Products
Products
Products
| HS Code | 213510 |
| Name | Ammonia |
| Chemical Formula | NH3 |
| Cas Number | 7664-41-7 |
| Molar Mass | 17.031 g/mol |
| State At 25c | gas |
| Appearance | colorless gas |
| Odor | pungent, suffocating |
| Density | 0.769 kg/m3 at STP |
| Melting Point | -77.73 °C |
| Boiling Point | -33.34 °C |
| Solubility In Water | approximately 31% w/w at 25 °C |
| Vapor Pressure | 857 kPa at 20 °C |
| Autoignition Temperature | 651 °C |
| Aqueous Solution Ph 0 1m | ~11.1 |
As an accredited Ammonia factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Ammonia is packaged in pressurized, leak-proof steel cylinders or bulk tankers, with quantities typically ranging from 25 kg to 1,000 kg. |
| Container Loading (20′ FCL) | Ammonia loaded in 20' FCL as liquefied gas via ISO tank, requiring pressure control, leak detection, and strict hazardous material handling. |
| Shipping | Ammonia is shipped as anhydrous liquefied gas under pressure or refrigeration, typically via dedicated pipelines, pressurized tank cars, tank trucks, and ocean tankers. Transport requires corrosion-resistant stainless steel or specialized tanks, strict temperature control, and hazard labeling. Safety protocols address its toxicity, corrosivity, and flammability risks. |
| Storage | Ammonia is typically stored as a liquefied gas in specialized pressure vessels or refrigerated tanks made from carbon steel. Storage must be cool, well-ventilated, and away from incompatible materials like acids, oxidizers, and halogens. Equip tanks with pressure-relief valves, leak detection, secondary containment, and follow strict safety protocols to prevent toxic vapor release. |
| Shelf Life | Shelf life varies; store tightly sealed, cool, and away from acids. Typically stable for years if unopened. |
The conversion of anhydrous ammonia into urea is executed in a high-pressure synthesis loop operating at 140–250 bar and 170–220 °C, with a reactor feed molar ratio of NH₃:CO₂ = 2.8–4.0. The equilibrium-limited carbamate dehydration sequence, 2 NH₃ + CO₂ ⇌ NH₂COONH₄ ⇌ (NH₂)₂CO + H₂O, restricts single-pass CO₂ conversion to 60–80%, which makes downstream stripping and recycling of unconverted carbamate obligatory for total CO₂ utilization above 99%. Industry compliance is anchored to Regulation EU 2019/1009, Annex I PFC 1(C)(I)(a)(i) for straight solid inorganic macronutrient fertilisers; biuret content is measured under ISO 18643:2015, and urea-derived automotive grade solution is controlled by ISO 22241-1:2019, which sets biuret at 0.3% maximum mass fraction. In CO₂-stripping configurations, the preheated CO₂ stream serves as stripping agent for carbamate decomposition, while in NH₃-stripping plants liquid ammonia performs the same function; both routes feed a vacuum evaporator train that raises melt concentration to 96–99.5% urea before solidification. The terminal production step is either prilling in a prilling tower or fluidized-bed granulation, where bed temperature is held at 105–115 °C and fluidization air humidity is controlled to prevent particle agglomeration and irregular size distribution. Finished product types include granular urea 2–4 mm, prilled urea 1–3 mm, urea-ammonium nitrate solution with 32% nitrogen, and 32.5% urea diesel exhaust fluid conforming to ISO 22241-2:2019.
At gauze temperatures above 850 °C, the oxidation of ammonia over 90/10 platinum-rhodium knitted gauze becomes diffusion-limited, and the process operates within a narrow ammonia-in-air concentration window of 9.5–10.5 vol%, safely below the lower flammable limit near 15 vol%. The principal addition ratio is therefore expressed as feed ammonia concentration rather than a liquid formulation ratio, because excess ammonia raises N₂O generation and premature gauze degradation, while deficient ammonia reduces nitric oxide yield. Medium-pressure Ostwald trains run at 0.3–1.0 MPa and 850–950 °C, producing NO gas that is cooled, oxidized to NO₂, and absorbed in water to yield 55–68 wt% nitric acid. Compliance for industrial nitric acid is governed by ISO 15515:2014 for total acidity and sulfate content, while ammonium nitrate derived from this acid is subject to detonation resistance testing under EU 2019/1009, Annex III. Platinum losses of 0.1–0.5 g/t HNO₃ are typical, and gauze campaign life frequently spans 90–180 days before replacement. Production-scale experience shows that simultaneous control of catalyst surface temperature and NH₃ preheat prevents the temperature cliff-edge associated with early gauze poisoning; above 950 °C, platinum oxide volatilization accelerates and mechanical gauze integrity deteriorates. Terminal products include concentrated nitric acid, ammonium nitrate solution, calcium ammonium nitrate fertiliser granules, and ammonium nitrate fuel oil after further mixing and granulation operations.
