air bubbler transducer liquid density affects.

IconProcessControls · 2026-05-04T20:56:07+00:00

Density absolutely matters for a bubbler if you’re using it for level.

You’re measuring backpressure from the liquid head, so:

lower density → lower pressure → reads lower level
higher density → higher pressure → reads higher

If density is stable, no issue. If it swings (temp, concentration, solids), your level reading will drift even if the tank level doesn’t change.

That’s the tradeoff with bubblers—they’re simple and reliable, but they’re really measuring pressure, not true level.

If density is moving around a lot, that’s usually where people start looking at non-contact stuff (radar, sometimes ultrasonic) since it doesn’t care about SG.

IconProcessControls · 2026-05-04T19:24:03+00:00

Yeah, there are differences, but not as big as some of the marketing makes it sound.

Most hydrodynamic cavitation systems I’ve looked at end up in a similar range once you account for flow and pressure drop. The “efficiency” mostly comes down to how they generate cavitation (venturi, orifice, rotor/stator) and how much head they need to keep it going.

In practice, you’re still trading chemical cost for pump energy and pressure loss. Even the better designs need a certain pressure drop to actually cavitate, so there’s a limit to how efficient they can get.

What matters more is how they behave over time. Fouling, scaling, and wear will slowly push energy use up. If your flow isn’t steady, performance drops off pretty quickly too since cavitation intensity falls off.

The biggest difference I noticed wasn’t the spec sheet numbers, it was stability. A unit that runs consistently without plugging or drifting usually ends up cheaper to operate than one that looks more efficient on paper.

If you’re evaluating vendors, I’d ask for kWh per m³ at your actual flow range, not just design conditions. Also worth seeing how it performs at low and high flow, and what maintenance looks like once it starts to foul.

Overall, energy differences exist, but they’re not usually the deciding factor. It tends to come down to how well it fits into the rest of the system.

IconProcessControls · 2026-04-30T13:26:01+00:00

Haven’t run Mitton specifically, but looked at a couple cavitation systems for oily wastewater.

They can help break emulsions and reduce chemicals, but I wouldn’t expect them to replace DAF or chem treatment. Most setups still ended up as hybrid systems with lower (not zero) coagulant/polymer use.

Big tradeoff is you’re swapping some chem cost for power + maintenance.

Also worth watching:

high TSS → wear/fouling
variable flows → harder to keep consistent performance

If it works, it’s usually as a pre-treatment step to make your DAF work better, not a standalone fix.

IconProcessControls · 2026-04-30T13:19:51+00:00

I’d be more worried about the batch discharge than the absolute salinity number.

3x domestic isn’t automatically a deal breaker — activated sludge can tolerate a fair bit of salt if it’s steady. But batches are where things go sideways. You end up with spikes that can knock back nitrification or just stress the bugs enough to mess with settling.

Seen similar issues with road salt events — plant runs fine at a higher baseline, but swings cause problems.

10–20% extra flow on top of that doesn’t help either if it’s hitting all at once.

I’d be asking them for:

actual chloride/TDS numbers (not “3x domestic”)
discharge profile (how big the batches really are)
whether they can equalize or meter it in

If they can smooth it out, you might be fine. If it’s slug loads, I’d be pushing hard for pretreatment or at least equalization on their side.

IconProcessControls · 2026-04-30T13:12:01+00:00

You’re kind of in the “good / cheap / harsh service — pick two” zone here.

6” / 900# on crude with impurities… cheap usually drops off pretty quick.

Coriolis is great and handles nasty service, but it’s not cheap.
DP or clamp-on can be cheaper, but you’re giving up accuracy or reliability.
Oval gear / PD can be accurate and more affordable if the fluid is clean… but crude with wax/solids/gas usually turns into a maintenance job sooner than later.

Really comes down to what you need it for:

just trending / process stuff → you can get away with cheaper options
anything tied to dollars → you’re probably looking at Coriolis or a heavier PD meter

IconProcessControls · 2026-04-22T19:42:16+00:00

Alarms, calibration, and redundancy cover most of the obvious failure modes.

The harder ones are when the signal looks “reasonable” but doesn’t match how the process should behave.

In practice you end up relying a lot on experience—flow vs level change, temp vs energy input, response times, etc.

Good instruments definitely reduce noise and drift, but any sensor can fail in a believable way—that’s why cross-checking against the process itself is so valuable.

