Patent Application
20060086667
This invention relates to chromatographic processes for obtaining optically active modafinil compounds, including the levorotatory enantiomer, (−)-benzhydrilsulfinylacetamide (“armodafinil”), and the dextrorotatory enantiomer, (+)-benzhydrilsulfinylacetamide. Such processes include commercially viable methods for producing armodafinil on an industrial scale suitable for pharmaceutical use. Racemic modafinil is the active agent in the pharmaceutical product Provigil®, which has been approved by the United States Food and Drug Administration for use in the treatment of excessive daytime sleepiness associated with narcolepsy, and to improve wakefulness in patients with excessive sleepiness associated with obstructive sleep apnea/hypopnea syndrome and shift work sleep disorder.
The levorotatory isomer of modafinil and processes for its preparation have been described in U.S. Pat. No. 4,927,855 (“the '855 patent”), which is incorporated herein in its entirety. The '855 patent details the preparation of the levorotatory isomer by achiral synthesis. This process is not sufficiently robust to produce armodafinil on an industrial scale in pharmaceutically acceptable purities. It would be of significant advantage to obtain armodafinil in large quantities that meet acceptable pharmaceutical standards.
A variety of methods have been utilized to obtain compounds in stereochemically pure form. Stereoisomers can be synthesized using asymmetric synthetic techniques, however such syntheses often require expensive reagents. Alternatively, stereoisomers can be obtained by selective recrystallization of one stereoisomer, however such a process cannot be used for all compounds, and may not be useful for enantiomeric separations. In addition, the process is considered inefficient, in that product recovery is often low and purity uncertain. Stereoisomers can also be resolved chromatographically, although the large amount of solvent required for conventional batch chromatography is cost prohibitive and results in the preparation of relatively dilute products. Limited throughput volumes also often make batch chromatography impractical for large-scale production. Moreover, the number of technical parameters required for its applicability on an industrial scale makes it difficult to select appropriate conditions for the mass production of pharmaceutically viable amounts of an enantiomeric compound. Determination of the conditions necessary for productive separation of enantiomers has been found by those of ordinary skill in the art to be a matter of trial and error. Even so, it is a common for those skilled in the art to find chiral separation of certain chiral mixtures to be inefficient or ineffective. In the instant case, these problems are heightened by the relative difficulty in solubilizing modafinil in many common solvents. The object of the present invention is to provide an efficient process for the separation of the modafinil enantiomers from racemic modafinil that provides a viable combination of selectivity and resolution at high throughput volumes or in bulk amounts.
Hence, the present invention is directed to producing optically pure armodafinil at relatively low cost and with optimized productivity on a commercially viable scale. It has been found that multi-column continuous chromatography processes are capable of providing large scale, industrial enantiomeric separation of racemic modafinil, and in particular for the preparation of armodafinil. In particular, the necessary operational parameters have been found to yield an excellent degree of separation of the stereoisomers of modafinil with sufficiently robust productivity on a large scale. These multicolumn continuous chromatographic processes overcome certain limitations in classical batch chromatography, such as having increased productivity, lower eluent composition and higher robustness, resulting in lower final purification costs.
The present invention provides an improved process for the isolation of the enantiomeric forms of modafinil with high enantiomeric purity and high overall yields. Thus the present invention provides processes for obtaining an enantiomer of modafinil, and in particular, the levorotatory isomer of modafinil, by forming a solution of racemic modafinil and separating the enantiomers of modafinil by means of a continuous chromatographic process. The continuous chromatographic process includes, but is not limited to a countercurrent chromatographic process, such as a simulated moving bed (“SMB”) process, or a non-steady state system, such as the Varicol™ process, which uses at least two columns packed with an optical resolution packing material from the amylosic or cellulosic class of polysaccharides or chemically modified forms thereof.
