Reuse, Recovery & Stormwater
Brine Treatment Companies
Brine concentration, crystallization, and disposal providers for desalination and industrial waste streams.
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Brine Treatment: From Volume Reduction to Zero Liquid Discharge
Brine treatment addresses the concentrated reject streams from RO, ion exchange regeneration, cooling tower blowdown, and industrial processes — typically 5,000–250,000 mg/L TDS. Treatment objectives range from volume reduction (2–5× via secondary RO or electrodialysis reversal) to zero liquid discharge (ZLD) producing salt cake at <5% moisture. Technology stack: HEROⓇ or HERO-like chemically softened RO operating at pH 10–11 to push recovery to 95%; mechanical vapor compression (MVC) evaporators with COP 15–25 producing 70,000–250,000 mg/L brine at 12–25 kWh/m³; crystallizers (forced-circulation or DT-type) producing salt at 40–60 kWh/m³ feed.
Pre-treatment for evaporators is critical: silica <120 mg/L, hardness <5 mg/L as CaCO₃, organics <10 mg/L TOC to prevent scaling and fouling of high-flux heat exchangers. Lime-soda softening or pellet reactors reduce hardness; degassing removes CO₂ and H₂S. Material selection: super-duplex stainless steel (UNS S32750) or titanium grade 7 for brines >50,000 mg/L chloride at temperatures >60°C; standard 316L only suitable for <10,000 mg/L Cl⁻. Crystallizer salt purity 95–99% NaCl achievable from chloride-dominant brines, enabling sale to chlor-alkali, road salt, or industrial markets at $40–100/tonne.
Emerging technologies: electrodialysis reversal (EDR) for organic-laden brines (membrane fouling tolerant), forward osmosis (FO) for high-temperature or high-fouling streams, membrane distillation (MD) using waste heat <80°C, and selective electrodialysis for resource recovery (lithium from oilfield brines at 200–1,500 mg/L Li, magnesium for fertilizers). Regulatory drivers: EU Industrial Emissions Directive 2010/75/EU BAT for water discharge, US EPA NPDES variability requirements, ZLD mandates in Indian textile and Chinese coal-chemical sectors. Aguato lists brine-treatment providers across volume-reduction, ZLD, and resource-recovery applications.
Frequently Asked Questions
When is ZLD justified vs. partial brine treatment?
ZLD is justified when concentrate disposal cost exceeds $1.50 to $2.50/m3 (typical inland sites with no deep-well injection option), when discharge permit is unavailable (zero-discharge zones in India, China, or the US arid west), or when the salt by-product has market value above $60/tonne for chlor-alkali grade NaCl. Partial brine treatment (volume reduction to 30 to 50% via MVC) is more cost-effective where disposal is available at below $1/m3. Typical capex saving is 40 to 60% versus full ZLD. Run a lifecycle TCO over 20 years before committing to ZLD.
What is HERO and how does it differ from standard RO?
HERO (High Efficiency Reverse Osmosis) operates RO at pH 10 to 11 after chemical softening to remove hardness and silica below saturation limits. At alkaline pH, silica solubility increases 10 to 50 times, allowing recovery to push from 75% (standard BWRO) to 95% on high-silica feeds. Capex is 30 to 60% higher than standard BWRO due to softening (lime, soda ash, ion exchange) and caustic-resistant materials, but reduces downstream brine volume by 4 to 5 times, dramatically cutting evaporator size and energy in ZLD trains.
What is the energy consumption of evaporation-based brine treatment?
Mechanical Vapour Compression (MVC) evaporators consume 12 to 25 kWh/m3 feed water, the dominant ZLD energy load. Forced-circulation crystallisers add 40 to 60 kWh/m3 of crystalliser feed. Multi-effect distillation (MED) using steam achieves 1.8 to 2.5 kWh thermal/m3 per effect with 4 to 8 effects. Total ZLD energy at $0.10/kWh equals $1.50 to $3.50/m3, dominated by evaporation. Waste-heat integration (refinery, power plant, cement) cuts this 40 to 70%. Siting next to a heat source is the single biggest ZLD cost lever.
Can I recover useful salts from brine, not just dispose of them?
Yes. Selective crystallisation fractionates mixed brines into commercial grades. Sequential cooling crystallisation separates Na2SO4 (Glauber's salt) at below 0 degrees C from NaCl at 20 degrees C; evaporative crystallisation separates CaSO4, then NaCl, then KCl. Selective electrodialysis recovers lithium (battery-grade Li2CO3 at $7,000 to $15,000/tonne from oilfield brines at 200 to 1,500 mg/L Li), magnesium, and bromine. Resource-recovery economics work above approximately $80/tonne salt and require consistent feed composition; high-variability industrial brines often cannot meet purity specs without upstream blending.
The power station's cooling tower blowdown at 28,000 mg/L TDS was subject to a Trade Effluent Consent limit of 2,000 mg/L chloride before sewer discharge. The discharge was failing consent due to rising cycle of concentration, with chloride reaching 6,500 mg/L. A ZLD solution was required before the EA would renew the site's Environmental Permit.