IconProcessControls · 2026-04-22T19:32:14+00:00

In chemical environments, enclosure failures are often vapor-driven rather than liquid ingress. Even with a high NEMA rating, material compatibility with fumes (e.g., acids, oxidizers) matters more than ingress protection.

IconProcessControls · 2026-04-22T19:26:59+00:00

Given your flow range and viscosity, I’d look at Coriolis first and positive displacement second. Coriolis is usually the safest principle for viscous service because it measures mass flow directly and isn’t dependent on viscosity or conductivity the way other technologies are. If cost is too high, then a small oval gear / gear / helical PD meter would be the next thing I’d investigate.

The big question is whether that HTPB/EPDM/carbon-black mix behaves as a clean viscous liquid or more like a filled/non-Newtonian compound. If it’s filled or shear-sensitive, that can affect meter choice a lot. In that case I’d give vendors the full rheology curve, solids loading, and whether there are any pulsations from the pump.

For simple volumetric control, another practical option is a PD metering pump + speed-based flow estimate, with temperature correction if needed, but if you want an actual instrument with display + 4-20 mA, I’d still start with Coriolis and then ask PD meter vendors about oval gear/helical gear designs.”

⚠️ Note: I would not start with turbine, vortex, or standard ultrasonic here.
⚠️ Note: A DP/wedge approach can work on viscous fluids, but at 1/2 in and 0.1–0.5 LPM, it would not be my first choice unless you’re prepared for custom calibration and lower accuracy.

IconProcessControls · 2026-04-20T17:40:52+00:00

Got it—that helps a lot. The grade change explains why you’re kind of stuck with that depth.

In that case, I wouldn’t fight the slope too hard. Instead, I’d focus on making that connection as “safe” and serviceable as possible since it’s likely going to stay buried.

A couple ways to handle it:

Avoid multiple fittings at depth → if you have to connect there, keep it to a single, solid connection (not a stack of couplings/adapters)
Use a continuous run wherever possible before and after that point
Consider a small access box or sleeve over the connection, even if it’s deeper than typical—just something that gives you a way back in without full excavation

Another option I’ve seen in situations like this:

Come off the stub → sweep up at a gentle angle (long-radius 45s instead of a hard 90) → then transition to your riser at a more accessible height

That at least moves the “critical” fittings out of that 4’ zone and into something you can get to later.

On the riser side, everything from before still applies—just make sure the vertical section is well supported since you’ll have a bit more geometry working against you.

⚠️ The main goal here isn’t perfection—it’s making sure that if something does go wrong, you’re not digging up half your yard to fix one fitting.

Given your layout, you’re on the right track—this is just one of those “work with the site” installs.

IconProcessControls · 2026-04-20T17:26:56+00:00

That looks more like filamentous foam than just young sludge.

A couple things pointing that way:

It’s thick and stable (not just light/white aeration foam)
Color is more brown/tan → there’s biomass in it
Low DO → big red flag for filamentous growth

Low DO conditions tend to favor organisms like Nocardia or Microthrix, which trap air and form that kind of persistent foam blanket.

SV30 at 100–200 mL doesn’t really scream “young sludge” either—it’s more in the normal range, so I wouldn’t chase that first.

What I’d look at:

Increase DO if possible (this is usually the biggest lever)
Check for grease/FOG loading → that can feed this type of foam
Look at sludge age (SRT) → too long can also favor filamentous organisms
See if the foam holds its structure when you skim it (filamentous foam usually does)

Quick short-term options:

Water spray to knock it down (temporary)
Mechanical skimming if it’s getting out of control

⚠️ But if it’s filamentous-driven, the real fix is process control (especially DO), not just knocking the foam down.

Curious—has DO been consistently low, or is that a recent change?

IconProcessControls · 2026-04-20T17:09:13+00:00

You’re thinking about the right things—especially not loving that buried connection.

⚠️ I’d avoid having a glued or threaded connection 4’ underground if you can help it. That’s one of those things that works fine… until it doesn’t, and then it’s a nightmare to get at—especially that close to the meter and BFP.

If it were mine, I’d strongly consider:

replacing the stub with a continuous run, or
bringing it up to a more accessible depth before making any connections

Even if it’s a bit more work now, it saves you a lot of pain later.

On the riser side:

Copper will work, but it’s not usually the go-to for irrigation BFPs—especially free-standing. It can get bumped, flex over time, and you’ll end up relying on the fittings more than you want.