Within the wet-process phosphoric acid downstream segment, ammonium phosphate granulation uses anhydrous ammonia to neutralize phosphoric acid in a pre-neutralizer and a pipe-cross reactor before the slurry is distributed onto a rotary drum granulator. The NH₃:H₃PO₄ mole ratio is maintained at 1.0 for monoammonium phosphate and 1.9–2.0 for diammonium phosphate, with pre-neutralizer temperature held at 140–170 °C to limit fluorine volatilization while keeping slurry viscosity suitable for pumping. Compliance falls under EU 2019/1009, Annex I PFC 1(C)(I)(a)(i), and phosphate rock-derived grades must also satisfy heavy metal limits specified in Annex II of the same regulation. The downstream production process requires a recycle ratio of 3:1 to 5:1 in the drum granulator to stabilize granule moisture and control dust formation; scrubbers recover ammonia and fluorine compounds from granulator off-gas. Terminal finished products include MAP with a nominal 11-52-0 N-P-K grade, DAP at 18-46-0, and blended NPK grades in which the ammonium phosphate granule serves as the phosphorus carrier.
In caprolactam by-product recovery and coke-oven gas treatment, ammonium sulfate crystallization is performed by injecting anhydrous ammonia into sulfuric acid-containing liquor; the stoichiometric consumption is 0.26 kg NH₃ per kilogram of ammonium sulfate formed. The saturator is operated at 60–70 °C and pH 3.8–4.2, where buffering from the NH₃-H₂SO₄ system minimizes free ammonia loss and keeps free acid in the crystal cake at 0.02–0.05 wt%. Compliance is applied under EU 2019/1009, Annex I PFC 1(C)(I)(a)(i), with REACH registration obligations for the substance itself. Crystals are withdrawn from the saturator cone, centrifuged, and dried to 0.1–0.3% free moisture; terminal product types include crystalline ammonium sulfate 21-0-0-24S, compacted ammonium sulfate granules, and technical grades used in protein separation and water treatment.
Because the Sohio process feeds ammonia in slight molar excess over propylene, the reactor outlet is continuously monitored for unreacted ammonia breakthrough as an indicator of catalyst activity loss. The feed ratio is maintained at NH₃:C₃H₆ = 1.05–1.20, with the fluidized-bed reactor operating at 430–470 °C and 50–200 kPa over bismuth molybdate catalyst. Compliance for acrylonitrile monomer exposure is set by OSHA 29 CFR 1910.1045 at a permissible exposure limit of 2 ppm as an 8-hour time-weighted average, while finished polymer migration into food-contact materials is constrained by EU 10/2011. The downstream process includes quench, absorption, and recovery of acrylonitrile from the reactor effluent; unreacted ammonia is neutralized with sulfuric acid, producing by-product ammonium sulfate at a ratio that varies with catalyst ammonia selectivity. Terminal products include acrylonitrile monomer, polyacrylonitrile fiber precursor, acrylonitrile-butadiene-styrene resin, and nitrile rubber, all of which require residual monomer stripping to meet resin-specific specification bands.
