| HS Code | 557081 |
| Productname | Magnesium Methoxide |
| Chemicalformula | C2H6MgO2 |
| Linearformula | Mg(OCH3)2 |
| Molecularweight | 86.37 g/mol |
| Casnumber | 109-64-8 |
| Ecnumber | 203-689-8 |
| Iupacname | magnesium dimethoxide |
| Synonyms | Magnesium methylate; magnesium dimethoxide |
| Appearance | White to off-white powder or colorless to pale yellow methanol solution |
| Physicalstate | Solid in pure form; liquid as methanol solution |
| Odor | Methanol-like |
| Density | 0.816 g/mL at 25 °C (typical 6-10 wt% methanol solution) |
| Meltingpoint | >200 °C with decomposition |
| Boilingpoint | 64.7 °C for methanol solution |
| Flashpoint | 11 °C (52 °F) closed cup for methanol solution |
| Solubility | Soluble in methanol; reacts with water |
| Basicity | Strongly basic |
| Waterreactivity | Reacts with water to form magnesium hydroxide and methanol |
| Moisturesensitivity | Yes |
| Stability | Stable under dry inert atmosphere; sensitive to moisture and air |
As an accredited Magnesium Methoxide factory, we enforce strict quality protocols—every batch undergoes rigorous testing to ensure consistent efficacy and safety standards.
| Packing | Magnesium Methoxide supplied in 100 g, 500 g, or 1 kg sealed, moisture-resistant containers with appropriate hazard labels. |
| Container Loading (20′ FCL) | Container Loading (20′ FCL) for Magnesium Methoxide: sealed, palletized drums; cargo secured; kept dry; IMDG-compliant with required hazardous-goods labels and documentation. |
| Shipping | Magnesium Methoxide is typically shipped as a flammable methanol solution under UN 3274, Alcoholates solution, n.o.s. (Magnesium methoxide, methanol), Class 3, Packing Group II. It requires sealed, moisture-resistant packaging, flammable-liquid labeling, and compliance with DOT/IMDG/IATA hazardous-material regulations; toxic/corrosive subsidiary risks may apply. |
| Storage | Store magnesium methoxide in a cool, dry, well-ventilated flammable-storage area away from heat, sparks, flames, oxidizers, acids, and moisture. Keep containers tightly closed, preferably under dry nitrogen, in compatible, clearly labeled vessels. Protect from sunlight, segregate from incompatibles, and use grounding/bonding when handling. Keep spill kit and PPE available. |
| Shelf Life | Magnesium methoxide is moisture-sensitive; store sealed under inert gas in a cool, dry place. Typical shelf life is about two years. |
In methyl ester production, magnesium methoxide is charged as a 6–10 wt% solution in methanol through a static mixer immediately upstream of the transesterification reactor. Published pilot-scale data for refined soybean and rapeseed oil indicate active catalyst dosages of 0.3–0.9 wt% relative to oil mass, with methanol-to-oil molar ratios of 6:1 to 9:1 and reactor jacket temperature held at 60–65 °C. Compared with sodium methoxide, magnesium methoxide generates lower concentrations of sodium soaps but requires longer residence times, typically 90–180 min in a continuous stirred-tank reactor or 45–90 min in a two-stage plug-flow reactor with downstream shear mixers. The compliance envelope for the resulting fatty acid methyl ester includes EN 14214:2012+A2:2019, ASTM D6751-23a, total ester content by EN 14103:2020, and alkaline earth metal residue control by EN 14538. Downstream processing consists of gravity separation at 55–60 °C, acidulated water washing, vacuum-assisted glycerin stripping, and final polishing through 10 µm bag filtration. Terminal finished product types are B100 FAME for blending into B7 and B20 transport fuels, as well as distilled methyl esters for solvent and lubricant base applications.
