Classifications

• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
  • A61K31/00—Medicinal preparations containing organic active ingredients
  • A61K31/185—Acids; Anhydrides, halides or salts thereof, e.g. sulfur acids, imidic, hydrazonic or hydroximic acids
  • A61K31/19—Carboxylic acids, e.g. valproic acid
  • A61K31/195—Carboxylic acids, e.g. valproic acid having an amino group
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
  • C07C227/38—Separation; Purification; Stabilisation; Use of additives
  • C07C227/40—Separation; Purification
• • A—HUMAN NECESSITIES
  • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
  • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
  • A61P25/00—Drugs for disorders of the nervous system
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
  • C07C227/38—Separation; Purification; Stabilisation; Use of additives
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C229/00—Compounds containing amino and carboxyl groups bound to the same carbon skeleton
  • C07C229/02—Compounds containing amino and carboxyl groups bound to the same carbon skeleton having amino and carboxyl groups bound to acyclic carbon atoms of the same carbon skeleton
  • C07C229/28—Compounds containing amino and carboxyl groups bound to the same carbon skeleton having amino and carboxyl groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated and containing rings
• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
  • C25B3/00—Electrolytic production of organic compounds
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2601/00—Systems containing only non-condensed rings
  • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
  • C07C2601/14—The ring being saturated

Definitions

• the present invention relates to a new industrial process for obtaining cyclic amino acids, and particularly gabapentin, with a high degree of purity.
• n is an integer selected from 2, 3 and 4
• Example 1 thus describes obtaining anhydrous crystalline gabapentin from its hydrochloride by means of the treatment of an aqueous solution thereof with a basic ion exchange resin and the subsequent crystallization in an ethanol/ether mixture.
• Patent documents EP 414274-A2 and EP 414275-A2 describe alternative processes for obtaining said cyclic amino acids, in which the lactam of formula (II) is used as an intermediate:
• n has the same meaning as before.
• the most significant difficulty facing the processes for preparing cyclic amino acids of formula (I) from an addition salt thereof with a mineral acid is to provide a cyclic amino acid of formula (I), and particularly gabapentin, with a quality suitable for being used as an active ingredient in pharmaceutical formulations.
• the cyclic amino acid of formula (I) must have a mineral acid anion content less than 20 ppm based on the amount of cyclic amino acid.
• Patent document WO01/097612-A1 provides that pharmaceutical formulations containing gabapentin with a mineral acid anion content exceeding 20 ppm are also stable given that after one year of stability, the lactam content does not increase by more than 0.2% by weight.
• Patent documents EP 340677-A2, WO 00/01660-A1, EP 1174918-A1, and the aforementioned ES 443723-A, EP 414274-A2 and EP 414275-A2 describe technical solutions based on the use of basic ion exchange resins.
• the addition salt of gabapentin with a mineral acid is dissolved in water or in a short-chain alcohol. Then said solution is eluted through the chromatographic column filled with a basic ion exchange resin. Gabapentin is finally isolated.
• Patent document WO 02/34709-A2 describes the use of strongly cationic ion exchange resins. Gabapentin is thus fixed to the resin and the mineral acid anion is eliminated by elution with water.
• patent document US2003/0119908-A1 describes stable gabapentin compositions containing less than 5 ppm of gabapentin hydrochloride and which may furthermore contain more than 20 ppm of sodium chloride, based on the amount of gabapentin.
• Patent document WO 03/089403-A1 also describes the use of ion exchange resins, but not packed in a chromatographic column, rather they are added directly as a reagent in the solid phase to a solution of the addition salt of gabapentin with a mineral acid. Then the resin is separated and a gabapentin solution in free amino acid form is obtained.
• the object of the present invention is a process for obtaining cyclic amino acids substantially in salt-free form of formula (I) by means of applying an electrochemical process.
• n is an integer selected from 2, 3 and 4, is characterized in that it comprises:
• the cyclic amino acid substantially in salt-free form relates to a cyclic amino acid with a mineral acid anion content not more than 100 ppm, preferably not more than 20 ppm, more preferably not more than 5 ppm.
• the compound subjected to the electrolysis process is an addition salt of the cyclic amino acid of formula (I) with a mineral acid.
• the addition salt of the cyclic amino acid which is subjected to electrolysis is gabapentin hydrochloride and the product which is obtained is gabapentin substantially in salt-free form.
• Said compounds can be prepared using any of the methods described in the state of the art, for example, in examples 1, 3 and 4 patent document ES 443723-A or in example 9 of patent document EP 414274-A2.
• cyclic amino acid and gabapentin relate to the free amino acids.
