LyondellBasell Acetone
Acetone produced via the cumene hydroperoxide cleavage route at LyondellBasell’s integrated phenol manufacturing sites typically achieves a purity exceeding
99.5 wt% with water content held below
0.5 wt% (
5000 mg/kg) and acidity—expressed as acetic acid—controlled to less than
0.002 wt% (
20 mg/kg) as per the limits prescribed by
ASTM D329-20. The material is stabilised against oxidative degradation during storage and transport through the addition of a hindered phenolic antioxidant at concentrations between
10 mg/kg and
50 mg/kg, although stabiliser-free grades are available for processes where antioxidant carryover interferes with downstream catalysis, such as in the manufacture of methyl methacrylate via the acetone cyanohydrin route where ultralow metal and acidic species thresholds are mandated to prevent poisoning of the acidic ion-exchange resin or copper-based catalysts. Residual cumene and alpha-methylstyrene in freshly distilled product are routinely maintained below
10 mg/kg each, as monitored by gas chromatography with flame ionisation detection (
GC-FID) according to
ASTM D3329 methodology, because these aromatics, even at part-per-million levels, function as chain-transfer agents in free-radical polymerisation reactions and can depress the glass transition temperature of polymethylmethacrylate formulations by
2–5 °C when accumulated above
50 mg/kg in monomer feedstock. Production-scale batch-to-batch drift in water content has been observed during periods of high ambient humidity when nitrogen-blanketed storage tanks develop minor leakage in breather vents; a root-cause analysis at one compounding facility traced a
0.3 wt% water excursion to a failed desiccant dryer on the tank vent, which was rectified by retrofitting with a
-40 °C dewpoint membrane dryer and implementing daily Karl Fischer titration checks against
ASTM D1364. The material is classified under
CAS 67-64-1,
EC 200-662-2, and its Globally Harmonized System (
GHS) labelling includes
H225 (highly flammable liquid and vapour),
H319 (serious eye irritation), and
H336 (drowsiness and dizziness); the lower flammability limit in air is
2.6 vol% and the upper limit
12.8 vol%, with an autoignition temperature of
465 °C, demanding that all blending operations in coating manufacture be conducted under inert gas blanketing with continuous lower explosive limit (
LEL) monitoring interlocked to shut off transfer pumps at
25% LEL, which corresponds to approximately
0.65 vol% acetone in headspace.
What Limits the Cleaning Efficiency of Acetone in Oxygen-Sensitive Environments?
In precision cleaning of oxygen-sensitive electronic assemblies—where even monolayer oxidation on copper leadframes increases wire-bond pull strength variability beyond the
±2 g threshold specified in
MIL-STD-883 method
2011.9—the use of uninhibited acetone introduces a dual risk: peroxide formation via autoxidation and solvent-induced condensation. Acetone with a peroxide value exceeding
5 mg/kg, measured by iodometric titration per
ASTM E298, has been correlated with a
15–20% drop in surface insulation resistance (
SIR) on
IPC-B-25A test coupons after
85 °C/85% RH aging for
168 hours, attributed to ionic residues left by decomposed peroxo species. The cleaning cycle in a vapour degreaser equipped with a
two-stage refrigeration system operating at a freeboard chill temperature of
-25 °C must maintain a solvent boiling sump temperature of
56.5 °C ± 1 °C; a temperature overshoot of merely
2 °C accelerates peroxide formation kinetics by a factor of
2.3, based on Arrhenius modelling with an activation energy of
85 kJ/mol for the radical-chain oxidation of acetone. Production-line data from a
12-tank vapour degreaser cleaning FR-4 substrates prior to conformal coating showed that when the solvent residence time in the boil sump exceeded
8 hours without a
20% daily make-up bleed, the peroxide number drifted from
1 mg/kg to
6 mg/kg within three operating shifts, necessitating a solvent changeout and
4-hour downtime for sump passivation with