For sol-gel deposition of magnesium oxide buffer layers on silicon, glass, and textured metallic tape substrates, magnesium methoxide is dissolved in anhydrous 2-methoxyethanol at a concentration of 0.10–0.50 mol dm⁻³. The hydrolysis step is controlled by adding a mixture of water and 0.1 mol dm⁻³ nitric acid to maintain a water-to-alkoxide molar ratio between 0.8:1 and 2.5:1 and a sol pH below 4.0; failure to maintain this window produces colloidal aggregation and increases surface roughness above 5 nm Ra. Deposition is carried out by spin coating at 2000–4000 rpm for 30–60 s or by dip coating with withdrawal speeds of 1–5 mm s⁻¹, followed by drying at 150–250 °C and annealing at 600–800 °C under flowing oxygen. Process compliance for electronics-grade precursor use is governed by ISO 14644-1:2015 Class 5 cleanroom limits, while film adhesion is evaluated according to ASTM D3359-23 and thermal cycling performance according to JEDEC JESD22-A104. Terminal products include MgO insulating buffer layers for plasma display panels, dielectric protective films in thin-film electroluminescent devices, and MgO buffer layers in coated conductor architectures for superconducting tapes.
In polyolefin catalyst manufacturing, magnesium methoxide serves as a controlled-morphology magnesium precursor for the formation of MgCl₂-based pro-catalyst supports. The methoxide is suspended in a paraffinic or aromatic diluent and contacted with excess TiCl₄ at an initial temperature of -5 °C to 10 °C in a jacketed glass-lined reactor, followed by stepwise heating to 90–110 °C over 2–4 h. The Mg:Ti molar charge ratio is maintained between 1:8 and 1:12, and an internal electron donor is introduced at 1–10 wt% relative to the MgCl₂ carrier to control stereo-specificity. The halogenation step is exothermic; pilot-plant data show that excursions above 12 °C during the initial addition generate uncontrolled TiCl₄ reduction and increase the fraction of sub-5 µm fines, which later impair polymer morphology. The process atmosphere must hold oxygen below 5 ppm and moisture below 10 ppm, because residual water hydrolyzes TiCl₄ and generates inactive TiOCl₂. Compliance for the resulting polyolefin resins is verified with ISO 1133-1:2022 for melt mass-flow rate, ASTM D1238-23 for polyethylene, and FDA 21 CFR 177.1520 or EU 10/2011 for food-contact grades. Terminal finished products are high-density polyethylene for blow-molded containers, isotactic polypropylene for injection-molded automotive parts, and impact copolymer polypropylene for appliance housings.
Alkyd resin alcoholysis reactors use magnesium methoxide as a low-color transesterification catalyst where lithium or calcium soap catalysts are unacceptable. Charge ratios typically range from 0.05 wt% to 0.20 wt% relative to the refined vegetable oil portion, and the catalyst is added as a methanolic solution after the reactor has been dried to less than 50 ppm moisture. The alcoholysis stage is run at 230–240 °C under inert gas for 60–120 min with pentaerythritol or glycerol to form monoglycerides; the subsequent polyesterification with phthalic anhydride is conducted at 200–220 °C with xylene azeotropic water removal until acid number falls below 10 mg KOH g⁻¹. Compliance for the resulting resins is assessed by ISO 3251:2019 for non-volatile content, ASTM D1544-04 for Gardner color, and ISO 3219:1994 for rheometry. Terminal product types include long-oil alkyd architectural coatings, medium-oil alkyd industrial primers, and unsaturated polyester gel coats for sanitary ware.
In pharmaceutical intermediate and fine chemical synthesis, anhydrous magnesium methoxide is metered into a nitrogen-blanketed reactor as a 1.5–2.5 mol dm⁻³ solution in methanol, where it functions as a deprotonation or condensation reagent for substrates that are incompatible with sodium ethoxide or potassium tert-butoxide. Typical charge ratios are 1.0–1.5 equivalents for stoichiometric enolate formation and 5–20 mol% for catalytic transesterification or Michael additions; reaction temperatures are maintained between -10 °C and 25 °C to suppress magnesium alkoxide aggregation. The process stream is quenched with 10 wt% aqueous ammonium chloride, extracted with ethyl acetate, and dried over molecular sieves before vacuum distillation. Compliance for this downstream segment is governed by ICH Q3D elemental impurity limits, ICH Q3C residual methanol Class 2 limits, and ISO 9001:2015 for process quality management where the intermediate is manufactured under contract. Terminal product types are pharmaceutical intermediates, chiral building blocks, and agrochemical intermediates requiring anhydrous alkoxide bases with controlled residual metal profiles.