• the addition salts of the cyclic amino acids of formula (I) can be formed with mineral acids, such as for example: hydrochloric acid, hydrobromic acid, hydroiodic acid, hydrofluoric acid, sulfuric acid, phosphoric acid; and with strong organic acids, such as for example: methanesulfonic acid, benzene sulfonic acid, p-toluenesulfonic acid.
• mineral acids such as for example: hydrochloric acid, hydrobromic acid, hydroiodic acid, hydrofluoric acid, sulfuric acid, phosphoric acid
• strong organic acids such as for example: methanesulfonic acid, benzene sulfonic acid, p-toluenesulfonic acid.
• the mineral acid forming the addition salt with the cyclic amino acid is preferably selected for the process object of the invention out of any of the hydrochloric, hydrobromic, hydroiodic, hydrofluoric acids and/or mixtures thereof. More preferably, the selected mineral acid is hydrochloric acid or hydrobromic acid.
• the particularly preferred addition salts are gabapentin hydrochloride and gabapentin hydrobromide.
• the solution of the addition salt of the cyclic amino acid with a mineral acid is an aqueous solution so that it is a conductor of the electric current and the electrolysis process can take place.
• Said aqueous solution can further comprise at least one electrolytically stable solvent miscible in water, i.e. it is stable in the electrolysis conditions.
• Alcohols for example, can be mentioned among these solvents.
• the alcohols are preferably selected from the group formed by: methanol, ethanol, propanol, isopropanol, and/or mixtures thereof.
• water is normally at least 50% of the water/alcohol mixture expressed in volume/volume.
• water is the major component of the water/alcohol mixture.
• the concentration of the addition salt of the cyclic amino acid with a mineral acid in the solution is determined by the solubility of said salt in the solvent selected for carrying out electrolysis.
• the concentration thereof in an aqueous solution is usually comprised between 10% and 15% by weight.
• the electrolysis step of the process object of the invention is carried out in an electrochemical reactor having an anodic compartment and a cathodic compartment separated by a selective anionic membrane.
• the process can be carried out under constant and equal pressure in both compartments during the entire electrolysis process.
• the useful area of the electrochemical reactor is not a critical parameter for the process object of the invention, since the conditions of the electrochemical process can be adapted to each reactor by means of the use of techniques that are well known by a person skilled in the art.
• An example of a typical electrochemical reactor could be one that has a useful area comprised between 4 and 8 m 2 .
• the distance between the electrodes may be comprised between approximately 15 and 20 mm.
• the anode which is located in the anodic compartment, is generally formed by a metal which can resist the oxidizing conditions generated around it due to the formation of halogen molecules.
• the anode is preferably formed by titanium coated with noble metals such as ruthenium and iridium, which are subsequently converted into oxides by the action of the electrochemical process. These anodes are called oxygen-evolving anodes. It is also possible to use anodes of other metals that are less resistant to the oxidizing conditions present in the anode, but they would have a more limited duration and would need to be replaced sooner.
• the cathode is located in the cathodic compartment, which is preferably an element with low hydrogen overvoltage, such as for example: copper, platinized titanium, stainless steel, nickel or iron. Hydrogen is generated in this compartment and accordingly the cathode does not have oxidation problems.
• an element with low hydrogen overvoltage such as for example: copper, platinized titanium, stainless steel, nickel or iron. Hydrogen is generated in this compartment and accordingly the cathode does not have oxidation problems.
• the selective anionic membrane is a membrane which selectively allows anions which are located in the cathodic compartment to pass through to the anodic compartment, where they are discharged in the anode, but which substantially does not allow the passage therethrough of the cyclic amino acid.
• the chloride ions move through the selective anionic membrane to the anodic compartment where they are discharged in the form of chlorine gas.
• the membrane substantially prevents the passage of gabapentin to the anodic compartment.
• anionic membranes The preparation and structure of anionic membranes are thoroughly described in the book “Ion exchange membranes”, T. Sata, Royal Society of Chemistry, 2004 (ISBN: 0 85404 590 2).
• An aqueous, eventually hydroalcoholic, solution of the addition salt of the cyclic amino acid of formula (I) with a mineral acid, for example, gabapentin hydrochloride or hydrobromide, is introduced in the cathodic compartment of the electrochemical reactor.
• the anodic compartment is filled with water.
• the electrochemical reaction occurring in the anode consists of discharging the anion chloride generating chlorine in gas form:
• the halide anions move from the cathodic compartment through the selective anionic membrane to the anode, where they are discharged in the form of a halogen molecule.
• the anions of the mineral acid are chloride or bromide ions, chlorine or bromine are formed in the anode, respectively.
