Treatment Technologies
Electrochemical Water Treatment Companies
Electrocoagulation, electrooxidation, and EDR providers for heavy metals, emulsions, and hard-to-treat industrial streams.
This page is a good fit if you need:
- Flat Sheet UF Membranes or Hollow Fiber RO capabilities
- Suppliers with food-beverage sector experience
- Providers operating in China or Indonesia
- Providers
- 7
- Verified
- 4
- Countries
- 6
Can't find the right fit? Post a brief and let qualified suppliers come to you.
Post a projectHow to choose a electrochemical water treatment provider
Start with providers that clearly operate in your target geography and project footprint.
Look for industry exposure that matches your water challenge, compliance constraints, and deployment context.
Use technologies, service scope, and proof signals to narrow the list before reaching out to suppliers.
Not sure where to start? Our experts can help.
Filter results
Verified providers
4 claimed companies in this category
Country
Industry
Technology
Find a Electrochemical Water Treatment Provider
Showing 1-7 of 7
7 results from 7 matched providers
Electrochemical Processes for Water and Wastewater Treatment
Electrochemical water treatment covers electrocoagulation (EC), electrooxidation (EO), electrodialysis (ED/EDR), capacitive deionization (CDI), and electro-Fenton processes. Each generates reactive species or charge-driven separation in situ, eliminating bulk chemical dosing. Electrocoagulation uses sacrificial Fe or Al anodes to release coagulant ions at typical current densities of 20 to 100 A/m2, removing colloidal organics, heavy metals (Cr6+, As, Pb), oil emulsions, and color with sludge yields 30 to 50 percent lower than chemical coagulation. Electrooxidation with boron-doped diamond (BDD) or mixed-metal-oxide (MMO) anodes produces hydroxyl radicals capable of mineralizing PFAS, pharmaceuticals, and 1,4-dioxane to COD under 30 mg/L.
Electrodialysis and EDR (reversal) separate dissolved ions through ion-selective membranes under DC potential, achieving 90 to 95 percent desalination at TDS 500 to 10,000 mg/L with energy demand 0.7 to 2.5 kWh per m3, typically below RO at low TDS. Capacitive deionization is emerging for brackish water under 3,000 mg/L TDS, with energy as low as 0.4 kWh per m3 and zero pressurization. Critical design parameters: current density, current efficiency (target above 85 percent), electrode lifetime (BDD 5 to 10 years, MMO 2 to 5 years, sacrificial Al/Fe consumed per Faraday law at about 0.34 g per Ah Al), and specific energy consumption (kWh per m3 or kWh per kg COD removed).
Aguato lists electrochemical treatment providers across EC, EO, ED/EDR, CDI, and electro-Fenton categories with applications spanning landfill leachate, produced water, semiconductor CMP wastewater, PFAS destruction, and brackish desalination. Shortlist criteria: pilot-test data on your actual matrix (electrochemistry is highly matrix-dependent), electrode lifetime warranty, specific energy consumption guarantee, and a clear plan for hydrogen off-gas management (LEL 4 percent in air, explosion risk if not vented per NFPA 2).
Frequently Asked Questions
When does electrocoagulation beat conventional chemical coagulation?
EC wins on high-emulsion oily wastewater (refineries, metal-finishing rinses), heavy-metal removal where chemical co-precipitation generates excess hydroxide sludge, and remote sites where chemical logistics are difficult. EC sludge volumes typically run 30 to 50 percent lower than alum or ferric coagulation, and the sludge is more dewaterable (often reaches 25 to 35 percent solids on a belt press). EC underperforms when feed alkalinity is low (under 50 mg/L as CaCO3: pH crashes), when target species are dissolved organics not destabilized by metal hydroxides, and when fouling species (Si, Mg) passivate the anodes faster than design life.
Can electrooxidation destroy PFAS?
