Products
Products
Products
| HS Code | 480292 |
| Product Name | Crude Salt |
| Chemical Formula | NaCl with natural impurities |
| Cas Number | 7647-14-5 (for NaCl) |
| Appearance | Granular or crystalline solid |
| Color | White, grayish, or yellowish depending on source |
| Odor | Odorless |
| Taste | Salty |
| Nacl Content Percent | 94.0 - 99.5 |
| Moisture Content Percent | 0.5 - 6.0 |
| Water Insoluble Matter Percent | 0.1 - 3.0 |
| Bulk Density G Per Cm3 | 1.2 - 1.3 |
| Melting Point Degc | 801 (for pure NaCl) |
| Boiling Point Degc | 1465 (for pure NaCl) |
| Solubility In Water | Soluble; about 35.9 g per 100 mL at 25 °C |
| Ph Of Aqueous Solution | 6.5 - 8.0 |
As an accredited Crude Salt factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Crude salt is packaged in 25 kg woven polypropylene bags with an inner PE liner, sealed to prevent moisture. |
| Container Loading (20′ FCL) | 20′ FCL container loaded with crude salt, packed in double-lined polypropylene bags, safely secured for bulk marine transport. |
| Shipping | Crude salt ships in bulk or bags as a heavy, free-flowing solid. Protect from excess moisture to avoid caking; use dry containers or covered conveyors. Ventilation is unnecessary, but proper segregation from foodstuffs and corrosive materials is essential. Avoid contamination and ensure contamination-free handling safeguards. |
| Storage | Crude salt should be stored in a cool, dry, well-ventilated area, protected from moisture and direct rainfall. Use sealed, corrosion-resistant containers or lined bulk storage to prevent caking and contamination. Keep it separated from incompatible materials, such as strong acids, and ensure proper drainage and spill containment to minimize environmental impact. |
| Shelf Life | Crude salt has a long shelf life; it remains stable indefinitely when stored dry, sealed, and away from contaminants. |
Before membrane electrolysis can accept sodium chloride from crude salt, the dissolution liquor passes through softening, settling, filtration, and ion-exchange polishing. In chlor-alkali plants using a saturated brine feed, crude salt is dissolved in process water or depleted return brine at 300–310 g/L NaCl; the resulting near-saturated solution is treated with sodium carbonate and sodium hydroxide to precipitate calcium and magnesium hardness. The clarifier overflow is then polished through anthracite and sulfonated co-polymer cation exchange columns to reduce total hardness to ≤20 µg/L as CaCO3. The specific salt consumption in membrane-cell operation is reported at 1.60–1.75 t crude salt per t chlorine, depending on recycle brine management and purge ratios. Compliance verification for crude salt entering the dissolver is based on ISO 2479 for acid-insoluble matter, ISO 2480 for sulfate, ISO 2482 for calcium and magnesium, ISO 2483 for moisture content, and EN 1484 for total organic carbon in treated brine.
| Brine feed parameter | Membrane-control limit | Analytical method |
|---|---|---|
| Total hardness as CaCO3 | ≤20 µg/L | ISO 2482, ICP-OES |
| Sulfate as SO4 | ≤5 g/L | ISO 2480 |
| Iron | ≤0.1 mg/L | ICP-OES after acidification |
| Silica | ≤5 mg/L | Photometric molybdate method |
| Suspended solids | ≤0.1 mg/L | ISO 2479 filtration |
| Total organic carbon | ≤1 mg/L | EN 1484 |
Electrolysis takes place in activated zero-gap membrane cells at 85–90 °C; caustic exiting the cathode compartment is concentrated by multiple-effect evaporation to 50% NaOH. The chlorine gas is cooled, dried with sulfuric acid, and compressed for liquefaction or downstream hydrogen chloride synthesis. Terminal products are chlorine gas, 32% or 50% sodium hydroxide, hydrogen, and derived sodium hypochlorite. Crude salt with magnesium chloride above 0.05% can overtax the precipitation step; organic carbon above 1 mg/L in feed brine is reported to foul membrane coatings. The process boundary is set by suspended solids below 0.1 mg/L; poor salt dissolution in saturators with worn rake arms has been observed to shorten candle filter runs and increase backwash frequency on production-scale brine lines.
