KHC-F2001 Read as a Specification Sheet: Carrier, Dual Acidity and Service Life

Ozone catalysts are usually sold on one number, and that number is nearly always a COD removal percentage. It is the least informative figure on the sheet. Removal depends on the water, the dose, the contact time and the reactor, so a percentage quoted without those conditions describes the test rather than the product. What does predict field behaviour is the combination of carrier chemistry, active-site design and physical strength — which is what the KHC-F2001 specification actually documents.

Carrier: why a composite oxide rather than alumina

The carrier is a silica-alumina composite oxide, produced through a sol-gel composite sintering process. Against single alumina or conventional carriers, the composite structure delivers both chemical stability and thermal stability at once, and that pairing is the foundation for long-term operation in strongly acidic or alkaline and high-salinity environments.

That matters more than it sounds. Ozone catalytic oxidation of industrial wastewater frequently runs at low pH — landfill leachate, dye effluent and many chemical streams sit well below neutral — and alumina alone will slowly lose surface area and strength under those conditions. A silica component in the lattice changes the picture: it suppresses the phase transformation that degrades pure alumina and holds the pore structure open across the service life. Thermal stability then covers the regeneration step, which is where a weaker carrier fails quietly and then catastrophically.

Active sites: two acidities, not one

The carrier surface hosts a large number of Lewis acid sites and Bronsted acid sites, forming a dual-acidity catalytic system that promotes reactant adsorption, activation and conversion. Multi-metal active components including manganese, iron and cobalt are then loaded for synergistic catalysis, which is what gives broad-spectrum oxidation across different organic pollutants rather than selectivity for one class.

The division of labour is worth understanding before comparing catalysts. Lewis sites coordinate electron-rich functional groups and pull organics onto the surface; Bronsted sites donate protons and help generate the hydroxyl radicals that do the actual mineralisation. A catalyst with only one type will perform on some pollutants and stall on others — which is exactly the pattern sites report when they switch products and find the removal rate changes shape rather than scale.

The specification, item by item

This is the part of the sheet that can be designed against:

• Appearance: spherical particles, available sizes 3~5 mm, customizable.
• Specific surface area 300~500 m²/g.
• Bulk density 0.6~0.8 g/cm³.
• Crush strength at least 120 N/particle; attrition rate no more than 1%.
• Applicable pH 2~12; service life 5~8 years.
• Ozone decomposition rate at least 95%; COD removal rate at least 75%; colour removal rate at least 98%.

Against conventional ozone oxidation, the COD removal rate increases by more than 30% and ozone utilisation by more than 50%. Those two comparisons are the commercial case, and they are also the two that must be verified on the actual stream, because utilisation gain depends on how the reactor is configured as much as on the catalyst.

From specification to field result

Specifications only mean something when they survive real water. In the landfill leachate case run by SINOKLE, raw water at a COD of 20000 mg/L — high salinity, heavy humus content and poor biodegradability — enters the KHC-F2001 catalytic oxidation unit after biochemical pretreatment. The catalytic unit achieves 99.5% COD removal, and the system effluent holds stable below 100 mg/L.

Two things about that case are worth extracting. The first is the load: a feed at 20000 mg/L is not a polishing duty, it is a destruction duty, and a catalyst that survives it is being tested on strength and fouling resistance as much as on activity. The second is the stability claim, which is the harder one: an effluent that holds below 100 mg/L over time implies the active sites are not being progressively poisoned by the humic fraction, and that the carrier is not shedding material into the bed.

Integration and selection

KHC-F2001 pairs with CDFU cyclonic dissolved air flotation and CDOF ozone oxidation equipment to build a process chain of front-end flotation pretreatment followed by silica-alumina-based ozone catalytic deep oxidation. The ordering is deliberate: flotation removes free and emulsified oil and suspended solids that would otherwise blind the catalyst surface, and the catalytic stage then works on dissolved organics at a much lower fouling load.

Within the product family it complements the carbon-based KHC-F1001, and the split is straightforward. Choose the silica-alumina-based catalyst where strength, long-term stability and resistance to complex water quality dominate — high salinity, low pH, abrasive service. Choose the carbon-based grade for adsorption-driven, cost-sensitive applications where the organic load is moderate and the budget is the binding constraint.

Six dimensions that have to interlock

Viewed as a technology chain rather than a product, the logic runs in six linked steps. The silica-alumina carrier provides a stable foundation. Dual-acidity sites ensure adsorption and activation efficiency. Multi-metal synergy amplifies catalytic activity. Hydrophilic modification improves mass transfer. High-strength forming supports a life of 5~8 years. Regeneration capability lowers whole-life cost. No single step carries the result; a weak carrier destroys the value of good active sites, and strong forming without hydrophilicity produces a durable pellet that transfers poorly.

Of those six, super-hydrophilicity is the one most often overlooked and most consequential in continuous duty. Because the surface is optimised for wettability, it contacts the water phase fully, so ozone and pollutants transfer more efficiently, the oxidation reaction runs faster and treatment stays stable. Under sustained high load, mass-transfer efficiency sets the reactor's real treatment capacity — not the catalyst mass, and not the nominal surface area.

What this means for a design basis

For engineering teams, the practical value is that surface area, strength, attrition rate, pH range and service life all arrive as explicit specifications, so process design, operation and maintenance planning, and cost estimation can rest on data rather than on a demonstration video. Two cautions complete the picture. A 5~8 year life assumes the bed is not being crushed by a support grid that was specified too lightly, and a 95% ozone decomposition figure assumes the reactor gives the gas enough contact time to reach the catalyst at all.

Reduced to its essentials, the design answers three questions separately. The carrier solves the problem of withstanding the environment. The dual-acidity sites and multi-metal loading solve the problem of driving the reaction. High-strength forming plus regenerability solve the problem of lasting long enough to be economic. When all three are answered, the headline figures of at least 75% COD removal, at least 98% colour removal and a 5~8 year service life follow as consequences rather than as claims.