Industrial refrigeration systems using R717 operate as single-stage or two-stage vapour compression cycles; low-charge flooded plate heat exchanger designs are specified at 0.20–0.45 kg NH₃ per kilowatt cooling capacity, while pumped overfeed systems at evaporating temperatures below -40 °C may exceed 0.8 kg/kW depending on wet suction accumulator inventory. Compliance is governed by EN 378-1:2016+A1:2020 for safety classification and charge limits, ISO 5149-1:2014 for system design, ASHRAE 15-2022 for mechanical room ventilation, and IIAR 2 for leak detection and alarm settings. Production-scale screw compressors with oil separators achieve oil carryover below 5–10 ppm, but low-side oil return in ammonia systems depends on thermosiphon oil cooling and controlled discharge superheat; published data for direct-expansion charge optimization in cascade configurations is limited. Copper and brass fittings are prohibited because ammonia reacts with copper-bearing alloys under moisture, producing stress corrosion cracking. Terminal applications include food processing cold storage, ice rinks, pharmaceutical freeze-drying, and petrochemical process cooling where ammonia is used as the secondary refrigerant in cascades with CO₂ in the low stage.
For coal-fired utility boilers and cement kilns, high-dust selective catalytic reduction is controlled by the normalized stoichiometric ratio, typically 0.85–1.00 mol NH₃ per mol NOx, with aqueous ammonia supplied at 19–29 wt% concentration and vaporized before an injection grid upstream of the static mixer. The catalytic reactor is operated at 300–420 °C, and ammonia slip is held at 2 ppmv or less to protect downstream air preheater surfaces from ammonium bisulfate deposition. Compliance is anchored to 40 CFR Part 75 for continuous emission monitoring and 40 CFR Part 76 for NOx trading program requirements, with European installations subject to EN 14181 quality assurance of automated measuring systems. The production process includes sootblower sequencing across layered vanadium-titanium catalyst modules, humidity-controlled ammonia vaporization, and periodic catalyst activity measurement against the initial K/K0 baseline. Terminal products are not a physical good but an operational compliance output: stack NOx reduction, minimized ammonia slip, and particulate matter protection for the air preheater and electrostatic precipitator trains.
Indirectly, dissociated ammonia functions as a process atmosphere source for reducing iron oxides on stainless steel surfaces and providing atomic nitrogen for gas nitriding. Anhydrous ammonia is cracked over a nickel-based catalyst in a retort furnace at 925–1010 °C, yielding a cracked gas composition of 25 vol% N₂ and 75 vol% H₂ with residual ammonia below 100 ppmv after adsorptive drying. The addition ratio downstream is atmosphere-dependent: bright annealing of stainless steel typically requires 5–15 vol% H₂ in N₂ at a dew point below -50 °C, while gas nitriding may use cracked ammonia blended with nitrogen to control nitriding potential. Compliance is defined by SAE AMS 2750F for pyrometry, AMS 2759/6 for gas nitriding process control, and CQI-9 for automotive heat-treatment audit requirements. The terminal production process includes retort temperature uniformity surveys, dew point monitoring, and residual oxygen analysis before atmosphere introduction. Finished product types include bright-annealed stainless steel strip, gas-nitrided gears and dies, and powder metal sintered components where the non-carburizing atmosphere preserves carbon control.
Competitive Ammonia prices that fit your budget—flexible terms and customized quotes for every order.
For samples, pricing, or more information, please contact us at +8615365186327 or mail to sales3@ascent-chem.com.
We will respond to you as soon as possible.
Tel: +8615365186327
Email: sales3@ascent-chem.com
Flexible payment, competitive price, premium service - Inquire now!
Ammonia is a colorless liquefied industrial gas with CAS 7664-41-7, molecular formula NH₃, and molar mass 17.031 g/mol. The technical-grade anhydrous product is specified at 99.5 wt% minimum NH₃, with water ≤0.5 wt%, oil ≤5 mg/kg, and non-condensables ≤0.2 vol%. At 101.3 kPa the saturated liquid boils at -33.34 °C; vapor pressure is 857 kPa at 20 °C and 1.55 MPa at 40 °C, which places anhydrous ammonia storage vessels under pressure-equipment rules such as ASME BPVC Section VIII Division 1 or EN 13445 and requires relief devices sized to ISO 4126-1. The flammable range in dry air is 15–28 vol% at 20 °C and 101.3 kPa, with autoignition temperature 651 °C. ASHRAE 34-2022 classifies R-717 as B2L. The product line is defined by delivery grade rather than a machine model: technical-grade anhydrous ammonia, refrigeration-grade anhydrous ammonia, 19 wt% aqueous ammonia, and 29 wt% aqueous ammonia. Each grade differs in water content, vapor pressure, transport classification, and materials compatibility. Carbon steel is acceptable for dry anhydrous ammonia, but copper and brass are excluded from ammonia service because of stress-corrosion cracking, while aqueous ammonia above 10 wt% is usually transferred through stainless steel or high-density polyethylene lines.
