Concentrate process liquors and grow product crystals under engineered control of supersaturation, particle size distribution (PSD), purity and yield — across inorganic salts (battery-grade Li₂CO₃ / LiOH, fertilizer-grade (NH₄)₂SO₄), organic acids (adipic, oxalic), and fermentation products (amino acids, MSG, citric acid).
Product crystallization is not one technology. Five independent variables must combine to specify a route — collapse them and you risk purity, yield or operability.
NaCl-style flat solubility, adipic-acid-style strongly-rising solubility, Li₂CO₃-style inverse solubility, or thermally sensitive curves like lysine — the slope and sign of ds*/dT dictates evaporative, cooling, vacuum cooling or reaction crystallization as the supersaturation route.
Decomposition, color body formation or activity loss at elevated temperature (common to amino acids, organic acids, API intermediates) caps the operating temperature and forces vacuum-cooling or low-temperature evaporative routes with residence time kept below the degradation threshold.
Co-crystallization of K⁺ / Na⁺ / Ca²⁺ impurities, mother-liquor occlusion within crystals, and surface adsorption threaten product grade. Impurity profiling (ICP, IC) at expected concentration determines seeding, wash-liquor strategy and purge ratio.
Integrated BPA wastewater treatment with low-temperature MVR evaporation and crystallization: phenol recovery first, salt recovery second, reusable condensate and compliant solids for epoxy resin and polycarbonate plants.
Convert by-product hydrochloric acid from soda ash, chlor-alkali and polysilicon plants into saleable calcium chloride: neutralization, forced circulation evaporation, dihydrate flake or anhydrous granule finishing.
Evaporation and crystallization systems for erythritol, sorbitol, and allulose: MVR falling film concentration to Maillard control, melt versus cooling crystallization routes, and viscosity boundaries.
Representative configuration of the evaporator system for a 70,000 tpy L-threonine plant in Northeast China: fermentation broth concentration and evaporative crystallization, with a comparable 80,000 tpy project running a 10
Representative configuration of a Canadian brine-to-lithium plant producing 99.9% battery-grade lithium carbonate, with UF/RO preconcentration ahead of evaporation and sodium carbonate precipitation crystallization.
Calcium chloride concentration and anhydrous granulation from soda ash distiller waste – high boiling-point-rise evaporation, spray granulation, 600,000 TPA reference practice.
Pre-concentration, supersaturation method and crystal growth configuration are orthogonal decisions. They combine — they are not alternatives.
Pre-concentration → Supersaturation → Crystal growth → Solid-liquid separation → Washing → Drying
Each stage is configured from your liquor’s solubility behavior, thermal limits, impurity profile and target PSD — never from a catalog.
Falling-film evaporation for clean low-viscosity feeds (MVR or multi-effect); forced-circulation for fouling, viscous or seed-bearing liquors. Target: approach saturation within the metastable zone.
Evaporative (NaCl, (NH₄)₂SO₄), cooling (adipic acid, PTA), vacuum cooling (lysine, MSG, citric) or reaction (LiFePO₄ precursor) — selected from the slope and sign of ds*/dT.
Forced-Circulation (0.2–0.8 mm), DTB (0.5–2 mm) or OSLO fluidized-bed (1–5 mm) — orthogonal to supersaturation method, prioritizes reliability, PSD or crystal quality respectively.
Pusher, peeler or scroll centrifuge with engineered wash stage to displace mother liquor and reduce impurity occlusion; wash-liquor quantity tuned to purity target.
Fluid-bed, conical or rotary dryer matched to crystal morphology, thermal limit and target moisture (typically < 0.5% free moisture for fertilizer-grade; < 0.1% for battery-grade).
Recycle to crystallizer, purge to control impurity accumulation, or secondary crystallization for residual product recovery — links to Solution S3.
Each chemical has its own solubility behavior, impurity profile and crystallization route. These dedicated pages translate the chemistry into equipment selection.
Battery-grade Li₂CO₃ (D50 5–10 μm, > 99.5%) requires hot evaporative DTB crystallization above 90 °C. Inverse solubility (solubility drops as T rises) drives surface scaling — material (titanium / Duplex 2205) and configuration must be matched.
