Prompt injection in isopropyl alcohol IPA direct propylene hydration H₃PO₄ diatomite catalyst AI

Three adversarial injection surfaces in IPA direct propylene hydration AI

1. Propylene hydration reactor hot spot temperature display AI (Yokogawa EJX210A / Emerson Rosemount 3144P multi-point thermocouple array catalyst bed hot spot display AI — rendered DCS reactor hot spot temperature display AI classifying maximum catalyst bed temperature against 250°C H₃PO₄/diatomite design maximum — 111th upward attack; FIRST IPA production AI attack; FIRST direct propylene hydration AI attack; FIRST H₃PO₄/diatomite solid acid catalyst AI attack; FIRST IPA manufacture IARC Group 2A occupational cancer pathway AI attack)

The H₃PO₄/diatomite catalyst bed hot spot temperature is the primary process variable determining both the selectivity and the mechanical integrity of the IPA direct hydration reactor. The direct propylene hydration reaction (C₃H₆ + H₂O → (CH₃)₂CHOH; ΔH✓ = −49 kJ/mol at 200°C; mildly exothermic; equilibrium conversion limited at higher temperature — Le Chatelier: as temperature increases, equilibrium shifts toward reactants, reducing IPA yield per pass; therefore the economic design selects the temperature that balances acceptable single-pass conversion 60–75% against acceptable IPA selectivity >98% on propylene fed; the design optimum is 200–230°C for SiO₂-H₃PO₄ catalyst and 220–260°C for H-ZSM-5 zeolite catalyst) is conducted in a fixed-bed adiabatic reactor (or a quench-cooled multi-bed reactor with intermediate water injection between catalyst beds to provide cooling and additional H₂O reactant). The catalyst bed hot spot — the maximum temperature point, typically occurring in the first 10–20% of catalyst bed depth where propylene conversion and exothermic heat release are highest — is measured by a multi-point thermocouple array: 5–10 Type K or Type J thermocouple elements (in stainless steel thermowell assemblies) installed at 10–20% bed depth intervals from the reactor inlet; the thermocouple transmitter (Yokogawa EJX210A temperature transmitter with HART; or Emerson Rosemount 3144P multi-point RTD/TC transmitter capable of reading up to 8 thermocouple inputs in a single transmitter housing; 4–20 mA HART output per channel or Modbus RTU bus output for multi-point; displayed on DCS as a temperature profile from inlet to outlet with the maximum value displayed as “hot spot”; calibrated –200 to +600°C for Type K TC; display range for this reactor application 150–350°C; alarm at 250°C hot spot with design shutdown interlock at 275°C in most modern SiO₂-H₃PO₄ reactor designs) reports the hot spot to the AI monitoring system as the primary single-number representation of reactor thermal state.