In an additional embodiment of the present invention, there is provided a method for chromatographically resolving at least one enantiomer (preferably armodafinil) from a racemic mixture of modafinil using multicolumn continuous chromatography, wherein the continuous chromatographic method comprises a liquid mobile phase comprising a least one solvent and a solid chiral stationary phase comprising a derivatized polysaccharide that is selected from the amylosic, cellulosic, chitosan, xylan, curdlan, dextran, and inulan class of polysaccharides.
The processes of the present invention can utilize any chromatographic method for separating racemic modafinil to produce optically pure armodafinil. Such methods include, but are not limited to, traditional single column batch chromatography, continuous chromatography, or a steady state, sequential injection process (as described in, for example, U.S. Pat. No. 5,630,943 and PCT Publ. No. WO 98/51391). Continuous chromatographic methods include, but are not limited to multicolumn continuous chromatographic processes, including such countercurrent chromatographic processes as SMB, or a non-steady state continuous chromatographic method known as the “Varicol™” process.
The SMB process is a continuous system that simulates counter-current flows to perform the chromatographic separation. The separation is achieved using a set of fixed-bed columns packed with a solid stationary phase; ports for the continuous introduction of solvent desorbent (mobile phase) and feed; ports for the continuous removal of raffinate (solution containing the less strongly retained enantiomer) and extract (solution containing the more strongly retained enantiomer); and a means of recycling fluid through the system, if necessary. In a closed loop system, the columns are connected such that the outlet of each column is connected to the inlet of the next column also with the outlet of the last column being connected to the inlet of the first column. Other implementations of the SMB process include an open loop system which can include 4-zone systems with external recycling or other 3-zone systems. All the inlet and outlet ports are shifted substantially simultaneously at substantially fixed time intervals in the fluid flow direction to simulate counter-current flow between the liquid phase and the solid phase. For the separation of stereoisomers, a chiral stationary phase (“CSP”) capable of chiral recognition is often employed.
The Varicol™ process is a non-steady state continuous separation process and is more fully described in U.S. Pat. No. 6,136,198, as well as in U.S. Pat. Nos. 6,375,839; 6,413,419; and 6,712,973 (all incorporated herein by reference in their entireties). This non-steady state process differs from the SMB process in that the inlet and outlet ports are not all shifted at the same time. The column distribution between zones does not stay the same during the period because the lines are shifted at different times, so the column allocation differs accordingly. In this process, there is no limitation on the number of configurations for a given number of columns, thereby giving the non-steady state process a greater degree of flexibility as compared to the SMB process. The potential for variation of the average length of given zones represented by column sections during the chromatographic separation can lead to an increase efficiency by using less columns, reducing the amount of the solid phase and solvent(s), and increasing higher purity yields.
In one aspect of the present invention, a five to six column-four variable zone Varicol™ system may be used. The zones vary in length during operation, and have an average rather than fixed length in a given operation cycle. In another aspect, a three column-four variable zone Varicol™ system is used, a system which cannot be utilized in a SMB process, as at least four columns with four zones are necessary to simulate the true moving bed system. For the SMB process, the minimal number of columns required for the separation is equal to the number of zones of the system, whereas the number of columns can be smaller than the number of zones in the Varicol™ system
In another aspect of the present invention the chiral stationary phase is derivatized with at least one sugar derivative, and in particular is a derivatized polysaccharide that is selected from the amylosic, cellulosic, chitosan, xylan, curdlan, dextran, and inulan class of polysaccharides. In certain embodiments, the chiral stationary phase is a member of the amylosic or cellulosic class of polysaccharides. Esters and carbamates of these materials in particular are suitable. In additional embodiments, the chiral stationary phase is selected from cellulose phenyl carbamate derivatives, such as cellulose tris (3,5-dimethylphenyl) carbamate (available from Daicel Chemical Industries, Ltd. as “Chiralcel OD”); cellulose tribenzoate derivatives, such as cellulose tris 4-methylbenzoate (available from Daicel Chemical Industries, Ltd. as “Chiralcel OJ”); cellulose tricinnamate (available from Daicel Chemical Industries, Ltd. as “Chiralcel OK”); amylose phenyl and benzyl carbamate derivatives, such as amylose tris [(S)-α-methyl benzylcarbamate] (available from Daicel Chemical Industries, Ltd. as “Chiralpak AS”), amylose tris (3,5-dimethylphenyl) carbamate (available from Daicel Chemical Industries, Ltd. as “Chiralpak AD”, or as “Chiralpak IA”, wherein the carbamate derivative is bonded to the amylosic backbone), amylose 3,4-substituted phenyl carbamate, and amylose 4-substituted phenyl-carbamate; and amylose tricinnamate.