At a sodium ion concentration below 15 g/L, exhaustion of bifunctional reactive dyes on mercerized cotton remains incomplete regardless of fixation time. The addition of crude salt to the dyebath is therefore determined by shade depth and dye substantivity rather than by a fixed recipe. In exhaust dyeing, the working range is 15–25 g/L for pale shades below 0.5% owf, 35–50 g/L for medium depths of 0.5–2.0% owf, 60–80 g/L for dark shades of 2.0–4.0% owf, and 80–100 g/L for black, navy, and turquoise formulations above 4.0% owf. Salt is staged in two portions: approximately 60% of the total charge is added after initial fabric-dye contact, and the balance is added before alkali fixation to reduce aggregation of high-substantivity chromophores.
| Shade depth | Dyebath electrolyte addition | Addition sequence |
|---|---|---|
| Pale (<0.5% owf) | 15–25 g/L | 60% initial / 40% before alkali |
| Medium (0.5–2.0% owf) | 35–50 g/L | 60% initial / 40% before alkali |
| Dark (2.0–4.0% owf) | 60–80 g/L | 50% staged over 15 min / 50% before alkali |
| Black, navy, turquoise (>4.0% owf) | 80–100 g/L | 50% staged over 20 min / 50% before alkali |
The textile substrate is wetted-out in a soft-flow overflow jet or jig; dyestuff is dosed first, followed by sodium chloride addition over 15–20 min. After salt-induced exhaustion, sodium carbonate or caustic soda is pumped into the bath to initiate monochlorotriazine or vinyl sulfone fixation at 60 °C. Unfixed dye is stripped by soaping with a non-ionic detergent at 95 °C, then the fabric is rinsed and neutralized with acetic acid. Finished-textile compliance is assessed through ISO 105-C06:2010 for laundering colour fastness, ISO 14184-1:2011 for formaldehyde release, ZDHC MRSL 3.1 for restricted dyehouse chemicals, and the finished article limits of OEKO-TEX Standard 100. Crude salt used in dyeing is screened according to ISO 2479 for insoluble matter because undissolved particles larger than 0.1 mm can clog the pump pack and jet nozzle. Calcium and magnesium in crude salt above 50 mg/L can precipitate with soda ash and deposit on fabric contact points; sulfate levels above 500 mg/L may reduce dye solubility at high salt concentrations. Terminal fabrics include cotton and viscose knitwear, woven shirting, bed linen, and cellulose blend apparel dyed with reactive chromophores.
Regeneration of sodium-cycle cation exchange resin does not treat brine concentration as a variable of convenience; it controls swelling pressure, diffusivity of calcium and magnesium ions, and rinse-water demand. Regeneration brines are prepared at 80–120 g/L NaCl, with 100 g/L as the common set point, and are injected through an eductor into the resin bed at 4–8 BV/h. The salt dose is standardized at 120–160 g NaCl per L of strong-acid cation resin for co-current softening service, yielding an operating capacity of approximately 45–70 g CaCO3 per L resin at 160 g/L regeneration level. The regeneration sequence comprises backwash, brine injection, slow rinse, and fast rinse. Brine is drawn from a salt-storage tank through a float-controlled eductor; the saturated stock solution is diluted to 10% w/v before contacting the resin to avoid osmotic shock and resin bead fracture. After slow rinse displaces the sodium chloride front, the fast rinse is run until hardness leakage falls below 0.03 mmol/L CaCO3. Equipment and materials are specified under EN 14743 for softener performance and NSF/ANSI 44-2022 for material safety and capacity ratings. Brine quality is controlled by ISO 2479 for insoluble matter and ISO 2482 for hardness; insoluble particulate larger than 0.2 mm is rejected to protect injector throats and control-valve seals. Crude salt containing more than 0.2% insoluble material increases brine tank sludge and has been observed in commercial rental skids to alter eductor draw rate and reduce field capacity reproducibility. Output is softened water for low-pressure boilers, cooling tower make-up, reverse-osmosis pre-treatment, bottle-washing lines, and food-contact sanitation services where total hardness is reduced to ≤5 mg/L CaCO3.