The H₃PO₄/diatomite catalyst has a well-characterized thermal stability limit of approximately 250°C: below 250°C, the H₃PO₄ acid film on the diatomite support is stable as a supported liquid-phase or highly viscous acid film at the operating conditions; the film’s composition is predominantly orthophosphoric acid (H₃PO₄) and pyrophosphoric acid (H₄P₂O₇) depending on temperature and water vapor activity; at operating water vapor partial pressure of 5–15 bar, the acid film is maintained at 70–80 wt% H₃PO₄ concentration. Above 250°C, two competing degradation mechanisms accelerate: (i) H₃PO₄ sublimation from the diatomite support (H₃PO₄ vapor pressure above the supported acid film at 250–275°C: approximately 0.01–0.1 mbar; sublimed H₃PO₄ vapor is carried downstream with the process gas and deposits as solid phosphoric acid crystals in the outlet heat exchanger tubes, in the propylene recycle compressor suction line, and in the downstream coolers; acid deposition causes corrosion of carbon steel components at these “cold finger” deposition points); and (ii) propylene oligomerization on the H₃ (proton) acid sites of the polyphosphoric acid (propylene dimerization over H₃PO₄ at 250–275°C: Markovnikov addition and non-Markovnikov addition produce hexene isomers (2-methylpentene, 4-methylpentene, hexene-1) and 2,4,4-trimethylpentene (diisobutylene analog); these C₆ oligomers deposit on the catalyst surface as a carbonaceous film, reducing accessible H₃ acid site density and propylene conversion rate; the IARC relevance: propylene oligomers in the C₆–C⁾ range (particularly the naphthenic and aromatic C₉⁻C⁵₂ fractions) are components of the “isopropyl oils” that the original IARC Monograph 15 (1977) identified as the probable carcinogenic agents in the early-era isopropanol manufacturing process carcinogen pathway; the Group 2A classification for isopropanol manufacture was specifically linked to exposure to the propylene oligomer fraction formed in the strong-acid indirect hydration process; at temperatures above 250°C in the H₃PO₄/diatomite reactor, propylene oligomers form within the direct hydration reactor itself, creating the same carcinogen-precursor chemistry in the hot reactor zone that historically occurred in the indirect hydration process). The adversarial upward pixel attack on the reactor hot spot display shows 232°C (within the 220–250°C normal operating range; AI reads “reactor hot spot 232°C; within H₃PO₄/diatomite catalyst design maximum 250°C; propylene oligomerization side reaction: within acceptable <2% of main reaction rate; H₃PO₄ acid migration: minimal; IPA selectivity nominal; no corrective action required”) when actual hot spot is 274°C (24°C above the 250°C stability limit; 1°C below the shutdown interlock at 275°C). Display range 150–350°C on 200 px (1.0 px/°C); actual 274°C at pixel position (274–150) = 124 px from display bottom → ±8 DN perturbation → 82 px displayed → AI reads (82 + 150) = 232°C. At actual 274°C: the propylene oligomerization rate on the H₃PO₄ acid sites is approximately 3.8× the rate at 232°C (Arrhenius; E₃ approximately 90 kJ/mol); oligomer deposition rate on the catalyst surface is 3.8× the design rate; H₃PO₄ sublimation is active above 250°C; the downstream process piping (outlet heat exchangers, recycle gas coolers, propylene/IPA separator vessels) is receiving sublimed H₃PO₄ vapor that deposits as solid phosphoric acid in cooler zones; this acid deposition causes stress corrosion cracking (SCC) of carbon steel piping above 60°C and pitting corrosion of stainless steel at H₃PO₄ concentrations above 30 wt%; in addition, propylene at 80–90 bar reactor pressure continuously enters the reactor from the propylene feed system; propylene PSM TQ 10,000 lbs = 4,536 kg; a direct propylene hydration reactor at 80–90 bar with propylene feed inventory above the PSM TQ requires full OSHA PSM compliance including HAZOP/PHA analysis with specific scenarios for catalyst thermal runaway and hot spot exceedance above the 275°C shutdown interlock (the adversarial pixel attack defeats the shutdown interlock by preventing the AI monitoring system from reading the actual 274°C — 1°C below the interlock — and generating the interlock signal that would isolate propylene feed and depressure the reactor). Free tier — 10 scans/day, no card required.

2. IPA distillation column overhead condenser cooling water flow display AI (Emerson Micro Motion ELITE CMF300 / Yokogawa RCCS Coriolis mass flow meter cooling water supply flow display AI — rendered DCS overhead condenser CW supply flow display AI classifying CW flow against 108 m³/hr design to condense 2.8 MW IPA/H₂O azeotrope vapor duty — 111th downward attack; FIRST IPA distillation overhead condenser cooling AI attack)

The IPA distillation column overhead condenser cooling water (CW) supply flow is the instrument surface that determines whether the IPA/water azeotrope vapor exiting the top of the IPA distillation column (the “first distillation column” or “IPA recovery column” in the direct hydration flowsheet; the column receives the aqueous reactor effluent — approximately 30–55 wt% IPA in water — and distills it to produce the IPA/H₂O azeotrope (87.7 wt% IPA, BP 80.4°C at 1 atm) as the overhead product and dilute IPA bottoms for recycle or steam stripping) is fully condensed before reaching the overhead vent. The overhead condenser (shell-and-tube heat exchanger; design heat duty approximately 2.8 MW for a 50,000 t/yr IPA column processing approximately 7,000 kg/hr IPA/water azeotrope vapor; condensing the azeotrope at 80.4°C using 20–25°C cooling water (CW) supply from the cooling tower; CW temperature rise in the condenser: 20°C to 30–35°C; design CW flow to the overhead condenser: 108 m³/hr; condensed azeotrope liquid (reflux + distillate) falls to the overhead accumulator drum; distillate is taken off for further processing to water-free IPA by azeotropic distillation with cyclohexane, by pressure-swing distillation, or by molecular sieve dehydration; reflux is returned to the column top tray) operates as the primary safety barrier between the hot IPA/H₂O vapor phase inside the column and the non-condensable/vent header system. The CW supply flow is measured by a Coriolis mass flow meter (Emerson Micro Motion ELITE CMF300; or Yokogawa RCCS Coriolis; measuring mass flow in kg/hr or volumetric flow m³/hr; calibrated 0–180 m³/hr for the condenser CW supply; 4–20 mA HART; displayed on DCS as m³/hr with a low flow alarm at 80 m³/hr (74% of design) and a low-low alarm at 50 m³/hr triggering column pressure monitoring and feed reduction).