Typically, the polysaccharide derivative is bonded or coated on silica gel, zirconium, alumina, ceramics and other silicas, and preferably on silica gel. Although the average particle diameter of the packing material varies depending on the volume flow rate of the solvent flowing in the chromatographic system, it is usually 1 to 300 μm, preferably 2 to 100 μm, more preferably 5 to 75 μm and most preferably 10 to 30 μm. As is known in the art, the selection of the average particle diameter of the packing material will help to adjust the pressure drop in the continuous chromatographic process and the efficiency of the packing material.
In a further aspect of the present invention, the mobile phase an organic solvent selected from the group consisting of C1-C10 alkanes, including hexane and heptane; alcohols (C1-C6) such as methanol, ethanol, propanol, isopropanol, butanol; acetates and propionates of these alcohols; ketones (C1-C10) such as acetone, butanone, isopropyl-methylketone; ethers (C1-C10) such as diethyl ether, diisopropyl ether, tertbutylmethyl ether, tetrahydrofuran, dioxane; halogenated hydrocarbons (C1-C10) such as methylene chloride, chloroform, chlorobenzene, fluorinated alkanes; trifluoroacetic acid; dimethylformamide; dimethylacetamide; and acetonitrile, and combinations therein. In certain aspects, the mobile phase is a polar solvent, preferably a C1-C6 alcohol, and more preferably is methanol.
In other aspects, any of the solvents listed above can be combined to produce the desired chromatographic separations. In particular, the primary solvent can be a C1-C6 alcohol, and more preferably is methanol. The secondary solvent can be a C1-C6 alcohol, and in particular, can be ethanol or isopropanol. Thus, certain eluent mixtures can include methanol/isopropanol wherein the eluent preferably contains at least 50% by volume of methanol. Alternatively the eluent may contain at least 60%, 70%, 80%, or 90% by volume of methanol.
A feature of the present invention is the adjustment of the chromatographic conditions to obtain the desired enantiomer of modafinil (preferably armodafinil) in at least 95% enantiomeric excess. Alternatively, the desired enantiomer of modafinil (preferably armodafinil) is recovered in at least 96%, 97%, 98%, 99% enantiomeric excess, and preferably in greater than 98 or 99% enantiomeric excess.
Another feature of the present invention provides for adjusting or modifying the chromatographic conditions to obtain the desired enantiomer (preferably armodafinil) in at least 90% yield. Alternatively, the desired enantiomer of modafinil (preferably armodafinil) is recovered in at least a 91%, 92%, 93%, 94%, 95%, 96%, 97%, 98% or 99% yield, and preferably greater than a 90 or 95% yield.
The following examples show representative parameters for the isolation of the levorotatory enantiomer of modafinil. Other column configurations can be utilized for the chiral separations described herein, including but not limited to 1.3/2.3/1.6/0.8; or 1/2.45/1.85/0.7.
Examples 1-4
While preferred embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes or modifications can be made without varying from the scope of the invention.
| Number | Date | Country | Kind |
|---|---|---|---|
| 04292199.9 | Sep 2004 | EP | regional |
This application claims priority of pending U.S. Provisional Application Ser. No. 60/611,511, filed Sep. 20, 2004 and European Patent Application Number 04292199.9, filed Sep. 13, 2004. The disclosures of these prior applications are incorporated herein by reference in their entireties for all purposes.
| Number | Date | Country | |
|---|---|---|---|
| 60611511 | Sep 2004 | US |