Unless the crude salt is dissolved under controlled shear, particle size distribution above 850 µm causes density lag in completion brines. A saturated sodium chloride brine at 20 °C contains approximately 26.5 wt% NaCl, corresponding to a density of 1.20 SG (10.0 lb/gal), and requires approximately 360 kg crude salt per 1,000 kg fresh water. This is the upper density ceiling for single-salt sodium chloride systems; higher-density completion brines require calcium bromide, zinc bromide, or powdered weighting solids. Sodium chloride brines for drilling and completion are mixed through high-shear hoppers or paddle-blade mixers; the salt is added to the fresh water under agitation, and the density is confirmed with a pressurized mud balance. In drilling fluid formulations, prehydrated bentonite is added at 3–5 wt%, then sodium chloride is incorporated at 10–15 wt% to suppress divalent-type shale swelling and maintain fluid-loss control. For workover and packer applications, filtered NaCl brine is circulated into the wellbore at a pump rate sufficient to displace the previous fluid, with differential density checks made at the suction and discharge sides of the pump. Drilling-grade sodium chloride is controlled under ISO 13500:2008 and API Spec 13A for drilling fluid materials; field brine testing is covered by ISO 10414-1:2008. Terminal products include water-based drilling mud, clear NaCl completion brine, workover fluid, and packer fluid for onshore and offshore wells. Because sodium chloride brine containing residual insoluble matter can plug formation cores, filtration to 2 µm is specified for clear completion applications. Crude salt with high calcium chloride or sulfate alters the solubility product and can raise the crystallization temperature; below the 1.20 SG density ceiling, cold offshore risers may force sodium chloride crystallization if the brine is formulated near saturation.
Because ammonia recovery is the rate-limiting step in the Solvay loop, the quality of crude salt entering the brine purification chain determines scaling rates in the carbonating tower and the ammonia still. The Solvay soda ash route consumes sodium chloride at a net ratio of 1.2–1.5 t crude salt per t dense soda ash, depending on the efficiency of ammonia recycle and the purge volume required for sulfate control. In the brine purification stage, dissolved crude salt is clarified with milk of lime and soda ash to precipitate calcium carbonate, magnesium hydroxide, and insoluble silicates before the brine enters the ammonia absorber. Absorption of ammonia produces ammoniated brine, which is carbonated in Solvay towers under a counter-current flow of kiln gas containing 38–42% CO2. Sodium bicarbonate precipitates as the temperature falls along the tower, is dewatered on continuous vacuum drum filters, and is calcined in rotary tubular calciners at 160–200 °C to yield light soda ash. Dense soda ash is obtained by wetting and recrystallizing the light material in a monohydrate process. Brine feed is tested by ISO 2479 for insoluble matter, ISO 2482 for calcium and magnesium, and ISO 2480 for sulfate; finished soda ash is specified under ASTM E359-17 for total alkalinity and sodium chloride content. Output soda ash enters flat glass, container glass, detergent, sodium silicate, and flue gas desulfurization markets. Crude salt with high magnesium content shortens the time between ammonia still descaling shutdowns because magnesium hydroxide fouling deposits on the plates; sulfate above 5 g/L in the brine loop accumulates in the ammonium sulfate purge and reduces sodium chloride conversion. Published data for the Solvay-specific impurity tolerance of individual plants is limited because it depends on purge capacity.
Wet-salting of freshly flayed hides relies on osmotic dehydration rather than chemical fixation; the sodium chloride does not denature collagen but lowers water activity below the threshold required for proteolytic bacterial growth. A short-term curing treatment uses 25–40 kg crude salt per 100 kg green hide weight, while tropical warehouse storage for 30 days is typically specified at 50 kg per 100 kg green weight. The salt is applied to the flesh side, with edge and neck areas receiving the highest loading because bacterial ingress is most rapid there. After fleshing, hides are cooled to reduce blood load and then salted manually or in hide raceways; stacking follows a drainage period of 24–48 h to allow brine run-off. Moisture content falls from the fresh-hide level of approximately 65% to 40–45% during the first 72 h. The hides are then folded flesh-to-flesh and palletized for shipment to tanneries. Finished leather compliance is evaluated under REACH Annex XVII Entry 72 for chromium VI with a limit of 3 mg/kg using EN ISO 17075-1:2017; raw material traceability and preservation conditions are assessed under the Leather Working Group auditing protocol. Salt used for hide curing is screened by ISO 2479 for insoluble matter to avoid sand contamination in beamhouse operations. Terminal products are wet-salted cattle hides, sheepskins, and goat skins that later enter footwear, upholstery, automotive interior, and leather goods production. Crude salt with magnesium chloride content above 0.1% is hygroscopic and can re-moisturize hide packs during sea freight; iron above 100 mg/kg may produce dark stains after tanning. Salt containing organic debris can generate halophilic red heat bacteria on stored hides.
