Organic compounds -- part of the class 532-570 series – Organic compounds – Phosphorus containing
Reexamination Certificate
2002-08-16
2004-05-04
Vollano, Jean F. (Department: 1621)
Organic compounds -- part of the class 532-570 series
Organic compounds
Phosphorus containing
Reexamination Certificate
active
06730813
ABSTRACT:
This application is a 371 of PCT/EP01/01749 filed Feb. 16, 2001, now WO 01/60830.
The present invention relates to a method for the production of N-(phosphonomethyl)glycine (PMG), which facil-itates a very effective and economical recycling of waste water streams from; the preceding processes for the production of N-(phosphonomethyl)glycine starting from N-(phosphonomethyl)imino-diacetic acid (PMIDA).
N-(Phosphonomethyl)glycine is a highly effective herbicide with full-systemic mode of action known in agriculture under the name of Glyphosate. It overcomes annual and perennial weeds and grass weed species. The application is multifarious and has acquired world-wide enormous economic importance.
According to the stand of technology, there are several manufacturing processes for the production of glyphosate. For example, in U.S. Pat. No. 3,950,402; EP 0 472 693 B1; U.S. Pat. No. 4,147,719 Monsanto describes methods for the oxidation of PMIDA with oxygen or peroxides such as hydrogen peroxide in the presence of a precious metal bound to activated carbon (Pt/C, Pd/C, Rh/C). In other methods, the conversion is carried out only with activated carbon as catalyst (EP-A 0 162 035; DE-OS 30 17 518; U.S. Pat. No. 3,969,398; WO 96/38455; WO 96/27602). Patent ES 9202254 describes a method for the conversion of PMIDA in the presence of an ion exchange resin—preferably a cation exchanger in a protonated form—with peroxides.
The described methods, even if they are highly efficient, have all a common disadvantage that in the production of glyphosate large quantity of waste water are accumulated. Typically, in the described processes an aqueous solution or suspension of N-(phosphonomethyl)iminodiacetic acid is converted, with peroxides or oxygen in the presence of a hetero-geneous catalyst, to glyphosate. The use of heterogeneous catalysts stipulates that after the reaction the product has to be dissolved in the solvent, since otherwise during the separation of the catalyst the product would be separated along. However, glyphosate is only slightly soluble in water (5° C.: 0.8%, 20° C.: 1.1%, 95° C.: 6.5%); the solubility in organic solvents is even much lower. Consequently, for these processes large volumes of water are required.
After the separation of the catalyst, the reaction solution has to be concentrated for isolating the product, whereby a condensate-waste water stream is formed (in the following named condensate). Then the product is filtered or centrifuged while a filtrate-waste water stream is formed (in the following named filtrate).
The condensate contains, as substantial impurities, formaldehyde and formic acid. The contamination profile of the filtrate consists of a number of by-products and cleavage products—mostly phosphorus-containing compounds. Typically, a filtrate still contains 1 to 4% by weight glyphosate. Because of the components, the disposal presents a problem, since several of the components have herbicidal properties. Moreover, due to the components, neither the condensate nor the filtrate can be recycled as a reaction medium. Therefore, it is of interest to minimize the residual quantities of glyphosate in the filtrate and to reduce the quantities of the filtrate. The advantages are in a higher efficiency of the production process, in a lowering of the disposal costs, and in the protection of the environment.
The recovery of glyphosate from the filtrate is described in WO 97/05149. The method is based on the separation of a difficultly soluble complexes which glyphosate forms with iron(III) salts (also: Ca, Mg, Al). By a variation of the pH value, glyphosate can be set free from the complex and can be isolated or can be recycled to the process. However, this type of recovery is very costly.
EP 0 323 821 B1 discloses a treatment of the filtrate from the glyphosate processes. For this purpose, after separation from the main quantity of the product, the remaining quantities of PMIDA, glyphosate, and other phosphonic acids (e.g., aminomethanephosphonic acid, briefly AMPS) remaining in the filtrate are destroyed with oxygen on transition metal catalysts (e.g., Mn, Co, Fe) typically at 35 bar and 120° C. (>85% after 6 hours). However, the destruction of the components is connected with a very high technical process cost and therewith in two ways very costly.
Consequently, the present invention has for its object to develop an improved method for the production of glyphosate, which at least partly avoids the indicated disadvantages according to the state of technology and recovers the available substances contained in the mother liquor, without higher technical costs. Moreover, a decrease of the waste water streams formed in the process should be achieved.
This problem is solved by a method for the production of N-(phosphonomethyl)glycine (glyphosate) by
(a) oxidation of N-(phosphonomethyl)iminodiacetic acid with peroxides or oxygen in an aqueous medium in the presence of a heterogeneous catalyst,
(b) followed by the separation of the catalyst from the aqueous reaction suspension from stage (a),
(c) concentration of the clear reaction solution from stage (b), especially by evaporation, and
(d) separation of N-(phosphonomethyl)glycine from the concentrated reaction solution from stage (c), especially by filtration,
which is characterized in that the aqueous reaction solution from stage (d) (mother liquor) is recycled to stage (b) (catalyst separation) and/or stage (c) (concentration).
Surprisingly, we discovered that the residual quantity of glyphosate in the mother liquor as well as the volume of the mother liquor itself can be significantly reduced when the latter is recycled to stage (b) and/or stage (c) and simultaneously glyphosate can be isolated in a high yield at unchanged high purity, by means of a method of the invention at a low technical expenditure.
According to the present invention, the method comprises at least four stages. In the first stage (a) N-(phosphonomethyl)iminodiacetic acid is oxidized in aqueous solution, whereby the reaction conditions can vary within very broad limits. Peroxides such as hydrogen peroxide or oxygen-containing gases as well as their mixtures can be used as oxidation agents. Likewise, the choice of the catalyst can be optional. Applied are, e.g., precious metal catalysts such as palladium, platinum, and rhodium, especially on activated carbon, pure activated carbon catalysts or pure precious metal catalysts. A choice of activated carbon is described, for example, in the following patents: EP-A 162 035, U.S. Pat. No. 3,969,398, WO 96/38 455, WO 96/27 602 and DE-OS 30 17 518. The reaction conditions for carrying out the oxidation reaction can be varied within broad limits. For example, reaction stage (a) is customarily carried out in aqueous medium at temperatures between 50 and 150° C., especially between 50 and 100° C., under pressure from 0.5 to 50 bar, and catalyst portions from 2 to 50% by weight based on the charged quantity of PMIDA. In the conversion with peroxides the molar ratio of PMIDA to peroxide is preferably adjusted to between 1:1.5 and 1:5. When the oxidation is carried out with an oxygen-containing gas, as a rule the gas is conveyed under pressure through the reaction mixture. The concentration of the reaction components in aqueous suspension can be varied in broad limits and is preferably adjusted to 1 to 30% by weight based on the charged N-(phosphonomethyl)iminodiacetic acid. The reaction times can vary depending on the reaction conditions and can move in a range from a few minutes to several hours.
In the following stage (b) the solid catalyst is separated from the aqueous reaction stage (a) which can occur according to known methods such as filtration or centrifugation. The separation is preferably done by filtration in a temperature range from 50 to 100° C. possibly also under pressure. The separated catalyst can then be recycled directly into reaction stage (a).
After the separation of the catalyst, the clear reaction solution from stage (b) is concentrated in stage (c) for example, by evaporation, whereb
Hammer Benedikt
Hitzler Martin
Thalhammer Franz
Monsanto Technology LLC
Schaper Joseph A.
Senniger Powers Leavitt & Roedel
Vollano Jean F.
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