Overbased magnesium sulfonate detergent manufacturing uses magnesium methoxide as an alternative magnesium source to magnesium oxide or magnesium hydroxide when lower reaction temperatures and faster carbonation are required. The methoxide is charged into a hydrocarbon solvent along with a branched alkylbenzene sulfonic acid, water, and carbon dioxide; the magnesium content in the finished overbased detergent is controlled between 9 wt% and 14 wt%, corresponding to a total base number of 300–500 mg KOH g⁻¹ by ASTM D2896-21. Carbonation is carried out at 40–70 °C, with methanol stripped under vacuum and recycled; failure to remove methanol raises flash point and limits downstream blending. Compliance for lubricant additive packages is verified with ASTM D2896-21 for total base number and ASTM D4951-14 for elemental magnesium. Terminal finished products are marine trunk piston engine oils, heavy-duty diesel engine oils, and gas engine oils where sulfated ash limits require controlled overbased detergent content.
Competitive Magnesium Methoxide prices that fit your budget—flexible terms and customized quotes for every order.
For samples, pricing, or more information, please contact us at +8615380400285 or mail to sales2@ascent-chem.com.
We will respond to you as soon as possible.
Tel: +8615380400285
Email: sales2@ascent-chem.com
Flexible payment, competitive price, premium service - Inquire now!
Magnesium methoxide (CAS 109-88-6), formula Mg(OCH3)2, has a molecular mass of 86.37 g mol−1. Commercial product models include a methanolic solution at 6–10 wt% and, where moisture-excluded handling is available, a neat solid grade with assay ≥98 wt%. The divalent magnesium centre carries 2 methoxide groups per metal atom, which differentiates its alkoxide delivery profile from sodium and potassium methoxide. In processing lines the solution is metered under nitrogen because each 1 mol of water hydrolyzes 2 mol of methoxide to magnesium hydroxide and methanol.
The control of methanolic magnesium methoxide begins with total alkalinity and water content because both determine active catalyst inventory and hydrolysis losses. A typical certificate of analysis reports assay as magnesium methoxide equivalent, free methanol, water, chloride, sulfate, insoluble matter, density, viscosity, and flash point. Table 1 lists the parameters used for incoming inspection and mass-flow calibration.
| Parameter | Typical specification | Reference method |
|---|---|---|
| Magnesium methoxide content | 6.0–10.0 wt% | Acid-base titration after hydrolysis |
| Total alkalinity | 1.4–2.3 mol kg−1 | Titration with hydrochloric acid |
| Methanol | balance | Gas chromatography |
| Water | ≤0.2 wt% | ASTM E203 / ISO 760 |
| Chloride | ≤50 mg kg−1 | ASTM D4327 |
| Sulfate | ≤100 mg kg−1 | ASTM D4327 |
| Insoluble matter | ≤0.1 wt% | Filtration through 0.45 μm membrane |
| Kinematic viscosity at 20 °C | 0.5–0.7 mm² s−1 | ASTM D445 |
| Density at 20 °C | 0.79–0.82 g cm−3 | ASTM D4052 |
| Flash point closed cup | 11 °C ±1 °C | ASTM D56 / DIN 51755 |
The acid-base titration is performed by quenching a known mass of solution in deionized water and titrating the resulting hydroxide with standardized hydrochloric acid. The result is reported as Mg(OCH3)2 equivalent. Water is kept below 0.2 wt% because each 1 mol of water destroys 2 mol of methoxide and produces 1 mol of magnesium hydroxide. Production-scale bulk tanks should be blanketed with dry nitrogen at 30–50 mbar positive pressure; pressure relief must be sized for methanol vapour at 64.7 °C boiling point.