Anhydrous ammonia is a single-component liquefied gas supplied under pressure and used where water cannot be tolerated in a synthesis loop or refrigerant circuit. Aqueous ammonia, sometimes called ammonium hydroxide solution, contains dissolved NH₃ in water and has substantially lower total vapor pressure. The 29 wt% solution is classified as UN 2672 and can be stored in low-pressure tanks with acid scrubbers or vapor return lines; the anhydrous product is classified as UN 1005 and requires pressure vessels or certified cargo tanks. The product grades are compared below.
| Parameter | Anhydrous technical | Refrigeration anhydrous | Aqueous 19 wt% | Aqueous 29 wt% |
|---|---|---|---|---|
| NH₃ minimum | 99.5 wt% | 99.8 wt% | 19.0–19.5 wt% | 29.0–29.5 wt% |
| Water | ≤0.5 wt% | ≤150 ppm | balance | balance |
| Oil | ≤5 mg/kg | ≤2 mg/kg | not detected | not detected |
| Vapor pressure at 20°C | 857 kPa | 857 kPa | low, vented | low, vented |
| UN class | UN 1005 | UN 1005 | UN 2672 | UN 2672 |
In industrial refrigeration, ammonia is specified as R-717 and is distributed in steel piping and pressure vessels. The high latent heat of vaporization of approximately 1370 kJ/kg at -33.4 °C means that a lower mass flow is required than for R-134a, whose latent heat at its normal boiling point is 217 kJ/kg. Flooded pump-recirculation systems with low-pressure receivers and liquid level control are common for cold storage in the -35 to 0 °C range, while low-charge direct-expansion packages operating at 0.08–0.15 kg/kW refrigerant charge are used for food processing. Oil-flooded screw compressors require discharge gas desuperheating and high-efficiency coalescing oil separators because ammonia discharge temperatures can exceed 110 °C at condensing temperatures above 35 °C. R-717 is incompatible with copper, zinc, and brass, so piping and shaft seals use carbon steel, stainless steel, or PTFE. Compared with R-134a and R-404A, ammonia has zero ozone depletion potential and zero global warming potential; however, B2L classification under ASHRAE 34-2022 and the NIOSH IDLH of 300 ppm require mechanical ventilation, gas detection, and emergency shutoff systems conforming to EN 378-1:2016 and ISO 5149-1:2014.
Anhydrous ammonia injected into soil with knife or coulter applicators at 15–20 cm depth and 50–76 cm row spacing is immediately protonated to NH₄⁺ in soil water and held on cation-exchange sites. At soil temperatures above 10 °C, Nitrosomonas-mediated oxidation to NO₂⁻ and Nitrobacter-mediated oxidation to NO₃⁻ can complete in 10–21 days; below 10 °C, nitrification is slowed and ammonium retention may exceed 30 days. Volatilization from injection is typically limited to 1–5% of applied N when soil moisture is 20–35 wt% and the injection slot closes behind the knife. This differs from surface urea, which depends on urease hydrolysis and can lose 10–30% of applied N as NH₃ within 7 days on calcareous or low-CEC soils. Unlike ammonium sulfate, anhydrous ammonia supplies no sulfur; unlike UAN solution, it contains no water and requires pressurized metering. Published field data for nitrous oxide flux after injection on claypan soils remains limited and site-dependent.
Aqueous ammonia at 19 wt% or anhydrous ammonia is injected into flue gas upstream of a TiO₂-WO₃-V₂O₅ monolithic catalyst for selective catalytic reduction. The stoichiometric reactions are 4 NH₃ + 4 NO + O₂ → 4 N₂ + 6 H₂O and 2 NH₃ + NO + NO₂ → 2 N₂ + 3 H₂O; the second pathway is faster when NO:NO₂ approaches 1:1 and can dominate at temperatures below 250 °C. Catalyst operating temperature for vanadia-titania SCR is typically 300–420 °C, with higher temperatures increasing SO₂-to-SO₃ oxidation and ammonium bisulfate formation in downstream air heaters. Injection grids use multiple lances downstream of economizers, with ammonia flow controlled to maintain NOx reduction of 80–95% and NH₃ slip ≤5 ppmvd at 3% O₂. Direct ammonia differs from urea-based SCR by eliminating urea decomposition; urea reagents require sufficient residence time above 200 °C to avoid cyanuric acid deposition, while anhydrous ammonia requires gas detection and emergency isolation valves under NFPA 55 and 29 CFR 1910.119.