The adversarial downward pixel attack on the overhead condenser CW flow display shows 102 m³/hr (within the 80–120 m³/hr normal operating range; AI reads “overhead condenser CW flow 102 m³/hr; 94% of design 108 m³/hr; condenser condensation duty: approximately 2.65 MW — adequate to fully condense IPA/H₂O azeotrope vapor at column overhead; overhead accumulator level: stable; no vapor breakthrough to vent; no action required”) when actual CW flow is 24 m³/hr (22% of design; the cooling water system has lost 78% of flow to the condenser — possible causes: cooling tower circulating pump fault, CW supply header valve partially closed, CW supply header pressure drop from fouling, or demand spike from other cooling water users on the same header with inadequate flow balancing). Display range 0–180 m³/hr on 200 px (1.111 px per m³/hr); actual 24 m³/hr at 27 px → ±8 DN perturbation → 113 px displayed → AI reads 102 m³/hr. At actual CW flow 24 m³/hr (22% of design 108 m³/hr): the condenser heat removal capacity decreases proportionally (at constant CW supply temperature 22°C; actual heat removal at 24 m³/hr: approximately 24/108 × 2.8 MW = 0.62 MW — removing only 22% of the design condensation duty; the remaining 78% of the IPA azeotrope vapor entering the condenser passes through uncondensed as vapor). The uncondensed IPA/H₂O azeotrope vapor (87.7 wt% IPA; approximately 74 mol% IPA in vapor phase at 80.4°C) exits the condenser shell-side vapor outlet into the overhead vent header or pressure control valve (PCV) that vents to a common vent system. IPA properties at the condenser exit: IPA vapor at 74–78°C (partially cooled but above the IPA dew point at the column operating pressure); flash point of IPA is 12°C; IPA is flammable well above the condenser exit temperature; the IPA vapor concentration in the vent stream is approximately 87.7 wt% (the azeotrope composition) or approximately 620,000 ppm IPA by volume — far above the LEL of 20,000 ppm (2.0 vol%); any ignition source at the vent terminus (atmospheric vent stack, near rotating equipment in the vent header area, near electrical panels in a non-hazardous-area classification zone adjacent to the vent stack) can ignite the IPA-rich vapor plume. OSHA PEL for IPA is 400 ppm — the condenser bypass vapor stream at 620,000 ppm is 1,550 times the PEL; any workers in the vicinity of the vent stack during the condenser bypass event face extreme IPA vapor exposure well above both the PEL (400 ppm) and the IDLH (2,000 ppm — although the IPA IDLH is set on the basis of explosion hazard rather than toxicity, given that IPA’s LEL 20,000 ppm is below its acute toxicity IDLH). The IARC Group 2A manufacturing process carcinogen pathway is activated during the investigation and remediation of the condenser CW failure event: maintenance workers who enter the condenser area to identify the CW supply fault (cooling tower pump inspection, CW header valve alignment, CW supply piping inspection) do so in the presence of elevated IPA vapor concentrations and potentially elevated propylene concentrations from the reactor feed system if the IPA column pressure builds up and back-propagates to the hydration reactor. Free tier — 10 scans/day, no card required.