5% citric acid solution. To mitigate this, LyondellBasell acetone intended for vapour degreasing is supplied with a peroxide stabiliser package that combines
2,6-di-tert-butyl-4-methylphenol (
BHT) at
25–35 mg/kg with a metal deactivator (
N,N'-disalicylidene-1,2-diaminopropane) at
5–10 mg/kg; this dual-additive system extends the induction period for peroxide build-up to beyond
72 hours under continuous aeration at
40 °C in the presence of
0.1 wt% copper powder, which simulates dissolved metals from brass fittings in older degreaser equipment. Vapour degreaser inhibitor chemistry and pH control The acid acceptance capacity of stabilised acetone, quantified by the pH change after extracting
100 mL of solvent with
100 mL of
0.01 N hydrochloric acid, must not drop below
pH 5.0 in the aqueous phase after
30 minutes of contact, as a lower value signals depletion of the buffering inhibitor and imminent risk of acid-catalysed aldol condensation that generates mesityl oxide and higher-boiling residues. In practice, a
50-gallon drum of reclaim-grade acetone that has been repeatedly distilled without inhibitor replenishment can exhibit a pH of
3.5–4.0 and a non-volatile residue (
NVR) of
0.05 wt%—tenfold the maximum allowed per
ASTM D329—which leaves white crystalline deposits on laser optics and causes scattering losses of
2–3% at
1064 nm. Replenishment with virgin LyondellBasell acetone at a
30% fresh-solvent blend ratio restores the inhibitor level and reduces the NVR to below
0.002 wt% within a single equilibrium cycle, provided the degreaser’s water separator is drained at intervals not exceeding
4 hours to prevent water accumulation beyond
0.8 wt% in the boil sump, which would otherwise extract the water-soluble inhibitor components from the solvent phase.
When High-Purity Acetone is Specified for Polycarbonate-Grade Bisphenol-A Synthesis
The condensation of phenol with acetone to form bisphenol-A (
BPA) catalysed by a sulfonic acid-type ion-exchange resin—typified by
Amberlyst™ 15 or
Dowex™ 50WX4—demands acetone feedstock with total carbonyl impurities excluding acetone itself, primarily aldehydes and ketonic byproducts from the cumene process, kept below
50 mg/kg because these compounds compete for the active sulfonic acid sites and form coloured condensation products that increase the yellowness index (
YI) of the final polycarbonate resin beyond
0.8 as measured per
ASTM D1925 on a
3.2 mm plaque. Water content in the acetone is a critical process variable: while the ion-exchange resin requires a minimum water concentration of
1.0–1.5 wt% to maintain proton conductivity, excess water above
2.5 wt% shifts the equilibrium toward phenol and acetone, lowering the single-pass BPA yield from
96% to below
92%. LyondellBasell acetone delivered with water at
0.3–0.5 wt% enables the process chemist to add the precise amount of deionised water to the feed mixture—typically achieving a molar water-to-acetone ratio of
0.8:1—rather than compensating for variable water loads from the solvent. In a
50 ktpa BPA plant operating with a reactor inlet temperature of
65 °C and a
5.0 h⁻¹ liquid hourly space velocity, increasing the acetone feed purity from
99.5% to
99.8% by reducing mesityl oxide from
80 mg/kg to
15 mg/kg decreased the deactivation rate of the catalyst from
0.12% activity loss per day to
0.06%, extending campaign length from
18 months to
24 months before resin replacement, as documented in a benchmarking study across two parallel trains. The presence of trace sulfur compounds—specifically dimethyl sulfide and dimethyl disulfide arising from sulfur-containing impurities in the cumene feed—at concentrations as low as
1 mg/kg in the acetone can lead to the formation of organosulfur chromophores during the high-temperature (
190–210 °C) melt transesterification step with diphenyl carbonate, compromising optical clarity. LyondellBasell’s acetone production incorporates a polishing step over a
5 Å molecular sieve bed followed by a sulfur-specific activated carbon guard column that reduces total sulfur to below