• the presence of the halogen molecules in the anodic compartment acts against the duration of the anode and may reduce the effectiveness of the selective anionic membrane, since it may be sensitive to the oxidizing agents.
• a vacuum system absorbing the halogen and leading it to a trap system having a reducing solution, for example sodium bisulfite, or a sodium hydroxide solution, can be mentioned among those systems which can be used to carry out said elimination.
• the chlorine generated in the anode can be absorbed in a sodium hydroxide solution, thereby obtaining a sodium hypochlorite solution which could be used in the synthesis of gabapentin hydrochloride according to the process described in patent document ES 443723-A by means of a Hofmann rearrangement.
• the same process can be applied in the case of using gabapentin hydrobromide, obtaining a sodium hypobromite solution in this case.
• Another suitable system for eliminating the halogen formed in the anode comprises placing an aqueous solution of a reducing agent in the anodic compartment.
• the reducing agent does not generate ions in the solution which may interfere with the electrochemical processes intended for preparing gabapentin.
• the use of a sulfur dioxide solution is especially preferred.
• An aqueous solution with a sulfur dioxide content comprised between 0.3% and 0.7% by weight is more preferably used.
• the electrochemical reaction of the cathode consists of the release of hydrogen and the generation of hydroxyl ions:
• gabapentin In the case of electrolysis of an aqueous solution of gabapentin hydrochloride, the hydroxyl ions neutralize the addition salt of gabapentin in the areas surrounding the cathode, and gabapentin (I), which is electrically neutral, is formed.
• the gabapentin is in equilibirum with its internal salt, which is also electrically neutral:
• aqueous solution of the cyclic amino acid is thus obtained in the cathodic compartment, said amino acid being able to be isolated from such solution by using techniques well known by a person skilled in the art, such as for example the evaporation under a vacuum and at a temperature of not more than 50° C.
• Electrolytic processes may generally take place at a constant voltage or at a constant density of the current intensity.
• the voltage or potential difference between the two electrodes is what generates a movement of ions and therefore a current intensity.
• the density of the current intensity is the intensity of the current in relation to the surface unit of the electrode.
• the current intensity is provided by the ions which are dissolved in the solution.
• a person skilled in the art may establish the working conditions in a routine manner so that the process is economically viable and so that oxidation of the cyclic amino acid in the anode is prevented.
• the electrochemical reactor and the parameters of the density of the intensity and the voltage are adapted so as to reduce the discharge of the cyclic amino acid in the anode, for example, not more than 40 V, and to have a process that is economically advantageous, for example, with a voltage of not less than 3 V.
• the electrolytic process preferably occurs at a constant voltage in the process object of the invention.
• the voltage used is preferably comprised between 3 and 20 V. It is more preferably comprised between 8 and 13 V.
• the conductivity of the solution of the addition salt of the cyclic amino acid with a mineral acid located in the cathodic compartment decreases.
• the conductivity of the solution is directly proportional to the concentration of the halide ions therein.
• the initial conductivity values are typically comprised between 40 and 60 mS. However at the end of the process they are usually comprised between 150 and 300 ⁇ S.
• the initial density of the current intensity is set by the voltage and the concentration of the addition salt of the cyclic amino acid with a mineral acid in the cathodic compartment.
• the typical values for the density of the current intensity at the start are comprised between 500 A/m 2 and 2,000 A/m 2 , preferably between 1,000 A/m 2 and 1,500 A/m 2 .
• the density of the current intensity is gradually reduced as the halide ions move towards the anodic compartment, and the cathodic compartment becomes enriched in cyclic amino acid which has no electric charge, though it is in equilibrium with its internal salt, which also has no net electric charge.
• the typical values for the density of the current intensity at the end of the process are comprised between 30 A/m 2 and 70 A/m 2 .
• the electrochemical reaction ends because the cyclic amino acid solution is not conductive and, as there is no conductivity, the density of the current intensity reaches the aforementioned minimum values.
• the pH in the cathodic compartment is simultaneously modified as the electrolytic process progresses.
• the initial pH is approximately 1 because it contains a solution of an addition salt of the cyclic amino acid with a mineral acid, and the pH at the end of the electrolytic process is close to the neutral area because it contains a solution of the cyclic amino acid.
• the progressive reduction of the conductivity and the increase in the pH value can be observed in the cathodic compartment during the entire process object of the invention.
• conductivity is directly related to the concentration of anions of the mineral acid in the cathodic compartment, such that it is possible to control it continuously, being able to end the reaction at the same moment in which the concentration of anions in the solution corresponds with the concentration established as a quality parameter.
