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Technology

Selecting a membrane system means working through hard constraints: rejection targets, osmotic pressure, fouling potential, viscosity, temperature, sanitary requirements and cleaning chemistry all narrow the field, and lifecycle cost decides between what remains. We work across the full range of classes and formats rather than promoting any single one.

The toolbox

Membrane classes

Pressure-driven membranes span four classes, ordered by how fine a separation they make. The finer the separation, the higher the pressure — and the more the design revolves around osmotic pressure, scaling limits and energy.

Class	Separation range	Retains	Characteristic duties
MF	0.1–10 µm	Suspended solids, bacteria, fat globules, casein micelles	Clarification, bacteria removal, milk fractionation
UF	~1–500 kDa MWCO	Colloids, macromolecules, proteins, viruses, oil emulsions	Pathogen barrier, protein concentration, pretreatment to NF/RO
NF	~150–1000 Da; charged-solute selective	Divalent ions, sugars, dyes, organics, hardness, color	Softening, lactose concentration, dye and caustic recovery, PFAS-tight duties
RO	<~100 Da	Dissolved salts and most low-molecular-weight organics	Desalination, demineralization, volume reduction, reuse polishing

Fundamentals

The concepts that decide a design

Whether a proposal is sound usually comes down to a handful of quantities. These are the ones we check first in any design or audit — and the vocabulary you will meet in our reports.

Cross-flow vs. dead-end

In cross-flow operation, feed sweeps along the membrane and continuously carries rejected material away with the concentrate; in dead-end operation, everything is pushed onto the membrane and removed by periodic backwash. Fouling-prone streams demand cross-flow; clean waters can run dead-end at lower energy. Format and mode must match the stream.

Recovery

The share of feed that becomes permeate. Higher recovery means less feed and a smaller concentrate — but concentrates every dissolved constituent toward its scaling or osmotic limit. Overstated recovery is the single most common flaw in optimistic proposals.

Flux

Permeate flow per membrane area (L/m²·h). Conservative flux means more membrane area and higher CAPEX, but slower fouling and longer element life. Aggressive flux does the opposite. Getting this trade-off right is a lifecycle-cost calculation.

Rejection & salt passage

How completely the membrane retains a given solute. Rejection differs by ion and molecule — boron, silica, nitrate and small neutral organics pass more easily than the conductivity number suggests. Product specifications must be checked constituent by constituent.

Fouling & scaling

Particulates, organics and biology foul the surface; sparingly soluble salts (CaCO₃, CaSO₄, silica) scale it as recovery rises. Managed by pretreatment, antiscalant dosing, flux discipline and cleaning — and predicted by indices (SDI, LSI/S&DSI) plus, where it matters, piloting.

CIP & normalization

Cleaning-in-place restores performance if run with the right chemistry, temperature and sequence. Normalization corrects operating data for temperature and pressure so that true fouling trends are visible from day one — the difference between scheduled cleaning and crisis cleaning.

Hardware

Module formats

The same membrane chemistry is packaged in very different geometries. The right choice depends on solids, viscosity, fouling potential and the cleaning chemistry the duty demands.

Format	Typical duty	Notes
Spiral-wound (polymeric)	RO/NF/UF/MF on low-solids feeds; water, desalination, dairy (sanitary grades)	Best packing density and cost per m²; the default where the feed allows it
Hollow-fibre UF	Potable barriers, tertiary filtration, SWRO pretreatment	Pressurized or submerged; air-scour backwash regimes
Tubular (polymeric)	Viscous, high-solids effluents: digestate, leachate, oily streams	Tolerates what destroys spirals; higher energy per m³
Plate-and-frame / disc-tube (DTRO)	Leachate and difficult high-osmotic feeds	Open channels; high-pressure variants up to ~120–160 bar
Ceramic (MF/UF/NF)	Hot caustic recovery, aggressive CIP, oily and abrasive streams	Long service life offsets CAPEX in the right duty

Engineered around the membranes. Mechanical screening and media filtration; coagulation–flocculation and DAF; softening and ion-exchange stages; electrodeionization (EDI) for polishing; degassing contactors for O₂/CO₂ control; UV disinfection and remineralization on the product side; chemical dosing verified against element warranties; CIP systems; and — where concentration limits are reached — the interface to evaporation and crystallization for ZLD-type schemes.

Anatomy of a line

A representative RO/NF train

Actual configurations vary widely across applications, but the layout logic is similar everywhere: pretreatment protects the membranes, post-treatment protects the product.

Generic pressure-driven membrane train. The automation layer spans every stage — interlocks, sequencing, CIP recipes and normalized performance monitoring.

Reference points

Representative configurations by duty

These are starting points; each train is adapted to the actual analysis, flows and constraints.

Duty	Representative train
Brackish potable, 5–50 m³/h	Fe/Mn media → cartridge → antiscalant → 2:1 RO → calcite remineralization → UV
Pharma Purified Water	Softener → break tank → RO → EDI → UV; hot-water-sanitizable loop
SWRO, containerized	UF pretreatment → 5 µm cartridge → HP pump + isobaric ERD → SWRO → remineralization / blend
Landfill leachate	pH trim → DTRO stage 1 → DTRO stage 2 → permeate RO polish
Biogas digestate	Decanter/screen → tubular UF → RO; NH₃ stripping sidestream
Whey to WPC-80 + lactose	MF (fat/fines) → UF + diafiltration → NF (lactose) → RO (volume) → polisher
Juice clarification	Enzymation → cross-flow UF → optional RO pre-concentration

Get an independent projection for your duty

We model your feed in the same design suites the manufacturers use — then tell you where their proposals are conservative, and where they are optimistic.

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