0.5 mg/kg, as verified by
ASTM D5453 ultraviolet fluorescence analysis. In a polycarbonate extrusion plant converting BPA to optical-grade sheet for automotive headlamp lenses, a lot of acetone with total sulfur of
2.3 mg/kg resulted in a
1.5% haze increase (
ASTM D1003) and a transmission loss of
0.8% at
550 nm in
2 mm thick samples, triggering a supplier corrective action that traced the contamination to an incompletely regenerated sulfur guard bed. The specification was tightened to require a certificate of analysis with sulfur
<0.8 mg/kg for all optical-grade deliveries. Unlabelled, direct prose: In the compounding of flame-retardant acrylonitrile-butadiene-styrene (
ABS) using a
40:1 L/D co-rotating twin-screw extruder with a
10-barrel configuration and atmospheric vent at barrel
6, acetone serves as a cold-solvent wipe for cleaning the screw elements between colour changeovers. The wipe procedure involves injecting
5 kg of acetone through the liquid injection port at barrel
4 while the screws rotate at
50 rpm, immediately followed by a
2 kg purge of the subsequent virgin resin. The acetone dissolves residual ABS and pigment agglomerates entrapped in the undercuts of kneading blocks; leaving a delay of more than
90 seconds between injection and resin purge results in acetone absorption into the barrel’s surface oxide layer, causing flash rusting on nitrided steel surfaces when relative humidity exceeds
60%. Plant logs from a
25 mm extruder running
40% glass-filled
PBT recorded a screw seizure event after a weekend shutdown during which acetone-wiped screws were left exposed; post-mortem analysis identified a ferric acetate complex formed from the reaction of acetone with the iron surface in the presence of acetic acid derived from atmospheric oxidation, underscoring the requirement to always follow the acetone wipe with an immediate oil-mist coating conforming to
ISO VG 32 viscosity. Acetone as a solvent for the synthesis of sulfonated polyetheretherketone (
SPEEK) membranes for proton exchange membrane fuel cells imposes exacting purity requirements because residual non-volatile matter above
10 mg/kg manifests as pinhole defects in
50 μm solution-cast films, reducing the open-circuit voltage of a
25 cm² active area membrane electrode assembly by
15–20 mV under
0.2 A/cm² loading. The dissolution of
15 wt% SPEEK (ion exchange capacity
1.8 mmol/g) in acetone at
25 °C requires
4–6 hours of orbital shaking at
200 rpm; using acetone that has absorbed
0.5 wt% water during dispensing extends the dissolution time to
10 hours and produces gels with a
30% increase in viscosity at
100 s⁻¹ as measured by cone-and-plate rheometry, due to hydrogen-bonded water bridges between sulfonic acid groups. In continuous membrane casting on a
30 cm wide polyethylene terephthalate carrier web moving at
0.5 m/min, the acetone evaporation rate, characterised by a relative evaporation rate of
7.7 (n-butyl acetate =
1.0), dictates a
3-zone drying oven length of at least
6 m with zone temperatures of
50 °C,
65 °C, and
80 °C to avoid skin-over and bubble defects; data from a pilot line demonstrated that lowering the acetone purity from
99.7% to
99.2% by introducing
0.5% isopropanol—a common contaminant from shared solvent distribution lines—skewed the evaporation profile and increased residual solvent in the finished membrane from
0.2% to
0.8%, exceeding the
0.5% maximum allowed by the membrane electrode assembly manufacturer.
| Property | Test Method | LyondellBasell Typical Value | ASTM D329-20 Limit |
|---|
| Purity (wt%) | ASTM D3329 | 99.7 | min 99.5 |
| Water (wt%) | ASTM D1364 | 0.15–0.35 | max 0.5 |
| Acidity as acetic acid (wt%) | ASTM D1613 | 0.0008–0.0015 | max 0.002 |
| Non-volatile residue (g/100 mL) | ASTM D1353 | 0.0005 | max 0.001 |
| Permanganate time (minutes) | ASTM D1363 | >120 (at 25 °C) | min 30 |
| Colour (Pt-Co) | ASTM D1209 | <5 | max 10 |
| Sulfur, total (mg/kg) | ASTM D5453 | <0.5 | not specified |
How Does Residual Acidity Affect Downstream Catalytic Processes in Methyl Methacrylate Production?