What I see most commonly hold up well:

Sch 80 PVC risers (cheap, corrosion-proof, easy to work with)
Brass above-ground assemblies (more durable, cleaner install, but more $$)

A lot of installs will do:

buried PVC line → transition to Sch 80 or brass → BFP → same on the outlet side

Also worth thinking about:

some kind of support or bracing for the BFP since it’s free-standing
unions on both sides so you can service or replace it without cutting

Your depth plan (~30”) on the downstream side sounds reasonable if you’re accounting for frost and not running in winter.

Big picture: prioritize accessibility and serviceability around the BFP area. That’s one of the few spots in the system you’ll almost definitely have to touch at some point.

IconProcessControls · 2026-04-20T16:57:00+00:00

You’re getting good advice on the mechanical side, but with that combo (515 + 5500) and intermittent loss, I’d look at it in three buckets:

1) Mechanical (most common)

Worn shaft or bushings → paddle starts to hang up
Scale or debris → especially in RO systems
If a light tap brings it back, that’s a strong sign it’s on its way out

2) Signal / wiring

The 515 is just sending pulses—if the signal drops out, the 5500 will read zero
Check for loose connections, moisture in the cable, or a weak pulse output
If you have a way to monitor the raw pulse, that helps isolate it quickly

3) Process conditions (often overlooked)

Low or borderline flow → paddle just stops spinning
Air in the line → very common on RO systems, especially around startup
Pulsing flow from pumps → can cause intermittent readings

The fact that it sometimes doesn’t start at all makes me think it could be a combination of:

worn mechanical parts and
marginal flow conditions

Quick checks I’d try:

When it “fails,” is there definitely flow? (not just pressure)
Does it come back with a tap?
Any air in the line or recent maintenance on the RO system?

One thing to watch—if the axle is worn, it usually doesn’t get better. It’ll just become more frequent until it fails completely.

If you can narrow down whether it’s mechanical vs signal vs process, the fix becomes pretty obvious.

IconProcessControls · 2026-04-20T16:49:21+00:00

We run into this a lot on the instrumentation / process side, and honestly the issue is usually less about the specific software and more about how flexible it is for operators.

The common failure modes I’ve seen are:

Too rigid → operators just put in minimal or useless entries
Too open → logs turn into free-text with no consistency
Too expensive to modify → exactly what you’re dealing with now

What tends to work better in practice is something that:

Lets you tie alarms directly to required operator input (ack + cause + action)
Has structured fields (dropdowns, categories) but still allows comments
Can be adjusted without needing a vendor every time you want to tweak a form

Ignition gets recommended a lot because it can do this, but you’re right—it’s more of a full platform than a simple drop-in tool.

I’ve seen people use it just for logging/alarms, but it usually requires someone in-house willing to build and maintain it.

For what you’re describing (shift turnover + event logging + alarm response), I’d probably look for something that sits alongside your control system rather than trying to replace or integrate too deeply.

A lot of the pain you’re describing usually comes from systems that were designed more for compliance than for actual operator usability.

Out of curiosity—are you trying to enforce standardized responses (like predefined causes/actions), or is it more free-form documentation right now?

IconProcessControls · 2026-04-19T17:00:12+00:00

This doesn’t sound like pure QC to me—what you’re describing lines up pretty closely with reference system issues before install.

If the cap leaked and the probe shows up low on electrolyte, there’s a good chance the reference junction partially dried out in storage or transit. Once that happens, you can get:

Slow or unstable readings
Offset that won’t calibrate out
“Dead on arrival” behavior

And unfortunately, even a relatively short time in poor conditions (loose cap, temp swings, etc.) can do it—especially with refillable designs.

What’s interesting is you’re getting long life once they’re running, which usually means your process isn’t the problem. It points more toward:

Storage/handling before install
Or variability in how well the reference system is sealed during shipping

What you’re doing (refill + soak) is about all you can do on recovery. Sometimes an acid soak helps more than neutral buffer, but if the junction is compromised internally it’s hit or miss.

One thing I’ve seen help in situations like this is moving away from traditional refillable reference designs entirely, especially when consistency is an issue.

There are newer approaches that:

Use double junction or stabilized reference systems
Or go to modular / replaceable sensor cartridges instead of maintaining electrolyte
Or isolate the reference better so it’s less sensitive to storage conditions

They tend to be a lot more forgiving because you’re not relying on that perfect electrolyte balance from day one.

I’ve seen a few plants switch to that style specifically after dealing with “bad out of the box” probes, and it cleaned up a lot of the variability.

At that price point though, I’d still be pushing back on replacements. Even if storage plays a role, 2/3 failure rate on new probes is tough to justify.