A HERO RO secondary stage was installed after softening (lime-soda, pellet reactor) to achieve 95% overall water recovery, reducing blowdown to 1.75 m3/hr brine at 180,000 mg/L TDS. An MVC evaporator concentrated the brine to 320,000 mg/L, and a forced-circulation crystalliser produced a sodium chloride cake for road-salt disposal at GBP 55/tonne.
Zero liquid discharge achieved. Environmental Permit renewed without challenge. Site water consumption fell 68% from eliminated blowdown. Salt cake production was 580 tonnes/year. Total capital cost was GBP 4.2M; operating cost GBP 380,000/year at GBP 0.16/kWh electricity.
Questions to Ask Shortlisted Providers
- 1
What overall water recovery are you designing for, and what is the specific energy at that recovery including MVC and crystallisation?
ZLD energy is dominated by evaporation. A 5% difference in evaporator COP on a 30 m3/hr system adds GBP 60K to GBP 120K/year in electricity cost. Specific energy quoted at a system level (not just blower shaft power) is the only meaningful metric for TCO comparison.
- 2
What pre-treatment do you require upstream of the evaporator to prevent silica, calcium, and organics fouling of heat exchange surfaces?
MVC evaporators with silica above 120 mg/L or hardness above 5 mg/L CaCO3 on the evaporator feed will scale within weeks. Pre-treatment scope (softening, degassing, media filtration) drives 20 to 30% of ZLD capital cost and is frequently underspecified in proposals.
- 3
What material specification do you use for evaporator and crystalliser bodies in contact with brines above 50,000 mg/L chloride at 80 degrees C?
316L stainless steel corrodes rapidly above 10,000 mg/L chloride at elevated temperature. Super-duplex (UNS S32750) or titanium grade 7 is required. Using incorrect materials leads to vessel perforation within 2 to 5 years, creating a catastrophic maintenance liability.
- 4
What is the purity and market specification of the salt cake you produce and who buys it?
ZLD crystalliser salt may contain 5 to 15% impurities (CaSO4, MgCl2, calcium carbonate) that make it unsuitable for chlor-alkali markets. Road salt disposal at GBP 40 to GBP 60/tonne is the realistic off-take for most industrial ZLD plants, not the chlor-alkali premium price sometimes cited.
- 5
What are the EA permit conditions for your proposed ZLD installation, and how have you addressed the solid waste classification of the salt cake?
Salt cake from ZLD crystallisers is classified as industrial solid waste in the UK under the Waste Framework Directive. Disposal to landfill requires a Hazardous Waste Consignment Note if the brine contains classified hazardous substances. Salt sold to road-salt markets must meet product standards, not waste classifications.
What Drives Cost in This Category
MVC at 15 to 20 kWh/m3 feed on a 30 m3/hr plant consumes 3,600 to 4,800 MWh/year. At GBP 0.16/kWh, this is GBP 576K to GBP 768K/year in electricity alone. For many ZLD projects, electricity is 60 to 75% of total operating cost.
Lime-soda softening plus pellet reactor ahead of HERO RO and MVC costs GBP 400K to GBP 1.2M capital for a 30 m3/hr ZLD system. Skimping on pre-treatment causes evaporator fouling that costs GBP 50K to GBP 200K/year in cleaning and replacement parts.
Super-duplex stainless or titanium evaporator bodies cost 2 to 3 times the equivalent 316L, adding GBP 300K to GBP 800K to capital. This cost is non-negotiable above 50,000 mg/L chloride and is often omitted from low-price ZLD proposals.
If the salt meets road-salt specifications, disposal income of GBP 40 to GBP 60/tonne partially offsets operating cost. If contaminated with calcium sulphate or organics, it is classified as industrial waste costing GBP 70 to GBP 120/tonne to landfill, reversing the economics entirely.
Key Regulations & Standards
ZLD installations at industrial sites in England require an Environmental Permit covering the evaporation and crystallisation operations as industrial waste treatment activities. The permit application requires BAT assessment, waste management plan, and air quality assessment for evaporator vapour management.
Large industrial plants operating ZLD brine treatment as part of a permitted installation must demonstrate compliance with BAT-AEL (Associated Emission Levels) for water and waste. UK IPPC permits incorporate IED requirements for water treatment technology.
If cooling tower blowdown or industrial brine contains classified hazardous substances (chromates, biocides, heavy metals), the ZLD salt cake is hazardous waste and requires a Hazardous Waste Consignment Note for disposal under the 2005 Regulations. This significantly changes disposal costs and route options.
Any ZLD system that avoids sewer discharge eliminates the need for Trade Effluent Consent, removing the sewer discharge tariff (typically GBP 0.50 to GBP 2/m3). Confirming permit conditions with the local sewerage undertaker is essential before finalising the concentrate disposal strategy.