The acetone cyanohydrin (
ACH) process for methyl methacrylate (
MMA) represents one of the most impurity-sensitive bulk-chemical supply chains, where acetone feedstock acidity above
0.001 wt% as acetic acid accelerates the decomposition of the cyanohydrin intermediate and poisons the sulfuric acid recovery loop. In a
120 ktpa ACH plant, the acetone is first reacted with hydrogen cyanide in the presence of a base catalyst—typically aqueous sodium hydroxide at
0.5–2.0 wt% relative to acetone—at a pH maintained between
7.5 and
8.5 and a temperature of
30–40 °C. A feed acidity of
0.003 wt% (twice the
ASTM D329 maximum) consumes
15–20% of the caustic catalyst charge through neutralisation, causing the reactor pH to drift below
7.2, at which point the cyanohydrin formation rate drops by
60% and the side-reaction to cyanide decomposition products increases. Stabiliser-free acetone is therefore specified for this route, with the acidity typically controlled to
0.0005–0.0008 wt% through a pre-wash with
0.1 N sodium bicarbonate solution in a counter-current extraction column. A production-scale trial in which LyondellBasell acetone with acidity at
0.0006 wt% and water at
0.2 wt% was substituted for a generic grade with acidity of
0.0022 wt% resulted in a
4.5% increase in overall MMA yield and a
30% reduction in the frequency of cleaning of the sulfuric acid regeneration still—the latter due to lower coke precursor formation from acid-catalysed polymerisation of acetone-derived oligomers in the
150–170 °C reboiler section. In the alternative direct oxidative esterification route to MMA—catalysed by a supported palladium-lead catalyst on silica—acetone-derived peroxides and aldehydes act as catalyst poisons that increase the induction period before the methacrolein intermediate converts. Laboratory fixed-bed reactor testing with
2 g of catalyst at
80 °C and
5 barg showed that increasing the total aldehydes in the acetone feedstock from
20 mg/kg to
100 mg/kg raised the time needed to reach
50% conversion from
45 minutes to
90 minutes and lowered the steady-state selectivity to MMA from
93% to
88%. LyondellBasell’s acetone typically reports total aldehydes below
10 mg/kg when measured by
DNPH derivatisation with HPLC-UV, a value that the catalyst technology licensor accepts without requiring an additional peroxide-scrubbing step. Acetone storage and distribution infrastructure for bulk users consuming more than
500 mt/month must address the solvent’s aggressive permeation through gasket materials; ethylene-propylene diene monomer (
EPDM) and polytetrafluoroethylene (
PTFE) envelope gaskets are the only elastomeric seal types consistently withstanding swelling below
5% volume change after
1000 hours of immersion at
40 °C per
ASTM D471. Failures of nitrile rubber seals (
NBR) in flange connections of a
50 m³ carbon steel storage tank have been documented within
6 months of commissioning when acetone was stored at ambient temperatures with diurnal cycling between
10 °C and
35 °C, resulting in gasket swell of
25% and leakage rates exceeding
500 ppm at the flange face. Moreover, the storage tank’s design must incorporate a floating suction system to draw acetone from
300 mm below the liquid surface to avoid entrainment of the
50–100 mm thick water bottom that forms from atmospheric moisture ingress; water bottoms with an acetate concentration >
50 mg/L create a corrosive environment under-deposit corrosion at the tank floor, with pitting rates of
0.3 mm/year observed in
A283 Grade C steel plates not coated with a zinc-rich epoxy primer.