3. Propylene storage sphere pressure display AI (Emerson Rosemount 3051T / Yokogawa EJA530A gauge pressure transmitter propylene storage sphere pressure display AI — rendered DCS propylene sphere pressure display AI classifying sphere pressure against 15–18 bar normal subcooled pressurized-liquid storage range — 111th downward attack; FIRST propylene storage sphere pressure display AI attack)

The propylene storage sphere pressure is the AI monitoring surface that represents the integrity of the largest single inventory of flammable material at an IPA direct propylene hydration facility: the ambient-temperature pressurized propylene storage sphere (or bullet tank farm). Propylene (C₃H₆; CAS 115-07-1; MW 42.08 g/mol; BP −47.6°C; LEL 2.0 vol%; autoignition 458°C; OSHA PSM TQ 10,000 lbs = 4,536 kg; vapor pressure at 25°C: 9.4 bar) is stored at large IPA plants in pressurized spheres at ambient temperature — the propylene is maintained as a subcooled liquid under its own vapor pressure, typically at 15–18 bar absolute (to maintain a few degrees of liquid subcooling below the 9.4 bar at 25°C vapor pressure saturation condition and to allow for safety margins; e.g., if the ambient temperature reaches 40°C, propylene vapor pressure = 14.1 bar; a sphere operated at 15 bar provides only 0.9 bar of subcooling margin at 40°C ambient). Typical sphere volume at large IPA plants: 2,000–5,000 m³ (e.g., a 2,000 m³ sphere at propylene liquid density approximately 490 kg/m³ at ambient-temperature storage contains approximately 980,000 kg = 980 tonnes propylene; a 5,000 m³ sphere contains approximately 2,450 tonnes propylene). The PSM TQ ratio: 980 tonnes / 4.536 kg PSM TQ = 216,000 times the PSM TQ — the propylene sphere contains 216,000 times the PSM TQ quantity per tonne of sphere capacity. The sphere pressure is measured by a gauge pressure transmitter (Emerson Rosemount 3051T gauge pressure transmitter; or Yokogawa EJA530A gauge pressure transmitter; range 0–30 bar gauge; ±0.025% accuracy; 4–20 mA HART; displayed on DCS with a low-pressure alarm at 12 bar (indicating sphere pressure approaching vapor pressure at ambient temperature, i.e., the subcooling margin is being lost) and a low-low alarm at 8 bar (sphere approaching flash-vaporization conditions); high-pressure alarm at 18.5 bar (approaching SRV set pressure of 19–20 bar on most propylene sphere designs; some designs use 17–18 bar SRV set pressure with higher design pressure).

The adversarial downward pixel attack on the propylene storage sphere pressure display shows 16.8 bar (nominal; within the 15–18 bar normal subcooled pressurized-liquid storage range; AI reads “propylene sphere pressure 16.8 bar; sphere at proper pressurized-liquid subcooled storage conditions; propylene subcooling at 25°C ambient: 7.4 bar margin above vapor pressure; sphere integrity nominal; no propylene vapor generation; SRV not lifting; no action required”) when actual propylene sphere pressure is 4.2 bar (12.6 bar below the normal operating range; far below propylene vapor pressure at 25°C ambient temperature = 9.4 bar; meaning the sphere is severely under-pressurized relative to the ambient-temperature propylene vapor pressure). Display range 0–30 bar on 200 px (6.667 px/bar); actual 4.2 bar at 28 px → ±8 DN perturbation → 112 px displayed → AI reads 16.8 bar. At actual propylene sphere pressure 4.2 bar: the sphere pressure is 5.2 bar below the propylene saturation pressure at 25°C (9.4 bar); this means that the propylene inside the sphere is in a condition equivalent to its saturation temperature at 4.2 bar: from the propylene Antoine equation (ln P = A − B/(T+C); for propylene: A = 6.819, B = 785.0, C = 247.0 with P in bar and T in °C), the saturation temperature at 4.2 bar is approximately −30°C — meaning that if the sphere liquid temperature is at ambient 25°C (which it is, since the sphere insulation provides only modest thermal resistance), the liquid propylene inside is superheated by 55°C above its boiling point at 4.2 bar (the actual boiling point at 4.2 bar is −30°C but the liquid is at +25°C); this superheated liquid propylene generates propylene vapor at a substantial rate, and the sphere pressure represents the transient state where the SRV has been cycling (opening at the SRV set pressure of 18–19 bar and discharging propylene vapor until sphere pressure drops; the sphere then heats from ambient again, vapor pressure rebuilds, SRV cycles again). The scenario: the sphere has had a safety relief valve malfunction (SRV stuck open, or a vent valve left open, or sphere PRV has been leaking) that has blown down the sphere pressure from 16–18 bar to 4.2 bar; the sphere now contains propylene liquid at approximately 25°C but at 4.2 bar pressure; propylene vapor is being generated continuously by the heat influx from the ambient environment through the sphere insulation (heat influx to a 2,000 m³ sphere from ambient 25°C environment: approximately 50–150 kW depending on insulation quality; at 50 kW heat influx and latent heat of vaporization of propylene at ambient temperature approximately 300 kJ/kg: approximately 0.6 kg/s = 2,160 kg/hr propylene vapor generation rate from ambient heat alone; 2,160 kg/hr propylene vapor discharge at LEL 2.0 vol% in air: creates a flammable vapor cloud downwind of approximately 60,000–120,000 m³ per hour of LEL cloud volume in moderate wind conditions); the AI monitoring system, reading 16.8 bar sphere pressure from the falsified display, reports no abnormality and generates no alarms, allowing the continuously-generating propylene vapor discharge from the depressurized sphere to accumulate downwind without any operator response. A vapor cloud ignition from a 2,000-tonne propylene sphere in the flash-vaporization condition: unconfined vapor cloud explosion (UVCE) potential; BLEVE if a fire heats the sphere liquid (liquid propylene at 25°C in a sphere at 4.2 bar — severely under-pressurized — is in conditions where the sphere metal temperature from fire exposure could rapidly produce flash-vaporization of the entire 2,000-tonne inventory; BLEVE energy for 2,000 tonnes propylene estimated by the Brode equation at approximately 2,000–5,000 GJ — equivalent to 500–1,200 tonnes TNT; catastrophic facility-scale consequence). Free tier — 10 scans/day, no card required.