Yes: boron-doped diamond (BDD) anodes at current densities 200 to 500 A/m2 produce hydroxyl radicals and direct electron transfer capable of mineralizing long-chain PFAS (PFOA, PFOS) to fluoride and CO2 with over 99 percent removal in 4 to 8 hours residence time. PFAS-EO works best on concentrated streams (post-IX regen, RO concentrate, foam fractionate) where TDS 5,000 to 50,000 mg/L. Specific energy is 50 to 200 kWh per m3: too costly for dilute streams (under 10 ug/L). Pair with foam fractionation or IX upstream to concentrate the load. Validate against EPA Method 533 or 537.1 with NDAA-listed labs.
How long do electrochemical electrodes last?
Boron-doped diamond on Nb or Si substrate: 5 to 10 years at under 500 A/m2 in neutral pH; under 2 years in fluoride-rich or strongly acidic service. Mixed-metal-oxide (Ti-Ru-Ir-Ta): 2 to 5 years at under 300 A/m2. Sacrificial aluminum or iron (EC): consumed per Faraday law: 0.34 g Al per Ah or 1.04 g Fe per Ah of current passed, with electrode-replacement frequency driven by plate thickness (typical 6 to 12 mm plates run 6 to 24 months). Specify electrode warranty as kWh-throughput or m3-treated rather than calendar years to align supplier incentive with real wear.
What hydrogen safety measures are required for electrochemical systems?
Cathodic water reduction generates H2 at about 0.42 mL per Ah of current passed. At 100 A through a 10-cell stack that is roughly 2.5 L H2 per min. NFPA 2 and IEC 60079 require: (1) sealed reactor with continuous N2 or air purge keeping headspace H2 under 25 percent of LEL (under 1 percent v/v); (2) explosion-proof or non-sparking electrical fittings in the gas space; (3) LEL gas detection with auto-shutdown at 20 percent LEL; (4) vent stack discharging at least 3 m above any ignition source and 5 m from intakes; (5) ATEX/IECEx Zone 1 classification for the cell room. Skip these and you have an explosion event waiting to happen.
A semiconductor fab in South Wales generated 400 m3/day of CMP (chemical mechanical planarization) wastewater containing silica particles, copper at 50 to 200 mg/L, and ammonia at 80 to 150 mg/L. Conventional coagulation-flocculation produced sludge volumes too large for the site disposal contract and failed to achieve copper below 1 mg/L for Trade Effluent Consent compliance.
Installed a continuous electrocoagulation (EC) unit using sacrificial iron anodes at 60 A/m2 current density, replacing the ferric sulphate dosing system. The EC process reduced copper to below 0.3 mg/L and TSS to below 30 mg/L in a single pass. Sludge volume fell 45 percent versus chemical coagulation (less non-process iron added). Added a compact H2 management skid with ATEX Zone 1 classification: forced air purge, LEL detector, and auto-shutdown at 20 percent LEL.
Trade Effluent Consent compliance on copper (limit 1 mg/L) achieved at 95th-percentile 0.28 mg/L. Sludge disposal cost reduced by 38 percent. Eliminated 40 tonnes per year of ferric sulphate chemical deliveries. Capital payback achieved in 2.8 years versus chemical treatment running costs.
Questions to Ask Shortlisted Providers
- 1
Have you pilot-tested this process on our actual wastewater matrix, and can you provide the pilot data?
Electrochemical processes are highly matrix-dependent: conductivity, pH, competing ions, and organic load all affect removal efficiency. Pilot data on your specific matrix is the only reliable predictor of full-scale performance. Generic references from different wastewaters should not be accepted as equivalent.
- 2
What electrode lifetime warranty do you offer, and how is it expressed: calendar years, kWh throughput, or m3 treated?
Electrode lifetime is the dominant operating cost. A warranty expressed in calendar years misaligns supplier incentive with actual wear. kWh throughput or m3 treated warranties properly tie the supplier's obligation to actual utilisation.