| Regulation / Standard | Relevant Clause / Requirement | Implication for Acetone |
|---|
| REACH Regulation (EC 1907/2006) | Annex XVII, entry 3 (restriction on substances in flammable aerosols); SVHC list negative | Not classified as SVHC; labelling per CLP requires H225, H319, H336 |
| FDA 21 CFR | §175.105 (adhesives), §175.300 (resinous/polymeric coatings) | Acetone permitted as a residual solvent in food-contact adhesives and coatings, subject to good manufacturing practice removal |
| EU 10/2011 (Plastics Food Contact) | Positive list; acetone not listed as monomer or additive, but allowed as production aid with 0.02 mg/kg specific migration limit | Requires validation of no detectable residual acetone (LOD 0.01 mg/L) in food simulant |
| ICH Q3C (R6) Guideline | Class 3 solvent (low toxic potential) | Permitted daily exposure 50 mg/day; residual acetone in pharmaceutical intermediates must be controlled per USP <467> |
| RoHS Directive 2011/65/EU | Not applicable to organic solvents | No heavy metal restrictions, but acetone used to clean electronic assemblies must leave no ionic residues exceeding 1.56 μg/cm² NaCl equivalent per IPC-TM-650 method 2.3.25 |
| DIN 55685 | Testing of solvents for coatings – purity and evaporation | Acetone evaporation number 2.8 (diethyl ether = 1); used as a viscosity reducer in high-solids acrylic lacquers at 5–10 wt% |
When acetone is deployed as a process solvent in the manufacture of pharmaceutical intermediates—such as the crystallisation of cefadroxil monohydrate from an acetone-water mixture—the residual solvent limit in the active pharmaceutical ingredient must comply with the
50 mg/g (Class
3 solvent) threshold of
ICH Q3C. Drying operations in a vacuum tumble dryer at
45 °C and
25 mbar absolute pressure must reduce acetone content from an initial
15 wt% in the wet cake to below
0.1 wt% within
8 hours; the drying curve is highly sensitive to the water content of the acetone-grade used for the final wash. A grade with
0.5 wt% water—the maximum permitted by
ASTM D329—extends the drying time by
2–3 hours compared to a low-water grade at
0.15 wt%, because water forms a higher-boiling azeotrope that retards the evaporation flux in the falling-rate drying period. LyondellBasell acetone with water content controlled to
0.2 wt% ± 0.05 wt% has been qualified in a current good manufacturing practice (
cGMP) environment under a type II drug master file, enabling its use without additional on-site distillation for crystallisation steps that are particle-size critical; a change from an uncontrolled source with
0.45 wt% water to the tighter specification reduced the final product’s particle size
d90 from
180 μm to
120 μm, meeting the micronisation target for inhalation-grade powders. In the formulation of alkyd-based coil coatings applied at
45 m/min line speed on a
0.5 mm galvanised steel substrate, acetone cuts the viscosity of the base resin from
2800 mPa·s to
350 mPa·s at
25 °C when added at
8 wt%, enabling application via a reverse-roll coater without the need for heated feed lines. The rapid evaporation—flash point
-18 °C, boiling range
56.1 ± 0.5 °C—requires that the coater pan be covered with a hood maintained at a face velocity of
0.5 m/s to prevent vapour accumulation above
10% LEL, and that the downstream oven be divided into a
4-zone profile:
70 °C,
100 °C,
140 °C,
230 °C peak metal temperature. Published data for the effect of trace mesityl oxide on the yellowing of titanium-dioxide-pigmented alkyd enamels during overbaking at
200 °C for
10 minutes indicates a
1.5-unit increase in Delta b* (CIE LAB) for every
50 mg/kg of mesityl oxide in the acetone; the LyondellBasell typical value of
<15 mg/kg therefore contributes negligibly to the colour drift budget of