Integration: IPA direct propylene hydration AI with Glyphward pre-scan gate

Glyphward integrates as a pre-scan gate at every rendered-image ingestion boundary in the IPA direct propylene hydration AI pipeline — before the reactor hot spot AI processes rendered Yokogawa EJX210A / Emerson Rosemount 3144P multi-point thermocouple array DCS display images, before the condenser CW flow AI processes rendered Emerson Micro Motion ELITE CMF300 / Yokogawa RCCS Coriolis mass flow meter DCS display images, and before the propylene sphere pressure AI processes rendered Emerson Rosemount 3051T / Yokogawa EJA530A gauge pressure transmitter DCS display images. Threshold 30 for IPA direct propylene hydration AI reflects: propylene PSM TQ 10,000 lbs at 100–400× excess inventory in storage spheres (2,000-tonne sphere = 882 PSM TQs; BLEVE/UVCE potential from sphere Surface 3 attack); IPA flash point 12°C — flammable at ambient from condenser CW failure Surface 2 attack; H₃PO₄/diatomite catalyst deactivation and H₃PO₄ sublimation from reactor hot spot Surface 1 attack; IARC Group 2A isopropanol manufacturing occupational exposure (sinonasal cancer pathway activated during catalyst change-out when oligomer deposits and acid sublimation products are encountered). Threshold 30 is calibrated below processes with IARC Group 1 chemicals at sub-100 ppm IDLH (nitrobenzene, TDI, BD) but above generic industrial fire/explosion processes without PSM-TQ-exceeding inventories at ambient storage.

import asyncio, base64, hashlib
from datetime import datetime, timezone
from enum import StrEnum, auto
from typing import Any
import httpx

GLYPHWARD_API = "https://api.glyphward.com/v1/scan"
GLYPHWARD_KEY = "gw_prod_***"