In the Ostwald process, anhydrous ammonia is vaporized, mixed with filtered air to 10–12 vol% NH₃, and reacted over a Pt-Rh catalyst gauze at 850–950 °C and 1–7 bar. The primary reaction 4 NH₃ + 5 O₂ → 4 NO + 6 H₂O achieves NO selectivity of 94–98% when the gauze pack is clean; side products include N₂ and N₂O. Catalyst gauze typically contains Pt-Rh 90/10 or Pt-Rh-Pd 95/5 wire with 76 µm diameter and 1024 mesh/cm², operated with 2–5 gauze layers. Ammonia slip below 5 ppm requires precise static mixing and distribution across the burner; local pockets above 12.5 vol% NH₃ can approach the lean flammability envelope under burner operating conditions, causing gas-phase ignition and damaging the burner and downstream heat exchanger. Compared with other nitrogen carriers, anhydrous ammonia is the only commodity feedstock that can be oxidized directly to NO without preliminary release of N₂, making it essential for nitric acid and subsequent nitrate production. Waste-heat boilers downstream recover reaction heat to raise steam at 4–6 MPa, and the NO stream is cooled before absorption into nitric acid.
Captive ammonia feedstock in urea synthesis is compressed with carbon dioxide to 140–200 bar and reacted at 180–200 °C in a carbamate condenser and urea reactor, with NH₃:CO₂ molar ratio of 2.8–3.5. The intermediate ammonium carbamate decomposes to urea and water; unconverted gases are stripped and recycled. The ammonia feed must contain ≤0.5 wt% water and low inerts because water suppresses conversion and inerts reduce compressor capacity. This differentiates ammonia from urea products: urea is a transportable solid nitrogen product with lower vapor pressure but requires CO₂ compression and decomposition energy, while anhydrous ammonia is the reactive precursor with higher vapor pressure and direct soil injection or scrubbing compatibility.
Municipal water treatment uses aqueous ammonia at 19 wt% or 29 wt% to generate chloramines by reaction with sodium hypochlorite at chlorine:ammonia weight ratio 4:1 to 5:1 and pH 7.5–9.0. Monochloramine formation is favored at pH 8.3, where NH₃ + HOCl → NH₂Cl + H₂O proceeds rapidly. The ammonia source must be low in transition metals to limit chloramine decomposition, so metering pumps use stainless steel wetted parts and PTFE diaphragms. Compared with gaseous chlorine, chloramination reduces regulated trihalomethane formation but requires longer contact time and a nitrification monitoring program in distribution systems.
Anhydrous ammonia storage terminals use horizontal pressure vessels with design pressure 17.2 barg at 50 °C and minimum design metal temperature matched to ambient -33 °C; carbon steel is permitted if sulfur and copper-bearing weld filler are restricted and post-weld heat treatment follows ASME BPVC Section VIII Division 1. Relief valves set at 75% of MAWP discharge to flares or absorbers; a closed-loop purge system prevents water vapor ingress because atmospheric moisture can form carbamate salts on valve seats. Piping systems are fabricated to ASME B31.3, with hydrostatic testing at 1.5 times design pressure and tightness testing per ASME B31.3 Chapter VI. Leak detection and emergency isolation thresholds should follow published IIAR 2 and EN 378-1:2016 settings, with anhydrous ammonia regulated as a hazardous substance under 29 CFR 1910.119 at threshold 10,000 lb and under EPA 40 CFR Part 68 risk management rules. Aqueous ammonia transfer pumps commonly use magnetic-drive sealless constructions to limit vapor escapes, while anhydrous ammonia pumps require high-suction-head can pumps or vertical submerged pumps to manage the liquid’s high vapor pressure and avoid cavitation at 20 °C.