Delta E < 1.0 required by the end-user specification for architectural cladding. The use of acetone in the extraction and purification of natural tocopherols (vitamin E) from deodoriser distillate involves a liquid-liquid extraction step in a
5-stage centrifugal extractor where the solvent-to-feed ratio is maintained at
3:1 (v/v). Acetone selectivity for tocopherols over free fatty acids is strongly influenced by water content: at
0.2 wt% water, the partition coefficient for alpha-tocopherol is
4.7, whereas at
0.6 wt% water it drops to
3.9, reducing recovery from
97% to
93%. The extract is subsequently concentrated in a wiped-film evaporator operating at
1 mbar and
120 °C jacket temperature; acetone with non-volatile residue above
0.002 wt% leaves a caramelised film on the evaporator’s heated wall, increasing the power draw of the rotor by
15% and necessitating a caustic clean-in-place cycle every
72 hours instead of the design basis of
200 hours. LyondellBasell’s low-residue acetone (
NVR 0.0005 g/100 mL) has been demonstrated in a production campaign of
30 days to maintain evaporator heat transfer coefficients within
10% of the clean value, thereby avoiding the throughput derate otherwise imposed by fouling. Thermal stability and byproduct formation during acetone recovery by distillation Closed-loop acetone recovery columns in pharmaceutical manufacturing—typically a
15-tray Oldershaw column operated at a reflux ratio of
2:1—must contend with the build-up of diacetone alcohol and mesityl oxide resulting from base-catalysed aldol condensation if the sump pH rises above
7.0. The presence of
10–20 mg/kg of sodium ions, leached from glass-lined equipment or introduced through poor-quality process water, provides sufficient alkalinity to initiate condensation at sump temperatures of
80–110 °C; this is suppressed by co-feeding
0.05 wt% of acetic acid into the feed, which depresses the pH to
5.0–5.5 without exceeding the acidity specification of the recovered acetone. Without acid buffering, the diacetone alcohol concentration in the recovered solvent has been observed to climb from
50 mg/kg to
1200 mg/kg within
48 hours of continuous operation, at which point the product fails the permanganate time test (
ASTM D1363 <
30 minutes) and becomes unsuitable for reuse in oxidation-sensitive reaction steps. LyondellBasell acetone, stabilised to resist aldol condensation through a low-residual-sodium profile (
<0.1 mg/kg by inductively coupled plasma mass spectrometry), reduces the need for acid addition and extends the interval between column boil-outs from
6 months to
12 months, based on operational data from a multi-purpose API facility. In the production of polyvinylidene fluoride (
PVDF) binders for lithium-ion battery electrodes, acetone functions as the principal solvent for dissolving
4–8 wt% PVDF homopolymer (
Kynar® HSV 900 or equivalent) to prepare a cathode slurry with
96 wt% lithium nickel manganese cobalt oxide (
NMC 811) and
2 wt% carbon black. The dissolution process in a planetary mixer under
200 mbar vacuum requires
2–4 hours at
25–30 °C; acetone containing water above
0.3 wt% induces the gelation of the PVDF solution, manifest as a rapid increase in complex viscosity from
15 Pa·s to
>80 Pa·s at
1 Hz oscillation, which prohibits the subsequent slot-die coating at
1.5 m/min onto
12 µm aluminium foil. The cohesive strength of the dried electrode, measured by a
180° peel test per
ASTM D903, drops from
12 N/cm to
6 N/cm when the acetone used for slurry preparation contains
0.5% isopropanol because the latter plasticises the PVDF binder and reduces its crystallinity from
45% to
32% as determined by differential scanning calorimetry. Manufacturers of battery-grade binders specify acetone purity of at least
99.8% with foreign alcohol content
<0.1%, a requirement that aligns with LyondellBasell’s alcohol-byproduct specification of
<500 mg/kg total.
