Glycol System Corrosion and Passivation Contractor in Tennessee

Yes, across Memphis, Nashville and statewide: fluid and system assessment, loop cleaning and flushing, passivation to ASTM A967 with cleaning per ASTM A380 on stainless components, and setting up a testing regime. We start with the fluid, because on these systems that is usually where the problem is.

Because they contain several dissimilar metals sharing one conductive fluid, which is a galvanic arrangement. What prevents it destroying the system is the inhibitor package forming protective films, and the inhibitor is consumed while doing that job. As it depletes, attack begins on the least noble metal present.

Because a closed loop circulates what it produces. Dissolved copper released at one point can deposit on aluminium or steel elsewhere, creating new galvanic couples where none existed. A system with copper corrosion does not remain a copper problem, which is why these failures tend to be system-wide by the time they are found.

Very possibly. Circulating corrosion products deposit on heat exchange surfaces and degrade performance progressively. The unhelpful response is running the system harder, which raises temperature and accelerates the glycol degradation that started the sequence. Test the fluid before adding capacity.

Where testing shows the inhibitor depleting but the fluid is otherwise sound and the supplier supports replenishment, yes, and it is much cheaper than replacement. That option is only available if you find out early, which is the practical argument for routine testing rather than waiting for a symptom.

Where damage has occurred, yes. Putting fresh inhibited fluid into a system full of corrosion products consumes the new inhibitor rapidly on the debris rather than on protection, so the new charge fails early. Flushing is part of the remedy rather than an optional extra.

Only the stainless part, which is usually the part coping best. Cleaning to ASTM A380 and passivating to ASTM A967 restores a proper passive film on stainless components and is worthwhile where they have been attacked or carry free iron or weld heat tint. It does nothing for copper, aluminium or steel in the same loop, and nothing for the fluid.

The least noble one present, which in most glycol loops means aluminium components or steel pipework. Aluminium failing first in a mixed loop with depleted inhibitor is the classic pattern, and it is worth recognizing because it points at the fluid rather than at the component that failed.

Barely for the work itself. It has an indirect bearing: cheap power at 6.21 cents per kilowatt-hour against a national average of 8.13 (EIA, 2024) makes it easier to compensate for declining heat transfer by running harder, which masks the underlying fluid problem for longer and makes the eventual damage worse.

Use the form on this page or call 201-450-8280. Useful inputs are the loop volume, which metals are present, the most recent fluid test results and when they were taken, where leaks or damage have appeared, and whether heat transfer performance has been declining.

A secondary loop typically contains steel pipework, copper coils and fittings, brass or bronze components, stainless heat exchangers and sometimes aluminium, all in one conductive fluid. That is a set of galvanic couples held in solution, and once the inhibitors fail each one becomes active.

It is, because aluminium requires an inhibitor package formulated for it and is attacked rapidly by packages that are not. A loop containing aluminium components charged with a fluid inhibited for ferrous and copper metals can lose those components quickly, and the substitution is often made without anyone checking.

Because corrosion products circulate. Once metal is being attacked anywhere, the debris travels, deposits in heat exchangers and low-velocity regions, and creates under-deposit conditions that initiate corrosion in places that were previously sound. A local problem becomes a system problem through the fluid.

It does at both ends. Low velocity allows deposits to settle and creates under-deposit attack, and excessive velocity in copper components causes erosion-corrosion that strips the protective film mechanically. Loops modified over the years frequently end up with both conditions in different branches.

They do, wherever a branch has been isolated or a circuit decommissioned without removal, and those sections hold stagnant degraded fluid that exchanges slowly with the rest. They are also the places where sampling gives a misleading picture, in either direction.

By the condition of the flush water at the end, by inspecting strainers and filters for the debris they collect, and where the system has been badly affected, by opening a heat exchanger to see the surfaces. A flush judged complete by volume rather than by result frequently leaves deposits in place.

One formulated for every metal in the loop, which requires knowing what those metals are, including components added over the years. The most common recharge error is selecting a fluid on glycol type and concentration alone without confirming the inhibitor package suits the system’s actual metallurgy.

Largely, through a closed system that does not draw in air, treated makeup water, a correctly matched inhibitor package, and annual testing that catches inhibitor depletion before the pH falls. The cost of that programme is trivial against a recharge and heat exchanger replacement.

By testing at intervals from the start, so that the depletion rate for that system is known rather than assumed, and by correcting the conditions that caused the previous failure. Recharging without addressing air ingress or makeup water quality simply restarts the same clock.

That air is entering wherever the system runs below atmospheric pressure, and that makeup water is being added, both of which accelerate degradation. A loop with a chronic small leak degrades far faster than a sealed one, so leak repair is fluid life protection rather than a housekeeping matter.

Where performance has declined or the fluid has been degraded, yes, because that is where deposits concentrate and where the consequence of fouling is felt. Opening a plate pack is the only way to see whether a flush achieved anything in the place it mattered most.

Fluid test results trended over time, makeup volumes, the metallurgy of the loop including later modifications, the inhibitor package in use, and the history of flushes and recharges. Plants with that record manage the fluid; plants without it replace equipment and wonder why.

A side-stream filter is inexpensive and catches the particulate that otherwise abrades seals and fouls exchangers, and it also acts as an indicator: what it collects tells you whether corrosion is active. It is one of the few maintenance items on a secondary loop that pays for itself repeatedly.

Coupons installed in a flowing section give a direct measure of attack rate on the metals of interest and are far cheaper than discovering the rate through a failure. They suit systems where the metallurgy is mixed and the history is unknown, which describes most older secondary loops.

Test the fluid and establish what metals are in the system, because every subsequent decision depends on those two facts. Recharging, treating or flushing without knowing the metallurgy and the fluid’s condition is how the wrong inhibitor package gets installed in a system that then fails faster.

Not through the whole loop. A secondary refrigerant system contains copper, brass and aluminium alongside steel, and citric acid attacks several of those. Any passivation on a mixed-metal system is done on isolated stainless sections with the dissimilar components removed or valved out, which is a very different job from circulating a water loop.

Inhibitor package management. The corrosion control in a glycol loop is chemical treatment monitored and topped up on a schedule, not a surface treatment. Depleted inhibitor is the root cause on most of these systems, and passivation of the stainless portion does nothing for the copper and aluminium that are failing.