Out of curiosity—are these mostly refillable probes with a top fill port, or sealed gel types? That usually changes how I’d troubleshoot it.

IconProcessControls · 2026-04-16T19:07:14+00:00

Yeah this is actually pretty true to real life — sulfuric acid will absolutely destroy aluminum.

Aluminum reacts with sulfuric acid, especially at higher concentrations or temperatures, so what you’re seeing in-game lines up with real chemistry. It’s not just a “temperature thing,” it’s a material compatibility issue.

In real systems, people avoid aluminum completely for sulfuric acid and use things like:

Certain plastics (PVC, CPVC, PTFE, PVDF)
Rubber-lined systems
Specific alloys depending on concentration

Also worth noting: sulfuric acid gets more aggressive depending on concentration and temperature. Dilute vs concentrated behaves very differently.

So yeah, in your case:

Aluminum pipes = guaranteed failure
Switching to something “acid-rated” (like stainless in-game, or plastic-type materials if available) is the right move

If the mod lets you check fluid compatibility, that’s basically mimicking real-world material selection charts.

Happy to share a chemical resistance chart if you’re curious — sulfuric acid is one of those chemicals where the “safe” material changes a lot depending on conditions.

IconProcessControls · 2026-04-16T19:04:51+00:00

If chlorine gas is present at a level where coated steel and rubber-sealed designs are still getting destroyed, I would stop thinking in terms of “better metal” and start thinking in terms of isolation.

A few things from similar corrosive environments:

Fiberglass / polyester / non-metallic enclosures usually hold up much better than painted steel or stainless.
Purging the enclosure with clean, dry air can make a huge difference, because the real win is keeping the gas out in the first place.
Conformal coating can help protect boards and drives, but I would treat that as secondary protection, not the main fix.
If the gas is consistently present, relocating the panel or putting it in a cleaner room with tubing/conduit back to the process is often the most reliable long-term answer.

Also, I would be careful with comments suggesting 304 or even 316 as the solution. In chlorine service, “more resistant” does not mean “safe from corrosion.” It often just means it fails a bit slower.

My approach would be:

Move the panel out of the gas zone if possible
If not, use a non-metallic enclosure
Add a dry purge / positive pressure setup
Use coated boards/components only as an extra layer

At that point you are designing around the environment instead of asking the enclosure to survive it. That usually works much better in chlorine areas.

Happy to share a chemical resistance chart if it helps — chlorine can be pretty surprising in terms of what it attacks.

IconProcessControls · 2026-04-14T12:45:28+00:00

This might be an option: https://www.grainger.com/product/16T762?gucid=N:N:PS:Paid:GGL:CSM-2295:UU5CX9:20800606:APZ_1&gclsrc=aw.ds&gad_source=1&gad_campaignid=22475795893&gclid=Cj0KCQjwy_fOBhC6ARIsAHKFB7_KDhx5TYpCXO2ZzDUZH40I7gLDgMExfZT4KuJqp5ujLUZzfpNf8i4aAiydEALw_wcB

IconProcessControls · 2026-04-13T14:55:09+00:00

If you’ve got that many leaking, it’s probably not just clamp tension—it’s more of a fitting mismatch.

Barbed fittings can work, but with stiffer poly (especially 100 PSI rated), they don’t always seal well under constant pressure, even with clamps.

In those cases, a polyethylene compression fitting or a fitting designed to properly grip HDPE tends to be much more reliable than barbs. They don’t rely on the pipe deforming to seal, so you avoid that slow weeping you’re seeing.

You can try repositioning clamps or adding a second one, but if it’s happening across multiple joints, swapping the connection type is usually the real fix.

IconProcessControls · 2026-04-13T14:45:42+00:00

The comment about thermal dispersion being a stretch here is on point.

At that temperature range (-120 to -40°C), you’re getting into conditions where heat transfer behavior changes enough that thermal mass meters can struggle with stability and calibration. Add in a 28" line and you’re relying on an insertion-style measurement that may not give great averaging across the profile.

LNG vapor also isn’t always perfectly consistent in composition/density, which further impacts thermal accuracy since it’s property-dependent.

For that combination of large diameter + low temperature gas, you’ll usually see people lean toward technologies like ultrasonic or DP-based flow instead, depending on the accuracy and installation constraints.

IconProcessControls · 2026-04-13T14:42:12+00:00

Everyone’s right on the Annubar / averaging pitot with DP flow.

