Patent Grant
10173979
The present invention relates to a process for producing 2-(2,2,6,6-tetramethylpiperidin-4-yl)propane-1,3-diamine, which can be used as hardener in epoxide applications.
2-(2,2,6,6-tetramethylpiperidin-4-yl)propane-1,3-diamine (TMP-PDA) has the chemical structure depicted in formula 1.
It is known that amines may be employed as hardeners in epoxy systems. Epoxy resins are prepolymers comprising two or more epoxy groups per molecule. The reaction of these resins with a range of hardeners affords crosslinked polymers. An overview of possible resins and hardeners, their use and properties is given in H. Schumann, “Handbuch Betonschutz durch Beschichtung”, Expert Verlag 1992, pages 396-428.
It is an object of the invention to find a process for producing 2-(2,2,6,6-tetramethylpiperidin-4-yl)propane-1,3-diamine.
It is also an object of the invention to find a novel amine suitable for hardening epoxy systems.
The invention provides a process for producing 2-(2,2,6,6-tetramethylpiperidin-4-yl)propane-1,3-diamine by
The production of the compound according to the invention 2-(2,2,6,6-tetramethylpiperidin-4-yl)propane-1,3-diamine proceeds in step A) via a Knoevenagel condensation between triacetonamine (TAA) and malononitrile. The reaction may be performed in a solvent or in a solvent-free reaction system under mild reaction conditions, preferably at 20-40° C. and atmospheric pressure. The catalyst employed is preferably zirconyl chloride or piperidine. After complete conversion of the reactants the intermediate 2-(2,2,6,6-tetramethylpiperidin-4-ylidene)malononitrile (cf. structure formula 2 in Example 1) may be precipitated out as solid by cooling the reaction solution. A further purification may be effected by distillation for example.
The production of TMP-PDA from 2-(2,2,6,6-tetramethylpiperidin-4-ylidene)malononitrile is effected in step B) by hydrogenation which may be performed in one or more stages. When a plurality of hydrogenation reactions are used the individual stages may be performed in a reactor having different catalyst zones or in a plurality of separate or serially connected reactors. The hydrogenation is preferably effected in fixed-bed reactors. Suitable reactor types are, for example, shaft furnaces, tray reactors or shell and tube reactors. It is also possible to connect a plurality of fixed-bed reactors in series for the hydrogenation, each of the reactors being operated in downflow mode or in upflow mode as desired.
The catalysts employed may in principle be any catalysts which catalyze the hydrogenation of nitrile groups with hydrogen. Particularly suitable catalysts are nickel, copper, iron, palladium, rhodium, ruthenium and cobalt catalysts, very particularly palladium, ruthenium and cobalt catalysts. To increase activity, selectivity and/or service life, the catalysts may comprise additional doping metals or other modifiers. Typical doping metals are, for example, Mo, Fe, Ag, Cr, Ni, V, Ga, In, Bi, Ti, Zr and Mn, and the rare earths. Typical modifiers are, for example, those with which the acid-base properties of the catalysts can be influenced, preferably alkali metals and alkaline earth metals or compounds thereof, preferably magnesium and calcium compounds, and also phosphoric acid or sulphuric acid and compounds thereof.
The catalysts may be employed in the form of powders or shaped bodies, for example extrudates or compressed powders. It is possible to employ unsupported catalysts, Raney-type catalysts or supported catalysts. Preference is given to Raney-type and supported catalysts. Suitable support materials are, for example, silicon dioxide, aluminium oxide, aluminosilicates, titanium dioxide, zirconium dioxide, kieselguhr, aluminium-silicon mixed oxides, magnesium oxide and activated carbon. The active metal can be applied to the support material in a manner known to those skilled in the art, for example by impregnation, spray application or precipitation. Depending on the method of catalyst production, further preparation steps known to those skilled in the art are necessary, for example drying, calcining, shaping and activation. Further assistants, for example graphite or magnesium stearate, may optionally be added for shaping. The required volume of the hydrogenation catalysts to be used is determined by the LHSV value (liquid hourly space velocity) which is dependent on operating pressure, temperature, concentration and catalyst activity and must be adhered to in order to ensure as complete a hydrogenation as possible.
Production of the inventive diamine TMP-PDA preferably employs hydrogenation catalysts based on palladium and/or cobalt. These catalysts show particularly good activity to achieve a high yield.
The catalysts may be employed in the form of powders or fixed-bed catalysts. The hydrogenation may be effected in batch mode or in continuously operated plants.
The reaction conditions for the hydrogenation are between 20-120° C. and 20-300 bar.