- 3
What specific energy consumption (kWh per m3) do you guarantee, and at what current density and removal target?
Specific energy is the primary OPEX driver for electrochemical systems and should be guaranteed at your operating conditions, not at the most favourable lab conditions. Understand the sensitivity: doubling current density typically quadruples energy consumption but only doubles reaction rate.
- 4
How is hydrogen off-gas managed, and what ATEX or IECEx zone classification applies to the cell room?
Hydrogen generation is inherent to electrochemical processes and is a legal safety obligation under DSEAR 2002 in the UK. If the supplier has not provided an ATEX zone classification and confirmed explosion-proof electrical fittings for the cell room, this is a compliance gap that transfers liability to the operator.
- 5
What are the electrode replacement procedure, downtime, and lead time for replacement electrodes from your UK stocking point?
Electrode replacement requires system shutdown. If lead time is 8 to 12 weeks from an overseas factory, the plant has unacceptable operational risk. Confirm stocked electrodes in the UK or EU, planned maintenance window requirements, and whether the system can be partially operational during electrode change-out.
What Drives Cost in This Category
Boron-doped diamond (BDD) electrodes cost 5 to 15x more than mixed-metal-oxide (MMO) or sacrificial iron/aluminium, but last 5 to 10 years versus 1 to 3 years for MMO and weeks for sacrificial at high current density. For continuous-duty industrial service, BDD total cost of ownership is often lower despite higher upfront cost.
Specific energy ranges from 0.5 to 2 kWh per m3 for electrocoagulation to 50 to 200 kWh per m3 for PFAS destruction by electrooxidation. At UK industrial electricity prices of 15 to 25 p per kWh, high-energy applications become the dominant OPEX line and must be modelled against alternative treatment technologies before committing to electrochemical.
Electrochemical processes require minimum conductivity of 500 to 1,000 uS/cm for efficient ion transfer. Low-conductivity feedwaters (surface water under 100 uS/cm, clean process rinses) require electrolyte addition (NaCl or Na2SO4), adding 0.1 to 0.5 GBP per m3 in chemical cost and a consent consideration if chloride or sulphate limits apply.
ATEX-rated enclosures, forced-ventilation skids, LEL detection, and explosion-proof electrical installations add 10 to 25 percent to system CAPEX. These costs are non-negotiable under DSEAR 2002 and omitting them creates unlimited liability under the Health and Safety at Work Act 1974.
Key Regulations & Standards
The Dangerous Substances and Explosive Atmospheres Regulations 2002 require the operator to carry out an explosion risk assessment for any area where hydrogen (generated by electrochemical cells) may form an explosive atmosphere. The cell room is typically classified ATEX Zone 1 (explosive atmosphere likely under normal operating conditions). Electrical equipment must be certified IECEx or ATEX Group IIC (hydrogen service).
Treated effluent from electrochemical systems discharging to public sewer requires Trade Effluent Consent. Electrocoagulation adds iron or aluminium to the effluent stream (Faraday law: 0.34 g Al per Ah or 1.04 g Fe per Ah); residual dissolved metals must be below consent limits. Chlorine generated from chloride-containing feeds (chloro-oxidation) must be quenched before discharge.
Boron-doped diamond electrode fabrication and MMO electrode manufacturing use substances subject to UK REACH (retained EU REACH Regulation 1907/2006). By-products of electrooxidation on chloride-containing feeds may include chlorate and perchlorate, which are regulated substances under WS(WQ)R 2016 for potable water applications. Confirm by-product formation profile with the supplier before commissioning.
Spent electrodes from electrocoagulation (iron/aluminium with adsorbed heavy metals) and MMO electrodes (Ru, Ir, Ti-based) may be classified as hazardous waste under the UK Hazardous Waste Regulations 2005 depending on the treated wastewater composition. A pre-disposal waste characterisation test is required. Confirm disposal route and cost with a licensed hazardous waste carrier before commissioning.