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Crude Salt is supplied as two industrial product models, Grade CS-96 and Grade CS-98.5, with model designations corresponding to the minimum sodium chloride content on a dry basis. The material originates from underground halite mining, solar evaporation of seawater or inland brines, and lake-bed crystallization, and is not refined for food, pharmaceutical, or reagent use. Typical lot release data for Grade CS-96 show sodium chloride between 96.0% and 97.5%, moisture between 0.8% and 2.5%, water-insoluble matter between 0.05% and 0.30% determined by ISO 2479:1972, calcium ion between 0.10% and 0.35%, magnesium ion between 0.03% and 0.15%, and sulfate between 0.10% and 0.60%. Loose bulk density ranges from 1.15 g/cm³ to 1.35 g/cm³ depending on particle-size distribution and compaction. The product is sold on a wet basis, and buyers should convert quoted sodium chloride content to dry basis when comparing shipments from different evaporative basins or mining faces.
| Parameter | Grade CS-96 | Grade CS-98.5 | Test Method |
|---|---|---|---|
| Sodium chloride, dry basis | 96.0% minimum | 98.5% minimum | ASTM E534-18 |
| Moisture, weight loss at 105°C | 0.8% to 2.5% | 0.3% to 0.8% | Gravimetric |
| Water-insoluble matter | 0.05% to 0.30% | 0.02% to 0.10% | ISO 2479:1972 |
| Calcium, as Ca | 0.10% to 0.35% | 0.03% to 0.12% | ASTM E534-18 |
| Magnesium, as Mg | 0.03% to 0.15% | 0.01% to 0.05% | ASTM E534-18 |
| Sulfate, as SO₄ | 0.10% to 0.60% | 0.05% to 0.20% | ASTM E534-18 |
In membrane chlor-alkali production, crude salt is dissolved to maintain saturated brine at 300 g/L to 320 g/L sodium chloride. The primary operational boundary is not the sodium chloride content itself, but the hardness load entering the secondary brine polishing system. Calcium ion from crude salt must be reduced to below 50 ppb and magnesium ion to below 20 ppb in the feed to membrane electrolyzers to prevent precipitation inside the ion-exchange membranes and to protect anode coatings. With Grade CS-96 containing up to 0.35% calcium, primary treatment requires sodium carbonate and sodium hydroxide dosing followed by clarification and filtration. Dosing rates are usually set to maintain a carbonate hardness excess of 0.2 g/L to 0.5 g/L as CaCO₃. Clarifier overflow turbidity is often controlled below 1 NTU using polyaluminum chloride at 5 mg/L to 20 mg/L, but actual dose depends on raw brine temperature and mixing energy. Sulfate concentration is equally critical in the brine circuit: sulfate above 5 g/L in the anolyte loop can precipitate as calcium sulfate dehydrate in heat exchangers and reduce chlor-alkali current efficiency. For crude salt with sulfate between 0.10% and 0.60%, a purge stream or barium carbonate precipitation step may be required in closed-loop plants. Published data for specific crude salt lot performance in membrane cells is limited because brine treatment is highly site-specific; operators typically pilot each new source before changing purchased salt grades.
Application in municipal de-icing and dust suppression depends on the sodium chloride-water phase diagram rather than the purity of the salt. At the eutectic concentration of 23.3% by weight, sodium chloride brine freezes at approximately -21.1°C. Anti-icing operations using Crude Salt brine are generally limited to pavement temperatures above -9°C, because the practical melting rate becomes too low for traffic safety below that threshold. De-icing rock salt is commonly specified with a particle-size range of 6.3 mm to 12.7 mm; fines passing 1.18 mm are restricted to 10% or less to reduce wind drift and bounce loss during spreading. Application rates for de-icing range from 150 kg/lane km to 400 kg/lane km depending on road-surface temperature, residual brine, and precipitation rate. For dust suppression on unpaved haul roads, a 25% brine solution is applied at 0.5 L/m² to 1.0 L/m². The hygroscopic effect of sodium chloride disappears below the deliquescence point of approximately 75% RH at 25°C; below this relative humidity, the crust loses retained moisture and dust control effectiveness declines. Municipal buyers should verify gradation and moisture against ASTM D632-12, but that standard does not replace field calibration of spreader discharge rates.