The hydrogenation may be performed in one or more stages. The hydrogenation is preferably performed in two stages. In the first of these stages, reaction conditions of 20-120° C. and 20-300 bar, preferably 40-100° C. and 25-150 bar and particularly preferably 60-90° C. and 40-80 bar are chosen. In the second stage of the hydrogenation, reaction conditions of 20-120° C. and 20-300 bar, preferably 50-115° C. and 50-200 bar and particularly preferably 80-110° C. and 80-140 bar are chosen.
The first stage of the hydrogenation preferably employs a palladium catalyst.
The second stage of the hydrogenation preferably employs a Raney-type catalyst. It is particularly preferable when after activation the catalyst in its entirety has the following composition in weight percent (wt %), the proportions summing to 100 wt % based on the metals present:
cobalt: 57 to 84 wt %
aluminium: 10 to 40 wt %
chromium: 1 to 2 wt %
nickel: 2 to 4 wt %
and
with particle sizes of the catalyst, i.e. of the pellet particles, having a statistical distribution between 3 to 7 millimeters (mm), wherein up to 10 percent of the particles may also be outside the stated range of the stated lower limit or upper limit but also in each case up to 10 percent may be outside the stated range of the stated lower limit and upper limit.
The reaction mixture leaving the hydrogenation is further purified by customary methods to obtain TMP-PDA of the desired quality. Any standard separation methods, for example distillation, flash evaporation, crystallization, extraction, sorption, permeation, phase separation or combinations of the above, may be employed here. The purification may be conducted continuously, batchwise, in one or more stages, under vacuum or under pressure. The purification of TMP-PDA is preferably performed by distillation, for example.
The purification is preferably achieved by distillation under pressure and/or under vacuum in a plurality of steps. Any desired distillation columns with or without internals may be used to this end, for example dephlegmators, dividing walls, unordered internals or random packings, ordered internals or structured packings, or trays with or without forced flow.
Use as Epoxy Hardener:
The invention also provides for the use of 2-(2,2,6,6-tetramethylpiperidin-4-yl)propane-1,3-diamine (TMP-PDA) as a hardener in epoxy resin compositions.
Contemplated as the epoxy resin component are in principle all epoxy resins that may be cured with amines. Epoxy resins include, for example, polyepoxides based on bisphenol A diglycidyl ether, bisphenol F diglycidyl ether or cycloaliphatic types. However, preference is given to using epoxy resins based on bisphenol A and optionally those based on bisphenol F, optionally also in admixture. The resins and hardeners are preferably employed in equivalent amounts. However, deviations from the stoichiometric ratio are also possible.
The yield of 2-(2,2,6,6-tetramethylpiperidin-4-ylidene)malononitrile was 90%.
150 ml of activated Raney cobalt alloy pellets were installed as a fixed bed in a 2 L pressure autoclave fitted with a catalyst cage. This catalyst had the following composition in weight percent (wt %), the proportions summing to 100 wt % based on the metals present:
cobalt: 75.9 wt %
aluminium: 20.0 wt %
chromium: 1.5 wt %
nickel: 2.6 wt %
A sieve fraction of the catalyst having a statistical distribution between 2.0 and 5.0 millimeters (mm) was employed, wherein up to 10% of the particles may be above the stated upper limit and up to 10% of the particles may be below the stated lower limit.
The yield of the two-stage hydrogenation was 85 wt % of TMP-PDA based on the employed substance 2-(2,2,6,6-tetramethylpiperidin-4-ylidene)malononitrile from step A.
The epoxy resin employed was the standard resin Epikote 828 from Hexion having an epoxy equivalent weight of 188 g/eq. Said resin was blended in stoichiometric equality of the H equivalents with the hardener component TMP-PDA (cf. Table 1) and the glass transition temperature (Tg) was determined after a dwell time of one hour at a defined curing temperature (Table 2). The respective reaction conversions were determined via the recorded evolution of heat from the curing reaction in relation to the maximum evolution of heat (Table 3).
As is readily apparent to a person skilled in the art from Table 1, Table 2 and Table 3, TMP-PDA is a suitable hardener component in epoxy resin systems.
| Number | Date | Country | Kind |
|---|---|---|---|
| 16173860 | Jun 2016 | EP | regional |
This application is a divisional application of U.S. application Ser. No. 15/605,268 filed May 25, 2017, currently pending, which claims the benefit of European Application No. DE 16173860.4 filed on Jun. 10, 2016, the disclosure of which is expressly incorporated herein by reference.
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| Number | Date | Country | |
|---|---|---|---|
| 20180093952 A1 | Apr 2018 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 15605268 | May 2017 | US |
| Child | 15832047 | US |