Moisture ingress beyond specification is first visible as a fine white haze and then as settleable precipitate. The hydrolysis product, magnesium hydroxide, has low methanol solubility and can blind 0.45 μm and 1 μm cartridge filters on catalyst dosing loops. Plant operators using 316L stainless steel day tanks and peristaltic or diaphragm metering pumps should avoid dead legs where humid air can accumulate. Batch-to-batch variation in commercial methanolic solutions is most often seen in insoluble matter and water content rather than total alkalinity; release testing under ISO 9001:2015 does not guarantee the absence of storage-induced hydrolysis after container opening.
Evaluation of magnesium methoxide as a transesterification catalyst requires normalization against total methoxide equivalents rather than mass addition. Sodium methoxide is usually supplied at 25–30 wt% in methanol; magnesium methoxide is typically supplied at 6–10 wt%. The lower concentration means larger volumetric dosing rates for the same methoxide inventory, but the divalent cation can reduce the concentration of soluble alkali-metal hydroxide byproducts after water contact.
| Property | Magnesium methoxide | Sodium methoxide | Potassium methoxide |
|---|---|---|---|
| Methoxide groups per metal atom | 2 | 1 | 1 |
| Molecular mass | 86.37 g mol−1 | 54.02 g mol−1 | 70.13 g mol−1 |
| Molar mass per methoxide equivalent | 43.19 g mol−1 | 54.02 g mol−1 | 70.13 g mol−1 |
| Typical commercial concentration | 6–10 wt% | 25–30 wt% | 25–32 wt% |
| Hydrolysis solid product | Mg(OH)2 precipitate | soluble NaOH | soluble KOH |
| Gelation or filter-binding tendency | high | low | low |
On a per-mole metal basis, magnesium methoxide transports double the methoxide equivalents of sodium methoxide; on an equal-mass basis the advantage is smaller because its molecular mass is higher. Process calculations should use total alkalinity measured by titration because residual water in feedstock consumes methoxide stoichiometrically before transesterification. For a 1000 kg oil batch at 0.4 mol methoxide per kg oil, the required methoxide inventory is 400 mol. An 8 wt% magnesium methoxide solution contains approximately 1.85 mol kg−1 total methoxide; therefore 216 kg of solution is required. The same methoxide inventory from 30 wt% sodium methoxide requires 72 kg of solution. This volumetric difference affects pump sizing and heat load because methanol introduced with the catalyst participates in downstream methanol recovery. Finished methyl ester specifications under ASTM D6751 or EN 14214 require residual methanol and water control; the additional methanol introduced by the lower concentration of magnesium methoxide increases the load on methanol recovery vacuum distillation.
In continuous methyl ester production at 5000 kg h−1, a magnesium methoxide stream at 8 wt% and 0.4 mol methoxide per kg oil corresponds to approximately 1080 kg h−1 of catalyst solution. This is 3 times the mass flow of a 30 wt% sodium methoxide stream for equal methoxide throughput. Static mixer length must account for the higher solvent fraction; Reynolds numbers below 10 in laminar dosing lines require longer residence zones to achieve homogeneous methoxide distribution. Use of a coriolis mass-flow meter is preferred over volumetric metering because density shifts with methanol temperature and concentration. Feedstock water above 0.05 wt% is the primary process conflict. Under these conditions magnesium methoxide produces solid Mg(OH)2, which can blind centrifuge bowls and plate-and-frame filters. In sodium methoxide systems the equivalent hydrolysis product is soluble sodium hydroxide, which tends to form soap and increase viscosity. Therefore magnesium methoxide may be selected when downstream soap minimization is required, but only if solids removal capacity is available. Published data for this specific continuous configuration is limited, and pilot runs with the actual feedstock are required before scale-up.