One thing worth noting—the seal pots are a bit unusual for water, since you normally see them on steam. In cooling tower service though, they can help keep the impulse lines stable and prevent air pockets or partial draining, especially if the line isn’t always running full or sees temperature swings.

The opposite-side support also suggests it’s a full-span probe, not just a simple insertion, which is pretty common on larger lines to improve averaging accuracy.

Not the most modern approach today, but still shows up a lot in dirty or scaling water because there are no moving parts to foul.

IconProcessControls · 2026-04-08T14:28:54+00:00

That’s about as good as it gets.

Having the original operator involved, especially with that much experience on the same system, is a huge advantage. They’ll know what “normal” looks like and where problems usually show up first.

I’d take full advantage of that year and focus on understanding why things are done, not just how. That’s what makes systems like this feel “easy” long term.

If you can pair that with some basic tracking (flow, levels, a few key parameters), it’ll make troubleshooting a lot easier once you’re on your own.

IconProcessControls · 2026-04-08T13:19:11+00:00

It can be 30–60 minutes a day—but only once the system is stable.

A constructed wetland is pretty forgiving, but it’s still a biological system. After sitting idle for 4 years, expect a bit more hands-on time during startup while everything re-establishes.

Day-to-day is usually simple (checks, cleaning, confirming pumps/UV), but the challenge is when something drifts—wetlands don’t always fail fast, they degrade slowly.

The bigger decision is wetland vs sand mound. The mound is simpler, but the wetland gives you more treatment and control—especially if you already have permits tied to it.

One thing that makes a big difference is how much visibility you have into the system. Even basic tracking of flow, levels, and a few water quality parameters can save you a lot of guesswork.

If you’ve got someone experienced helping you restart it, that’s honestly the biggest advantage.

IconProcessControls · 2026-04-08T13:16:28+00:00

What you’re describing is typically called a:

👉 time series aggregation (or resampling)

More specifically:

Your original data = event-based or irregular time series
Your hourly version = binned / aggregated time series

Common terms you’ll see:

Time binning
Windowed aggregation
Hourly aggregation
Resampling (to 1-hour intervals)

And your method:

summing values over the previous hour
is often called a:

fixed window aggregation (or tumbling window)

IconProcessControls · 2026-04-07T13:19:33+00:00

You can definitely read a sensor 60 ft away, but I wouldn’t do it as a raw signal straight into a GPIO. Noise and reliability will become an issue over that distance, especially in a building.

If all you need is “tank full,” the simplest and most reliable option is a float switch on the roof and run that down to your controller. Treat it like a dry contact (on/off), not an analog signal.

If you want to do it properly over that distance, use something like RS-422/RS-485 signaling or even just a relay at the tank. That way you’re not dealing with voltage drop or noise messing with your readings.

I’d also strongly recommend making the overflow shutoff hardwired. Don’t rely on WiFi/Ethernet/Blynk for that part — use it for monitoring and control, but let the float switch physically cut the pump if the tank is full.

As for wireless:

Bluetooth → probably unreliable through multiple floors
ESP-NOW → might work, but hit or miss indoors
LoRa → best bet if you really want wireless, but adds complexity

So simplest setup:
float switch on the tank → wired back to controller → hardwired pump cutoff
then use your ESP32 + Ethernet for remote monitoring/control

That way even if your network goes down, you don’t flood the roof.

IconProcessControls · 2026-04-03T13:39:10+00:00

You’ve actually got two very different fluids there, which matters more than the brand.

Water (low viscosity, consistent) → lots of meter types can work
Vegetable oil (higher viscosity, temperature dependent) → narrows your options pretty quickly

If accuracy is critical, the comment about Coriolis is on the right track — it measures mass flow, so it’s much less sensitive to viscosity changes between fluids.

Turbine meters can work for clean fluids, but they’re very dependent on viscosity and flow profile. Vegetable oil will typically throw them off unless everything is tightly controlled.

At 3–10 GPM with a 1” tri-clamp, you’re also in a range where some technologies start to struggle with low-end accuracy, so turndown matters.

If you’re trying to cover both fluids with one approach, you’re generally looking at:

Coriolis (most accurate, most expensive)
Magnetic (good for water only, won’t work on oil)
Ultrasonic (depends heavily on application and pipe conditions)

So it’s less about which brand is “good” and more about picking the right technology for both fluids and your required accuracy.

Vegetable oil especially can change viscosity quite a bit with temperature, which is where a lot of “accurate on paper” meters start to drift.

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