Use of crude salt in sodium-cycle cation exchange water softeners is confined to industrial regeneration systems equipped with brine saturators and filtration. The limiting impurity is water-insoluble mineral matter, because particulate carryover blinds resin exchange sites and increases bed pressure drop. Grade CS-98.5 is specified at 0.10% maximum water-insoluble matter for this service; Grade CS-96 is generally not recommended unless the brine is settled for 24 h and filtered through a 10 µm cartridge. Iron also presents a fouling risk: resin manufacturers commonly set a maximum regenerant iron concentration of 0.5 mg/L as Fe, because ferric hydroxide precipitation above pH 8.5 produces irreversible resin fouling. Crude salt batches containing between 0.01% and 0.03% iron on dry basis can be used only when brine clarification, iron removal, and pH adjustment are included. Rinse volume requirements are higher than those for evaporated pellet salt because of elevated calcium and magnesium in the regenerant brine; field measurements show 5 to 8 bed volumes for crude salt systems compared with 3 to 4 bed volumes for vacuum-dried salt. Where the treated water may enter drinking-water systems, the regeneration chemical should meet EN 973:2009.
Crude salt is applied in oilfield drilling fluids as a brine-activity and density-control agent for drilling halite sections and water-sensitive shales. Saturated brine density is maintained at 1.20 g/cm³ to 1.22 g/cm³ by carrying an excess of undissolved salt in the mud system, with chloride concentration typically between 180,000 mg/L and 190,000 mg/L. Field experience indicates that sulfate above 0.80% in crude salt contributes to gypsum scaling on shale shaker screens and flowline surfaces, requiring citric acid circulation at pH 2.5 to 3.0 for removal. Dusting and hopper lumping during continuous mixing operations increase when the fraction below 75 µm exceeds 5%; pneumatic transfer equipment should be sized for a bulk material with an angle of repose near 35°. Published data for this specific crude salt configuration is limited because formulation adjustments are managed at the well site based on mud density and chloride titration rather than vendor literature.
In leather preservation and hide curing, crude salt functions as an osmotic dehydrating agent. The minimum sodium chloride content on a wet basis should remain above 94%, because lower purity reduces the osmotic gradient and increases water activity in the cure pack. Salt application rates of 40% to 50% of green hide weight are used in pile curing, and cured-hide moisture is maintained below 45% to suppress bacterial activity. Calcium and magnesium impurities may raise brine alkalinity and promote slime formation; sodium metabisulfite is added at 0.2% for microbial control, but addition above 0.5% can damage hide grain. In textile dyeing, crude salt is used to exhaust reactive dyes in batch dyeing at 50 g/L to 100 g/L, but iron content below 0.01% is preferred to avoid shade dulling and dye agglomeration. Published data for crude salt performance in low-liquor-ratio jet dyeing machines is limited; most dye houses specify a filtered brine of 1.15 g/cm³ minimum density and hold the solution for 20 min before injection.
Relative to vacuum-dried sodium chloride, Crude Salt contains higher residual magnesium, sulfate, and moisture, which makes it unsuitable for membrane chlor-alkali feed without secondary polishing and less desirable for high-efficiency resin regeneration. Compared with solar salt, crushed rock salt may have higher insoluble silicate contamination but more angular particle morphology, which can improve traction in de-icing applications. Differences in bulk handling should also be considered: vacuum-dried salt typically has a loose bulk density of 1.28 g/cm³ to 1.38 g/cm³, whereas Crude Salt CS-96 ranges from 1.15 g/cm³ to 1.35 g/cm³. The table below summarizes the principal technical distinctions for product selection.
| Characteristic | Crude Salt CS-96 | Vacuum-Dried Industrial Salt | Food-Grade Granulated Salt |
|---|---|---|---|
| Sodium chloride, dry basis | 96.0% to 97.5% | 99.0% to 99.5% | 99.5% minimum |
| Calcium plus magnesium, as CaCO₃ | 0.30% to 0.90% | 0.02% to 0.10% | 0.05% maximum |
| Sulfate, as SO₄ | 0.10% to 0.60% | 0.02% to 0.10% | 0.05% maximum |
| Moisture | 0.8% to 2.5% | 0.05% to 0.30% | 0.10% maximum |
| Primary application boundary | De-icing, hide curing, drilling fluids | Chlor-alkali, water softening | Food processing, potable water |
