (g/100 mL) | 97 | 330 | 16.6 |
| Saturated brine density at 20°C (g/cm³) | 1.33 | 1.57 | Not practical as brine |
| Eutectic temperature of aqueous solution (°C) | -20 | -50 | Not applicable to ice-melting brines |
| Chloride content (wt%) | < 0.01 | < 0.01 | < 0.01 |
| Typical industrial role | De-icing, drilling fluid, concrete acceleration, leather tanning | High-density brine, heat-transfer fluid, de-icing | Concrete acceleration, animal feed preservative, leather tanning |
Where saturated brine density above 1.40 g/cm³ is required, sodium formate is not a substitute for potassium formate or cesium formate brines. In cementitious systems, calcium formate is selected when additional calcium ion is desired, but sodium formate offers faster dissolution at low mixing-water temperatures. De-icing selection depends on the lower eutectic temperature of potassium formate and the higher runoff oxygen demand of sodium formate relative to acetate-free chloride formulations.