By-product of caprolactam, coke-oven gas and rare-earth extraction. Flat solubility requires evaporative DTB crystallization to deliver fertilizer-grade 1–3 mm prills; mother-liquor purge controls organic build-up.
Solubility rises from ~2 g/L at 20 °C to ~160 g/L at 90 °C — cooling crystallization is the natural route. DTB with controlled cooling profile (≤ 5–8 °C/h) protects crystal morphology and avoids fine-formation spikes.
Vacuum-cooling crystallization at 35–55 °C avoids decomposition and color body formation. Hygienic 316L / duplex construction, residence time kept under 2 hours, metastable-zone width mapped before specifying seed strategy.
Battery-grade LiOH·H₂O (> 56.5% LiOH, Na < 0.003%) uses vacuum-cooling crystallization followed by centrifugation and drying. Nickel-clad or specialty alloy construction resists strong alkalinity and chloride traces.
Glyphosate, dichlorvos, atrazine and similar generate high-COD (10–50 g/L) mixed-salt mother liquors with surfactant-driven foaming. Forced-circulation evaporator + advanced oxidation upstream for engineering reliability.
Three crystal growth configurations — each prioritizes a different outcome. Selection is orthogonal to the supersaturation method.
Typical ranges for preliminary screening — final selection requires lab solubility, metastable-zone and impurity profiling.
Selection questions that engineers ask before committing to a crystallization route.
Because they are orthogonal. Supersaturation method (evaporative, cooling, vacuum cooling, reaction) describes how you create the supersaturation that drives nucleation and growth. Crystal growth configuration (FC, DTB, OSLO) describes how you manage the suspension, classify the crystals and control PSD inside the vessel. A DTB can use evaporative, cooling or vacuum-cooling supersaturation — the two decisions are independent. Conflating them is the most common source of misselection in this field.
Choose DTB when product quality — narrow PSD (CV < 40%) and easy centrifugation — is the priority, and the feed is clean enough not to scale or foul the baffle / draft tube. Choose FC when the priority is engineering reliability under scaling, fouling, high-TDS, high-viscosity or composition-swing conditions. Fertilizer-grade (NH₄)₂SO₄, KCl and urea typically favor DTB; mixed-salt ZLD and difficult-stream crystallization favor FC.
Vacuum-cooling crystallization operates at 35–55 °C, using flash evaporation of water to provide both cooling and supersaturation. This avoids the high tube-wall temperatures of indirect cooling (which can cause incrustation and thermal decomposition) and shortens the high-temperature exposure window. Combined with short residence time, hygienic 316L or duplex construction, and tight metastable-zone-width control, vacuum cooling is the standard route for lysine, MSG, citric acid, and many API intermediates.
Lithium carbonate has inverse solubility — its solubility drops from ~13 g/L at 20 °C to ~7 g/L at 100 °C. Hot evaporative DTB crystallization above 90 °C exploits this property to precipitate battery-grade Li₂CO₃. The same inverse solubility drives wall-scaling risk, because the hottest surface in the system (the heat-transfer tube wall) is where solubility is lowest — which is why titanium / Duplex 2205 construction and tight ΔT control across the heater are mandatory.
The metastable zone is the concentration–temperature window between the saturation line and the spontaneous-nucleation line. Inside the zone, existing crystals grow but few new nuclei form — giving controlled PSD. Outside it, spontaneous nucleation floods the magma with fines and broadens PSD. Lab measurement of metastable-zone width (typically via polythermal method) is required before specifying operating ΔC, cooling ramp or evaporation rate for any quality-critical crystallization.
If product spec is not your dominant driver, one of these lines may fit better.
Preliminary screening: T4 · Crystallizer Selector → · T1 · Evaporation Calculator →
Share your solubility data, target purity and PSD, throughput and feed composition. We will respond with a supersaturation method + crystal growth configuration recommendation, indicative sizing and material selection within 2 business days.
Send your feed characterization (TDS, COD, main salts, viscosity), throughput and product targets — we respond with a preliminary process route within two business days.