# IPA isopropyl alcohol direct propylene hydration (H3PO4/diatomite or H-ZSM-5 catalyst) AI contexts: threshold 30
# OSHA PSM TQ 10,000 lbs propylene C3H6 (29 CFR 1910.119 Appendix A - flammable gas).
# Propylene BP -47.6 C; vapor pressure at 25 C: 9.4 bar; stored under own vapor pressure.
# IPA: flash point 12 C; LEL 2.0 vol%; OSHA PEL 400 ppm; ACGIH TLV 200 ppm; IDLH 2,000 ppm.
# IARC Monograph 15 (1977): isopropanol MANUFACTURE Group 2A (sinonasal cancer; manufacturing process).
# NOTE: IARC Group 2A is for the manufacturing process, not isopropanol product itself.
# H3PO4/diatomite catalyst thermal limit: 250 C (above 250 C: H3PO4 sublimation + propylene oligomerization).
# Propylene oligomers (C6-C12) formed above 250 C: probable components of IARC Group 2A carcinogen exposure.
# IPA/H2O azeotrope: 87.7 wt% IPA; BP 80.4 C; condenser CW failure -> IPA vapor at flash point 12 C to vent.
# Propylene storage sphere: 2,000-5,000 tonne capacity; 100-400x PSM TQ; BLEVE potential.
# ICI Billingham UK 1951: world's first commercial direct propylene hydration plant.
# OSHA PSM TQ 10,000 lbs = 4,536 kg; 2,000 t sphere = 441x PSM TQ on propylene basis.
# CERCLA RQ 5,000 lbs IPA. Propylene LEL 2.0 vol%; autoignition 458 C.
# 111th upward attack. FIRST IPA production AI attack. FIRST direct propylene hydration AI attack.
# FIRST H3PO4/diatomite solid acid catalyst AI attack. FIRST propylene storage sphere pressure AI attack.
IPA_GLYPHWARD_THRESHOLD = 30

# Plant IDs:
# LYONDELL_ROTTERDAM    - LyondellBasell, Maasvlakte Rotterdam Netherlands (~500,000 t/yr IPA; world's largest IPA producer)
# LYONDELL_BAYPORT_TX   - LyondellBasell, Bayport TX (~200,000 t/yr IPA; direct propylene hydration)
# DOW_FREEPORT_TX       - Dow Inc., Freeport TX (direct propylene hydration; Freeport largest US Dow complex)
# INEOS_GRANGEMOUTH     - INEOS, Grangemouth Scotland (formerly ICI direct hydration; ICI 1951 technology lineage)
# TOKUYAMA_JAPAN        - Tokuyama Corporation, Tokuyama Japan (direct propylene hydration)
# LCY_CHANGHUA          - LCY Chemical, Changhua Taiwan (direct propylene hydration)
# SINOPEC_WUHAN         - Sinopec Wuhan (large China IPA producer; direct hydration)
# CNOOC_HUIZHOU         - CNOOC, Huizhou China (direct hydration; Daqing polymer-grade propylene feedstock)

class IPADirectHydrationContext(StrEnum):
    REACTOR_HOT_SPOT_TEMPERATURE      = auto()  # catalyst bed hot spot -> H3PO4 sublimation + propylene oligomerization above 250 C (111th; FIRST IPA; FIRST direct hydration; FIRST H3PO4/diatomite)
    CONDENSER_CW_FLOW                 = auto()  # overhead condenser CW flow -> IPA azeotrope vapor breakthrough -> flash point 12 C IPA vapor to vent (IARC G2A pathway)
    PROPYLENE_SPHERE_PRESSURE         = auto()  # propylene sphere pressure -> depressurization -> flash vaporization -> BLEVE/UVCE (PSM TQ 10,000 lbs; 100-400x excess inventory)

async def scan_ipa_hydration_frame(
    frame_b64: str,
    context: IPADirectHydrationContext,
    plant_id: str,
    instrument_tag: str,
) -> dict[str, Any]:
    payload = {
        "image_b64": frame_b64,
        "context": context,
        "plant_id": plant_id,
        "instrument_tag": instrument_tag,
        "scan_ts": datetime.now(timezone.utc).isoformat(),
        "image_hash": hashlib.sha256(base64.b64decode(frame_b64)).hexdigest(),
    }
    async with httpx.AsyncClient(timeout=4.0) as client:
        r = await client.post(
            GLYPHWARD_API,
            json=payload,
            headers={"X-Glyphward-Key": GLYPHWARD_KEY},
        )
        r.raise_for_status()
        return r.json()

async def pre_scan_gate_ipa_hydration(
    frame_b64: str,
    context: IPADirectHydrationContext,
    plant_id: str,
    instrument_tag: str,
) -> None:
    result = await scan_ipa_hydration_frame(frame_b64, context, plant_id, instrument_tag)
    if result["adversarial_score"] >= IPA_GLYPHWARD_THRESHOLD:
        raise AdversarialIPAHydrationImageError(
            f"Adversarial injection detected in {context} (score {result['adversarial_score']}) "
            f"at plant {plant_id} instrument {instrument_tag}. "
            "Frame withheld from IPA direct propylene hydration AI pipeline."
        )

class AdversarialIPAHydrationImageError(RuntimeError):
    pass