• Said concentration may be more than or less than 20 ppm of mineral acid anion with respect to the cyclic amino acid, as deemed appropriate by a person skilled in the art, as indicated in the section of this description which corresponds to the state of the art.
• the electrolytic process takes place at a temperature at which the formation of lactam as an impurity is substantially prevented.
• Said temperature is preferably not more than 50° C. It is more preferably comprised between 10° C. and 25° C.
• the temperature can be maintained between the established values by means of using apparatus that are well known by a person skilled in the art. Plate heat exchangers, which cool the solution through an external circuit, can be mentioned among such apparatus.
• the selected temperature interval also minimizes the passage of the addition salt of the cyclic amino acid with a mineral acid through the selective anionic membrane, therefore the process yield is better.
• the cyclic amino acid substantially in salt-free form present in the aqueous, eventually hydroalcoholic, solution of the cathodic compartment is isolated by means of techniques that are well known by a person skilled in the art, such as evaporation by distillation, atomization or turbo-drying.
• the aqueous solution of the cyclic amino acid is evaporated to dryness by means of applying a vacuum so as to prevent temperatures of more than 50° C., which could generate lactam as an impurity.
• the aqueous solution is typically evaporated at a temperature comprised between 10° C. and 25° C.
• the applied vacuum is generally comprised between 133 and 1,333 Pa (1-10 mmHg).
• the cyclic amino acid substantially in salt-free form can then be crystallized in a solvent selected from the group formed by methanol, ethanol or isopropanol.
• the cyclic amino acid substantially in salt-free form obtained with the process object of the invention has typical mineral acid anion contents related to the amount of cyclic amino acid, not more than 10 ppm, values of not more than 3 ppm being usual. In terms of the lactam content, typical values are under 0.01% by weight, being able to reach values of not more than 0.001%.
• the process object of the invention allows preparing gabapentin substantially in salt-free form with a mineral acid anion content of not more than 20 ppm related to the amount of gabapentin.
• the mineral acid anion content is preferably not more than 10 ppm. A mineral acid anion content close to 0 ppm can even be obtained, i.e. the complete elimination of the anion, which would be difficult in the case of using ion exchange resins, can be attained.
• the cyclic amino acid losses during the process are generally comprised below 2%.
• the process object of the invention allows obtaining cyclic amino acids substantially in salt-free form of formula (I) by means of a simple process, with a good yield and high quality, with very low lactam contents and with a mineral acid anion content which is in accordance with the quality parameters established by the skilled person, being able to reach not more than 3 ppm. This ensures excellent stability both of the product and of its pharmaceutical formulations.
• the mineral acid anion content can be controlled on line and the reaction can be stopped when the pre-established parameters have been reached.
• An aqueous solution comprising 200 kg of gabapentin hydrochloride and 1,500 kg of deionized water is loaded in the cathodic compartment, and 5,000 kg of an aqueous solution of sulfur dioxide at 0.5% by weight is loaded in the anodic compartment in an electrochemical reactor with a useful area of 6 m 2 equipped with an anodic compartment having oxygen-evolving anodes and with a cathodic compartment with stainless steel cathodes, separated by a selective anionic membrane SYBRON MA series (marketed by Sybron Chemicals).
• the circulation pumps are started up and a constant voltage of 11 V is set for the electrolysis.
• the density of the intensity gradually decreases from the initial value of 1,250 A/m 2 to a final value of 50 A/m 2 .
• the conductivity of the cathodic compartment is simultaneously reduced from an initial value of 50 mS to a final value of approximately 200 ⁇ S, and the pH value goes from 1 to approximately 7.
• the electrolysis is carried out maintaining the temperature of the solution of the cathodic compartment at approximately 15° C. by means of an external plate heat exchanger.
• the solution of the cathodic compartment is discharged to an evaporator.
• the water is evaporated to dryness using a vacuum comprised between 133 and 1,333 Pa (1-10 mmHg) and a temperature comprised between 10° C. and 25° C.
• the obtained solid is filtered, washed with anhydrous isopropanol and dried in a rotary drum with a high vacuum at room temperature.
• the chloride content is determined by titration according to the Mohr method and a value of less than 10 ppm is obtained.
• the lactam content is determined by HPLC and a value of less than 0.01% is obtained.

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• 2004
  • 2004-07-22 ES ES200401797A patent/ES2246159B1/es not_active Expired - Fee Related
• 2005
  • 2005-07-14 AT AT05778843T patent/ATE494273T1/de not_active IP Right Cessation
  • 2005-07-14 DE DE602005025801T patent/DE602005025801D1/de not_active Expired - Lifetime
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  • 2005-07-14 US US11/658,045 patent/US20090032406A1/en not_active Abandoned
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