Beyond methyl ester catalysis, magnesium methoxide serves as a sol-gel precursor for magnesium oxide films and mixed-metal oxides. Hydrolysis and condensation are controlled by adding the methanolic solution to a water-alcohol mixture under vigorous agitation in a 250–500 mL laboratory reactor or, for production, in a jacketed stainless steel vessel with a high-shear disperser. The hydrolysis ratio R = [H2O]/[Mg(OCH3)2] determines gelation time: at R = 2 hydrolysis is stoichiometric, while R > 4 can produce gelation in less than 30 min at 25 °C. Coating baths are usually maintained below 0.5 M magnesium and filtered through 0.22 μm membrane filters; dip-coating withdrawal rates of 1–10 mm s−1 yield films in the 50–300 nm thickness range, but published data for this specific configuration is limited above pilot scale.
Sol-gel reactors require pH control. Addition of magnesium methoxide to neutral water can cause rapid condensation and precipitation; acetic acid or acetylacetone is used as a chelating agent to moderate the hydrolysis rate. These additives shift the coordination sphere of magnesium and can increase bath pot life. Viscosity is monitored with a Brookfield viscometer at 25 °C; if viscosity exceeds 10 mPa·s, the coating bath is usually discarded because particle formation reduces film uniformity. Adhesion of calcined MgO films to glass or silicon is evaluated by tape testing per ASTM D3359-17, although film performance depends on substrate cleaning and thermal history.
The main impurity classes in commercial magnesium methoxide solutions are water, chloride, sulfate, and magnesium hydroxide oligomers formed by partial hydrolysis. Chloride and sulfate are typically specified below 50 mg kg−1 and 100 mg kg−1, respectively, because residual anions influence the surface charge of precipitated magnesium hydroxide and the sintering behaviour of magnesium oxide powders. Storage stability is not indefinite: over 6 months at 5–30 °C, a sealed container under nitrogen may develop a fine precipitate due to slow reaction with trace water; the precipitate can often be redispersed by agitation but not fully re-dissolved.
The operational boundary is strict with regard to water. At relative humidity above 60%, transfer of methanolic magnesium methoxide without nitrogen purge leads to surface crusting on fittings and progressive loss of alkalinity. The compound is incompatible with strong oxidizing agents, strong acids, and water; mixing with amine-based additives can accelerate condensation in sol-gel systems and should be avoided where colloidal stability is required. All transfer lines should be low-dead-volume and constructed from 316L or PTFE-lined components; carbon steel is unsuitable because trace water and chloride can initiate pitting. Chloride is particularly important in electronic-grade MgO because residual chloride can segregate at grain boundaries during sintering. Sulfate can retard densification and is controlled to 100 mg kg−1. The insoluble-matter specification is set by filtration performance rather than chemical purity; particles above 0.45 μm can plug catalyst injection nozzles and spin-coating filters. For sol-gel use, the solution is typically refiltered at 0.22 μm immediately before use. Incoming inspection should include Karl Fischer water ASTM E203, acidity/alkalinity titration, and visual clarity check against a 10 NTU turbidity standard.
Relative to magnesium ethoxide, formula Mg(OC2H5)2 and molecular mass 114.43 g mol−1, magnesium methoxide releases methanol rather than ethanol during hydrolysis; this matters when residual solvent must meet fuel or pharmaceutical specifications. Magnesium ethoxide releases ethanol, which is a separate azeotrope and requires different distillation cut points. Compared with aluminium and titanium alkoxides, magnesium methoxide hydrolyzes less violently but forms a more insoluble hydroxide network; the resulting MgO has a compact cubic rock-salt structure after calcination. In applications requiring a soluble divalent methoxide source, magnesium methoxide is used rather than calcium methoxide because of its lower molecular mass per metal and higher methoxide solubility in methanol. Selection between these products must be made on the basis of total alkalinity, cation tolerance, solvent compatibility, downstream separation burden, and equipment materials of construction.
